WO2005044959A1 - Composition d'essence sans plomb et procede de production associe - Google Patents

Composition d'essence sans plomb et procede de production associe Download PDF

Info

Publication number
WO2005044959A1
WO2005044959A1 PCT/JP2004/016115 JP2004016115W WO2005044959A1 WO 2005044959 A1 WO2005044959 A1 WO 2005044959A1 JP 2004016115 W JP2004016115 W JP 2004016115W WO 2005044959 A1 WO2005044959 A1 WO 2005044959A1
Authority
WO
WIPO (PCT)
Prior art keywords
gasoline
naphtha fraction
volume
sulfur
gen
Prior art date
Application number
PCT/JP2004/016115
Other languages
English (en)
Japanese (ja)
Inventor
Yasuhiro Araki
Katsuaki Ishida
Original Assignee
Japan Energy Corporation
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Japan Energy Corporation filed Critical Japan Energy Corporation
Priority to KR1020067010974A priority Critical patent/KR101114742B1/ko
Priority to US10/577,951 priority patent/US20070068849A1/en
Priority to EP04793223A priority patent/EP1686166A4/fr
Priority to CA2543953A priority patent/CA2543953C/fr
Priority to JP2005515277A priority patent/JP4932257B2/ja
Publication of WO2005044959A1 publication Critical patent/WO2005044959A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • 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
    • C10G29/00—Refining of hydrocarbon oils, in the absence of hydrogen, with other chemicals
    • C10G29/04—Metals, or metals deposited on a carrier
    • 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
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
    • 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
    • C10G2300/20—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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline

Definitions

  • the present invention relates to a lead-free gasoline composition with reduced impact on the environment and a method for producing the same.
  • the present invention relates to a lead-free gasoline composition having a sulfur content reduced to 1 ppm by mass or less and ensuring sufficient operation characteristics while considering the effect on the environment, and a method for producing the same.
  • JIS K 2202 stipulates car gasoline No. 1 with a research octane number (RON) of 96.0 or more and gasoline No. 2 with a gasoline of 89.0 or more.
  • the former is a high-performance premium gasoline, and the latter is gasoline.
  • premium gasoline has been used in catalytic reforming gasoline bases, bases with more than 100 RON, such as methyl tbutyl ether (MTBE), alkylate gasoline bases, and catalytic cracking gasoline bases, with more than 93 RONs.
  • the sulfur content of the cracked gasoline base material can be easily reduced by a known technique of hydrorefining in the presence of high-pressure hydrogen and a catalyst.
  • the catalytic cracking gasoline base material contains a large amount, and the high RON containing olefins are hydrogenated and the RON of the base material is reduced. If you can't get rid of the problem, you'll need to clarify the problem.
  • Patent Document 1 Japanese Patent Application Laid-Open No. 2003-277768
  • An environmentally friendly gasoline with a low sulfur content of 1 mass ppm or less and sufficient practical performance, and a method for producing the same have not yet been established.
  • An object of the present invention is to provide a lead-free gasoline composition that reduces sulfur content and ensures sufficient operating characteristics under such circumstances, and a method for producing the same.
  • the inventors of the present invention have conducted intensive studies in order to solve the above-mentioned problems. As a result, when a desulfurization treatment other than hydrorefining is performed using a low-V ⁇ cracked naphtha fraction, a high ⁇ content is obtained. It has been found that sulfur content can be reduced efficiently while maintaining the above, and that a lead-free gasoline composition with sufficient operating characteristics can be obtained by using the base material thus obtained.
  • a lead-free gasoline composition of the present invention and a method for producing the same have been conceived.
  • the method for producing a lead-free gasoline composition having a sulfur content of 1 mass ppm or less and a research octane number (RON) of 89.0 or more comprises:
  • a decomposed naphtha fraction having a Gen value of 0.3 gZlOOg or less, which has been subjected to a Gen reduction treatment in advance is used. That is, it is preferable that the method for producing a lead-free gasoline composition of the present invention includes a step of subjecting a crude oil of a cracked naphtha fraction to a Gen reduction treatment in advance. At this time, it is preferable to contact the feedstock oil of the cracked naphtha fraction with a catalyst containing an element of Group 8 of the periodic table. At least selected: preferably containing L species.
  • a porous desulfurizing agent having a sulfur sorption function is decomposed in the presence of hydrogen having a hydrogen partial pressure of IMPa or less.
  • desulfurization treatment is preferably performed by contacting with a sulfur fraction, and the porous desulfurizing agent preferably contains at least one selected from copper, zinc, nickel and iron.
  • blending step (2) it is preferred to mix a 10 90 Capacity 0/0 desulfurizing cracked naphtha fraction and 90- 10 capacity% other gasoline components.
  • the method for producing a lead-free gasoline composition of the present invention has a high octane number, for example, a research-method octane number of 93.0 or more, particularly 96.0 or more.
  • Light naphtha has a 5% by volume distillation temperature of 25-43 ° C, a 95% by volume distillation temperature of 55-100 ° C, an olefin component of 5% by volume or more, and a Gen value of 0.3gZl00g or less.
  • the fraction is preferably used in the desulfurization step (1).
  • Such a light cracked naphtha fraction may be obtained by subjecting the cracked naphtha fraction to a feedstock oil after the gen reduction treatment and then fractionating the crude cracked naphtha fraction, or may be a fractionated fraction of the cracked naphtha fraction. It may be obtained by performing a Gen reduction process later, or by performing a fractionation and a Gen reduction process simultaneously.
  • the raw material oil of the cracked naphtha fraction or the raw oil of the cracked naphtha fraction that has been subjected to the gen reduction treatment is used to reduce the sulfur compounds contained therein. It is preferable to perform a pretreatment for increasing the molecular weight, so that the sulfur content in the light cracked naphtha fraction can be easily reduced.
  • a preferable method for producing the unleaded gasoline composition of the present invention is such a light cracked naphtha. After the fraction is desulfurized in the step (1), in the blending step (2), the light desulfurized cracked naphtha fraction of 10 to 60% by volume and another gasoline base material of 90 to 40% by volume are mixed. Is a method for producing unleaded gasoline compositions with a octane number of 93.0 or higher.
  • the unleaded gasoline composition according to the present invention has a research octane number of 89.0 or more, a 50% by volume distillation temperature of 105 ° C. or less, an olefin content of 10% by volume or more, a total sulfur content of 1 mass ppm or less, and The ratio of thiophene sulfur compounds to the total sulfur content is 50% by mass or more as the sulfur content.
  • the unleaded gasoline composition of the present invention has a research octane number of 93.0 or more. More preferably, the olefin content in the boiling range of 35-100 ° C in the total olefin content is 90% by volume or more, and the total amount of thiophene and 2-methylthiophene in the total sulfur content is 50% by mass or more as the sulfur content. , And the content of Z or thiols is 0.1 mass ppm or less as sulfur content.
  • cracked naphtha fractions such as catalytic cracked gasoline and various cracked gasolines, inevitably contain genes.
  • the gens preferentially adsorb to the porous desulfurization agent in the treatment with the porous desulfurization agent, and the function of adsorbing (sorbing) sulfur is hindered.
  • the present invention since a process for reducing the Gen is performed in advance and the Gen value is limited to 0.3 gZ100 g or less, a high sulfur sorption function can be maintained for a long time.
  • the desulfurization cracked naphtha fraction obtained by treating with a porous desulfurizing agent having a sulfur sorption function in the presence of a small amount of hydrogen and a sulfur content of 10 mass ppm or less By mixing with another gasoline base material, it becomes possible to produce a lead-free gasoline composition having a sulfur content of 1 mass ppm or less. It is also possible to remove thiophene-sulfur disulfides in cracked naphtha fractions such as catalytic cracked gasoline, so desulfurization of light cracked naphtha fractions such as cracked naphtha fractions rich in thiophene-sulfur compounds is also possible. Is possible.
  • the power of the unleaded gasoline composition obtained in the past is almost the same as other properties. It is possible to reduce only the sulfur content to less than 1 ppm by mass with little change.
  • the present invention provides a desulfurization step of desulfurizing a cracked naphtha fraction having a specific property, and a blending step of mixing the obtained desulfurized cracked naphtha fraction with another gasoline base material.
  • This is a method for producing a lead-free gasoline composition with a octane number of 19.0 ppm or less and a research octane number of 89.0 or more.
  • FCC gasoline fluid catalytic cracking gasoline
  • Processes such as petroleum refining and petrochemicals, products that can obtain equipment power, and intermediate products, for example, thermal decomposition naphtha that also generates pyrolysis equipment power, dewaxing equipment power that generates dewaxing naphtha, and naphtha cracker power that generates cracking naphtha Can be used as a cracked naphtha fraction.
  • the 5% by volume distillation temperature of these cracked naphtha fractions is preferably 25 to 130 ° C, and the 95% by volume distillation temperature is preferably 55 to 210 ° C.
  • a cracked naphtha fraction such as FCC gasoline is subjected in advance to a gen reduction treatment to obtain a cracked naphtha fraction having a gen value of 0.3 gZl00 g or less. It is even more preferred that the Gen value be less than O.lgZlOOg. If the gender value exceeds 0.3 g / 100 g, the desulfurization performance of the porous desulfurizing agent having a sulfur sorption function used in the subsequent desulfurization step will be reduced, and it will be particularly difficult to desulfurize thiophene sulfur conjugates.
  • the decrease in the desulfurization performance can be known from the decrease in the desulfurization rate in the unit treatment amount or the increase in the frequency of regeneration of the porous desulfurization agent for maintaining the predetermined desulfurization rate. Therefore, it is preferable to perform a pre-treatment for reducing the amount of the jenny-dangling product and provide it to the subsequent desulfurization step. Good.
  • this jen reduction treatment step if the olefin is hydrogenated and converted into paraffin, the octane number is greatly reduced. Therefore, it is preferable to perform a selective gen reduction treatment so that the olefin is not hydrogenated.
  • Gen value here is a value measured by UOP326-82.
  • the sulfur content can be reduced at the same time by selecting the catalyst and conditions to be used. By doing so, it is possible to extend the life of the porous desulfurizing agent having a sorption function.
  • a gen-reducing catalyst is contacted with a catalytic cracking naphtha fraction in the presence of hydrogen to convert gen to monoolefin or to react sulfide with a sulfur compound coexisting to form sulfide.
  • U ⁇ is preferred.
  • a catalyst in which at least one metal belonging to Group 8 of the periodic table is supported on an inorganic porous carrier such as alumina is preferably used.
  • catalysts containing nickel or cobalt that are resistant to feedstocks containing sulfur are even more preferred.
  • reaction conditions must be set so that the Gen value in the catalytically-decomposed naphtha fraction is 0.3 gZlOOg or less and the olefin hydrogenation rate is 20% or less.
  • the hydrogenation rate of the olefin is the reduction rate of the olefin content after the treatment, assuming that the olefin content before the treatment is 100%.
  • Preferred reaction conditions for contacting in the coexistence are reaction temperature 40-300 ° C, reaction pressure 0.0-4.0MPa (gauge pressure), LHSV 1.0- / OIL ratio 1
  • One is 100NL / L.
  • the hydrogen in olefins is selectively hydrorefined, and the present invention can be applied as a method for reducing gen.
  • the IFP Selective Hydrogenation process and the Hules Selective Hydrogenation process are preferably used (see Petroleum Refining Process, edited by The Japan Petroleum Institute, p.62, Kodansha Sientifik, 1998).
  • catalytic cracking gasoline is typically used as a cracked naphtha fraction.
  • the process for producing this catalytic cracking gasoline can employ any known production process that does not particularly limit the catalytic cracking device, the feedstock, and the operating conditions.
  • the catalytic cracking unit uses catalysts such as amorphous silica alumina and zeolite to separate petroleum fractions from gas oil to vacuum gas oil, as well as direct gas oil obtained from heavy oil indirect desulfurization unit and direct oil desulphurization unit obtained from heavy oil direct desulfurization unit. This equipment obtains high octane gasoline base material by catalytic cracking of heavy oil, residual oil at normal pressure, etc.
  • UOP catalytic cracking For example, UOP catalytic cracking, flexicracking, ultra-ortho-flow, Texaco fluid catalytic cracking and other fluid catalytic cracking methods, RCC method, HOC method, etc.
  • a petroleum fraction from gas oil to reduced pressure gas oil particularly the sulfur content of 4000 mass ppm or less, is used as the feed oil for the catalytic cracking unit. It is preferable to use a fraction reduced to 2,000 mass ppm or less, 1000 mass ppm or less, and especially 500 mass ppm or less by hydrorefining or the like.
  • a cracked naphtha fraction having a Gen value of 0.3 g ZlOOg or less is desulfurized to obtain a desulfurized cracked naphtha fraction to be subjected to the next blending step.
  • the sulfur content of the desulfurized cracked naphtha fraction obtained in the desulfurization step is desirably desulfurized to 2 mass ppm or less, more preferably 1 mass ppm or less, and even more preferably 0.5 mass ppm or less.
  • the thiophene-based sulfur conjugate is the most likely to remain among the sulfur compounds, and thus the thiophene-based sulfur conjugate included in the total sulfur in the desulfurized cracked naphtha fraction.
  • the proportion of the substance is preferably 50% by mass or more, more preferably 70% by mass or more as a sulfur content.
  • the dithiophene sulfur compound means a sulfur-containing compound having a thiophene skeleton in a molecule such as thiophene, 2-methylthiophene, and 2,5-dimethylthiophene.
  • Orefuin content of desulfurized catalytically cracked gasoline is 5- 60 volume 0/0, and particularly preferably from 20- 40 volume%.
  • the desulfurization method in the desulfurization step is preferably a method in which a desulfurizing agent having a sorption function and a cracked naphtha fraction are brought into contact in the presence of hydrogen.
  • a desulfurizing agent having a sorption function and a cracked naphtha fraction are brought into contact in the presence of hydrogen.
  • the RON of the gasoline base material obtained by hydrogenation of olefins is reduced, and the RON is formed again immediately after hydrodesulfurization.
  • Hydrogen sulfate reacts with olefin to easily regenerate thiols, which is not suitable because V ⁇ cannot be sufficiently desulfurized.
  • It is preferable to use a desulfurizing agent having a sorption function since sulfur removed from the organic sulfur compound is immobilized on the desulfurizing agent and does not react with olefin to regenerate thiols.
  • the desulfurizing agent is not particularly limited as long as it has a sorbing function for the sulfur-containing compound.
  • a porous desulfurizing agent containing at least one selected from copper, zinc, nickel and iron is preferably used.
  • Preferred desulfurizing agents contain 0.5 to 85% by weight, especially 118 to 80% by weight of a metal component such as copper.
  • the production method of the desulfurizing agent is not particularly limited, but a production method in which a porous carrier such as alumina is impregnated with a metal component such as copper and supported and fired, or a metal component such as copper and a component such as aluminum are coprecipitated. Is preferable as a production method of precipitating and subjecting to steps such as molding and baking. Further, the metal component may be further impregnated and supported on the shaped and fired desulfurizing agent and fired. As the desulfurizing agent, the fired one may be used as it is, or may be used after being treated in a hydrogen atmosphere.
  • the specific surface area of the desulfurizing agent is preferably 30 m 2 Zg or more, particularly 50 to 600 m 2 Zg.
  • the composition and production method of the desulfurizing agent are not particularly limited, but desulfurizing agents such as those disclosed in Japanese Patent Nos. 3324746, 3230864 and JP-A-11-61154 are preferred. Can be
  • the porous desulfurizing agent having a sulfur sorbing function of the present invention refers to a method of immobilizing a sulfur atom in an organic sulfur compound to a desulfurizing agent, and a method of removing a hydrocarbon residue other than a sulfur atom in the organic sulfur compound.
  • a porous desulfurizing agent having a function of releasing from a desulfurizing agent by cleavage of a carbon-sulfur bond in the organic sulfur conjugate is used.
  • hydrogen existing in the system is added to the carbon in which the bond with sulfur has been cleaved.
  • hydrocarbon compounds from which sulfur atoms have been removed are obtained as products. Will be done.
  • the hydrocarbon compound from which the sulfur atom has been removed may give a product that has undergone a reaction such as hydrogenation, isomerization, or decomposition.
  • sulfur is immobilized in the desulfurizing agent, so unlike sulfur refining, it does not generate sulfur sulfides such as hydrogen sulfide as products.
  • the desulfurization treatment may be performed by a notch type or a flow type. However, the desulfurization treatment may be performed by flowing the decomposed naphtha fraction through a fixed-bed desulfurization tower filled with a desulfurizing agent. This is preferable because the agent and the desulfurized cracked naphtha fraction obtained can be easily separated.
  • a force in a range of 0 to 400 ° C can be selected, and a force in a range of 20 to 380 ° C is preferably selected.
  • desulfurization treatment may be performed in the presence of hydrogen.
  • the hydrogen partial pressure is preferably less than IMPa, and more preferably less than 0.6 MPa, in order to avoid the olefin being hydrogenated and the RON of the resulting gasoline substrate being reduced.
  • the LHSV is preferably selected from the range of 0.01 to 100 hr- 1 .
  • the gasoline base material used has a high octane number.
  • a gasoline base material having a high octane number is also preferable for blending for producing regular gasoline in order to increase the flexibility of the blend.
  • the cracked naphtha fraction is further fractionated, and the light cracked naphtha fraction having a relatively high octane number is mixed with the above-mentioned gen reduction treatment and desulfurized product with another gasoline base material. Unleaded gasoline compositions can be produced.
  • the lightly decomposed naphtha fraction after the fractionation and the Gen reduction treatment has a 5% by volume distillation temperature of 25 to 43 ° C, a 95% by volume distillation temperature of 55 to 100 ° C, and an olefin component of 5%. It is preferable that the light cracked naphtha fraction, which preferably has a volume percentage of not less than 0.3 g and a value of not more than 0.3 g of Z00 g, is fractionated, even if it is obtained by fractionation after the treatment of reducing gen. It may be obtained by performing a Gen reduction process later, or may be obtained by performing a Gen reduction process and a fractionation simultaneously.
  • the catalytic cracking gasoline is fractionated to have a 5% by volume distillation temperature of 25.0 to 43.0 ° C and a 95% by volume distillation temperature of 55.0%.
  • the 5% by volume distilling temperature exceeds 43.0 ° C or the 95% by volume distilling temperature is less than 55.0 ° C, it becomes difficult to adjust the distillation properties of the unleaded gasoline composition, or in the fractionation process. The yield of the resulting catalytic cracked light gasoline is reduced, and the cost of unleaded gasoline compositions is increased.
  • the catalytic cracking light gasoline obtained in the fractionation step preferably contains 0.1 to 50 mass ppm of thiophene sulfur compounds as sulfur. Even more preferably, it is at most 20 ppm by mass, more preferably at most 10 ppm by mass. Since the thiophene sulfur ligated product is a sulfur ligated gasoline easily remaining in the desulfurized catalytically cracked light gasoline obtained in the desulfurization treatment in the subsequent step, the catalytically cracked light gasoline obtained in the fractionation process is used. If the thiophene sulfur conjugate having a sulfur content exceeding 50 ppm by mass is contained, the operation cycle of the desulfurizing agent in the desulfurization step is undesirably short. It is not preferable that the catalytically cracked light gasoline obtained in the fractionation step does not contain thiophene having a sulfur content of less than 0.1 ppm by mass, since the yield of the catalytically cracked light gasoline is reduced.
  • a catalytically cracked gasoline is fractionated in the fractionation step to obtain a lightly cracked naphtha fraction, naturally a relatively heavy cracked naphtha fraction is also produced.
  • the present invention does not exclude a heavy cracked naphtha fraction.
  • the 5% by volume distillation temperature is 25 ° C or more, preferably 25 to 130 ° C, and the 95% by volume distillation temperature is 210 ° C. Below, preferably 55-210 ° C, if the olefin content is 5% by mass or more and the Gen value is 0.3gZlOOg or less, the production of the unleaded gasoline composition of the present invention, particularly the gasoline composition having a relatively low octane number, is recommended.
  • catalytic cracking heavy gasoline has a higher sulfur content than catalytic cracking light gasoline.
  • the sulfur content in catalytic cracking heavy gasoline is 50 mass ppm or more, only gen is removed and hydrogen is removed in the presence of hydrogen.
  • Treatment with a sorbent desulfurizing agent significantly shortens the life of the desulfurizing agent.
  • catalytic cracking heavy gasoline has a relatively small amount of olefin, desulfurization can be performed without impairing octane number loss even in the case of hydrodesulfurization in the presence of high-pressure hydrogen, up to a sulfur content of about 5 ppm by mass. It is.
  • the sulfur content in catalytically cracked heavy gasoline is reduced to 20 mass ppm or less, preferably 10 mass pp while keeping the olefin hydrogenation rate at 20% or less, preferably 10% or less.
  • desulfurization is preferably carried out by treatment with a desulfurizing agent having a sorption function in the presence of hydrogen.
  • the amount of gen can be reduced simultaneously with desulfurization in hydrodesulfurization.
  • the thiophene sulfur compound having an alkyl group at the 2-position is the sulfur compound most likely to remain in the desulfurized catalytically cracked light gasoline obtained in the desulfurization step.
  • thiophenes which mainly contain thiophene, 2-methylthiophene, and 3-methylthiophene, are contained as thiophenes.
  • Metalthiophene is applicable. Therefore, it is preferable to reduce 2-methylthiophene in the fractionation step.
  • the 95% by volume distillation temperature during fractionation is preferably 100.0 ° C, particularly 85.0 ° C, and more preferably 75 ° C or less.
  • the sulfur-based compound is mainly chioffen. Therefore, if the 95% by volume distillation temperature during fractional distillation is 75 ° C or less, it is most likely to remain in the desulfurized catalytically cracked light gasoline obtained in the desulfurization process! /, And the sulfur compound is thiophene.
  • a method for increasing the molecular weight of the sulfur-containing compound a method of reacting the sulfur-containing compound and the olefins contained in the decomposed naphtha fraction is also suitably used. Specifically, a method of reacting thiols and olefins (see Japanese Patent Application Laid-Open No.
  • gasoline base materials to be mixed in the blending process include a catalytic reforming gasoline base material, an alkylate gasoline base material, a base material obtained by desulfurizing a straight-run naphtha, a isomeride gasoline base material, and a naphtha formed from a naphtha cracker.
  • Base material toluene, xylene and MTBE, ethyl t-butyl ether (ETBE), t-amyl ethyl ether (TAEE), ethanol, methanol, etc.
  • a known gasoline base material such as an oxygen-containing gasoline base material can be used.
  • the other gasoline base material mixed in the blending step has a sulfur content of 10 mass ppm or less, preferably 3 mass ppm or less, more preferably 1 mass ppm or less, and particularly preferably 0.5 mass ppm or less. If the sulfur content of another gasoline base exceeds 10 ppm by mass, the amount of the gasoline base in the blending step is undesirably limited.
  • Preferable blending amounts will be described for each research octane number.
  • the preferred compounding amount is 25-80% by volume, particularly 30-50% by volume of the desulfurized cracked naphtha fraction, and 25-50% by volume of the catalytic reforming gasoline base material. , especially 30 to 45 volume 0/0 of catalytically reformed gasoline, and 10 40 volume 0/0, especially from 15 30 volume 0/0.
  • the preferred compounding amount is 50-90% by volume, particularly 60-80% by volume of the desulfurized cracked naphtha fraction, and 5-35% by volume of the catalytic reforming gasoline base material. 10- 25 vol. 0/0 of catalytically reformed gasoline, and 10 25 volume 0/0, and particularly a 5-15 capacity%.
  • the preferred compounding amount is 55-90% by volume, particularly 65-85% by volume of the desulfurized cracked naphtha fraction, and 0-20% by volume of the catalytic reforming gasoline base material. 5-15% by volume, alkylate gasoline base material is 0-15% by volume, especially 0-10% by volume.
  • fuel oil additives known in the art can be added to the gasoline composition of the present invention as needed.
  • the amount of these additives can be appropriately selected. Usually, it is preferable to maintain the total amount of additives at 0.1% by mass or less.
  • fuel oil additives that can be used in the gasoline of the present invention include phenol-based and amine-based antioxidants, metal deactivators such as Schiff-type compounds and thioamide-type compounds, and organic phosphorus-based additives.
  • Surface ignition inhibitors such as compounds, detergents and dispersants such as succinimide, polyalkylamines and polyetheramines, antifreeze agents such as polyhydric alcohols or their ethers, alkali metal salts of organic acids or alkaline acids
  • Antistatic agents such as lithium earth metal salts, sulfuric esters of higher alcohols, etc., anionic surfactants, cationic surfactants, amphoteric surfactants, etc.
  • Coloring agents such as blocking agents and azo dyes can be mentioned.
  • the unleaded gasoline composition of the present invention has a research octane number of 89.0 or more, a 50% by volume distillation temperature of 105 ° C or less, an olefin content of 10% by volume or more, a total sulfur content of 1 mass ppm or less, and a total sulfur content of
  • the ratio of thiophene-based sulfur conjugates in the total is 50-100% by mass in terms of sulfur content.
  • the lower limit of the octane number of the research method is 93.0 or more, particularly 96.0 or more
  • the upper limit is usually 102.0 or less
  • the boiling point occupying 35 to 100 ° C in the total olefin content is 90% by volume or more
  • the total sulfur content is 90% or more.
  • the total weight of thiophene and 2-methylthiophene in sulfur is 50% by mass or more, more preferably 70% by mass or more, and the content of thiols is 0.1% by mass or less as sulfur.
  • the catalytic cracking gasoline A obtained by fluid catalytic cracking using the hydrorefining of the vacuum gas oil fraction of the crude oil as the main feed oil is passed through the oil to perform the gen reduction treatment to obtain catalytic cracking gasoline B.
  • a reaction tube was charged with 5 cm 3 of copper-zinc-aluminum composite oxide (copper content 35% by mass, zinc content 35% by mass, aluminum content 5% by mass) prepared by a coprecipitation method, and hydrogen gas was added thereto.
  • catalytic cracking gasoline B is passed through this reaction tube for 20 hours under the conditions of a reaction temperature of 100 ° C, a reaction pressure of normal pressure, and an LHSV of 2.0 hours—HZOil ratio of 0.06NLZL for 20 hours for sorption function.
  • Catalytically cracked gasoline C desulfurized with a desulfurizing agent having Table 1 shows the properties of catalytic cracking gasoline A, catalytic cracking gasoline B, and desulfurizing catalytic cracking gasoline C.
  • the density ⁇ ISK 2249, the vapor pressure ⁇ IS K 2258, the distillation properties ⁇ IS K 2254, and the Gen value were measured in accordance with UOP326-82.
  • the sulfur content was measured according to ASTM D 5453 (ultraviolet fluorescence method).
  • the sulfur compound content is determined by chemiluminescence.
  • using a gas chromatograph made by Shimadzu Corporation equipped with an ANTEK sulfur chemiluminescence detector for selectively detecting and quantifying sulfur compounds the measurement was carried out by gas chromatography.
  • the hydrocarbon component composition and RON were measured by gas chromatography using a PIONA apparatus manufactured by Hewlett-Packard Company.
  • Catalytic cracking gasoline A had a Gen value of 0.6g / 100g.
  • Catalytic cracking gasoline B had a Gen value of O.lgZlOOg, and almost all of the Gen was removed.
  • Catalytic cracking gasoline B had a sulfur content of 5.0 mass ppm and was treated with a force desulfurizing agent to obtain desulfurization catalytic cracking gasoline C with a sulfur content of 0.2 mass ppm.
  • the resulting desulfurized catalytic cracking gasoline C had a power containing 0.2 mass ppm of thiophenes and no other sulfur-containing compounds.
  • Catalytic cracking light gasoline E had a Gen value of 1.6g and 100g.
  • Catalytic cracking light gasoline F had a Gen value of O.lg / lOOg and almost all of the Gen was removed.
  • Catalytic cracked light gasoline F contained 14 mass ppm of sulfur.
  • Treatment with a force desulfurizing agent yielded desulfurized catalytically cracked light gasoline G with a sulfur content of 0.2 mass ppm.
  • the resulting desulfurized catalytic cracking light gasoline G did not contain thiophene and 3-methylthiophene which contained 0.2 mass ppm of 2-methylthiophene! /.
  • Catalytic cracking gasoline D was subjected to sweet Jung treatment to obtain catalytic cracking gasoline H.
  • Catalytic cracking gasoline H was fractionated into light and heavy fractions to obtain catalytic cracking light gasoline I.
  • catalytic cracking light gasoline I was subjected to gen reduction treatment to obtain catalytic cracking light gasoline J.
  • This catalytic cracked light gasoline J was subjected to desulfurization treatment using the copper-zinc composite oxidized product prepared in gasoline base material preparation 1 under the same conditions as in gasoline base material preparation 1.
  • Table 3 shows the properties of catalytic cracking gasoline H, catalytic cracking light gasoline I, catalytic cracking light gasoline J without gen, and desulfurization catalytic cracking light gasoline K.
  • Hydrocarbon component composition [% by volume]
  • Sulfur compound content is the value in terms of sulfur (ppm by mass).
  • Catalytic cracking light gasoline I had a Gen value of 1.6gZl00g.
  • Catalytic cracking light gasoline J had a Gen value of O.lgZlOOg, and gen was almost completely removed.
  • Catalytically cracked light gasoline J contained 11 mass ppm of sulfur, but by treatment with a desulfurizing agent, desulfurized catalytically cracked light gasoline K with a sulfur content of 0.2 mass ppm was obtained.
  • the resulting desulfurized catalytically cracked light gasoline K contains 0.2 mass ppm of 2-methylthiophene! /, But contains thiophene and 3-methylthiophene!
  • Catalytic cracking gasoline A and catalytic cracking light gasoline E were each desulfurized using the copper-zinc composite oxide prepared in gasoline base preparation 1 under the same conditions as gasoline base preparation 1.
  • Catalytic cracking gasoline L and desulfurization catalytic cracking light gasoline M were obtained.
  • Table 4 shows the properties of desulfurized catalytic cracked gasoline L and desulfurized catalytic cracked light gasoline M.
  • the desulfurized catalytic cracking gasoline L contains 3.6 mass ppm of sulfur
  • the desulfurized catalytic cracking light gasoline M contains 11 mass ppm of sulfur, and neither removes gen. It is clear that it is difficult to remove the thiophene sulfur conjugate particularly when the sorption treatment is performed.
  • Gasoline base materials obtained by known techniques other than catalytic cracking include desulfurized straight-run naphtha N, catalytically modified medium oil 0, catalytically modified heavy oil P, alkylated gasoline Q, and ETBE substrate R.
  • the properties are as shown in Table 5.
  • Catalytic reforming medium oil O is obtained by distilling off a fraction rich in toluene from catalytic reforming gasoline.
  • the catalytically modified heavy oil P is obtained by distilling and separating aromatics having 9 or more carbon atoms and less than 11 carbon atoms from catalytically modified gasoline.
  • Sulfur compound content is a value (mass ppm) converted to sulfur.
  • Example 2 [0057] Further, the desulfurized straight run naphtha N 3.5 volume%, contacting the reformed fuel oil O 19.0% by volume, catalytically reformed heavy oil P 15.0 capacitance 0/0, and 23.0 volume% alkylate gasoline Q Preparation of Gasoline Base Material 39.5% by volume of desulfurized catalytic cracking light gasoline K described in 3 was blended to prepare a lead-free gasoline composition T. Table 6 shows the properties of unleaded gasoline composition T.
  • Gasoline base material 6.0% by volume of desulfurized straight-run naphtha N, 9.0% by volume of catalytic reforming medium oil O, 8.0% by volume of catalytic reforming heavy oil P, and 10.0% by volume of alkylated gasoline Q
  • Preparation of desulfurized catalytically cracked gasoline C described in 1 above, 57.0% by volume of gasoline base material, and 10.0% by volume of desulfurized catalytically cracked light gasoline K described in 3 were blended to prepare a lead-free gasoline composition V.
  • Table 6 shows the properties of lead-free gasoline composition V.
  • An unleaded gasoline composition W was prepared with exactly the same formulation as in the unleaded gasoline composition S of Example 1, except that catalytic cracking gasoline A was used instead of desulfurized catalytic cracking gasoline C. Table 6 shows the properties of unleaded gasoline composition W. Comparative Example 2
  • the unleaded gasoline composition S provided by the present invention is compared with the unleaded gasoline composition W provided by the prior art, and has almost no change in other properties. It is clear that the fraction can be reduced to less than 1 ppm by mass.
  • the unleaded gasoline composition T provided by the present invention can reduce the sulfur content to 1 mass ppm or less without substantially changing other properties as compared with the corresponding unleaded gasoline composition X.
  • the unleaded gasoline compositions U and V provided by the present invention can also reduce the sulfur content to 1 ppm by mass or less.
  • Catalytic cracking gasoline AA obtained by treating a Middle Eastern crude oil different from the above-mentioned gasoline base material preparation 1 in the same manner as gasoline base material preparation 1 and then subjecting it to sweet jung processing is converted to light and heavy components.
  • the heavy fraction was obtained as catalytic cracking heavy gasoline BB.
  • the catalytic cracking heavy gasoline BB was used at a reaction temperature of 220 ° C using a catalyst in which cobalt, molybdenum and phosphorus were supported on alumina (cobalt content 2.4% by mass, molybdenum content 9.4% by mass, phosphorus content 2.0% by mass). , Reaction pressure 1.0MPa, ZOil ratio 307NLZL
  • Unleaded gasoline composition Z was prepared in exactly the same manner as in Example 5, except that the desulfurized catalytic cracked heavy gasoline EE described in 7 was used. did. Table 6 shows the properties of unleaded gasoline composition Z.
  • the cracked gasoline fraction is removed with a gen, it is treated with a porous desulfurizing agent having a sulfur sorbing function in the presence of a small amount of hydrogen to reduce the sulfur content and leave the olefin component.
  • a lead-free gasoline composition with a sulfur content of 1 mass ppm or less which is obtained by mixing a desulfurization cracked naphtha fraction obtained by avoiding octane loss due to desulfurization treatment with another gasoline base material with a sulfur content of 10 mass ppm or less . Therefore, it was possible to reduce only the sulfur content to 1 mass ppm or less without changing the properties of the conventional unleaded gasoline composition and other properties. Therefore, the unleaded gasoline composition of the present invention is useful as a V-vehicle fuel with low environmental load while maintaining high driving performance.

Abstract

L'invention concerne un procédé de production d'une composition d'essence sans plomb qui possède une teneur en soufre inférieure ou égale à 1 ppm en masse et un indice d'octane fondé sur un procédé de recherche supérieur ou égal à 89,0. Ce procédé comprend une étape qui consiste à soumettre à un traitement de désulfurisation une fraction de naphta craquée présentant une température pour une distillation de 5% en volume supérieure ou égale à 25°C et une température pour une distillation de 95% en volume inférieure ou égale à 210°C, une teneur en oléfines supérieure ou égale à 5% en masse et un indice diénique inférieur ou égal à 0,3g/100g ; et une étape de mélange qui consiste à mélanger la fraction de naphta craquée désulfurisée obtenue à une autre matière première d'essence. L'invention concerne également une composition d'essence sans plomb qui possède un indice d'octane fondé sur un procédé de recherche supérieur ou égal à 89,0 ; qui présente une température pour une distillation de 50% en volume inférieure ou égale à 105°C ; une teneur en oléfines supérieure ou égale à 10% en volume et une teneur totale en soufre inférieure ou égale à 1 ppm en masse ; et dont le pourcentage d'un composé sulfureux de type thiophène dans la teneur totale en soufre est supérieur ou égal à 50 en termes de soufre. Ladite composition d'essence sans plomb possède une teneur en soufre inférieure ou égale à 1% et affiche des caractéristiques associées à la conduite satisfaisantes.
PCT/JP2004/016115 2003-11-07 2004-10-29 Composition d'essence sans plomb et procede de production associe WO2005044959A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
KR1020067010974A KR101114742B1 (ko) 2003-11-07 2004-10-29 무연 가솔린 조성물 및 그의 제조 방법
US10/577,951 US20070068849A1 (en) 2003-11-07 2004-10-29 Lead-free gasoline composition and method for production thereof
EP04793223A EP1686166A4 (fr) 2003-11-07 2004-10-29 Composition d'essence sans plomb et procede de production associe
CA2543953A CA2543953C (fr) 2003-11-07 2004-10-29 Composition d'essence sans plomb et procede de production associe
JP2005515277A JP4932257B2 (ja) 2003-11-07 2004-10-29 無鉛ガソリン組成物及びその製造方法

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
JP2003-378503 2003-11-07
JP2003378503 2003-11-07
JP2004-168365 2004-06-07
JP2004168365 2004-06-07

Publications (1)

Publication Number Publication Date
WO2005044959A1 true WO2005044959A1 (fr) 2005-05-19

Family

ID=34575930

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2004/016115 WO2005044959A1 (fr) 2003-11-07 2004-10-29 Composition d'essence sans plomb et procede de production associe

Country Status (6)

Country Link
US (1) US20070068849A1 (fr)
EP (1) EP1686166A4 (fr)
JP (2) JP4932257B2 (fr)
KR (1) KR101114742B1 (fr)
CA (1) CA2543953C (fr)
WO (1) WO2005044959A1 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106179177A (zh) * 2015-05-28 2016-12-07 赢创德固赛有限公司 从烯烃混合物中氢辅助吸附硫化合物

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2009067893A1 (fr) * 2007-11-09 2009-06-04 Ranfeng Ding Système et procédé de recombinaison d'hydrocarbure catalytique pour produire une essence de haute qualité
US8142646B2 (en) * 2007-11-30 2012-03-27 Saudi Arabian Oil Company Process to produce low sulfur catalytically cracked gasoline without saturation of olefinic compounds
CN104511283B (zh) * 2013-09-30 2016-10-05 中国石油化工股份有限公司 一种脱硫催化剂及其制备方法和烃油脱硫的方法
US20230098592A1 (en) * 2021-09-27 2023-03-30 ExxonMobil Technology and Engineering Company Method of refinery processing of renewable naphtha

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5851382A (en) 1995-12-18 1998-12-22 Texaco Inc. Selective hydrodesulfurization of cracked naphtha using hydrotalcite-supported catalysts
US6007704A (en) 1996-09-24 1999-12-28 Institut Francais Du Petrole Process for the production of catalytic cracking gasoline with a low sulphur content
JP2001303070A (ja) * 2000-04-24 2001-10-31 Idemitsu Kosan Co Ltd 燃料油組成物及び自動車の駆動システム
WO2002031090A1 (fr) * 2000-10-11 2002-04-18 Nippon Oil Corporation Combustible a double fonction pour automobile a essence et systeme de pile a combustible, et systeme de stockage et/ ou de distribution de combustible a double fonction
US6444118B1 (en) 2001-02-16 2002-09-03 Catalytic Distillation Technologies Process for sulfur reduction in naphtha streams
JP2003073677A (ja) 2001-09-06 2003-03-12 Idemitsu Kosan Co Ltd 燃料油組成物
JP2003277768A (ja) 2002-03-27 2003-10-02 Cosmo Oil Co Ltd 炭化水素油中の硫黄化合物の低減方法
JP2003301186A (ja) * 2002-04-12 2003-10-21 Jomo Technical Research Center Co Ltd 環境対応ガソリン

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5352354A (en) * 1991-08-15 1994-10-04 Mobil Oil Corporation Gasoline upgrading process
AU1893101A (en) * 1999-12-17 2001-06-25 Idemitsu Kosan Co. Ltd Fuel oil for fuel cell, fuel oil composition and automobile driving system
US6913688B2 (en) 2001-11-30 2005-07-05 Exxonmobil Research And Engineering Company Multi-stage hydrodesulfurization of cracked naphtha streams with interstage fractionation

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5851382A (en) 1995-12-18 1998-12-22 Texaco Inc. Selective hydrodesulfurization of cracked naphtha using hydrotalcite-supported catalysts
US6007704A (en) 1996-09-24 1999-12-28 Institut Francais Du Petrole Process for the production of catalytic cracking gasoline with a low sulphur content
JP2001303070A (ja) * 2000-04-24 2001-10-31 Idemitsu Kosan Co Ltd 燃料油組成物及び自動車の駆動システム
WO2002031090A1 (fr) * 2000-10-11 2002-04-18 Nippon Oil Corporation Combustible a double fonction pour automobile a essence et systeme de pile a combustible, et systeme de stockage et/ ou de distribution de combustible a double fonction
US20030213728A1 (en) 2000-10-11 2003-11-20 Kenichirou Saitou Dual purpose fuel for gasoline driven automobile and fuel cell system, and system for storage and/or supply thereof
US6444118B1 (en) 2001-02-16 2002-09-03 Catalytic Distillation Technologies Process for sulfur reduction in naphtha streams
JP2003073677A (ja) 2001-09-06 2003-03-12 Idemitsu Kosan Co Ltd 燃料油組成物
JP2003277768A (ja) 2002-03-27 2003-10-02 Cosmo Oil Co Ltd 炭化水素油中の硫黄化合物の低減方法
JP2003301186A (ja) * 2002-04-12 2003-10-21 Jomo Technical Research Center Co Ltd 環境対応ガソリン

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP1686166A4 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN106179177A (zh) * 2015-05-28 2016-12-07 赢创德固赛有限公司 从烯烃混合物中氢辅助吸附硫化合物
JP2016222658A (ja) * 2015-05-28 2016-12-28 エボニック デグサ ゲーエムベーハーＥｖｏｎｉｋ Ｄｅｇｕｓｓａ ＧｍｂＨ オレフィン混合物からの硫黄化合物の水素支援吸着
US10370311B2 (en) 2015-05-28 2019-08-06 Evonik Degussa Gmbh Hydrogen-assisted adsorption of sulphur compounds from olefin mixtures

Also Published As

Publication number Publication date
KR101114742B1 (ko) 2012-02-29
JP2008156663A (ja) 2008-07-10
EP1686166A1 (fr) 2006-08-02
EP1686166A4 (fr) 2010-04-21
KR20060113721A (ko) 2006-11-02
JPWO2005044959A1 (ja) 2007-05-17
JP5024884B2 (ja) 2012-09-12
JP4932257B2 (ja) 2012-05-16
US20070068849A1 (en) 2007-03-29
CA2543953C (fr) 2012-10-23
CA2543953A1 (fr) 2005-05-19

Similar Documents

Publication Publication Date Title
Song An overview of new approaches to deep desulfurization for ultra-clean gasoline, diesel fuel and jet fuel
KR20080044768A (ko) 옥탄가 손실이 적은 크래킹 가솔린의 심도 탈황 방법
JP5219247B2 (ja) 低硫黄分解ガソリン基材の製造方法および無鉛ガソリン組成物
JP5024884B2 (ja) 無鉛ガソリン組成物及びその製造方法
JP2003520889A5 (fr)
JP4889095B2 (ja) 環境対応型ガソリン組成物及びその製造方法
JP2004269871A (ja) 無鉛ガソリン組成物およびその製造方法
JP4371937B2 (ja) 接触分解ガソリン基材の製造方法およびそれを用いた無鉛ガソリン組成物
JP4803785B2 (ja) ガソリン基材の製造方法、環境対応ガソリン、およびその製造方法
JP4632738B2 (ja) 無鉛ガソリン組成物およびその製造方法
JP4626950B2 (ja) 環境対応ガソリンおよびその製造方法
JP5036074B2 (ja) 環境対応ガソリン
JP4633409B2 (ja) ガソリン組成物
JP4633411B2 (ja) ガソリン組成物
JP4850412B2 (ja) 環境対応型ガソリン組成物の製造方法
JP4599545B2 (ja) 無鉛ガソリン組成物の製造方法
JP4553352B2 (ja) ガソリン組成物
CN113122320B (zh) 一种环保型橡胶填充油的生产方法
JP2009263681A (ja) 接触分解ガソリン基材の製造方法およびそれを用いた無鉛ガソリン組成物
JP4633410B2 (ja) ガソリン組成物
CN108659879B (zh) 一种汽油脱硫的方法
CN108659884B (zh) 汽油脱硫的方法
JP5280625B2 (ja) 無鉛ガソリン組成物
JP4371925B2 (ja) 無鉛ガソリン組成物およびその製造方法

Legal Events

Date Code Title Description
AK Designated states

Kind code of ref document: A1

Designated state(s): AE AG AL AM AT AU AZ BA BB BG BR BW BY BZ CA CH CN CO CR CU CZ DE DK DM DZ EC EE EG ES FI GB GD GE GH GM HR HU ID IL IN IS JP KE KG KP KR KZ LC LK LR LS LT LU LV MA MD MG MK MN MW MX MZ NA NI NO NZ OM PG PH PL PT RO RU SC SD SE SG SK SL SY TJ TM TN TR TT TZ UA UG US UZ VC VN YU ZA ZM ZW

AL Designated countries for regional patents

Kind code of ref document: A1

Designated state(s): BW GH GM KE LS MW MZ NA SD SL SZ TZ UG ZM ZW AM AZ BY KG KZ MD RU TJ TM AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HU IE IT LU MC NL PL PT RO SE SI SK TR BF BJ CF CG CI CM GA GN GQ GW ML MR NE SN TD TG

121 Ep: the epo has been informed by wipo that ep was designated in this application
WWE Wipo information: entry into national phase

Ref document number: 2004793223

Country of ref document: EP

WWE Wipo information: entry into national phase

Ref document number: 2005515277

Country of ref document: JP

WWE Wipo information: entry into national phase

Ref document number: 2543953

Country of ref document: CA

WWE Wipo information: entry into national phase

Ref document number: 1020067010974

Country of ref document: KR

WWE Wipo information: entry into national phase

Ref document number: 2007068849

Country of ref document: US

Ref document number: 10577951

Country of ref document: US

WWP Wipo information: published in national office

Ref document number: 2004793223

Country of ref document: EP

WWP Wipo information: published in national office

Ref document number: 1020067010974

Country of ref document: KR

WWP Wipo information: published in national office

Ref document number: 10577951

Country of ref document: US