WO2012161017A1 - Composition d'essence et son procédé de fabrication - Google Patents

Composition d'essence et son procédé de fabrication Download PDF

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Publication number
WO2012161017A1
WO2012161017A1 PCT/JP2012/062310 JP2012062310W WO2012161017A1 WO 2012161017 A1 WO2012161017 A1 WO 2012161017A1 JP 2012062310 W JP2012062310 W JP 2012062310W WO 2012161017 A1 WO2012161017 A1 WO 2012161017A1
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gasoline
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PCT/JP2012/062310
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Japanese (ja)
Inventor
青木　剛
忠豪 曽根
泰之 岩佐
柳川　真一朗
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Ｊｘ日鉱日石エネルギー株式会社
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Priority claimed from JP2011117597A external-priority patent/JP5667513B2/ja
Priority claimed from JP2011117598A external-priority patent/JP5639531B2/ja
Application filed by Ｊｘ日鉱日石エネルギー株式会社 filed Critical Ｊｘ日鉱日石エネルギー株式会社
Publication of WO2012161017A1 publication Critical patent/WO2012161017A1/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
    • C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/104—Light gasoline having a boiling range of about 20 - 100 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1037—Hydrocarbon fractions
    • C10G2300/1044—Heavy gasoline or naphtha having a boiling range of about 100 - 180 °C
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1096—Aromatics or polyaromatics
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/201—Impurities
    • C10G2300/202—Heteroatoms content, i.e. S, N, O, P
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/301—Boiling range
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/305—Octane number, e.g. motor octane number [MON], research octane number [RON]
    • 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
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/20—Characteristics of the feedstock or the products
    • C10G2300/30—Physical properties of feedstocks or products
    • C10G2300/308—Gravity, density, e.g. API
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline

Definitions

  • the present invention relates to a gasoline composition useful as a fuel for automobiles and a method for producing the same.
  • deposits in the combustion chamber of a gasoline engine can cause deterioration of power performance, fuel consumption, exhaust gas, and carbon knock due to disturbance of the combustion state of the engine.
  • Examination of the relationship between fuel properties and combustion chamber deposits has pointed out that when conventional reformate gasoline is blended, the deposits in the combustion chamber are significantly increased (see Non-Patent Document 1, for example). If the amount of reformed gasoline in the product gasoline can be reduced, the combustion chamber deposit may be reduced.
  • the reformed gasoline base material is a main base material for achieving a high octane number, and the reduction causes a decrease in the octane number.
  • the octane number decreases, the engine may be damaged due to knocking, and the engine performance may not be maximized in a premium gasoline specification vehicle.
  • the distillation property of gasoline changes greatly, there is a risk that the drivability and acceleration of the vehicle will deteriorate.
  • the present invention has been made in view of such circumstances, and a method for producing a gasoline composition having a low combustion gas deposit generation ability and low exhaust gas (NOx) performance while maintaining an octane number and distillation properties. The purpose is to provide.
  • the inventors of the present invention have found that in a method for producing a gasoline composition, a cracked and reformed gasoline base material, a catalytic cracked gasoline base material, and a hydrocarbon base material having 4 carbon atoms having predetermined properties. It is found that by adding a predetermined amount of the fuel, the combustion chamber deposit can be reduced, the engine performance can be maximized, and further, high-performance gasoline with less carbon dioxide emission can be obtained, and the present invention has been completed. It came to do. That is, the present invention is as follows.
  • Aromatic content is 90 vol% or more
  • Olefin content is 5 vol% or less
  • C8 aromatic content is 5-50 vol%
  • Aromatic content of 9 or more carbon atoms is 30 vol% or less
  • Sulfur content is 20 mass ppm or less
  • Research octane number is 110 or more (7)
  • Density at 15 ° C. is 0.8 to 0.95 g / cm 3
  • Catalytic reforming gasoline base material having the following properties (1) to (7) 1 to 40% by volume, light catalytic cracking gasoline base material 25 to 50% by volume, and contact containing light catalytic cracking gasoline base material
  • Aromatic content is 90 vol% or more
  • Olefin content is 5 vol% or less
  • C8 aromatic content is 5-50 vol%
  • Aromatic content of 9 or more carbon atoms is 30 vol% or less
  • Sulfur content is 20 mass ppm or less
  • Research octane number is 110 or more
  • Density at 15 ° C. is 0.8 to 0.95 g / cm 3
  • Distillation temperature 70 [5] The method for producing a gasoline composition according to the above [3], wherein the amount of distillation (E70) at 40 ° C. is 40% by volume or less [5]
  • the gasoline composition satisfies the following (1) to (8): .
  • (1) Density at 15 ° C. is 0.783 g / cm 3 or less
  • Sulfur content is 10 mass ppm or less
  • Total aromatic content is 45% by volume or less
  • Benzene is 1% by volume or less
  • 10% by volume distillation temperature is 70 ° C. or less, 50% by volume distillation temperature is 110 ° C. or less, and 90% by volume distillation temperature is 180 ° C. or less.
  • Distillation temperature 70 Distillation amount at 70 ° C. (E70) is 45% by volume or less (8)
  • the content of the cleaning dispersant is 80 mg / L or more and 500 mg / L or less
  • [6] The gasoline composition according to any one of [1] to [5], wherein the cracked and reformed gasoline base material is blended so as to satisfy 0.10 ⁇ A / B ⁇ 1.0.
  • Production method. (A represents the content (volume%) of the aromatic component derived from the cracked and reformed gasoline base material, and B represents the content (volume%) of the total aromatic content in the gasoline composition.)
  • the cracked and reformed gasoline base material contains medium-pore zeolite and / or large-pore zeolite containing 10% by volume distillation temperature of 140 ° C. or more and 90% by volume distillation temperature of 380 ° C. or less. Characterized in that it is produced by contacting with a catalyst for cracking and reforming reaction, and performing a cracking and reforming reaction at a reaction temperature of 400 to 650 ° C., a reaction pressure of 1.5 MPaG or less, and a contact time of 1 to 300 seconds.
  • a method for producing a gasoline composition according to any one of [6].
  • the present invention is described in detail below.
  • the method for producing a gasoline composition of the present invention comprises a cracked and reformed gasoline base material having a predetermined property of 1 to 40% by volume, a catalytic cracked gasoline base material of 10 to 90% by volume, and a hydrocarbon base material having 4 carbon atoms. It is characterized by containing 0.1 to 10% by volume.
  • the cracked and reformed gasoline base material is blended in an amount of 1 to 40% by volume based on the total amount of the gasoline composition.
  • the cracked and reformed gasoline base material is preferably 3% by volume or more, more preferably 5% by volume or more, and further preferably 15% by volume or more.
  • the ratio (A / B) of the aromatic content A (volume%) derived from the cracked and reformed gasoline base to the total aromatic content B (volume%) in the gasoline composition is 0 in terms of suppressing increase in combustion chamber deposits. It is preferable to mix
  • the cracked and reformed gasoline base material according to the present invention contains medium-oil zeolite and / or large-pore zeolite in a feed oil having a 10% by volume distillation temperature of 140 ° C or higher and a 90% by volume distillation temperature of 380 ° C or lower. It is produced by contacting with a catalyst for cracking reforming reaction to be performed, and performing a cracking reforming reaction at a reaction temperature of 400 to 650 ° C., a reaction pressure of 1.5 MPaG or less, and a contact time of 1 to 300 seconds.
  • the cracking / reforming substrate used in the present invention is produced by fractional distillation from the cracking / reforming reaction product obtained by the following cracking / reforming reaction.
  • the feedstock oil is brought into contact with the catalyst for cracking and reforming reaction, the saturated hydrocarbon contained in the feedstock oil is used as a hydrogen donor source, and polycyclic aromatic hydrocarbons are converted by hydrogen transfer reaction from the saturated hydrocarbon.
  • polycyclic aromatic hydrocarbons are converted by hydrogen transfer reaction from the saturated hydrocarbon.
  • the fuel base material mainly containing aromatic hydrocarbons can be produced.
  • the feed oil for the cracking and reforming reaction is preferably an oil having a 10 vol% distillation temperature of 140 ° C or higher and a 90 vol% distillation temperature of 380 ° C or lower, and the 10 vol% distillation temperature of the raw oil is 150 ° C or higher. More preferably, the 90 vol% distillation temperature of the feedstock is more preferably 360 ° C or lower.
  • the 10 vol% distillation temperature and 90 vol% distillation temperature mentioned here mean values measured in accordance with JIS K2254 “Petroleum products-distillation test method”. Examples of the feed oil having a 10% by volume distillation temperature of 140 ° C. or higher and a 90% by volume distillation temperature of 380 ° C.
  • LCO cracked light oil
  • Examples include coal liquefied oil, heavy oil hydrocracked refined oil, straight-run kerosene, straight-run light oil, coker kerosene, coker light oil, and oil sand hydrocracked refined oil.
  • a fixed bed, a moving bed, a fluidized bed and the like can be mentioned.
  • a fluidized bed capable of continuously removing the coke component adhering to the catalyst and performing the reaction stably is preferable, and the space between the reactor and the regenerator is preferable.
  • a continuous regenerative fluidized bed in which the catalyst circulates and allows continuous reaction-regeneration is particularly preferred.
  • the feedstock oil in contact with the cracking reforming reaction catalyst is preferably in a gas phase. Moreover, you may dilute a raw material with gas as needed.
  • the catalyst for the cracking reforming reaction contains crystalline aluminosilicate.
  • the crystalline aluminosilicate is preferably a medium pore zeolite and / or a large pore zeolite because the yield of monocyclic aromatic hydrocarbons can be further increased.
  • the medium pore zeolite is a zeolite having a 10-membered ring skeleton structure. Examples of the medium pore zeolite include AEL type, EUO type, FER type, HEU type, MEL type, MFI type, NES type, and TON type. And zeolite having a WEI type crystal structure. Among these, the MFI type is preferable because the yield of monocyclic aromatic hydrocarbons can be further increased.
  • the large pore zeolite is a zeolite having a 12-membered ring skeleton structure.
  • Examples of the large pore zeolite include AFI type, ATO type, BEA type, CON type, FAU type, GME type, LTL type, and MOR type. , Zeolites of MTW type and OFF type crystal structures.
  • BEA type, FAU type, and MOR type are preferable in terms of industrial use, and the BEA type is more preferable because the yield of monocyclic aromatic hydrocarbons can be further increased.
  • the crystalline aluminosilicate may contain, in addition to the medium pore zeolite and the large pore zeolite, a small pore zeolite having a skeleton structure having a 10-membered ring or less, and a very large pore zeolite having a skeleton structure having a 14-membered ring or more.
  • examples of the small pore zeolite include zeolites having crystal structures of ANA type, CHA type, ERI type, GIS type, KFI type, LTA type, NAT type, PAU type, and YUG type.
  • Examples of the ultra-large pore zeolite include zeolites having CLO type and VPI type crystal structures.
  • the content of the crystalline aluminosilicate in the cracking and reforming reaction catalyst is 60 to 100% by weight when the entire catalyst for cracking and reforming reaction is 100% by weight. Preferably, 70 to 100% by mass is more preferable, and 90 to 100% by mass is particularly preferable. If the content of the crystalline aluminosilicate is 60% by mass or more, the yield of monocyclic aromatic hydrocarbons can be sufficiently increased.
  • the content of crystalline aluminosilicate in the cracking and reforming reaction catalyst is 20 to 60% by weight when the entire catalyst for cracking and reforming reaction is 100% by weight.
  • the content of the crystalline aluminosilicate is 20% by mass or more, the yield of monocyclic aromatic hydrocarbons can be sufficiently increased.
  • the content of the crystalline aluminosilicate exceeds 60% by mass, the content of the binder that can be blended with the catalyst is reduced, which may be unsuitable for fluidized beds.
  • the catalyst for decomposition reforming reaction preferably contains phosphorus and / or boron.
  • the catalyst for cracking and reforming reaction contains phosphorus and / or boron, it is possible to prevent the yield of monocyclic aromatic hydrocarbons from decreasing with time and to suppress the formation of coke on the catalyst surface.
  • Examples of the method for incorporating phosphorus into the cracking reforming reaction catalyst include an ion exchange method and an impregnation method. Specifically, a method in which phosphorus is supported on crystalline aluminosilicate, crystalline aluminogallosilicate, or crystalline aluminodine silicate, a phosphorus compound is contained during zeolite synthesis, and a part of the crystalline aluminosilicate skeleton is incorporated with phosphorus. Examples include a replacement method, a method using a crystal accelerator containing phosphorus during zeolite synthesis, and the like.
  • the phosphate ion-containing aqueous solution used at that time is not particularly limited, but was prepared by dissolving phosphoric acid, diammonium hydrogen phosphate, ammonium dihydrogen phosphate, and other water-soluble phosphates in water at an arbitrary concentration. Can be preferably used.
  • Examples of the method for incorporating boron into the cracking reforming reaction catalyst include an ion exchange method and an impregnation method. Specifically, a method in which boron is supported on crystalline aluminosilicate, crystalline aluminogallosilicate, or crystalline aluminosilicate, a part of the skeleton of crystalline aluminosilicate is incorporated with boron at the time of zeolite synthesis. Examples include a replacement method, a method using a crystal accelerator containing boron at the time of zeolite synthesis, and the like.
  • the phosphorus and / or boron content in the cracking reforming reaction catalyst is preferably 0.1 to 10% by mass relative to the total weight of the catalyst, and more preferably the lower limit is 0.5% by mass or more.
  • the upper limit is more preferably 9% by mass or less, and particularly preferably 8% by mass or less.
  • the cracking and reforming reaction catalyst may contain gallium and / or zinc as necessary. If gallium and / or zinc is contained, the production rate of monocyclic aromatic hydrocarbons can be increased.
  • the gallium-containing form in the catalyst for cracking and reforming reaction includes those in which gallium is incorporated in the lattice skeleton of crystalline aluminosilicate (crystalline aluminogallosilicate), and those in which gallium is supported on crystalline aluminosilicate (gallium) Supported crystalline aluminosilicate) and those containing both.
  • Zinc-containing forms in the catalyst for cracking and reforming reaction include those in which zinc is incorporated in the lattice skeleton of crystalline aluminosilicate (crystalline aluminodin silicate), and in which zinc is supported on crystalline aluminosilicate (zinc Supported crystalline aluminosilicate) and those containing both.
  • Crystalline aluminogallosilicate and crystalline aluminodine silicate have a structure in which SiO 4 , AlO 4 and GaO 4 / ZnO 4 structures are present in the skeleton.
  • the crystalline aluminogallosilicate and the crystalline aluminodine silicate can be obtained by, for example, gel crystallization by hydrothermal synthesis, or a method of inserting gallium or zinc into the lattice skeleton of the crystalline aluminosilicate.
  • Crystalline aluminogallosilicate and crystalline aluminozine silicate can be obtained by a method of inserting aluminum into the lattice skeleton of crystalline gallosilicate or crystalline zincosilicate.
  • the gallium-supporting crystalline aluminosilicate is obtained by supporting gallium on a crystalline aluminosilicate by a known method such as an ion exchange method or an impregnation method.
  • the gallium source used in this case is not particularly limited, and examples thereof include gallium salts such as gallium nitrate and gallium chloride, and gallium oxide.
  • the zinc-supporting crystalline aluminosilicate is obtained by supporting zinc on a crystalline aluminosilicate by a known method such as an ion exchange method or an impregnation method. Although it does not specifically limit as a zinc source used in that case, Zinc salts, such as zinc nitrate and zinc chloride, zinc oxide, etc. are mentioned.
  • the content of gallium and / or zinc in the cracking reforming reaction catalyst is 0.01-5.
  • the content is preferably 0% by mass, and more preferably 0.05 to 2.0% by mass. If the content of gallium and zinc is 0.01% by mass or more, the production rate of monocyclic aromatic hydrocarbons can be increased, and if it is 5.0% by mass or less, the yield of monocyclic aromatic hydrocarbons Can be higher.
  • the catalyst for cracking and reforming reaction is made into, for example, a powder form, a granular form, a pellet form or the like according to the reaction format.
  • a fluidized bed it is in the form of powder, and in the case of a fixed bed, it is in the form of particles or pellets.
  • the average particle size of the catalyst used in the fluidized bed is preferably 30 to 180 ⁇ m, more preferably 50 to 100 ⁇ m.
  • the bulk density of the catalyst used in the fluidized bed is preferably 0.4 to 1.8 g / cc, more preferably 0.5 to 1.0 g / cc.
  • the average particle size represents a particle size of 50% by mass in the particle size distribution obtained by classification with a sieve, and the bulk density is a value measured by the method of JIS standard R9301-2-3.
  • an inert oxide may be blended into the catalyst as a binder and then molded using various molding machines.
  • the cracking reforming reaction catalyst contains an inorganic oxide such as a binder, a binder containing phosphorus may be used.
  • the reaction temperature when the raw material oil is brought into contact with and reacted with the cracking reforming reaction catalyst is not particularly limited, but is preferably 400 to 650 ° C. If the minimum of reaction temperature is 400 degreeC or more, raw material oil can be made to react easily, More preferably, it is 450 degreeC or more. Moreover, if the upper limit of reaction temperature is 650 degrees C or less, the yield of monocyclic aromatic hydrocarbon can be made high enough, More preferably, it is 600 degrees C or less.
  • the reaction pressure when the raw material oil is brought into contact with and reacted with the cracking reforming reaction catalyst is preferably 1.5 MPaG or less, more preferably 1.0 MPaG or less. If the reaction pressure is 1.5 MPaG or less, the by-product of light gas can be suppressed and the pressure resistance of the reactor can be lowered.
  • the contact time between the feedstock and the cracking reforming reaction catalyst is not particularly limited as long as the desired reaction proceeds substantially.
  • the gas passage time on the cracking reforming reaction catalyst is 1 to 300 seconds.
  • the lower limit is more preferably 5 seconds or more
  • the upper limit is more preferably 150 seconds or less. If the contact time is 1 second or longer, the reaction can be performed reliably, and if the contact time is 300 seconds or shorter, accumulation of carbonaceous matter in the catalyst due to coking or the like can be suppressed. Or the generation amount of the light gas by decomposition
  • the cracking and reforming gasoline base material according to the present invention can be produced.
  • a known distillation apparatus or gas-liquid separation apparatus can be used.
  • a distillation apparatus what can distill and isolate
  • the cracked and reformed gasoline base material according to the present invention is preferably a fraction mainly containing hydrocarbons having 7 and 8 carbon atoms.
  • the cracked and reformed gasoline base material according to the present invention is obtained by the above-described production method and has the following properties.
  • the total aromatic content of the cracked and reformed gasoline base material according to the present invention is 90% by volume or more, preferably 98% by volume or more, and more preferably 99% by volume or more.
  • the total aromatic content here means the content of the aromatic content measured by JIS K2536 “Petroleum product-component test method”.
  • the aromatic component having 8 carbon atoms of the cracked and reformed gasoline base material according to the present invention is 5% by volume or more and 50% by volume or less.
  • the aromatic component having 9 or more carbon atoms of the cracked and reformed gasoline base material according to the present invention is 30% by volume or less, preferably 25% by volume or less, more preferably 20% by volume or less.
  • the aromatic content having 8 or 9 or more carbon atoms means the content of the aromatic content measured by JIS K2536 “Petroleum product-component test method”.
  • the olefin content of the cracked and reformed gasoline base material according to the present invention is 5% by volume or less, preferably 3% by volume or less, and more preferably 1% by volume or less.
  • the olefin content here is a value measured by JIS K2536 “Petroleum products—component test method”.
  • the sulfur content of the cracked and reformed gasoline base material according to the present invention is 20 mass ppm or less, preferably 10 mass ppm or less, more preferably 5 mass ppm or less.
  • the sulfur content here is a value measured by JIS K2541 “Crude oil and petroleum products—sulfur content test method”.
  • the research octane number of the cracked and reformed gasoline base material according to the present invention is 110 or more.
  • the research octane number referred to here is a value measured by JIS K2280 “Petroleum products—fuel oil—octane number and cetane number test method and cetane index calculation method”.
  • the density at 15 ° C. of the cracked and reformed gasoline base material according to the present invention is 0.8 g / cm 3 or more and 0.95 g / cm 3 or less.
  • the density at 15 ° C. is a value measured according to JIS K2249 “Crude oil and petroleum products—density test method and density / mass / capacity conversion table”.
  • the cracked and reformed gasoline base is 1 to 40% by volume based on the total amount of gasoline composition
  • the catalytic cracked gasoline base is 10 to 90% by volume based on the total amount of gasoline composition
  • carbon The hydrocarbon base material of Formula 4 is blended in an amount of 0.1 to 10% by volume based on the total amount of the gasoline composition.
  • catalytic cracking gasoline full range cracking gasoline obtained by the catalytic cracking method, light fraction of catalytic cracking gasoline (light catalytic cracking gasoline), medium fraction of catalytic cracking gasoline (medium cracking gasoline) ), Heavy fraction of catalytic cracking gasoline (heavy cracking gasoline), and hydrocarbon base having 4 carbon atoms
  • butane obtained from crude oil distillation equipment, naphtha reforming equipment, alkylation equipment, etc.
  • straight-cut butane fraction centered on methane straight-run desulfurized butane fraction centered on butane desulfurized from them, cracked butane fraction centered on butane / butene obtained from catalytic cracking equipment, etc.
  • it is a base material containing normal butane, isobutane, 1 butene, 2 butene, iso-2-butene, butadiene and butyne.
  • the cracked and reformed gasoline base is 1 on the basis of the total amount of the gasoline composition.
  • light catalytic cracking gasoline base is 25-50% by volume based on total gasoline composition
  • catalytic cracking gasoline base containing the above light catalytic cracking gasoline base is 25-90% based on total gasoline composition %
  • a hydrocarbon base having 4 carbon atoms is blended in an amount of 0.1 to 10% by volume based on the total amount of gasoline composition.
  • the light catalytic cracking gasoline base material is a base material obtained by distilling and separating a light fraction in the catalytic cracking gasoline obtained by the catalytic cracking method, and is sometimes referred to as light cracked gasoline.
  • An example of the distillation range is a fraction at 20 to 120 ° C.
  • the above-mentioned catalytic cracking gasoline base containing 25 to 90% by volume including the light catalytic cracking gasoline base includes 25 to 50% by volume of the light catalytic cracking gasoline base based on the total amount of the gasoline composition.
  • catalytically cracked gasoline base material containing 0 to 65% by volume (totally 25 to 90% by volume as a catalytically cracked gasoline base material) of the catalytically cracked gasoline base material other than the material based on the total amount of the gasoline composition.
  • gasoline bases are blended.
  • propane fractions mainly composed of propane obtained from crude oil distillation equipment, naphtha reforming equipment, alkylation equipment, etc.
  • straight-run desulfurization propane fractions obtained by desulfurizing them are not particularly limited, but specifically, for example, straight-run propane fractions mainly composed of propane obtained from crude oil distillation equipment, naphtha reforming equipment, alkylation equipment, etc., straight-run desulfurization propane fractions obtained by desulfurizing them.
  • Propane / propylene cracked propane fraction obtained from catalytic crackers naphtha fraction (full range naphtha) obtained by atmospheric distillation of crude oil, naphtha light fraction (light naphtha), naphtha Heavy fraction (heavy naphtha), desulfurized full range naphtha desulfurized full range naphtha, desulfurized light naphtha desulfurized light naphtha, desulfurized heavy desulfurized heavy naphtha
  • Alkaline obtained by adding (alkylating) lower olefins to hydrocarbons such as isomerized gasoline and isobutane obtained by converting fusa and light naphtha into isoparaffin using an isomerizer, modified by catalytic reforming method Quality raffinate, a residue of aromatics extracted from reformed gasoline, light fraction of reformed gasoline (light reformed gasoline), medium heavy fraction of reformed gasoline (medium heavy reformed gasoline) FT (Fischer-Tropsch) after
  • a regular gasoline composition having a research octane number (RON) of 89 or more and less than 96 and a premium gasoline composition having a research method octane number (RON) of 96 or more and less than 105 can be produced.
  • the research octane number (RON) of the gasoline composition used in the premium gasoline specification vehicle is required to be 96 or more from the viewpoint of preventing knocking and improving the acceleration performance and driving performance, and is 98 or more. It is preferable.
  • it is less than 105.
  • the motor octane number (MON) is preferably 85 or more from the viewpoint of improving the anti-knocking performance during high-speed traveling.
  • the research method octane number (RON) of the gasoline composition used in the regular gasoline specification vehicle is required to be 89 or more and 90 or more from the viewpoint of preventing knocking and improving acceleration performance and driving performance. It is preferable.
  • the motor octane number (MON) is preferably 80 or more from the viewpoint of improving the anti-knocking performance during high-speed traveling.
  • the research method octane number and the motor method octane number referred to in the present invention mean the research method octane number and the motor method octane number measured by JIS K2280 “Octane number and cetane number test method”, respectively.
  • the density at 15 ° C. of a fraction having a boiling point range of 100 to 150 ° C. is preferably 0.730 g / cm 3 or more, It is preferably 0.860 g / cm 3 or less.
  • the density at 15 °C gasoline compositions of the present invention (the density of the overall composition) is preferably 0.783g / cm 3 or less, 0.765 g / cm 3 or less is more preferable.
  • the lower limit is preferably 0.710 g / cm 3 or more. If the density of the gasoline is less than 0.710 g / cm 3 , the fuel efficiency may be deteriorated.
  • the density as used in the field of this invention means the density measured by JISK2249 "The density test method and density / mass / capacity conversion table of crude oil and petroleum products".
  • the sulfur content of the gasoline composition of the present invention is preferably 10 mass ppm or less, and more preferably 8 mass ppm or less. If the sulfur content exceeds 10 ppm by mass, the performance of the exhaust gas treatment catalyst may be adversely affected, and the concentration of NOx, CO, and HC in the exhaust gas may increase, and the amount of benzene emitted is also high. May increase.
  • the sulfur content in the present invention means the sulfur content measured by JIS K2541 “Crude oil and petroleum products—Sulfur content test method”.
  • the total aromatic content in the gasoline composition is preferably 45% by volume or less, and more preferably 44% by volume or less.
  • the total aromatic content in the gasoline composition is preferably 35% by volume or less.
  • the aromatic component contained in the gasoline composition of the present invention includes, for example, benzene having 6 carbon atoms, toluene having 7 carbon atoms, xylene and ethylbenzene having 8 carbon atoms, and 1,2 having 9 carbon atoms. , 4-trimethylbenzene, 1-methyl-3-ethylbenzene and the like, and C10-containing 1,3-diethylbenzene and the like are included.
  • the aromatic content derived from the cracked and reformed gasoline base relative to the total aromatic content in the gasoline composition satisfies the following formula (1).
  • aromatic content derived from cracked and reformed gasoline base material and “content of total aromatic content in gasoline composition” are based on JIS K2536 “Petroleum products-component test method”. Means the aromatic content (unit: volume%) derived from the cracked and reformed gasoline base material and the total aromatic content (unit: volume%) in the gasoline composition. 0.1 ⁇ A / B ⁇ 1.0 (1) (In the formula, A represents the content (volume%) of the aromatic component derived from the cracked and reformed gasoline base material, and B represents the content (volume%) of the total aromatic content in the gasoline composition.)
  • the content of aromatics derived from cracked and reformed gasoline base relative to the content of total aromatics in the gasoline composition represented by the above formula (1) is more preferably 0.2 or more, and further preferably 0.3 or more.
  • the aromatic content of the gasoline composition of the present invention if the content of the aromatic component derived from the cracked and reformed gasoline base relative to the total aromatic content in the gasoline composition satisfies the above formula (1), the aromatic content
  • the breakdown is not particularly limited, but when the gasoline composition according to the present invention is a premium gasoline composition, the proportion of aromatic hydrocarbons having 9 or more carbon atoms in the gasoline composition is 30% by volume or less with respect to the total amount of gasoline. It is preferably 25% by volume or less. Further, when the gasoline composition according to the present invention is a regular gasoline composition, the proportion of aromatic hydrocarbons having 9 or more carbon atoms in the gasoline composition is preferably 20% by volume or less with respect to the total amount of gasoline. More preferably, it is not more than 15% by volume, and still more preferably not more than 15% by volume.
  • Benzene content in the gasoline composition of the present invention is preferably 1% by volume or less, and more preferably 0.5% by volume or less.
  • the benzene content referred to in the present invention means a value measured by JIS K2536 “Petroleum product-component test method”.
  • the content of olefin in the gasoline composition of the present invention is preferably 30% by volume or less, and more preferably 25% by volume or less.
  • the olefin content referred to in the present invention means the content (volume%) of the olefin content in the gasoline composition measured in accordance with JIS K2536 “Petroleum product-component test method”.
  • the 10% by volume distillation temperature (T10) is preferably 70 ° C. or lower, more preferably 65 ° C. or lower.
  • T10 exceeds 70 ° C., there is a possibility that a problem occurs in the low-temperature startability.
  • T10 is preferably 35 ° C. or higher. If T10 is less than 35 ° C., hydrocarbons in the exhaust gas may increase, and vapor lock may cause a problem in high-temperature operability.
  • the 50 volume% distillation temperature (T50) of the gasoline composition of the present invention is preferably 110 ° C. or lower from the viewpoint of improving acceleration and suppressing increase in hydrocarbons (HC) in the exhaust gas. ° C or lower is more preferable, 100 ° C or lower is further preferable, and 90 ° C or lower is most preferable. T50 is preferably 75 ° C. or higher from the viewpoint of preventing deterioration of fuel consumption.
  • the 90 volume% distillation temperature (T90) of the gasoline composition of the present invention prevents malfunctions in low-temperature operability during cold operation, suppresses increase in hydrocarbons in exhaust gas, and increases dilution of engine oil with gasoline.
  • the temperature is preferably 180 ° C or lower, and 170 ° C or lower. Is more preferable.
  • T90 is preferably 115 ° C. or higher from the viewpoint of preventing deterioration of fuel consumption.
  • the distillation end point (EP) of the gasoline composition of the present invention is preferably 220 ° C. or less, preferably from 220 ° C. or less, from the viewpoints of suppressing an increase in intake valve deposits and combustion chamber deposits and preventing plug smoldering. Is more preferably 210 ° C. or less, and particularly preferably 200 ° C. or less.
  • the 70 ° C. distillate (E70) of the gasoline composition of the present invention is preferably 45% by volume or less from the viewpoint of improving acceleration and suppressing increase in hydrocarbons (HC) in the exhaust gas, and is 40 volumes. % Or less is more preferable. Moreover, it is preferable that E70 is 25 volume% or more from a viewpoint of preventing a fuel consumption deterioration.
  • T10, T50, T90, EP and E70 in the present invention mean T10, T50, T90, EP and E70 measured by JIS K2254 “Petroleum product-distillation test method”, respectively.
  • the content of dienes is preferably 0.1% by volume or less based on the total amount of the composition from the viewpoint of ensuring the storage stability of the gasoline composition. It is more preferably at most 05% by volume, still more preferably at most 0.01% by volume.
  • the manganese content is preferably 2 mass ppm or less
  • the iron content is preferably 2 mass ppm or less
  • the sodium content is 2 mass ppm or less.
  • the potassium content is preferably 2 mass ppm or less
  • the phosphorus content is preferably 2 mass ppm or less. If these metal components exceed the upper limit, the efficiency of the exhaust gas purification system may be reduced due to an increase in the amount accumulated on the exhaust gas purification catalyst, deterioration of the catalyst carrier, deterioration of the air-fuel ratio sensor, or the like.
  • the contents of manganese, iron, and sodium are “combustion ashing—inductively coupled plasma emission method”
  • the potassium content is “combustion ashing—atomic absorption method”
  • the phosphorus content is ASTM D3231 “Standard”. It means the value measured by “Test Method for Phosphorus in Gasoline”.
  • combustion ashing-inductively coupled plasma emission method and “combustion ashing-atomic absorption method” can be measured according to the procedures shown in the following (i) to (vi).
  • (I) A 20 g sample is taken on a platinum dish.
  • (Ii) 0.4 g of powdered sulfur is added to suppress the volatilization of the component elements, and the volatile matter is removed at 150 ° C. for 1 hour on a sand bath.
  • Ashing in an electric furnace at 500 ° C. for 2 to 3 hours.
  • V Dissolve in 2 to 3 mL of concentrated sulfuric acid and make up to 20 mL.
  • the lead vapor pressure (RVP) of the gasoline composition of the present invention needs to be adjusted depending on the season and region in which the gasoline is used. However, in general, the summer ( In the period from May to September, it is desirable to adjust to 44 to 65 kPa, more preferably 50 to 65 kPa, and most preferably 55 to 65 kPa. On the other hand, in the winter season (October to April), it is desirable to adjust to 65 to 93 kPa, more preferably 70 to 93 kPa, and most preferably 70 to 90 kPa.
  • the reed vapor pressure in the present invention means a reed vapor pressure (RVP) measured by JIS K2258 “Crude oil and fuel oil vapor pressure test method (reed method)”.
  • the oxidation stability of the gasoline composition of the present invention is preferably 240 minutes or more, more preferably 480 minutes or more, and most preferably 900 minutes or more. If the oxidative stability is less than 240 minutes, gums can form during storage.
  • the oxidation stability as used in the field of this invention means the value measured by JIS K2287 "gasoline oxidation stability test method (induction period method)".
  • the copper plate corrosion (50 ° C., 3 h) of the gasoline composition of the invention is preferably 1 or less, more preferably 1a. If the copper plate corrosion exceeds 1, the fuel system conduit may corrode.
  • the copper plate corrosion referred to in the present invention means a value measured according to JIS K2513 “Petroleum products—copper plate corrosion test method” (test temperature 50 ° C., test time 3 hours).
  • the unwashed actual gum content of the gasoline composition of the present invention is preferably 20 mg / 100 mL or less, and more preferably 18 mg / 100 mL or less. Moreover, it is preferable that it is 5 mg / 100 mL or less, it is more preferable that it is 2 mg / 100 mL or less, and it is still more preferable that it is less than 1 mg / 100 mL.
  • the unwashed actual gum amount and the washed actual gum amount in the present invention mean values measured by JIS K2261 “Petroleum products—automobile gasoline and aviation fuel oil—existing gum test method—injection evaporation method”.
  • the amount of kerosene mixed in the gasoline composition of the present invention is preferably 4% by volume or less, and more preferably 1% by volume or less.
  • the amount of kerosene mixed in the present invention means a value measured by JIS K2536 “Petroleum product-component test method”.
  • an oxygen-containing compound may be further blended as necessary in addition to the oxygen-containing compound that can be inherently contained in a gasoline base material.
  • the oxygen-containing compound to be blended include alcohols having 2 to 4 carbon atoms and ethers having 4 to 8 carbon atoms.
  • Specific examples of the oxygen-containing compound include ethanol, methyl-tert-butyl ether (MTBE), ethyl-tert-butyl ether (ETBE), tert-amyl methyl ether (TAME), and tert-amyl ethyl ether.
  • Methanol is not preferable because the aldehyde concentration in the exhaust gas may be high and corrosive.
  • the content of the oxygen-containing compound in the gasoline composition of the present invention is preferably 5.0% by mass or less, more preferably 3.0% by mass or less, most preferably in terms of oxygen element, based on the total amount of the composition. Preferably it is 2.0 mass% or less. When it exceeds 5.0 mass%, NOx in exhaust gas may increase.
  • the content of oxygen-containing compounds referred to here is the sum of the contents of oxygen-containing compounds that can be inherently contained in gasoline base materials and the like, and the contents of the oxygen-containing compounds added as additives. means.
  • an antioxidant in order to improve the oxidation stability.
  • the antioxidant include N, N′-diisopropyl-p-phenylenediamine, N, N′-diisobutyl-p-phenylenediamine, 2,6-di-t-butyl-4-methylphenol, Known compounds such as hindered phenols can be used as gasoline antioxidants.
  • a metal deactivator examples include amine carbonyl condensed compounds such as N, N′-disalicylidene-1,2-diaminopropane.
  • the compounding amount of the metal deactivator is preferably 0 to 100 g / kL, more preferably 0 to 10 g / kL based on the total amount of the gasoline composition.
  • the effect of preventing the intake valve deposit and the effect of reducing the combustion chamber deposit can be improved.
  • the cleaning dispersant include gasoline cleaning dispersants such as succinimide, polyalkylamine, and polyetheramine. Among these, those having no residue when thermally decomposing at 300 ° C. in air are preferable, and polyisobutenylamine and / or polyetheramine are particularly preferable.
  • the content of the cleaning dispersant is preferably 80 to 500 mg / L based on the total amount of the composition. 100 to 450 mg / L is more preferable, and 200 to 300 mg / L is more preferable from the viewpoint of preventing the intake valve deposit and further reducing the combustion chamber deposit.
  • a surface ignition preventing agent such as an organic phosphorus compound; an anti-icing agent such as a polyhydric alcohol or an ether thereof; an alkali metal salt or an alkaline earth metal salt of an organic acid; Ancillary surfactants; cationic surfactants; antistatic agents such as amphoteric surfactants; colorants such as azo dyes; organic carboxylic acids or their derivatives; alkenyl succinic acid Rust preventive agents such as esters; draining agents such as sorbitan esters; discriminating agents such as kilyzanine and coumarin; and odorants such as natural essential oil synthetic fragrances may be blended as necessary.
  • These additives can be added singly or in combination of two or more. The total content of these additives is preferably 0.1% by mass or less based on the total amount of the composition.
  • gasoline base material As base materials for preparing gasoline compositions, butane, light cracked gasoline, medium cracked gasoline, heavy cracked gasoline, full range cracked gasoline, light straight run gasoline, heavy straight run gasoline, medium reformed gasoline, heavy Quality reformed gasoline and cracked reformed gasoline base material were prepared. The properties of each substrate are shown in Tables 1 and 2.
  • the cracking reformed gasoline base material shown in Table 2 is a base material obtained by the following method.
  • Fluid catalytic cracking light oil LCO (10 vol% distillation temperature is 215 ° C, 90 vol% distillation temperature is 318 ° C, density at 15 ° C is 0.9258 g / cm 3 , saturation is 23 vol%, olefin content is 2 vol %, Total aromatic content is 75 vol%)
  • reaction pressure 0.3 MPaG
  • contact time between LCO and catalyst is 60 seconds in a fluidized bed reactor.
  • the catalyst was brought into contact with and reacted with a catalyst for use (MFI type zeolite carrying 0.2% by mass of gallium and 0.7% by mass of phosphorus and containing a binder) to carry out a decomposition and reforming reaction. Subsequently, the cracking and reforming reaction product was fractionated to produce cracking and reforming gasoline base materials having the properties shown in Table 2.
  • a catalyst for use MFI type zeolite carrying 0.2% by mass of gallium and 0.7% by mass of phosphorus and containing a binder
  • Examples 1 to 5 and Comparative Examples 1 and 3 gasoline compositions having the properties shown in Table 3 were prepared using the base materials shown in Tables 1 and 2, respectively.
  • gasoline composition of Comparative Example 2 commercially available regular gasoline was prepared.
  • the property measurement of the gasoline base material and the gasoline composition was performed based on the above-described test method and measurement method.
  • Example 6 to 10 Comparative Examples 4 to 6
  • gasoline compositions having the properties shown in Table 4 were prepared using the base materials shown in Tables 1 and 2, respectively.
  • gasoline composition of Comparative Example 5 commercially available high-octane gasoline was prepared.
  • Comparative Example 1 commercially available regular gasoline (Comparative Example 2)
  • Comparative Example 3 commercially available high-octane gasoline (Comparative Example 5)
  • Comparative Example 6 are gasoline compositions whose combustion chamber deposits and exhaust gases are examples. It is getting worse or it is out of the standard of automobile gasoline specified in JIS K2202.
  • the method of the present invention makes it possible to produce a gasoline composition that enables reduction of combustion chamber deposits and reduction of discharged carbon dioxide while maintaining the octane number and distillation properties, which is extremely useful industrially.

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

L'invention concerne un procédé de fabrication d'une composition d'essence ayant une performance de faible émission de gaz d'échappement (NOx) et une faible incidence de dépôt sur la chambre de combustion sans aucun changement dans l'indice d'octane ou les caractéristiques de distillation. Ce procédé de fabrication d'une composition d'essence est caractérisé en ce que 1 à 40 % en volume d'une matière de base d'essence modifiée par pyrolyse, ayant les propriétés (1) à (7), 10 à 90 % en volume d'une matière de base d'essence de craquage catalytique et 0,1 à 10 % en volume d'une matière de base d'hydrocarbure en C4 sont combinés au minimum. (1) La fraction aromatique est de 90 % en volume ou plus ; (2) la fraction oléfinique est de 5 % en volume ou moins ; (3) la fraction aromatique en C8 est de 5 à 50 % en volume ; (4) la fraction aromatique ayant au moins 9 atomes de carbone est de 30 % en volume ou moins ; (5) la teneur en soufre est de 20 ppm en masse ou moins ; (6) l'indice d'octane recherché est de 110 ou plus ; et (7) la masse volumique à 15°C est de 0,8 à 0,95 g/cm3.
PCT/JP2012/062310 2011-05-26 2012-05-14 Composition d'essence et son procédé de fabrication WO2012161017A1 (fr)

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Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2982734A1 (fr) 2014-08-01 2016-02-10 Ekobenz So. z o. o. Mélange de carburant, en particulier pour des moteurs à allumage par étincelle
WO2018106397A1 (fr) * 2016-12-07 2018-06-14 Exxonmobil Research And Engineering Company Conversion combinée d'oléfines et de composés oxygénés pour la production d'aromatiques
US10590353B2 (en) 2016-12-07 2020-03-17 Exxonmobil Research And Engineering Company Integrated oxygenate conversion and olefin oligomerization

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JP2004124056A (ja) * 2002-08-05 2004-04-22 Idemitsu Kosan Co Ltd 無鉛ガソリン及び無鉛ガソリンに使用するガソリン基材
JP2009227693A (ja) * 2008-03-19 2009-10-08 Cosmo Oil Co Ltd ガソリン組成物
JP2010116469A (ja) * 2008-11-12 2010-05-27 Japan Energy Corp ガソリン組成物
JP2010235694A (ja) * 2009-03-30 2010-10-21 Jx Nippon Oil & Energy Corp 筒内直接噴射式ガソリンエンジン用無鉛ガソリン組成物
JP2010275486A (ja) * 2009-05-29 2010-12-09 Idemitsu Kosan Co Ltd ガソリン組成物

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2004124056A (ja) * 2002-08-05 2004-04-22 Idemitsu Kosan Co Ltd 無鉛ガソリン及び無鉛ガソリンに使用するガソリン基材
JP2009227693A (ja) * 2008-03-19 2009-10-08 Cosmo Oil Co Ltd ガソリン組成物
JP2010116469A (ja) * 2008-11-12 2010-05-27 Japan Energy Corp ガソリン組成物
JP2010235694A (ja) * 2009-03-30 2010-10-21 Jx Nippon Oil & Energy Corp 筒内直接噴射式ガソリンエンジン用無鉛ガソリン組成物
JP2010275486A (ja) * 2009-05-29 2010-12-09 Idemitsu Kosan Co Ltd ガソリン組成物

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2982734A1 (fr) 2014-08-01 2016-02-10 Ekobenz So. z o. o. Mélange de carburant, en particulier pour des moteurs à allumage par étincelle
WO2018106397A1 (fr) * 2016-12-07 2018-06-14 Exxonmobil Research And Engineering Company Conversion combinée d'oléfines et de composés oxygénés pour la production d'aromatiques
US10590353B2 (en) 2016-12-07 2020-03-17 Exxonmobil Research And Engineering Company Integrated oxygenate conversion and olefin oligomerization

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