WO2004078885A1 - Preparation de gazole et son procede de production - Google Patents

Preparation de gazole et son procede de production Download PDF

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Publication number
WO2004078885A1
WO2004078885A1 PCT/JP2004/002917 JP2004002917W WO2004078885A1 WO 2004078885 A1 WO2004078885 A1 WO 2004078885A1 JP 2004002917 W JP2004002917 W JP 2004002917W WO 2004078885 A1 WO2004078885 A1 WO 2004078885A1
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gas oil
content
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volume
oil composition
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PCT/JP2004/002917
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English (en)
Japanese (ja)
Inventor
Kenichirou Saitou
Hideaki Sugano
Hideshi Iki
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Nippon Oil Corporation
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Priority to EP04717859A priority Critical patent/EP1619232A4/fr
Publication of WO2004078885A1 publication Critical patent/WO2004078885A1/fr

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    • 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
    • C10L1/08—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/06—Gasoil

Definitions

  • the present invention relates to a gas oil composition and a method for producing the same.
  • a base material for gas oil a straight-run gas oil obtained by distilling crude oil at normal pressure and a straight-run kerosene that have been subjected to hydrorefining treatment and hydrodesulfurization treatment have been used.
  • a base material for gas oil a straight-run gas oil obtained by distilling crude oil at normal pressure and a straight-run kerosene that have been subjected to hydrorefining treatment and hydrodesulfurization treatment.
  • conventional light oils one or more of the above base materials are used, and if necessary, a cetane number improver, a detergent, etc. are blended (for example, “Introduction to Fuel Engineering”, Seiichi Konishi, Author, Shokabo, published March 1991, see pages 136-144).
  • the kerosene base material since the kerosene base material generally has a lower aromatic content than the light oil base material (up to about 30% by volume, on average about 15% by volume), Mix aromatic kerosene base with diesel base to reduce aromatic content to some extent It is possible.
  • the light oil composition obtained in this way is low in density and very light, and may cause deterioration of fuel efficiency and output.
  • such a light oil composition has a low viscosity and is not preferable in terms of lubricity of a fuel injection pump or the like.
  • the present invention has been made in view of such circumstances, and an object thereof is to achieve a high level of balance between reduction of environmental load and improvement of fuel efficiency when used as diesel fuel. And a method for producing the same.
  • the gas oil composition of the present invention comprises: A hydrorefined oil having a yellow content of 5 to 10 mass ppm and a boiling range of 150 to 380 ° C is obtained by further hydrotreating in the presence of a hydrogenation catalyst. 90% Distillation temperature is 200 to 380 ° C, density at 150 ° C is 780 to 870 kg / Sulfur content is 5 mass ppm or less, and aromatic content is 10% by volume or less, Naphthene content is 30% by volume. /.
  • the sulfur content of the gas oil composition is 5% by mass or less
  • the aromatic content is 10% by volume or less
  • the aromatic content of two or more rings Content is 1 volume ° /.
  • the naphthene content is 30 volumes. /.
  • the density at 15 ° C is 82 to 84 kg / m 3
  • the 10% distillation temperature is 250 ° C or less
  • the 90% distillation temperature is 32 ° C or less. It is characterized by the following.
  • the specific deep hydrorefined gas oil (hereinafter, simply referred to as "deep hydrorefined gas oil”) is used to obtain the sulfur content of the entire gas oil composition and the aromatic content.
  • the deep hydrorefined gas oil is contained in the gas oil composition in an amount of 20% by volume or more, and the sulfur content, the aromatic content, the aromatic content of two or more rings, the naphthene content of the gas oil composition are obtained.
  • the content, the density at 15 ° C, the 10% distilling temperature, and the 90% distilling temperature within the above ranges, the required properties as a future-type diesel fuel are satisfied and the environmental load is reduced.
  • a gas oil composition that achieves both reduction and improvement in fuel efficiency at a high level in a well-balanced manner is realized.
  • the gas oil composition of the present invention preferably further contains at least one selected from hydrocracked gas oil, hydrocracked kerosene, hydrorefined kerosene, synthetic gas oil and synthetic kerosene. .
  • the end point of the composition is 350 ° C. or less, the cetane number is 55 or more, the cetane index is 52 or more, and the temperature is 40 ° C.
  • the method for producing the gas oil composition of the present invention comprises the steps of: further hydrotreated in the presence of a hydrogenation catalyst, 9 0 0% distillation temperature of 2 0 ⁇ 3 8 0 ° C, 1 5 ° density at C is 7 8 0 ⁇ 8 7 0 kg / m 3,
  • the above-mentioned specific deep-hydrogenated gas oil is used, and further, the above-mentioned specific base material is mixed with the deep-hydrogenated gas oil to form the deep-hydrogenated gas oil.
  • the sulfur content of the gas oil composition, the aromatic content, the aromatic content of two or more rings, the naphthene content, the density at 15 ° C, the 10% distillation temperature, 90% distillation temperature in the manufacturing method of each gas oil composition of t [0 0 1 6] the present invention gas oil composition can be easily obtained and reliably of the present invention is within the above range
  • the second The end point of the gas oil composition obtained in the process is 350 ° C or less
  • the cetane number is 55 or more
  • the cetane index is 52 or more
  • the kinematic viscosity at 40 ° C is 2 to 4 mm 2 / s
  • HF RR It is preferred that the wear scar diameter be 400 ⁇ m or less and the pour point be 17.5 ° C or less.
  • FIG. 1 is a schematic configuration diagram showing the scanning mobility particle size analyzer used in the examples.
  • the gas oil composition of the present invention has a temperature of 90 ° / °. Distillation temperature: 200 to 380 ° C, density at 150 ° C: 780 to 870 kgm Sulfur content: 5 mass ppm or less, aromatic content: 10% by volume or less
  • a deep hydrorefined gas oil with a naphthene content of 30% by volume or more, containing at least 20% by volume of the total composition the sulfur content of the gas oil composition is 5 mass ppm or less, aromatic The content is 10% by volume or less, the aromatic content of two or more rings is 1% by volume or less, the naphthene content is 30% by volume or more, and the density at 15 ° ⁇ is 82 to 84.
  • Such a deep hydrorefined gas oil is obtained by further hydrotreating a hydrorefined oil having a sulfur content of 5 to 10 mass ppm and a boiling point range of 150 to 380 ° C in the presence of a hydrogenation catalyst. It is obtained by a chemical treatment.
  • the hydrorefined oil used in the production of deep hydrorefined gas oil is not particularly limited as long as it is a hydrogenated refined oil of petroleum hydrocarbon having a sulfur content and a boiling point within the above ranges.
  • a hydrorefining treatment and / or a hydrodesulfurization treatment can be used.
  • the feedstock oils for hydrorefined refinery include straight-run gas oil obtained from a normal-pressure distillation unit, reduced-pressure gas oil obtained by treating straight-run heavy oil and residual oil obtained from a normal-pressure distillation unit with a vacuum distillation unit, Catalytic cracking gas oil and hydrocracked gas oil obtained by catalytic cracking or hydrocracking of reduced pressure heavy gas oil or desulfurized heavy oil, hydrorefined gas oil or hydrodesulfurization obtained by hydrorefining these petroleum hydrocarbons Light oil etc. I can do it.
  • the hydrorefining conditions for the above feedstock were as follows: 90% distillation temperature of the resulting hydrorefined oil, density at 15 ° C, sulfur content, aromatics and naphthenes content Although but not particularly limited as long as it is within the above respective ranges, preferably, the processing temperature 3 0 0 ⁇ 3 8 0 ° C , hydrogen pressure 3 ⁇ 8MP a, LH SV 0. S ⁇ S h 1, hydrogen / oil ratio of 1 0 0 to 500 N LZL.
  • a catalyst used for hydrorefining a general hydrodesulfurization catalyst can be applied.
  • the active metal species of such hydrodesulfurization catalysts usually include sulfides of Group 6A and Group 8 metals (Co-Mo, Ni-Mo, Co-W, Ni-W).
  • a porous inorganic oxide containing alumina as a main component is used as the carrier.
  • the deep hydrorefined light oil according to the present invention can be obtained.
  • the configuration of the apparatus used for the hydrogenation treatment is not particularly limited, and may be a single reactor or a combination of a plurality of reactors. Good. Further, in the case of an apparatus having a plurality of reaction towers, additional hydrogen may be injected between two adjacent reaction towers. Further, the hydrotreating apparatus may be provided with equipment for a gas-liquid separation operation and a hydrogen sulfide removal operation.
  • the reaction system of the hydrotreating apparatus is preferably a fixed bed system.
  • the hydrogen may be distributed in a countercurrent or cocurrent flow with the hydrorefined oil. Further, in the case of an apparatus having a plurality of reaction towers, countercurrent and cocurrent may be combined.
  • As a general distribution system there is a down-flow gas-liquid dual co-current system. For the purpose of removing the heat of reaction or increasing the partial pressure of hydrogen, hydrogen gas may be injected as a solvent in the middle stage of the reaction tower.
  • Hydrotreating conditions are 15 ° C of the obtained deep hydrorefined light oil.
  • the density, sulfur content, aromatic content and naphthene content in the above are not particularly limited as long as they are within the above ranges, respectively, but the reaction temperature is preferably 170 to 320 ° C, and more preferably Is from 175 to 300 ° C, more preferably from 180 to 280 ° C.
  • the hydrogen pressure is preferably 2 to 1 MPa, more preferably 2.5 to 8 MPa, and still more preferably 3 to 7 MPa.
  • LH SV is preferably 0. l to 2 h- more preferably 0. 2 ⁇ 1. 5 h 1, more preferably 0. 3 ⁇ 1. 2 h _ 1.
  • the hydrogen oil ratio is preferably from 100 to 800 NL / L, more preferably from 150 to 600 NL / L, and still more preferably from 150 to 500 NL / L. .
  • the lower the reaction temperature the more advantageous for the hydrogenation reaction, but is not preferred for the desulfurization reaction.
  • the hydrogen pressure and the hydrogen / oil ratio are higher, both the hydrogenation reaction and the desulfurization reaction are promoted, but an excessively high pressure is not economically preferable.
  • the lower the LHSV the more advantageous the reaction.
  • an excessively low LHSV requires a very large reactor volume, which is not preferable in terms of equipment costs.
  • Examples of the hydrogenation catalyst used in the hydrogenation treatment include, for example, those in which a hydrogenation active metal is supported on a porous carrier.
  • a porous carrier for the hydrogenation catalyst a porous inorganic oxide can be used, and specific examples include alumina, titaure, zirconia, polya, silica, zeolite, and the like.
  • One of these porous carriers may be used alone, or two or more thereof may be used in combination.However, at least one of titania, zirconia, polya, silylite and zeolite is used. Those composed of alumina are preferred.
  • the method for producing the porous carrier is not particularly limited.
  • the porous carrier can be prepared by an arbitrary preparation method using raw materials in the form of various sols, salt compounds and the like corresponding to the constituent elements of the porous carrier.
  • silica alumina, silica zirconia, alumina titania, silica After preparing a composite hydroxide or a composite oxide such as tania and alumina binder, a porous carrier may be prepared by adding alumina gel or other hydroxide as it is or in an appropriate solution.
  • the proportion of alumina and other oxides in the porous carrier is arbitrary, but the proportion of alumina is preferably 90% or less, more preferably 60% or less, and still more preferably 40% or less. is there.
  • Zeolites are crystalline aluminosilicates. More specifically, examples include faujasite, pentasil, and mordenite. Among them, faujasite and mordenite are preferable, and Y-type and beta-type are more preferable.
  • These zeolites can be used after being ultra-stabilized by a predetermined hydrothermal treatment and Z or acid treatment, or can be used after adjusting the alumina content in the zeolites. In particular, when using a ⁇ -type zeolite, it is preferable to use a super-stabilized one. In the zeolite ultra-stabilized by hydrothermal treatment, new pores are formed in the range of 20 to 100 A in addition to the original pore structure (micropores) of 20 A or less. Known hydrothermal treatment conditions can be applied.
  • the active metal of the hydrogenation catalyst at least one metal selected from Group 8 metals is preferable, and selected from Ru, Rd, Ir, Pd and Pt. At least one is more preferred, and Pd and / or Pt are even more preferred.
  • One active metal may be used alone, or two or more active metals may be used in combination.
  • Common inorganic salts and complex chlorides can be used as the metal source.
  • the amount of the active metal carried is not particularly limited, but the total amount of the metal with respect to the total amount of the hydrogenation catalyst is preferably 0.1 to 10% by mass.
  • the content is more preferably 0.15 to 5% by mass / 0 , and even more preferably 0.2 to 3% by mass.
  • any of the supporting methods used for ordinary hydrogenation catalysts such as an impregnation method and an ion exchange method, can be used.
  • a plurality of metals When a plurality of metals are supported, they may be simultaneously supported using a mixed solution, or may be sequentially supported using a single solution.
  • the metal solution may be an aqueous solution or an organic solvent.
  • the loading of the active metal on the porous carrier may be carried out after completion of the entire process of preparing the porous carrier, or the active metal may be activated to an appropriate oxide, complex oxide, zeolite, etc. in the intermediate step of the preparation of the porous carrier. After the metal is supported, a gel preparation step, heat compression, kneading and the like may be performed.
  • the hydrogenation catalyst is preferably subjected to a hydrogenation treatment after being subjected to a preliminary reduction treatment in a hydrogen stream. For example, by heating at a temperature of 200 ° C or more according to a predetermined procedure while flowing a gas containing hydrogen, the active metal on the catalyst can be sufficiently reduced and a high level of hydrogenation activity can be exhibited. Can be.
  • the 90% distillation temperature (hereinafter sometimes referred to as "T90" in some cases) of the deep hydrorefined gas oil according to the present invention obtained by the above hydrotreating is reduced to an excessively light weight in distillation properties.
  • T90 it is necessary to maintain the temperature at 200 ° C. or higher, preferably 200 ° C. or higher, more preferably 220 ° C. or higher, and more preferably Is at least 230 ° C, particularly preferably at least 240 ° C.
  • the T90 is required to be not higher than 380 ° C as described above from the viewpoint of suppressing an increase in particulate matter (PM) discharged from the engine, and is preferably used.
  • the 90% distilling temperature (T90) as used herein means a value measured by JISK 2254 “Oil product single distillation test method”.
  • the density of the deep hydrorefined light oil according to the present invention at 15 ° C may be 780 kg ni 3 or more as described above from the viewpoint of securing the calorific value. It is necessary, and it is preferably at least 790 kg / m 3 , more preferably at least 800 kgZm 3 . Further, the density, NO x, from the viewpoint of reducing the emission of PM, it is necessary as described above 8 7 is 0 kg Zm 3 or less, preferably 8 6 0 kg / m 3 or less, more preferably Is at most 850 kg / m 3 , more preferably at most 800 kg Zm 3 . In addition, the density here means the density measured by JISK2249 “Density test method for crude oil and petroleum products and density-mass-volume conversion table”.
  • the sulfur content of the deep hydrorefined light oil according to the present invention is 5 mass as described above from the viewpoint of reducing harmful exhaust components discharged from the engine and improving the performance of the exhaust gas aftertreatment device. ppm or less, preferably 3 mass ppm or less, more preferably 2 mass! ): Not more than pm, more preferably not more than 1 mass P Pm.
  • the sulfur content means the mass content of sulfur based on the total amount of the gas oil composition measured by JIS K2541 “Sulfur content test method”.
  • the naphthene content of the deep hydrorefined gas oil according to the present invention needs to be 30% by volume or more, as described above, and is preferably 32% by volume or more. Preferably, it is more preferably at least 35% by volume.
  • the naphthene content referred to here is ASTMD 2786 "Standard Test Methodfor Hydrocarbon Tye A nalysisof G a s — means the volume percentage (% by volume) of naphthene measured according to “Oil Saturates Fractions by High Ionizing Mass Spectrometry”.
  • the aromatics content of the deep hydrorefined gas oil according to the present invention needs to be 10% by volume or less, and may be 8% by volume or less. More preferably, it is more preferably 5% by volume or less.
  • the aromatic content mentioned here is based on the journal of the Japan Petroleum Institute, published by the Japan Petroleum Institute. JPI — 5S—499-197 “Hydrocarbon Type Test Method—High-Performance Liquid Chromatography” Means the volume percentage (% by volume) of the aromatic content measured according to
  • the deep hydrorefined gas oil having the above structure By using the deep hydrorefined gas oil having the above structure, it is possible to easily and surely control all of the sulfur content, the aromatic content and the density of the entire gas oil composition. Thus, the light oil composition of the present invention can be obtained efficiently and reliably.
  • the gas oil composition of the present invention has a sulfur content, an aromatic content, an aromatic content of two or more rings, a naphthene content, 15 ° C.
  • the content of deep hydrorefined gas oil must be at least 20% by volume. If no deep hydro-refined gas oil is contained, and if the content of deep hydro-refined gas oil is less than 20% by volume, reduction of environmental load and improvement of fuel efficiency cannot be achieved at the same time.
  • the content of the deep hydrorefined gas oil according to the present invention is preferably 30% by volume or more, More preferably 4 0 volume 0/0 or more, more preferably Ru der 5 0% by volume or more.
  • the sulfur content of the gas oil composition of the present invention must be 5 mass ppm or less, preferably 3 mass 1> pm or less, more preferably 2 mass ppm or less.
  • the content is even more preferably 1 ppm by mass or less. If the sulfur content exceeds 5 mass ppm, the effect of reducing the environmental load becomes insufficient.
  • the sulfur content means the sulfur content measured by JIS K2541 “Sulfur content test method” and based on the total amount of the gas oil composition.
  • the aromatic content of the gas oil composition of the present invention is required to be 10% by volume or less as described above from the viewpoint of reducing environmental load, and is preferably It is at most 8% by volume, more preferably at most 5% by volume.
  • the content of aromatics having two or more rings in the aromatics needs to be 1% by volume or less, preferably 0.8% by volume or less, more preferably 0.5% by volume or less. If the aromatic content and the aromatic content of the two or more rings each exceed the upper limit, NO x and PM emissions in the exhaust gas increase, and the effect of reducing the environmental load is insufficient. Become.
  • the aromatic content and the aromatic content of two or more rings are based on the JPI-5S-49-97, a petroleum society journal published by the Japan Petroleum Institute. It means the aromatic content and the volume percentage (volume%) of the aromatic content of two or more rings measured according to the “High performance liquid chromatography method”.
  • the naphthene content of the gas oil composition of the present invention must be 30% by volume or more, as described above, from the viewpoint of improving fuel efficiency and output, and 32% by volume or more. And more preferably 35% by volume or more.
  • the naphthene content referred to here is AS TM D 2 7 8 6 "Standard Test Methodfor Hydrocarbon T ypes A nalysis of Gas—Oil Saturates Fractions by High Ionizing Mass Spectrometry %).
  • the density of the gas oil composition of the present invention at 15 ° C. needs to be at least 220 kgZm 3 as described above from the viewpoint of fuel consumption rate and acceleration. And preferably at least 82 22 kg / m 3 , more preferably at least 82 kgZm 3 . Further, the density, in terms of PM concentration decreases in the exhaust gas, 8 4 0 kg Zm 3 is required to be less, preferably rather is 8 3 7 kg / m 3 or less, more preferably 8 It is 35 kg / m 3 or less.
  • the density referred to here means the density measured by JIS 2249 “Density test method for crude oil and petroleum products and density / mass / volume conversion table”.
  • the distillation properties require that the 10% distillation temperature be 250 ° C. or less, more preferably 240 ° C. or less, It is more preferably at most 230 ° C, still more preferably at most 25 ° C, most preferably at most 220 ° C. If the 10% distillation temperature exceeds the upper limit, the exhaust gas performance deteriorates. Further, the 10% distillation temperature is preferably at least 160 ° C, more preferably at least 170 ° C, and even more preferably at least 180 ° C. If the 10% distillation temperature is less than the lower limit, the engine output and the startability at high temperatures are deteriorated.
  • the 90% distillation temperature of the gas oil composition of the present invention is not higher than 320 ° C., preferably not higher than 31 ° C., and more preferably not higher than 31 ° C.
  • the temperature is 5 ° C or lower, more preferably 312 ° C or lower, and most preferably 310 ° C or lower. If the 90% distillation temperature exceeds the upper limit, PM or minute Particle emissions tend to increase.
  • the 90% distillation temperature is preferably at least 270 ° C, more preferably at least 275 ° C, even more preferably at least 280 ° C.
  • the distillation property of the gas oil composition of the present invention is 10 ° / °.
  • the distillation temperature and the 90% distillation temperature are not particularly limited as long as they are within the above range, but the 50% distillation temperature is preferably 310 ° C or lower, and is preferably 300 ° C or lower. More preferably, it is still more preferably 295 ° C. or less,
  • the temperature is not higher than 290 ° C. If the 50% distillation temperature exceeds the upper limit, the exhaust gas performance tends to deteriorate. Further, the 50% distillation temperature is preferably at least 240 ° C, more preferably at least 245 ° C, even more preferably at least 250 ° C, The temperature is particularly preferably at least 55 ° C, and most preferably at least 260 ° C.
  • the 95% distillation temperature of the gas oil composition of the present invention is preferably at least 290 ° C, more preferably at least 295 ° C.
  • the end point of the gas oil composition of the present invention is preferably at least 300 ° C, more preferably at least 300 ° C. If the 95% distilling temperature and the end point are below the lower limits, respectively, the effect of improving the fuel becomes insufficient and the engine output tends to decrease.
  • the 95% distillation temperature is preferably 34 ° C. or lower, more preferably 33 ° C. or lower, and even more preferably 330 ° C. or lower.
  • the endpoint is preferably below 350 ° C., more preferably below 35 ° C., even more preferably
  • the cetane number of the gas oil composition of the present invention is preferably from the viewpoint of suppressing the concentration of NO x, PM and aldehydes in the exhaust gas to be low.
  • the cetane number is based on JISK 2280 “Method for calculating cetane number” in “Test methods for petroleum products, fuel oil, octane number and cetane number and cetane index calculation method”. Means the cetane number measured.
  • the cetane index of the gas oil composition of the present invention is preferably at least 52, more preferably at least 52, from the viewpoint of suppressing the concentration of NO X ⁇ PM and aldehydes in the exhaust gas. It is 53 or more, more preferably 55 or more.
  • the cetane index refers to the calculation of the cetane index using the 8.4 variable equation in JISK 228, “Test Methods for Petroleum Products, Fuel Oil, Ottatan Number and Cetane Number, and Calculation of Cetane Index”. Means the value calculated according to “Method”.
  • the cetane index in the above JIS standard is usually not applied to those to which a cetane number improver is added, but the light oil composition of the present invention may contain a cetane number improver as described later.
  • the above “8.4 Calculation method of cetane index using variable equation” is applied to the gas oil composition to which the cetane number improver is added, and the value calculated by the calculation method is expressed as the cetane index.
  • the kinematic viscosity of the gas oil composition of the present invention at 40 ° C. is preferably 2 mm 2 / s or more, more preferably 2.2 mm 2 / s, and still more preferably 2.4 mm mm 2 / s or more. If the kinematic viscosity is less than 2 mm 2 / s, control of the fuel injection timing on the fuel injection pump side tends to be difficult, and lubricity in each part of the fuel injection pump may be impaired. Further, the kinematic viscosity is preferably 4 mm 2 Z s or less, more preferably 3.8 mm 2 Z s or less, and still more preferably 3.6 ram 2 Z s or less.
  • the kinematic viscosity as used herein refers to the kinematic viscosity measured by JISK 2283 “Crude oil and petroleum product kinematic viscosity test method and viscosity index calculation method”.
  • the lubricating performance of the gas oil composition of the present invention can be represented by using the HFR R wear scar diameter (W S 1.4) as an index.
  • the HFRR wear scar diameter of the gas oil composition of the present invention is preferably 400 ⁇ m or less, more preferably 3900 ⁇ m or less, and still more preferably 38 O / xm or less.
  • the diameter of the HFRR wear scar exceeds 400 ⁇ m, especially in a diesel engine equipped with a distributive injection pump, it causes an increase in the driving torque of the pump during operation and an increase in wear of each part of the pump.
  • the engine itself may be destroyed as well as the particle performance deteriorates.
  • the HF RR wear scar diameter is a value measured by the Japan Petroleum Institute standard JPI — 5 S — 50 — 98 “Diesel oil-lubricity test method” issued by the Japan Petroleum Institute. means.
  • the pour point of the gas oil composition of the present invention is determined from the viewpoint of low-temperature startability or low-temperature operation, and also from the viewpoint of maintaining the injection performance of an electronically controlled fuel injection pump. ⁇ It is preferable that the temperature be 5 ° C or lower. C or lower, more preferably 120 ° C. or lower.
  • the pour point means the pour point measured by JIS K 2269 “Pour point of crude oil and petroleum products and cloud point of petroleum products”.
  • the ash content of the gas oil composition of the present invention is preferably less than 0.01% by mass.
  • the ash content here means the mass content of ash based on the total amount of light oil composition measured by JISK 2272 “Test method for ash and sulfated ash of crude oil and petroleum products”.
  • the clogging point of the gas oil composition of the present invention is not particularly limited, but is preferably 15 ° C or lower, more preferably -8 ° C or lower, and 1 ° C or lower.
  • the temperature is more preferably 2 ° C or lower, and even more preferably 119 ° C or lower.
  • the clogging point means a clogging point measured by JIS K2288 “Diesel oil single clogging point test method”.
  • the total insoluble content after the oxidation stability test may be 2.0 mg / 10 OmL or less. Preferably, it is more preferably 1.0 mg / 100 mL or less, even more preferably 0.5 mg / 100 niL or less, and 0.3 mg / 100 mL. Is even more preferable, and most preferably 0.1 mg Z 100 mL or less.
  • the oxidation stability test mentioned here is conducted at 95 ° C under oxygen bubbling for 16 hours in accordance with ASTM D2274-94.
  • the total insoluble content after the oxidation stability test means a value measured in accordance with the oxidation stability test.
  • the peroxide value after the oxidation stability test is 10 mass% or less. It is preferably at most 5 ppm by mass, more preferably at most 2 ppm by mass, particularly preferably at most 1 ppm by mass.
  • the peroxide value here means a value measured in accordance with the Japan Petroleum Institute standard JPI — 5 S — 46 — 96 I do.
  • additives such as an antioxidant and a metal deactivator described below may be appropriately added in order to reduce the total insoluble content and the peroxide value. it can.
  • the electrical conductivity of the light oil composition of the present invention is not particularly limited, but is preferably 50 pS / m or more from the viewpoint of safety.
  • the electrical conductivity means a value measured in accordance with JIS K 2 276 “Petroleum products-Aero fuel oil test method”.
  • the gas oil composition of the present invention may be appropriately added with an antistatic agent and the like described below in order to improve the electrical conductivity.
  • these light oil base materials are referred to as “other light oil base materials”.
  • the properties of other gas oil base materials are not particularly limited, but in order to easily and reliably achieve the desired properties of the gas oil composition of the present invention, it is preferable to have the specific properties described below. .
  • T 90 of the other light oil base is preferably 2
  • the temperature is at least 100 ° C, more preferably at least 210 ° C, still more preferably at least 220 ° C, even more preferably at least 230 ° C, most preferably at least 240 ° C.
  • the T90 is preferably at most 380 ° C, more preferably at most 370 ° C, still more preferably at most 360 ° C, still more preferably at most 350 ° C. Below, most preferably, it is not more than 340 ° C.
  • the density of 1 5 ° C for other gas oil bases preferred properly is 7 8 0 kg Zm 3 or more, more preferably 7 9 0 kg / m 3 or more, preferably to La 8 is 0 0 kg / m 3 or more. Further, the density is preferably rather is 8 7 0 kg Zm 3 or less, more preferably 8 6 0 kg / m 3 or less, preferably a further 8 5 0 kg / m 3 or less, even more preferably 8 4 0 kg / m 3 or less.
  • the sulfur content of the other gas oil base materials is preferably 10 mass ppm or less, more preferably 5 mass ppm or less, and still more preferably 3 mass ppm or less.
  • the aromatic content of the gas oil base material is not particularly limited, but is preferably 20% by volume or less, and more preferably 15% by volume or less. , 10% by volume or less.
  • the content of the other gas oil base material in the gas oil composition of the present invention is such that the content of the deep hydrorefined gas oil is 20% by volume or more, the sulfur content of the gas oil composition, and the aroma.
  • Group content, aromatic content of two or more rings, naphthene content, density at 15 ° C, 10% distillation temperature and 90% distillation temperature are within the above ranges, respectively.
  • it can be set as appropriate according to the practical performance as a commercial fuel oil (for example, low-temperature fluidity performance and lubrication performance).
  • the blending amount of the light oil base material is preferably 5% by volume or more, more preferably 10% by volume / 0 or more, and further preferably More than 15% by volume.
  • the formulation The amount is preferably at most 80% by volume, more preferably at most 70% by volume / 0 , even more preferably at most 60% by volume.
  • the content of the deep hydrorefined gas oil, the sulfur content of the gas oil composition, the aromatic content, the aromatic content of two or more rings, the naphthene content Synthetic gas oil can be blended with the gas oil composition as long as the minute content, the density at 15 ° C., the 10% distillation temperature, and the 90% distillation temperature are within the above ranges, respectively.
  • the synthetic gas oil according to the present invention refers to a synthetic gas oil obtained by using natural gas, asphalt, coal or the like as a raw material and chemically synthesizing it.
  • Chemical synthesis methods include indirect liquefaction method and direct liquefaction method.
  • a typical synthesis method includes Fischer-Trops synthesis method.
  • the synthetic gas oil used in the present invention is produced by these methods. It is not limited.
  • Synthetic gas oils generally contain saturated hydrocarbons as the main component, and more specifically, normal paraffins, isoparaffins, and naphthenes. That is, synthetic gas oil generally contains almost no aromatic components.
  • the synthetic gas oil In order to easily and reliably achieve the desired properties of the gas oil composition of the present invention, it is preferable that the synthetic gas oil has the specific properties described below.
  • density of 1 5 ° C of the synthetic gas oil preferably 7 2 0 kg / m 3 or more, more preferably 7 3 0 kg Zm 3 or more, more preferably 7 4 0 kg / m 3 or more, still more preferably 7500 kg / m 3 or more.
  • the density is preferably 8 4 0 kg / m 3 or less, good Ri preferably 8 3 0 kg Zm 3 or less, more preferably 8 2 0 kg / m 3 or less, even more preferably 8 1 0 kg Zm 3 or less.
  • the sulfur content of the synthetic gas oil is preferably 5 mass ppm or less, more preferably 3 mass ppm or less, and still more preferably 2 mass ppm or less. ppm or less, still more preferably 1 ppm by mass or less.
  • the compounding amount of the synthetic gas oil according to the present invention includes the content of the deep hydrorefined gas oil, the sulfur content of the gas oil composition, the aromatic content, and the aromatic content of two or more rings.
  • the content is preferably 2% by volume or more, and more preferably 5% by volume or more.
  • the amount is preferably 30% by volume or less, more preferably 20% by volume or less, and further preferably 10% by volume or less.
  • the kerosene base material can be blended if the fractional content, the density at 15 ° C., the 10% distillation temperature, and the 90% distillation temperature are respectively within the above ranges.
  • Such kerosene base materials include: straight kerosene obtained by atmospheric distillation of crude oil; cracked kerosene obtained by cracking a gas oil fraction obtained by atmospheric distillation of straight crude oil; hydrogenation Hydrocracked kerosene produced with cracked gas oil; Hydrorefined kerosene obtained by hydrorefining the above kerosene fraction; Synthetic kerosene made from natural gas, asphalt, coal, etc. can be used is there.
  • kerosene base material it is also possible to use a deep hydrorefined kerosene that has been subjected to advanced hydrorefining so that the sulfur content and the aromatic content are extremely reduced.
  • the properties of these kerosene base materials are not particularly limited, but in order to easily and surely achieve the desired properties in the gas oil composition of the present invention,- It preferably has the specific properties described below.
  • the T90 of the kerosene base material is preferably at least 140, more preferably at least 144 ° C, and even more preferably at least 150 ° C. Further, the T90 is preferably 280 ° C or less, more preferably 270 ° C or less, and further preferably 260 ° C or less.
  • the density at 1 5 ° C kerosene base material preferably 7 5 0 kg / m 3 or more, more preferably 7 6 0 kgm 3 or more, further preferred properly is 7 7 0 k GZm 3 or more.
  • the density is preferably 82 kg / m 3 or less, more preferably 8 10 kg Zm 3 or less, and still more preferably 800 kg / m 3 or less.
  • the sulfur content of the kerosene base material is preferably 10 mass ppm or less, more preferably 5 mass ppm or less, and still more preferably 3 mass ppm or less.
  • the content of the aromatic component in the kerosene base material is not particularly limited, but is preferably 30% by volume / 0 or less, more preferably 25% by volume or less, and 2% by volume or less. It is still more preferably 0% by volume or less, even more preferably 15% by volume or less, and most preferably 10% by volume or less.
  • the blending amount of the kerosene base material according to the present invention includes the content of the deep hydrorefined gas oil, the sulfur content of the gas oil composition, the aromatic content, and the aromatic structure of two or more rings. If the fraction content, the naphthene content, the density at 15 ° C, the 10% distilling temperature and the 90% distilling temperature are respectively within the above ranges, the practical performance as a commercial fuel oil (for example, low temperature fluidity) Performance and lubrication performance).
  • the content is preferably 5% by volume or more, more preferably 10% by volume or more.
  • the amount is preferably 60 volumes. / 0 or less, more preferred Is 50% by volume or less, more preferably 40% by volume / o or less, and even more preferably 30% by volume or less.
  • the gas oil composition of the present invention may contain various base materials in addition to the deep hydrorefined gas oil.
  • the deep hydrorefined gas oil the hydrocracked gas oil
  • the content of the deep hydrorefined gas oil, the sulfur content, the aromatic content, the aromatic content of two or more rings, the naphthene content of the gas oil composition, 15 The density at 10 ° C., the 10% distillation temperature and the 90% distillation temperature can be controlled more easily and reliably.
  • an appropriate amount of a cetane number improver may be added as needed.
  • cetane number improver various compounds known as cetane number improvers for gas oils can be arbitrarily used, and examples thereof include ester nitrate and organic peroxides. .
  • One of these cetane number improvers may be used alone, or two or more thereof may be used in combination.
  • nitrate ester examples include 2-chloroethenylate, 2-ethoxyethinolaterate, isopropylaterate, butylnitrate, dairy amiliterate, and 2nd-amylnitrate.
  • Amilny rate Isoamylate rate, 1st hexilone rate, 2nd hexynolenate rate, n—Heptinolenate rate, n—Octinolenate rate, 2—Echinolenate rate
  • nitrites such as ethyl hexyl nitrate and ethylenglycol resinate, and the like, in particular, alkyl nitrates having 6 to 8 carbon atoms. Is preferred.
  • the content of the cetane number improver is preferably at least 500 ppm by mass, more preferably at least 600 ppm by mass, and more preferably at least 700 mass ppm based on the total amount of the composition. It is more preferably at least ppm, even more preferably at least 800 ppm by mass, and most preferably at least 900 ppm by mass. If the content of the cetane number improver is less than 500 ppm by mass, a sufficient cetane number increase effect cannot be obtained, and PM, aldehydes, and NOX in diesel engine exhaust gas are sufficiently reduced. Tend not to be.
  • the upper limit of the content of the cetane number improver is not particularly limited, but is preferably 1400 mass 1 > 111 or less, and 1250 mass ppm or less, based on the total amount of the gas oil composition. More preferably, it is more preferably 1100 ppm by mass or less, most preferably 10000 ppm by mass or less.
  • cetane number improver those synthesized according to a conventional method may be used, or a commercially available product may be used. It is to be noted that those sold as cetane number improvers are generally obtained by diluting an active ingredient contributing to cetane number improvement (that is, the cetane number improver itself) with an appropriate solvent. is there.
  • the gas oil composition of the present invention is prepared using such a commercially available product, the content of the active ingredient in the gas oil composition is preferably within the above range.
  • additives other than the above-mentioned cetane number improver can be blended as necessary.
  • a lubricity improver and Z or a clarifier are preferable. Be blended.
  • lubricity improver for example, one or more of a carboxylic acid type, an ester type, an alcohol type and a phenol type lubricity improver can be arbitrarily used.
  • carboxylic acids and carboxylic acids Stell based lubricity improvers are preferred.
  • Examples of the carboxylic acid-based lubricity improver include two kinds of linoleic acid, oleic acid, salicylic acid, palmitic acid, myristic acid, hexadecenoic acid, and the above carboxylic acids. A mixture of the above is mentioned.
  • ester-based lubricity improver examples include glycerin carbonate.
  • the carboxylic acid ester may comprise one kind or two or more kinds of carboxylic acids, and specific examples thereof include linoleic acid, oleic acid, salicylic acid, palmitic acid, myristic acid, and carboxylic acid. Xadecenoic acid and the like.
  • the compounding amount of the lubricity improver is preferably 35 mass ppm or more, more preferably 50 mass PM or more based on the total amount of the composition.
  • the upper limit of the compounding amount is preferably 150 ppm by mass or less, more preferably 150 ppm by mass or less based on the total amount of the composition, since an effect equivalent to the addition of gold cannot be obtained even if it is added more. More preferably, there is.
  • Detergents include, for example, imid-based compounds; arke-noresuccinic acid imids such as polybutenyl succinic anhydride synthesized from polybutenyl succinic anhydride and ethylene polyamines; Mid; Polyester alcohol such as pentaerythritol and polybutenyl succinic anhydride synthesized from polybutenyl succinic anhydride, etc. Estenole succinate; Copolymers such as copolymers of relay and vinylpyrrolidone with anolequinolemethacrylate, ashless detergents such as reaction products of carboxylic acid and amine, etc. Is mentioned. Among these, alkenyl succinic acid imide and a reaction product of carboxylic acid and amide are preferable. These detergents can be used alone or in combination of two or more.
  • alkenyl succinic acid imides examples include the case where alkenyl succinic acid imide having an average molecular weight of about 100 to 300 is used alone and the case where the average molecular weight is 7 In some cases, a mixture of alkenyl succinic acid having an average molecular weight of about 100 to 2000 and an alkenyl succinic acid having an average molecular weight of about 100 to 2000 may be used. .
  • the carboxylic acid constituting the reaction product of the carboxylic acid and the amine may be one kind or two or more kinds, and specific examples thereof include those having 12 to 24 carbon atoms.
  • Examples include fatty acids and aromatic carboxylic acids having 7 to 24 carbon atoms.
  • Fatty acids having 12 to 24 carbon atoms include, but are not limited to, linoleic acid, oleic acid, palmitic acid, myristic acid, and the like.
  • the aromatic carboxylic acids having 7 to 24 carbon atoms include, but are not limited to, benzoic acid and salicylic acid.
  • the amine constituting the reaction product of the carboxylic acid and the amine may be one kind or two or more kinds.
  • the amine used herein is typically oleynoleamine, but is not limited thereto, and various amines can be used.
  • the amount of the detergent is not particularly limited. However, in order to obtain the effect of adding the detergent, specifically, the effect of suppressing the clogging of the fuel injection nozzle, the amount of the detergent is determined based on the total amount of the composition. It is preferably at least 0 mass ppm, more preferably at least 60 mass pm, even more preferably at least 80 mass p. Addition of less than 30 ppm by mass may have no effect. On the other hand, if the compounding amount is too large, a corresponding effect cannot be expected, and on the contrary, NOx, PM, aldehydes, etc. in the exhaust gas of diesel engine may increase. Therefore, the amount of detergent is 300 mass! pm or less, more preferably 180 mass pm or less.
  • those commercially available as lubricity improvers or detergents have appropriate active ingredients that contribute to lubricity improvement or cleaning, respectively. It is usually obtained as diluted with a solvent.
  • the content of the active ingredient in the gas oil composition is preferably within the above range.
  • additives include, for example, low-temperature fluidity improvers such as ethylene-vinyl acetate copolymer and alkenyl succinate amide; antioxidants such as phenol-based and amine-based; metal deactivators such as salicylidene derivatives Antifreezing agents such as polyglycol ethers; Corrosion inhibitors such as aliphatic amines and alkenyl succinates; Antistatic agents such as ayuon, cationic and amphoteric surfactants; Coloring agents: silicone-based antifoaming agents and the like.
  • low-temperature fluidity improvers such as ethylene-vinyl acetate copolymer and alkenyl succinate amide
  • antioxidants such as phenol-based and amine-based
  • metal deactivators such as salicylidene derivatives
  • Antifreezing agents such as polyglycol ethers
  • Corrosion inhibitors such as aliphatic amines and alkenyl succinates
  • the addition amount of the other additives can be arbitrarily determined, but the addition amount of each additive is preferably 0.5% by mass or less, more preferably 0% by mass or less, based on the total amount of the gas oil composition. 2% by mass or less.
  • a hydrorefined gas oil having the specified properties is converted to a hydrogenation catalyst (Pt ZP d (Hydrogen-silica-alumina) under the conditions shown in Table 1 to obtain deep hydrorefined light oil 11 and deep hydrorefined light oil 12.
  • Pt ZP d Hydrofluoride-silica-alumina
  • Table 2 shows the amounts (the total aromatic content and the content of aromatics having two or more rings), the naphthene content, and the cetane index.
  • the thus obtained deep hydrorefined diesel oils 1 and Z or Z or the deep hydrorefined diesel oils 1 and 2 are each composed of hydrocracked gas oil, synthetic gas oil, deep hydrorefined kerosene, and hydrorefined kerosene. One or more of these were mixed, and the following additives were further blended to obtain each of the light oil compositions of Examples 1 to 3 having the compositions shown in Table 3.
  • Table 2 shows the properties of hydrocracked gas oil, synthetic gas oil, deep hydrorefined kerosene, and hydrorefined kerosene.
  • Lubricity improver carboxylic acid mixture containing linoleic acid as a main component
  • Detergent Reaction product of oleic acid with oleic acid as a main component
  • Low temperature fluidity improver Ethylene vinyl acetate copolymer.
  • Each gas oil composition of Comparative Examples 1 and 2 having the composition shown in Table 3 was prepared using the hydrorefined gas oil shown in Table 2, the synthetic gas oil, the deep hydrorefined kerosene, and the above additives.
  • Table 3 shows various properties of the light oil compositions of Comparative Examples 1 and 2.
  • Deep hydro-refined gas oil Deep hydro-refined gas oil
  • the scanning mobility particle size analyzer shown in Fig. 1 was used to separate the particles and detect the number of particles.
  • the flow path 11 for passing the diluted exhaust gas sample is provided with a charge distribution control unit 12, a classification unit 13, and a particle number measurement unit 14 in order from the upstream. .
  • the fine particles in the diluted exhaust gas are brought into an equilibrium charge distribution state in the charge distribution control unit 12, and are classified (separated) in the classification unit 13 according to the electric mobility of each particle. Then, in the particle number measuring section 14, the particles separated for each particle diameter are measured.
  • Table 4 shows the measurement results of the total number of PM particles. The values in Table 4 are relative to the total number of microparticles discharged during mode 13 when the gas oil composition of Comparative Example 1 was used as the test fuel and the result without DPF was 100. It is evaluated by value. [0110] (Evaluation of fuel efficiency characteristics)
  • a predetermined amount of the deep hydrorefined gas oil is contained in the gas oil composition, and the sulfur content, the aromatic content, the aromatic content of two or more rings, the naphthene content,
  • the density is set at 5 ° C, the 10% distilling temperature and the 90% distilling temperature within the above ranges respectively, the required characteristics as a future-type diesel fuel are provided, and the environmental load is reduced.
  • a gas oil composition capable of achieving a high level of reduction and improvement in fuel efficiency is realized.

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  • 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 une préparation de gazole contenant au moins 20% vol. de gazole, obtenue par un procédé hydraulique d'affinage par hydrotraitement d'une huile d'hydrofining ayant une teneur en soufre de 5 à 10 ppm en poids et une plage de points d'ébullition comprise entre 150 et 380 °C en présence d'un catalyseur d'hydrogénation et possédant une température de fonctionnement à 90 % comprise entre 200 et 380 °C, une densité à 15 °C de 780 à 870 kg/m3, une teneur en soufre de 5 ppm en poids ou moins, et une teneur en naphtène de 30 % en volume ou plus. Ladite préparation présente les propriétés suivantes : la teneur en soufre est de 5 ppm en poids ou moins ; la teneur en hydrocarbures aromatiques est de 10 % volume ou moins ; la teneur en hydrocarbures aromatiques bicycliques et supérieurs est de 1 % volume ou moins ; la teneur en naphtène est de 30 % en volume ou moins ; la densité à 15 °C est de 820 à 840 kg/m3 ; la température de fonctionnement à 10 % est de 250 °C ou moins ; et la température de fonctionnement à 90 % est de 320 °C ou moins.
PCT/JP2004/002917 2003-03-07 2004-03-05 Preparation de gazole et son procede de production WO2004078885A1 (fr)

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EP1956070A1 (fr) * 2005-11-30 2008-08-13 Nippon Oil Corporation Composition de gasoil
US8125327B2 (en) 2008-09-11 2012-02-28 Edward J. Ognibene Method for increasing vehicle brake/safety/hazard light visibility
US8541635B2 (en) 2006-03-10 2013-09-24 Shell Oil Company Diesel fuel compositions
US10494579B2 (en) 2016-04-26 2019-12-03 Exxonmobil Research And Engineering Company Naphthene-containing distillate stream compositions and uses thereof
US10550335B2 (en) 2015-12-28 2020-02-04 Exxonmobil Research And Engineering Company Fluxed deasphalter rock fuel oil blend component oils
US10550341B2 (en) 2015-12-28 2020-02-04 Exxonmobil Research And Engineering Company Sequential deasphalting for base stock production
US10590360B2 (en) 2015-12-28 2020-03-17 Exxonmobil Research And Engineering Company Bright stock production from deasphalted oil

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JP4987485B2 (ja) 2004-12-28 2012-07-25 Ｊｘ日鉱日石エネルギー株式会社 超低硫黄軽油基材又は超低硫黄軽油組成物の製造方法及び超低硫黄軽油組成物
CN101007969B (zh) * 2006-01-27 2011-04-20 中国石油化工股份有限公司 调合柴油的制备方法
JP5392993B2 (ja) * 2007-04-06 2014-01-22 Ｊｘ日鉱日石エネルギー株式会社 超低硫黄軽油基材の製造方法
US8632675B2 (en) * 2008-12-24 2014-01-21 Exxonmobil Research And Engineering Company Co-processing of diesel biofeed and heavy oil
JP5361499B2 (ja) * 2009-04-01 2013-12-04 Ｊｘ日鉱日石エネルギー株式会社 改質器付き予混合圧縮着火エンジン用燃料油組成物
WO2011061576A1 (fr) * 2009-11-20 2011-05-26 Total Raffinage Marketing Procédé pour la production de fluides hydrocarbures ayant une faible teneur en aromatiques
WO2011061575A1 (fr) 2009-11-20 2011-05-26 Total Raffinage Marketing Procédé pour la production de fluides hydrocarbures ayant une faible teneur en aromatiques
FR3015514B1 (fr) 2013-12-23 2016-10-28 Total Marketing Services Procede ameliore de desaromatisation de coupes petrolieres
CN103865577B (zh) * 2014-02-24 2015-05-27 中国海洋石油总公司 一种由催化裂化柴油生产轻质芳烃及清洁燃料油品的方法
US11441089B2 (en) * 2020-05-22 2022-09-13 ExxonMobil Technology and Engineering Company High napthenic content distillate fuel compositions

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EP1956070A1 (fr) * 2005-11-30 2008-08-13 Nippon Oil Corporation Composition de gasoil
EP1956070A4 (fr) * 2005-11-30 2013-06-19 Nippon Oil Corp Composition de gasoil
US8541635B2 (en) 2006-03-10 2013-09-24 Shell Oil Company Diesel fuel compositions
US8125327B2 (en) 2008-09-11 2012-02-28 Edward J. Ognibene Method for increasing vehicle brake/safety/hazard light visibility
US10550335B2 (en) 2015-12-28 2020-02-04 Exxonmobil Research And Engineering Company Fluxed deasphalter rock fuel oil blend component oils
US10550341B2 (en) 2015-12-28 2020-02-04 Exxonmobil Research And Engineering Company Sequential deasphalting for base stock production
US10590360B2 (en) 2015-12-28 2020-03-17 Exxonmobil Research And Engineering Company Bright stock production from deasphalted oil
US10647925B2 (en) 2015-12-28 2020-05-12 Exxonmobil Research And Engineering Company Fuel components from hydroprocessed deasphalted oils
US10808185B2 (en) 2015-12-28 2020-10-20 Exxonmobil Research And Engineering Company Bright stock production from low severity resid deasphalting
US10947464B2 (en) 2015-12-28 2021-03-16 Exxonmobil Research And Engineering Company Integrated resid deasphalting and gasification
US10494579B2 (en) 2016-04-26 2019-12-03 Exxonmobil Research And Engineering Company Naphthene-containing distillate stream compositions and uses thereof

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CN1745161A (zh) 2006-03-08
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CN100510017C (zh) 2009-07-08
JP2004269685A (ja) 2004-09-30

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