WO2004078887A1 - 軽油留分の水素化処理方法 - Google Patents
軽油留分の水素化処理方法 Download PDFInfo
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- WO2004078887A1 WO2004078887A1 PCT/JP2004/002784 JP2004002784W WO2004078887A1 WO 2004078887 A1 WO2004078887 A1 WO 2004078887A1 JP 2004002784 W JP2004002784 W JP 2004002784W WO 2004078887 A1 WO2004078887 A1 WO 2004078887A1
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- Prior art keywords
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- gas oil
- volume
- sulfur
- aromatic
- Prior art date
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- 238000000034 method Methods 0.000 title claims abstract description 32
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 79
- 239000011593 sulfur Substances 0.000 claims abstract description 78
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 77
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 45
- 239000003054 catalyst Substances 0.000 claims abstract description 43
- 238000009835 boiling Methods 0.000 claims abstract description 14
- 125000003118 aryl group Chemical group 0.000 claims description 94
- 239000007789 gas Substances 0.000 claims description 83
- 238000006243 chemical reaction Methods 0.000 claims description 37
- 229910052739 hydrogen Inorganic materials 0.000 claims description 29
- 239000001257 hydrogen Substances 0.000 claims description 29
- 229910052751 metal Inorganic materials 0.000 claims description 29
- 239000002184 metal Substances 0.000 claims description 29
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 28
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 16
- 229910021536 Zeolite Inorganic materials 0.000 claims description 15
- 239000007788 liquid Substances 0.000 claims description 15
- 239000010457 zeolite Substances 0.000 claims description 15
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 14
- 239000000203 mixture Substances 0.000 claims description 13
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 claims description 11
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 9
- 239000012188 paraffin wax Substances 0.000 claims description 8
- 239000003209 petroleum derivative Substances 0.000 claims description 8
- -1 polya Chemical compound 0.000 claims description 8
- 239000002994 raw material Substances 0.000 claims description 8
- 239000000377 silicon dioxide Substances 0.000 claims description 7
- 229910052763 palladium Inorganic materials 0.000 claims description 6
- 150000002739 metals Chemical class 0.000 claims description 5
- 229910052697 platinum Inorganic materials 0.000 claims description 5
- 229910052741 iridium Inorganic materials 0.000 claims description 4
- 229910052707 ruthenium Inorganic materials 0.000 claims description 4
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 3
- 229910052698 phosphorus Inorganic materials 0.000 claims description 3
- 239000011574 phosphorus Substances 0.000 claims description 3
- 229910052782 aluminium Inorganic materials 0.000 claims description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims 1
- 239000003205 fragrance Substances 0.000 claims 1
- 239000010936 titanium Substances 0.000 claims 1
- 229910052719 titanium Inorganic materials 0.000 claims 1
- 239000003208 petroleum Substances 0.000 abstract description 5
- 229930195733 hydrocarbon Natural products 0.000 abstract description 4
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 4
- 239000003921 oil Substances 0.000 description 114
- 238000006477 desulfuration reaction Methods 0.000 description 19
- 230000023556 desulfurization Effects 0.000 description 19
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 17
- 239000003350 kerosene Substances 0.000 description 13
- 239000002904 solvent Substances 0.000 description 12
- 239000000463 material Substances 0.000 description 10
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 8
- 239000010779 crude oil Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- KDLHZDBZIXYQEI-UHFFFAOYSA-N palladium Substances [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 8
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Substances [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 7
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 6
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000002131 composite material Substances 0.000 description 5
- 238000004821 distillation Methods 0.000 description 5
- 230000007613 environmental effect Effects 0.000 description 5
- 239000000446 fuel Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 150000003464 sulfur compounds Chemical class 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 3
- 150000001491 aromatic compounds Chemical class 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000010335 hydrothermal treatment Methods 0.000 description 3
- 238000011068 loading method Methods 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- 239000011148 porous material Substances 0.000 description 3
- 238000002360 preparation method Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 229910052703 rhodium Inorganic materials 0.000 description 3
- 238000003786 synthesis reaction Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- KHCPSOMSJYAQSY-UHFFFAOYSA-L azane;dichloroplatinum Chemical compound N.N.N.N.Cl[Pt]Cl KHCPSOMSJYAQSY-UHFFFAOYSA-L 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- IYYZUPMFVPLQIF-ALWQSETLSA-N dibenzothiophene Chemical class C1=CC=CC=2[34S]C3=C(C=21)C=CC=C3 IYYZUPMFVPLQIF-ALWQSETLSA-N 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 239000012013 faujasite Substances 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000005755 formation reaction Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 238000005342 ion exchange Methods 0.000 description 2
- 238000005555 metalworking Methods 0.000 description 2
- 239000011259 mixed solution Substances 0.000 description 2
- 229910052680 mordenite Inorganic materials 0.000 description 2
- 230000009257 reactivity Effects 0.000 description 2
- 125000001424 substituent group Chemical group 0.000 description 2
- 238000010998 test method Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- DGUACJDPTAAFMP-UHFFFAOYSA-N 1,9-dimethyldibenzo[2,1-b:1',2'-d]thiophene Natural products S1C2=CC=CC(C)=C2C2=C1C=CC=C2C DGUACJDPTAAFMP-UHFFFAOYSA-N 0.000 description 1
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 description 1
- MYAQZIAVOLKEGW-UHFFFAOYSA-N 4,6-dimethyldibenzothiophene Chemical compound S1C2=C(C)C=CC=C2C2=C1C(C)=CC=C2 MYAQZIAVOLKEGW-UHFFFAOYSA-N 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 1
- 241000640882 Condea Species 0.000 description 1
- 229910020515 Co—W Inorganic materials 0.000 description 1
- 229910003296 Ni-Mo Inorganic materials 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 229910002848 Pt–Ru Inorganic materials 0.000 description 1
- 229910018879 Pt—Pd Inorganic materials 0.000 description 1
- 229910018967 Pt—Rh Inorganic materials 0.000 description 1
- 239000004115 Sodium Silicate Substances 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 239000010692 aromatic oil Substances 0.000 description 1
- 238000005899 aromatization reaction Methods 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 230000000711 cancerogenic effect Effects 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 238000006757 chemical reactions by type Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000002734 clay mineral Substances 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000013527 degreasing agent Substances 0.000 description 1
- 238000005237 degreasing agent Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000004231 fluid catalytic cracking Methods 0.000 description 1
- 238000004128 high performance liquid chromatography Methods 0.000 description 1
- 150000004678 hydrides Chemical class 0.000 description 1
- 150000004679 hydroxides Chemical class 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 229910021432 inorganic complex Inorganic materials 0.000 description 1
- 229910052809 inorganic oxide Inorganic materials 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 239000002917 insecticide Substances 0.000 description 1
- 238000004898 kneading Methods 0.000 description 1
- 239000004922 lacquer Substances 0.000 description 1
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 229910052750 molybdenum Inorganic materials 0.000 description 1
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
- 229910052911 sodium silicate Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 125000004434 sulfur atom Chemical group 0.000 description 1
- 238000010557 suspension polymerization reaction Methods 0.000 description 1
- 150000004685 tetrahydrates Chemical class 0.000 description 1
- 239000000341 volatile oil Substances 0.000 description 1
- ZXAUZSQITFJWPS-UHFFFAOYSA-J zirconium(4+);disulfate Chemical compound [Zr+4].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O ZXAUZSQITFJWPS-UHFFFAOYSA-J 0.000 description 1
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
- C10G45/44—Hydrogenation of the aromatic hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/08—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y
- B01J29/10—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the faujasite type, e.g. type X or Y containing iron group metals, noble metals or copper
- B01J29/12—Noble metals
- B01J29/126—Y-type faujasite
-
- 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
- C10G2300/1048—Middle distillates
- C10G2300/1059—Gasoil having a boiling range of about 330 - 427 °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
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4018—Spatial velocity, e.g. LHSV, WHSV
-
- 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 method for hydrotreating a gas oil fraction.
- the petroleum gas oil fraction contains 1 to 3% by mass of sulfur in an unrefined state, and is used as a gas oil base material after hydrodesulfurization.
- Other gas oil base materials include cracked gas oil obtained from hydro-desulfurized kerosene fractions, catalytic crackers and hydrocrackers. After mixing with these base materials, it becomes the product light oil.
- sulfur compounds present in the gas oil fraction hydrodesulfurized by the hydrodesulfurization catalyst,
- Dibenzothiophene derivatives having a plurality of methyl groups as substituents are extremely poor in reactivity, so that even if the depth of hydrodesulfurization is increased, such compounds cannot be used. There is a tendency to remain until the end. Therefore, in order to advance desulfurization to a lower sulfur region of 1 mass ppm or less using conventional technologies, a very high hydrogen partial pressure or an extremely long contact time, that is, an extremely large reactor volume, is required. I will.
- the unrefined petroleum gas oil fraction generally contains 20 to 40% by volume of an aromatic component. It exists in the state of the above-mentioned condensed aromatic compound. In the aromatic hydrogenation reaction, there is a restriction on the chemical equilibrium. In general, the equilibrium shifts to aromatics on the high temperature side and naphthenes as ring hydrides on the low temperature side. For this reason, the low temperature side is advantageous for promoting aromatic hydrogenation, but it has been pointed out that the reaction at a low temperature requires reaction conditions and a catalyst having a sufficient aromatic hydrogenation reaction rate at the low temperature side. There are major challenges in this regard. Noble metal-based catalysts are catalysts that exhibit sufficient aromatic hydrogenation activity at low temperatures.
- the catalyst has insufficient sulfur resistance and the sulfur content in the feedstock is high, the catalyst hydrogen Activity is inhibited and sufficient aromatic hydrogenation ability is not exhibited.
- the hydrodesulfurization reaction ultimately cleaves the carbon-sulfur bond, and the higher the temperature, the faster the reaction. Therefore, in the conventional technology, if the reaction conditions are set on the low temperature side in order to promote aromatic hydrogenation, the desulfurization activity becomes insufficient, and it is necessary to achieve both ultra-low sulfur and low aromaticity. Was extremely difficult.
- JP-A-7-155610 and JP-A-8-2837474 disclose a desulfurization step (first step), a zeolite clay mineral, and a desulfurization step.
- the production technology combining the two steps of the aromatic hydrogenation step (second step) using the compound as a catalyst has been proposed. Disclosure of the invention
- the present invention has been made in view of the above-mentioned problems of the related art, and has a sulfur content of 1 mass ppm or less excellent in environmental characteristics and a total aromatic content of 1 volume. Hydrogen treatment of gas oil fractions that can efficiently and surely produce so-called “sulfur zero” and “aloma zero” gas oil fractions of less than 10% without special operating conditions or capital investment. It aims to provide a method.
- the present inventors have conducted intensive studies to achieve the above object, and as a result, have found that a sulfur content, a total aromatic content, and a gas oil equivalent fraction having a boiling point within a predetermined range are obtained.
- a sulfur content, a total aromatic content, and a gas oil equivalent fraction having a boiling point within a predetermined range are obtained.
- the present invention provides a sulfur content of 5 to 15 mass ppm.
- a hydrogenated refined oil of a petroleum hydrocarbon having a total aromatic content of 10 to 25% by volume and a boiling point range of 150 to 380 ° C is used as a feedstock, and the feedstock is subjected to a hydrogenation catalyst.
- Hydrotreatment in the presence of a solvent provides an ultra-low sulfur / low aromatic gas oil fraction with a sulfur content of 1 mass ppm or less and a total aromatic content of 1% by volume or less. Hydrogen treatment method for gas oil fraction.
- the present invention is characterized by being obtained by the method of the present invention, wherein the sulfur content is 1 mass ppm or less and the total aromatic content is 1 volume% or less. Ultra low sulfur ⁇ In low aromatic gas oil fractions.
- the present invention relates to an ultra-low sulfur / low sulfur content in which the sulfur content obtained by the method of the present invention is 1 mass ppm or less and the total aromatic content is 1 vol% or less.
- a gas oil composition comprising an aromatic gas oil fraction.
- reaction conditions in the hydrogenation treatment are as follows: reaction temperature: 170 to 320 ° C., hydrogen partial pressure: 2 to 10 MPa, liquid space velocity: 0.1 to 2 ! ! — 1 , preferably a hydrogen / oil ratio of 100 to 800 NL / L.
- reaction temperature 170 to 320 ° C.
- hydrogen partial pressure 2 to 10 MPa
- liquid space velocity 0.1 to 2 ! ! — 1
- a hydrogen / oil ratio of 100 to 800 NL / L preferably a hydrogen / oil ratio of 100 to 800 NL / L.
- the one-ring aromatic content in the raw material oil is 9 to 18% by volume, and the two- or more-ring aromatic content is 1 to 7% by volume.
- the content of two or more rings in the ultra-low sulfur / low aromatic gas oil fraction is not more than 0.2% by volume, and (ii) the paraffin content in the feedstock oil.
- the amount is 30 to 60% by volume
- the naphthene content is 25 to 60% by volume
- the content of paraffin in the ultra-low sulfur / low aromatic gas oil fraction is 30 to 60% by volume. %
- the naphthene content is preferably 40 to 70% by volume.
- the hydrogenation catalyst according to the present invention is one in which at least one active metal of Group 8 metals is supported on a porous carrier.
- the porous carrier is composed of alumina and at least one selected from the group consisting of titania, zirconia, polya, silica, phosphorus and zeolite; or Z or (Ii) More preferably, the active metal is at least one metal selected from the group consisting of Ru, Rd, Ir, Pd and Pt.
- a petroleum system having a sulfur content of 5 to 15 mass ppm, a total aromatic content of 10 to 25% by volume, and a boiling range of 150 to 38 ° C. Hydrorefined hydrocarbon oil is used as a feedstock oil.
- the crude feedstock to be hydrorefined is a fraction corresponding to a predetermined boiling point range obtained from an atmospheric distillation unit, and is obtained from a hydrocracking unit and a residual oil direct desulfurization unit.
- a fraction having a corresponding boiling point range may be mixed and used.
- the kerosene fraction and the gas oil fraction may be mixed separately after hydrorefining in a predetermined boiling point range.
- a gas oil-equivalent fraction obtained from a fluid catalytic cracking unit (FCC) may be mixed and subjected to hydrorefining. Power
- the gas oil-equivalent fraction from FCC has a higher aromatic content than the above-mentioned respective fractions.
- the mixing amount is preferably 40 volumes. / 0 or less, more preferably 30% by volume or less.
- the conditions for hydrorefining the crude feed oil may be the conditions for processing using a general hydrodesulfurization unit in petroleum refining. That is, generally, the reaction temperature is 250 to 380 ° (hydrogen partial pressure is 2 to 8 MPa, liquid space velocity (LHSV) is 0.3 to: 10.Oh— 1 , hydrogen Z Oil ratio 100 to 500 NL
- the crude oil is divided into a kerosene fraction and a gas oil fraction in a normal-pressure distillation unit, and each hydrorefined separately, and then mixed and used as a feedstock. Is also good.
- a catalyst used for hydrorefining of crude oil a general hydrodesulfurization catalyst can be used. That is, as the active metal, a sulfide of a Group 6A or Group 8 metal is usually used, and examples thereof include Co—Mo, Ni—Mo, Co—W, and Ni—W. .
- the carrier a porous inorganic oxide containing alumina as a main component is used.
- the reaction conditions and catalyst used in the hydrorefining of crude oil are not particularly limited as long as the properties of the obtained oil satisfy the above conditions.
- the configurations of the respective devices and the combination of the devices in the hydrorefining of the crude feedstock and the hydrotreating of the feedstock are not particularly limited, but are obtained by hydrorefining. It is desirable to remove the hydrogen sulfide contained in the product by a gas-liquid separation column or specified hydrogen sulfide removal equipment as much as possible. In a general gas oil or kerosene desulfurizer, gas and liquid are separated by a gas-liquid separation tower after being desulfurized by a reaction tower.
- the present invention can be implemented by setting appropriate hydrogenation treatment conditions.
- the feedstock according to the present invention is obtained by hydrorefining the above crude feedstock, and has a sulfur content of 5 to 15 mass ppm, a total aromatic content of 10 to 25% by volume, and a boiling range of 1 It has properties such as 50-380.
- the feedstock oil used in the present invention has a boiling point range of 150 to 380 ° C, but a kerosene fraction having a boiling point range of 150 to 240 ° C. And a gas oil fraction having a boiling point range of 200 to 380 ° C. may be mixed after hydrorefining individually.
- the temperature at which kerosene and gas oil are classified may fluctuate due to trends in supply and demand of each product and the characteristics of the distillation apparatus, and the classification temperature is not particularly limited to the above temperature.
- the boiling point range in the present specification is a value measured according to the method described in JISK2254 “Petroleum product-evaporation test method”.
- the feedstock used in the present invention has a sulfur content of 5 to 15 mass ppm, preferably 5 to 10 mass ppm. If the sulfur content of the feedstock is greater than 1 5 mass pp m is the low activity of the hydrogenation catalyst And the desulfurization reaction and aromatic hydrogenation reaction do not proceed sufficiently.
- the sulfur content in this specification refers to the total amount of gas oil fraction measured according to the method described in JISK2541 “Sulfur content test method” or ASTM-D5453. Means the mass content of the sulfur component.
- the total aromatic content of the feedstock oil used in the present invention is from 10 to 25% by volume, and preferably from 11 to 20% by volume. If the total aromatic content of the feedstock exceeds 25% by volume, a long contact time, that is, an excessive reactor volume, is required to achieve a total aromatic content of 1% by volume or less, If the capital investment is excessive, on the other hand, if it is less than 10% by volume, the operating conditions required for aromatic hydrogenation become excessive compared to desulfurization, and the economic advantage of the present invention is reduced.
- the content of one-ring aromatic component is 9 to 18% by volume
- the content of two- or more-ring aromatic component is
- the content is 1 to 7% by volume
- the content of one-ring aromatics is 10.5 to 15% by volume
- the content of aromatics having two or more rings is 1.5 to 5% by volume. More preferred.
- the total aromatic component content is 1% by volume or less. In order to achieve a content of 0.2% by volume or less, capital investment tends to be excessive.
- the content is less than the above lower limit, the operating conditions required for aromatic hydrogenation are excessive compared to desulfurization. Therefore, the economic advantage of the present invention tends to decrease.
- the total aromatic content, the one-ring aromatic content, and the two- or more-ring aromatic content in this specification are those published by the Japan Petroleum Institute. Journal of the Japan Petroleum Institute JPI — 5 S— 4 9 1 9 7 “Hydrocarbons Thailand Means the percentage by volume (volume%) of each aromatic content measured in accordance with the method described in "Test Method-High Performance Liquid Chromatography".
- the composition other than the aromatic component in the feedstock oil according to the present invention has a paraffin content of 3 from the viewpoint of maintaining the fuel oil density of the product gas oil and improving fuel efficiency.
- the content is 0 to 60% by volume
- the naphthene content is 25 to 60% by volume
- the olefin content is 1% by volume or less.
- the naphthene content, paraffin content, and olefin content in this specification are defined as ASTM D2786-91 "Standardlest Methodfor Hydrocarbon Types A nalysisof Gas-O il Saturates
- F r a c t i o n b y H i g h I o n i z i n g V o 1 t a g e Ma s s S p e c t r o m e t r y means the volume percentage (volume%) of each component measured in accordance with the method described in “Fr a c t i o n b y H i g h I o n i z i n g i
- the feedstock (hydrorefined oil) having a sulfur content, a total aromatic content and a boiling point within a predetermined range is used as a hydrogenation catalyst.
- a hydrogenation catalyst By hydrotreating in the presence, an ultra-low sulfur / low aromatic gas oil fraction having a sulfur content of 1 mass ppm or less and a total aromatic content of 1% by volume or less is obtained.
- the feedstock is subjected to hydrotreatment in the presence of a hydrogenation catalyst.
- a hydrogenation active metal is supported on a porous carrier.
- a porous carrier a carrier composed of at least one kind selected from the group consisting of titania, zirconia, polya, silica, phosphorus and zeolite and alumina is preferable.
- the production method is not particularly limited, any preparation method can be adopted using raw materials in a state such as various sols and salt compounds corresponding to each element.
- any of the preparation steps in the state of alumina gel or other hydroxide or in the form of an appropriate solution It may be prepared by adding in the step.
- the ratio of alumina to other components may be any ratio to the porous carrier, but preferably the alumina content is 90% by mass or less, more preferably 60% by mass or less, more preferably 4% by mass or less. 0 mass. / 0 or less.
- the lower limit of the alumina content is not particularly limited, but the alumina content is preferably 20% by mass or more.
- zeolite is a crystalline aluminosilicate, and includes faujasite, pentasil, mordenite, and the like.
- the zeolite is prepared by adjusting the alumina content in zeolite during the synthesis of zeolite, or Those which are ultra-stabilized by a predetermined hydrothermal treatment and a no or acid treatment can be used.
- faujasite, beta and mordenite are used, particularly preferably Y-type and beta-type. It is preferable that the Y-type is ultra-stabilized.
- the zeolite ultra-stabilized by hydrothermal treatment has a pore structure of 20 to 100 A in addition to the original pore structure called micropores of 20 A or less. It is preferable that new pores are formed in the fin.
- Known conditions can be used as such hydrothermal treatment conditions.
- the active metal of the catalyst used in the hydrogenation treatment is preferably at least one metal selected from Group 8 metals, and is preferably Ru, Rd, Ir, Pd and Pt. More preferably, it is at least one metal selected from the group consisting of: Pd and Z or Pt are particularly preferred.
- Such an active metal may be a combination of these metals, for example, Pt—Pd, Pt—Rh, Pt-Ru, Ir-Pd, Ir-Rh, Ir -Ru, Pt-Pd-Rh, Pt-Rh-Ru, Ir-Pd-Rh, Ir-Rh-Ru, etc. .
- a common inorganic salt or complex salt compound can be used, and as a supporting method, any of a supporting method used for a normal hydrogenation catalyst such as an impregnation method and an ion exchange method can be used.
- a plurality of metals When a plurality of metals are supported on the porous carrier, they may be simultaneously supported using a mixed solution, or may be sequentially supported using a single solution.
- a metal salt solution may be an aqueous solution or a solution using an organic solvent.
- the metal loading on the porous carrier may be carried out after completion of all the steps of preparing the constituted porous carrier, and an appropriate oxide or complex oxide may be used in the intermediate step of preparing the porous carrier. After pre-loading the metal on the material, zeolite, etc., a further gel preparation step, heat concentration, kneading, etc. may be performed.
- the amount of the active metal supported on the catalyst used for the hydrotreating is not particularly limited, but preferably 0.1 to 10% by mass, more preferably 0.1 to 10% by mass of the total amount of the metal relative to the total amount of the catalyst. It is from 5 to 5% by mass, particularly preferably from 0.2 to 3% by mass.
- the hydrogenation catalyst according to the present invention is preferably used after performing a preliminary reduction treatment under a hydrogen stream. That is, in general, a gas containing hydrogen flows through a reaction tube filled with a hydrogenation catalyst, and heat of 200 ° C. or more is given according to a predetermined procedure, whereby the active metal on the catalyst is reduced. However, it will exhibit hydrogenation activity.
- the conditions of the hydrogenation treatment in the present invention include a reaction temperature of 170 to 320 ° C., a hydrogen partial pressure of 2 to 10 MPa, a liquid hourly space velocity (LHSV) of 0.1 to 2 h—Hydrogen / oil ratio 100-800 N LZL is preferred, reaction temperature 175-310 ° C, hydrogen partial pressure 2.5-8 MPa, liquid space velocity (LH SV) 0.2 to 1.5 h—], hydrogen oil ratio is more preferably 150 to 0.60 N LZ L, reaction temperature is 180 to 300 ° C, hydrogen is Partial pressure 3 -7 MPa, liquid hourly space velocity (LH SV) 0.3-1.2 h Hydrogen / oil ratio of 150-500 NL / L is particularly preferred.
- reaction temperature is lower than the lower limit, the desulfurization reaction tends not to proceed sufficiently.On the other hand, the reaction temperature is lower than the upper limit. If it exceeds, the aromatic formation reaction tends to be advantageous. Also, the higher the hydrogen partial pressure and the hydrogen oil ratio, the more the desulfurization and hydrogenation reactions tend to be promoted. However, if the hydrogen partial pressure and the hydrogen Z oil ratio are below the lower limits, desulfurization and aroma When the group hydrogenation reaction does not proceed sufficiently, on the other hand, when the hydrogen partial pressure and the hydrogen Z oil ratio exceed the upper limits, excessive capital investment tends to be required.
- liquid hourly space velocity LHSV
- desulfurization and aromatic hydrogenation reaction tend not to proceed sufficiently.
- the apparatus for hydrotreating the feedstock thus hydrorefined may be of any configuration, and the reaction tower may be used alone or in combination of two or more to reduce the concentration of hydrogen sulfide in the reaction tower.
- a gas-liquid separation facility or other hydrogen sulfide removal facility may be provided before the reaction tower or between a plurality of reaction towers, and hydrogen may be additionally injected.
- the reaction type of the hydrotreating apparatus used in the present invention may be a fixed bed system. That is, hydrogen can be in either a countercurrent or co-current form with respect to the feed oil, or can be a type having a plurality of reaction towers and a combination of counter-current and co-current. As a general form, there is a down flow, and there is a gas-liquid dual co-current form.
- the reaction tower may be composed of a plurality of catalyst beds, and between each catalyst bed, heat of reaction is removed, or hydrogen is removed. Hydrogen gas may be injected as a quench for the purpose of increasing the pressure.
- the sulfur content is reduced to 1 mass ppm or less.
- the ultra-low sulfur / low aromatic gas oil fraction of the present invention having a total aromatic content of 1% by volume or less can be obtained efficiently and reliably without special operating conditions and no capital investment.
- the desulfurization reaction can proceed extremely efficiently besides performing hydrotreating using a distillate that has been hydrorefined to a sulfur content of 5 to 15 mass ppm. This is due to the fact that the sulfur compound, which is one of the factors that cause a decrease in the activity of the hydrogenation catalyst, is small, and the desulfurization reaction speed is improving.
- the hydrorefined oil desulfurized to a sulfur content of 5 to 15 mass ppm still contains aromatics of 10 to 25% by volume, but the raw material oil contains few sulfur compounds. As a result, the aromatic hydrogenation reaction is promoted simultaneously with the desulfurization reaction.
- the sulfur content is 1 mass ppm or less and the total aromatic content is 1 vol% or less.
- the present inventors presume that characteristics that could not be achieved at the same time will be achieved at the same time.
- the ultra-low sulfur / low aromatic gas oil fraction of the present invention has a sulfur content of 1 mass ppm or less and a total aromatic content of 1% by volume obtained by the method of the present invention.
- the following are equivalent to so-called ultra-clean diesel fuel. According to such ultra-low sulfur and low aromatic gas oil, the generation of particulates in diesel vehicle exhaust gas is sufficiently prevented, and the prolonged life of the exhaust gas purification device can be achieved without lowering fuel efficiency etc. It is possible.
- the content of two or more rings and aromatic components can be set to 0.2% by volume or less. In such a case, the remaining aromatics are all one-ring aromatics.
- the aromatic compound having two or more rings is preferably extremely small, and the aromatic compound having two or more rings is preferably used.
- the content is more than 0.2% by volume, it tends to be unfavorable from the viewpoint of preventing the formation of particulates.
- the composition other than the aromatic component in the ultra-low sulfur / low aromatic gas oil fraction of the present invention has a paraffin content of 30 to 60 from the viewpoint of reducing the environmental load and maintaining the fuel oil density, that is, fuel efficiency. It is preferable that the content by volume, the naphthene content be 40 to 70 volume%, and the content of the olefin component be 1 volume% or less.
- the ultra-low sulfur / low aromatic gas oil fraction of the present invention described above may be used alone as diesel gas oil.
- the light oil composition of the present invention in which components such as a base material are mixed may be used as diesel light oil. That is, the gas oil composition of the present invention has a sulfur content obtained by the method of the present invention of 1 mass ppm or less and It is characterized by containing an ultra-low sulfur / low aromatic gas oil fraction with a total aromatic content of 1% by volume or less. Even when the diesel composition of the present invention is used as diesel gas oil, due to the excellent characteristics of the ultra-low sulfur and low aromatic gas oil fraction of the present invention, generation of particulates in diesel vehicle exhaust gas is maintained while maintaining fuel efficiency. Is sufficiently prevented, and the life of the exhaust gas purification device can be extended easily.
- other base materials that can be blended with the gas oil composition of the present invention include a gas oil base material other than the ultra-low sulfur / low aromatic gas oil fraction of the present invention, a kerosene base material, and the like.
- a gas oil base material other than the ultra-low sulfur / low aromatic gas oil fraction of the present invention a kerosene base material, and the like.
- These synthetic kerosene and synthetic diesel oil are characterized by containing almost no aromatic components and mainly containing saturated hydrocarbons.
- a known method can be used as a method for producing the synthesis gas, and is not particularly limited.
- the blending ratio of such a synthetic gas oil is preferably 30% by volume or less, more preferably 20% by volume or less, further preferably 10% by volume or less in the gas oil composition.
- the blending ratio of the synthetic kerosene in the light oil composition is preferably 60% by volume or less, more preferably 50% by volume or less, and further preferably 40% by volume or less.
- the ultra-low sulfur / low aromatic gas oil fraction of the present invention can be used not only for diesel gas oil, but also for ink solvents, cleaning solvents, insecticide solvents, aerosol solvents, and solutions. Or solvent for suspension polymerization, degreasing agent, solvent for lacquer, solvent for washing, extraction, paint, etc., rubber volatile oil, solvent for cleaning metal parts, metalworking oil such as aluminum rolling, sealing oil It can be suitably used as a base material for agents and solvents for coating. [Example] Hereinafter, the present invention will be described more specifically with reference to Examples and Comparative Examples, but the present invention is not limited to the following Examples.
- the zirconia-alumina composite hydroxide was adjusted from the slurry, the water content was adjusted by heat concentration, extrusion molding, drying, and calcination to obtain a catalyst carrier (porous carrier).
- the ratio of each component in the obtained carrier was 20% by mass of alumina, 57% by mass of silica, and 23% by mass of zirconia as oxides.
- catalyst 1 (55.2 g) was charged into a reaction tube having an inner diameter of 20 mm, and the reaction tube was attached to a fixed-bed flow-type reactor. a, Pre-reduction treatment was performed under the condition of 300 ° C. Then, under the conditions shown in Table 1, a hydrotreating test was conducted using feedstock A having the properties shown in Table 2. gave.
- Feedstock A was obtained by hydrorefining a distillate equivalent to light oil (crude feedstock) obtained by atmospheric distillation of Middle Eastern crude oil and had a sulfur content of 11. It is 0 mass ppm and has a total aromatic content of 17.9% by volume. Also, in Table 2 ', 18? Is the first stop point defined in 13K2254, and EP is the end point defined in JISK2254.
- the sulfur content in the product oil obtained on day 10 from the start of the hydrotreating test was 0.5 mass ppm and the total aromatic content was 0.6 vol%. there were. Table 2 shows the properties of this oil.
- the sulfur content in the product oil obtained 30 days after the start of the hydrotreating test was 0.8 mass ppm.
- ammonium zeolite was treated with tetraammineplatinum (II) chloride and tetraamminepalladium (II) whose concentration was adjusted to a volume corresponding to the water absorption of the carrier.
- the mixture was added to a mixed solution of chloride, stirred at 70 ° C, and supported on a metal by an ion exchange method. After loading the metal, zeolite was separated by filtration, dried, and fired. Then, the obtained zeolite was kneaded with a commercially available alumina gel (manufactured by Condea Corporation), and was molded to obtain a hydrogenation catalyst 2.
- the supported amounts of platinum and palladium in Catalyst 2 were 0.3% by mass and 0.5% by mass, respectively, based on the entire catalyst.
- the ratio between zeolite and alumina was 70:30 by mass.
- Example 2 a hydrotreating test was performed in the same manner as in Example 1 except that the catalyst 2 was used.
- the sulfur content in the product oil obtained on the 10th day from the start of the hydrotreating test was 0.2 mass ppm, and the total aromatic content was 0.2% by volume.
- Table 2 shows the properties of this oil.
- Feedstock B is obtained by hydrorefining a light oil equivalent fraction (crude feedstock) obtained by atmospheric distillation of Middle Eastern crude oil and has a sulfur content of 25.3 mass ppm. in and total aromatic content is of 1-9. 5 vol 0/0.
- the sulfur content in the product oil obtained on day 10 from the start of the hydrotreating test was 4.9 mass ppm and the total aromatic content was 4.5 vol%. there were. Table 2 shows the properties of this oil.
- the sulfur content in the product oil obtained 30 days after the start of the hydrotreating test was 7.2 mass ppm.
- a gas oil fraction having excellent environmental properties and having a sulfur content of 1 mass ppm or less and a total aromatic content of 1 vol% or less is obtained. Efficient and reliable production without special operating conditions or capital investment
Abstract
Description
Claims
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JP2005503113A JP4576333B2 (ja) | 2003-03-07 | 2004-03-05 | 軽油留分の水素化処理方法 |
US10/548,315 US20060260983A1 (en) | 2003-03-07 | 2004-03-05 | Method of hydrotreating gas oil fraction |
EP04717744A EP1614739A4 (en) | 2003-03-07 | 2004-03-05 | PROCESS FOR HYDROTREATING A GAS-OIL FRACTION |
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US (1) | US20060260983A1 (ja) |
EP (1) | EP1614739A4 (ja) |
JP (1) | JP4576333B2 (ja) |
CN (1) | CN100412171C (ja) |
WO (1) | WO2004078887A1 (ja) |
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JP2006160885A (ja) * | 2004-12-07 | 2006-06-22 | Japan Energy Corp | 軽油基材及び軽油、並びにそれらの製造方法 |
JP2007153937A (ja) * | 2005-11-30 | 2007-06-21 | Nippon Oil Corp | 軽油組成物 |
JP2007153938A (ja) * | 2005-11-30 | 2007-06-21 | Nippon Oil Corp | 軽油組成物 |
WO2007114505A1 (ja) * | 2006-03-31 | 2007-10-11 | Nippon Oil Corporation | 多機能性炭化水素油組成物 |
JP2008007579A (ja) * | 2006-06-28 | 2008-01-17 | Japan Energy Corp | 超低硫黄軽油基材の製造方法及び該超低硫黄軽油基材を含む超低硫黄軽油組成物 |
JP2013514433A (ja) * | 2009-12-16 | 2013-04-25 | シェブロン ユー.エス.エー. インコーポレイテッド | ディーゼル組成物及びその作製法 |
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JP2008007579A (ja) * | 2006-06-28 | 2008-01-17 | Japan Energy Corp | 超低硫黄軽油基材の製造方法及び該超低硫黄軽油基材を含む超低硫黄軽油組成物 |
JP2013514433A (ja) * | 2009-12-16 | 2013-04-25 | シェブロン ユー.エス.エー. インコーポレイテッド | ディーゼル組成物及びその作製法 |
JP2015172206A (ja) * | 2009-12-16 | 2015-10-01 | シェブロン ユー.エス.エー. インコーポレイテッド | ディーゼル組成物及びその作製法 |
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JPWO2004078887A1 (ja) | 2006-06-08 |
CN1759163A (zh) | 2006-04-12 |
EP1614739A4 (en) | 2012-11-21 |
EP1614739A1 (en) | 2006-01-11 |
CN100412171C (zh) | 2008-08-20 |
US20060260983A1 (en) | 2006-11-23 |
JP4576333B2 (ja) | 2010-11-04 |
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