TWI458819B - 高品質環烷基油之製造方法 - Google Patents
高品質環烷基油之製造方法 Download PDFInfo
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- TWI458819B TWI458819B TW097139715A TW97139715A TWI458819B TW I458819 B TWI458819 B TW I458819B TW 097139715 A TW097139715 A TW 097139715A TW 97139715 A TW97139715 A TW 97139715A TW I458819 B TWI458819 B TW I458819B
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- 238000004519 manufacturing process Methods 0.000 title description 10
- 239000002199 base oil Substances 0.000 title description 5
- 238000000034 method Methods 0.000 claims description 64
- 239000003054 catalyst Substances 0.000 claims description 46
- 239000002002 slurry Substances 0.000 claims description 25
- 125000003118 aryl group Chemical group 0.000 claims description 24
- 239000002994 raw material Substances 0.000 claims description 23
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 22
- 238000005984 hydrogenation reaction Methods 0.000 claims description 21
- 239000002904 solvent Substances 0.000 claims description 21
- 239000001257 hydrogen Substances 0.000 claims description 18
- 229910052739 hydrogen Inorganic materials 0.000 claims description 18
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 17
- 229910052751 metal Inorganic materials 0.000 claims description 16
- 239000002184 metal Substances 0.000 claims description 16
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 14
- 229910052717 sulfur Inorganic materials 0.000 claims description 14
- 239000011593 sulfur Substances 0.000 claims description 14
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 13
- 238000005336 cracking Methods 0.000 claims description 13
- 239000012530 fluid Substances 0.000 claims description 12
- 239000000203 mixture Substances 0.000 claims description 12
- PXHVJJICTQNCMI-UHFFFAOYSA-N nickel Substances [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims description 11
- 229910052757 nitrogen Inorganic materials 0.000 claims description 11
- 230000000694 effects Effects 0.000 claims description 8
- 239000010426 asphalt Substances 0.000 claims description 7
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 claims description 7
- 239000002808 molecular sieve Substances 0.000 claims description 7
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 7
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 claims description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 6
- 238000009835 boiling Methods 0.000 claims description 6
- 150000002739 metals Chemical class 0.000 claims description 6
- 229910052750 molybdenum Inorganic materials 0.000 claims description 6
- 229910052759 nickel Inorganic materials 0.000 claims description 6
- 230000000737 periodic effect Effects 0.000 claims description 6
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 6
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 claims description 5
- 125000005842 heteroatom Chemical group 0.000 claims description 5
- 239000011733 molybdenum Substances 0.000 claims description 5
- 239000004215 Carbon black (E152) Substances 0.000 claims description 4
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 4
- 125000000753 cycloalkyl group Chemical group 0.000 claims description 4
- 239000003502 gasoline Substances 0.000 claims description 4
- 229930195733 hydrocarbon Natural products 0.000 claims description 4
- 150000002430 hydrocarbons Chemical class 0.000 claims description 4
- 229910052721 tungsten Inorganic materials 0.000 claims description 4
- PSNPEOOEWZZFPJ-UHFFFAOYSA-N alumane;yttrium Chemical compound [AlH3].[Y] PSNPEOOEWZZFPJ-UHFFFAOYSA-N 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 229910017052 cobalt Inorganic materials 0.000 claims description 3
- 239000010941 cobalt Substances 0.000 claims description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 3
- 229910052763 palladium Inorganic materials 0.000 claims description 3
- 229910052697 platinum Inorganic materials 0.000 claims description 3
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 claims description 3
- 239000010937 tungsten Substances 0.000 claims description 3
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 claims description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims 1
- 239000003921 oil Substances 0.000 description 136
- 239000000047 product Substances 0.000 description 28
- 238000006243 chemical reaction Methods 0.000 description 16
- 239000012535 impurity Substances 0.000 description 16
- 229910021536 Zeolite Inorganic materials 0.000 description 6
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 6
- 239000007789 gas Substances 0.000 description 6
- 239000010457 zeolite Substances 0.000 description 6
- 238000010521 absorption reaction Methods 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 239000003209 petroleum derivative Substances 0.000 description 3
- 239000010970 precious metal Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- 230000001965 increasing effect Effects 0.000 description 2
- 238000006317 isomerization reaction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000012188 paraffin wax Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000007858 starting material Substances 0.000 description 2
- 241000269350 Anura Species 0.000 description 1
- 239000005662 Paraffin oil Substances 0.000 description 1
- QXZUUHYBWMWJHK-UHFFFAOYSA-N [Co].[Ni] Chemical compound [Co].[Ni] QXZUUHYBWMWJHK-UHFFFAOYSA-N 0.000 description 1
- 238000007792 addition Methods 0.000 description 1
- LEHUDBPYSAPFFO-UHFFFAOYSA-N alumane;bismuth Chemical compound [AlH3].[Bi] LEHUDBPYSAPFFO-UHFFFAOYSA-N 0.000 description 1
- JNDMLEXHDPKVFC-UHFFFAOYSA-N aluminum;oxygen(2-);yttrium(3+) Chemical compound [O-2].[O-2].[O-2].[Al+3].[Y+3] JNDMLEXHDPKVFC-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 239000010724 circulating oil Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 150000001924 cycloalkanes Chemical class 0.000 description 1
- 238000006356 dehydrogenation reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000010763 heavy fuel oil Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 239000000976 ink Substances 0.000 description 1
- 150000002736 metal compounds Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- MGRWKWACZDFZJT-UHFFFAOYSA-N molybdenum tungsten Chemical compound [Mo].[W] MGRWKWACZDFZJT-UHFFFAOYSA-N 0.000 description 1
- MOWMLACGTDMJRV-UHFFFAOYSA-N nickel tungsten Chemical compound [Ni].[W] MOWMLACGTDMJRV-UHFFFAOYSA-N 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- -1 polycyclic aromatic compounds Chemical class 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 238000001577 simple distillation Methods 0.000 description 1
- 238000000638 solvent extraction Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 239000000341 volatile oil Substances 0.000 description 1
- 238000004073 vulcanization Methods 0.000 description 1
Classifications
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- 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
- C10G45/46—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used
- C10G45/48—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
- C10G45/04—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used
- C10G45/06—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof
- C10G45/08—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof
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- 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
- C10G21/00—Refining of hydrocarbon oils, in the absence of hydrogen, by extraction with selective solvents
- C10G21/003—Solvent de-asphalting
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/44—Hydrogenation of the aromatic hydrocarbons
- C10G45/46—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used
- C10G45/52—Hydrogenation of the aromatic hydrocarbons characterised by the catalyst used containing platinum group metals or compounds thereof
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
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- C10G45/62—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing platinum group metals or compounds thereof
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
- C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
- C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
- C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
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- C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
- C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
- C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
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- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
- C10G67/0454—Solvent desasphalting
- C10G67/0463—The hydrotreatment being a hydrorefining
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- 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
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
- C10G67/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only including solvent extraction as the refining step in the absence of hydrogen
- C10G67/0454—Solvent desasphalting
- C10G67/0481—The hydrotreatment being an aromatics saturation
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G69/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process
- C10G69/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only
- C10G69/04—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one other conversion process plural serial stages only including at least one step of catalytic cracking in the absence of hydrogen
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M101/00—Lubricating compositions characterised by the base-material being a mineral or fatty oil
- C10M101/02—Petroleum fractions
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
- C10M105/00—Lubricating compositions characterised by the base-material being a non-macromolecular organic compound
- C10M105/02—Well-defined hydrocarbons
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- 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
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- 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
- C10G2300/205—Metal content
- C10G2300/206—Asphaltenes
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Description
本發明係關於一種自具有高芳香族含量及大量不純物之碳氫油餾分(oil fractions)中製備環烷基油之方法，尤指一種製備高品質環烷基油之方法，其係利用一種將油漿(SLO)經由溶劑脫瀝青(solvent deasphalting,SDA)所得之脫瀝青油(deasphalted oil,DAO)做為原料以通過一氫化處理單元以及一脫蠟/加氫精製(hydrofinishing)單元來進行，其中該油漿(SLO)係為一種流體化裂媒(FCC)單元之流出物。
環烷基油為一種具有黏度指數85或更少之基油，且根據ASTM D-2140方法檢測，此基油之至少30%的碳鍵為環烷型。
近年來，環烷基油廣泛地被使用於各種工業領域中以達到各種目的，包括變壓器油、絕緣油、冷凍機油、用於加工橡膠與塑膠之油、印刷墨水或油脂之基礎材料、以及金屬加工油之基油。
習知製備環烷基油之方法主要是以具有高環烷含量(環烷含量：30～40%)之環烷天然油作為原料，通過真空蒸餾單元分離石蠟成分，之後利用萃取及/或氫化單元將芳香族成分分離出來，及/或將其轉化成環烷，最後移除不純物。
然而，習知方法在具有高環烷含量之環烷天然油作為必要原料時，因有其供給上之限制而有問題，此外，由於必須實施萃取芳香族成分之萃取程序，更是造成不欲見到之總產量降低與產物品質劣化之情形。
國際專利號WO 2004/094565揭露一種製備環烷基油之方法，其係利用由各種處理單元之流出物組成之混合物提供作為原料，進行氫化精製得到之油餾分，將其脫去(stripped)以分離出具有預定範圍內之沸點之油餾分，然後對此被分離出之油餾分進行脫蠟。然而，上述方法有其缺點，因為在加氫精製單元的流出物中，除去輕油餾分與重底油餾分外，只有中間的油餾分可用於生產環烷基油，因此降低了總產量。再者，因為加氫精製程序中對於移除不純物之操作不充分，經由脫去分離步驟所得到之中間油餾分則會含有大量硫，此則明顯降低用於下游脫蠟單元中之催化劑之活性與選擇性。
此外，發展出一種可有效增加總製程產量之方法亦為本領域當務之急需。
因此，本發明提供一種方法，其係自具有高芳香族含量和大量不純物且價格低廉之碳氫原料中，製備出昂貴高產量環烷基油。其中，為流體化裂媒(FCC)流出物之油漿由於經由溶劑脫瀝青處理，因而增加可穩定處理之油漿餾分之產量，繼而減少油餾分之損失與移除。
根據本發明，自其特性為具有高於汽油之沸點，含有雜原子類與芳香族材料之碳氫原料製備環烷基油之方法，其包括：(a)將經由流體化裂媒(FCC)得到之油餾分分離出輕循環油與油漿；(b)將自(a)中分離之油漿經由溶劑脫瀝青分離，以分離出一脫瀝青油與一瀝青；(c)使用氫化處理催化劑來氫化處理分離自(a)之輕循環油、分離自(b)之脫瀝青油、或其混合物，以減少雜原子類之含量；(d)使用脫蠟催化劑將自(c)得到之氫化油餾分進行脫蠟以降低傾點(pour point)；(e)使用加氫精製催化劑來加氫精製自(d)得到之一脫蠟油餾分，以調整芳香族類之含量而符合產物標準值；以及(f)根據黏度範圍將自(e)得到之加氫精製油餾分進行分離。
在此，將詳述本發明。
參考圖1，其為根據本發明製備環烷基油之程序，包括將石油碳氫化合物經由流體化裂媒(FCC)所得之油漿(SLO)進行溶劑脫瀝青(SDA)，產生脫瀝青油(DAO)；將輕循環油(LCO)、脫瀝青油(DAO)、或其混合物以一氫化處理單元進行氫化處理(HDT)；將該氫化處理後之油餾分以脫蠟單元進行脫蠟(DW)；加氫精製該脫蠟後之油餾分；以及根據黏度範圍分離該加氫精製後之油餾分。
本發明製備環烷基油之方法具有以下特徵：環烷基油產自輕循環油或油漿。其中，此輕循環油及油漿係具有高芳香族含量與大量不純物，且係分離自經由流體化裂媒(FCC)石油碳氫化合物得到之產物流出物。
本發明所用之輕循環油或油漿是經由流體化裂媒(FCC)產生的。流體化裂媒(FCC,Fluidized Catalytic Cracking)程序是利用在500～700℃以及1～3atm下將常壓渣油原料進行流體化裂媒(FCC)而產生輕石油產物。此流體化裂媒(FCC)程序可產生揮發性油餾分，為主產物；並產生丙烯、重裂解石腦油(HCN)、輕循環油、油漿等，為副產物。將輕循環油或油漿，但非輕油餾分，利用分離塔分離。因為油中含有大量不純物與高含量雜原子類以及芳香族類，難以用做為高價值產物之輕油餾分來使用，反之係主要使用作為高硫輕油產物或價格低廉之重燃料油。
根據本發明之方法，如圖1所示，高品質環烷基油可由脫瀝青油、或輕循環油與脫瀝青油之混合物製備得到。其中，脫瀝青油是藉由引入常壓渣油(atmospheric residue,AR)至流體化裂媒(FCC)單元來製備，得到輕循環油(LCO)與油漿(SLO)，之後將其彼此分離，並將分離出之油漿進行溶劑脫瀝青。輕循環油是一種具有高芳香族含量且沸點(300～380℃)高於汽油之油餾分；而油漿是一種具有高芳香族含量且沸點(350～510℃)高於汽油之油餾分。
溶劑脫瀝青(SDA)程序是利用三碳或四碳化合物做為溶劑經由萃取分離油餾分之操作，且操作條件包括：瀝青質分離器之壓力為40~50kg/cm2
，脫瀝青油與瀝青之分離溫度為40~180℃，以及溶劑與油之比(L/kg)為4:1~12:1。
比較做為原料之輕循環油、脫瀝青油、與其混合物之性質，總結於下表1。
如表1所示，上述原料具有硫含量高於0.5wt%且氮含量高於1000ppm。至於本發明之原料，具有總芳香族含量60wt%或更多，不純物與芳香族類之含量遠高於環烷天然油(其為一般生產環烷基油程序中所使用之原料)。一般環烷天然油具有芳香族含量約10~20%，硫含量約0.1~0.15%以及氮含量約500~1000ppm(做為參考)。
輕循環油、脫瀝青油、或其混合物含有高芳香族含量以及大量不純物，因此其中所含之硫、氮、氧、以及金屬成分須經由氫化處理(HDT)移除，且其中所含之芳香族成分須經由加氫飽和作用被轉化為環烷成分。
根據本發明之製備環烷基油之方法，實施氫化處理程序之條件包括：溫度280~430℃，壓力30~220kg/cm2
，流體每小時空間流速(LHSV)0.1~3.0h-1
，以及氫與原料之體積比500~2500Nm3
/m3
。當提供大量的氫且施以極端溫度/壓力條件，可大大地減少原料中芳香族類與不純物之含量。
用於氫化處理程序之氫化處理催化劑包括選自週期表中第6、9、及第10金屬族類之金屬，更甚者，含有一或以上選自鈷鉬、鎳鉬、及鈷鉬與鎳鉬之組合。然而，本發明所用之氫化處理催化劑不僅限於此，只要對於加氫飽和作用與移除不純物有效之任何催化劑皆可使用。
此氫化處理後之油餾分之不純物與芳香族類之含量已大大地降低。根據本發明之方法，氫化處理後之油餾分之硫含量少於200ppm，氮含量少於100ppm，以及芳香族含量少於60wt%。更甚者，多環芳烴含量減少至不多於5%。
根據本發明之方法，因為氫化處理後之油餾分中不純物的含量相當低，下游程序單元中的反應可更穩定地發生，因此可以高產率生產富有環烷、含有少量不純物的產物。
以上述適當操作條件進行氫化處理後，將整個氫化處理後之油餾分，唯氣體成分除外，移至脫蠟單元，而不需額外分離或移除輕油餾分或底油餾分。
本發明之脫蠟程序是經由裂化或異構化作用以降低標準石蠟量之操作。
於脫蠟程序中，透過石蠟油餾分之選擇性反應與異構化瞭解到，傾點標準係直接與產物之低溫表現相關。
更甚者，脫蠟(DW)程序係以以下條件進行，包括：溫度250~430℃，壓力10~200kg/cm2
，流體每小時空間流速(LHSV)0.1~3h-1
，以及氫與原料之體積比300~1000Nm3
/m3
。
用於脫蠟程序之脫蠟催化劑包括一支承，其具有酸中心選自：分子篩、氧化鋁、與矽鋁；以及一或以上之金屬選自週期表中第6、9、與第10金屬族類，尤其是，具有氫化活性之金屬如：鉑、鈀、鉬、鈷、鎳、與鎢。
具有酸中心之支承之實例包括：分子篩、氧化鋁、以及矽鋁。其中，分子篩包括結晶矽鋁酸鹽(沸石)、SAPO、ALPO、或其他類似物，具有10-元氧環之中孔分子篩之實例包括：SAPO-11、SAPO-41、ZSM-5、ZSM-11、ZSM-22、ZSM-23、ZSM-35、以及ZSM-48，且具有12-元氧環之大孔分子篩之實例包括：FAU、Beta、與MOR。
具有氫化活性之金屬包括一或以上選自週期表中第6、8、9、與第10金屬族類，尤其有用的是第9與第10金屬族類之鈷與鎳(即第VIII族)，以及第6金屬族類之鉬與鎢(即第VIB族)。
本發明中，係使用由鎳(鈷)/鉬(鎢)所組成之脫蠟催化劑，其效果如下。特別地i)，就其效果而言，上述之催化劑所呈現之脫蠟效果與習知之脫蠟催化劑相同；以及ii)，就其經濟效能而言，上述之催化劑抑制製程中之加熱反應以及降低氫之消耗，且由於此催化劑不含貴重金屬，於是減低了催化劑之費用。而且iii)，就其性質與穩定性而言，上述之催化劑可防止單環芳香組成物之飽和，因此可藉由控制用於下游加氫精製單元之加氫精製催化劑之反應溫度以調整環烷基油產物之氣體吸收性能，因此可達到用於加氫精製過程中產物所需性質與穩定性之適當標準需求。而且iv)，就其原料之條件而言，因為含有貴重金屬之催化劑受到油餾分中不純物允許含量相當之限制規範，可用於脫蠟過程之原料之條件也較寬鬆了。而且v)，就其脫蠟催化劑之壽命而言，脫蠟催化劑係接收經過氫化處理過程之精鍊之油餾分，因此可增加其壽命。
再者，於加氫精製催化劑存在下，本發明之加氫精製過程係操作用來調整脫蠟油餾分之芳香族含量、氣體吸收性能、以及氧化穩定性，以符合產物所需之標準。加氫精製過程係以以下條件進行，包括：溫度150~400℃，壓力10~200kg/cm2
，流體每小時空間流速0.1~3h-1
，氫與供給之油餾分之體積比300~1000Nm3
/m3
。
用於加氫精製過程中之加氫精製催化劑包括一或以上具有氫化活性之金屬選自週期表中第6、8、9、10、與第11金屬族類。特別是，加氫精製催化劑可包括複合金屬選自鎳鉬、鈷鉬與鎳鎢，或選自鉑與鈀之貴重金屬。
具有大表面積支承之實例包括：二氧化矽(silica)、氧化鋁(alumina)、矽鋁(silica-alumina)、氧化鈦(titania)、氧化鋯(zirconia)、以及沸石(zeolite)。特別有用的是氧化鋁或矽鋁。支承作為增加上述金屬之分散性以增進氫化效能。作為支承之功能，控制用以防止產物裂解與焦化之酸中心被認為是相當重要的。
對於以上催化劑(用於氫化處理、脫蠟、與加氫精製之催化劑)之活性與前處理，乾燥、還原、與預硫化是必須的，而此前處理程序如有必要可省略或變更。
在經過所有氫化處理、脫蠟、與加氫精製反應處理後，雖然流出物在此狀況下已可被使用作為環烷基油，然而在本發明中，考慮到環烷基油之各種應用，最終油餾分仍係利用分餾器分離成具有適合個別應用之黏度之複數個環烷基油產物。例如：以分離步驟將油餾分分離出環烷基油產物，該環烷基油產物分別在40℃具有運動黏度(kinetic viscosity)3~5cSt、8~10cSt、18~28cSt、43~57cSt、90~120cSt、200~240cSt、與500cSt或以上。
透過以下實施例可更佳認識本發明，惟需了解的是，以下實施例並非用以限制本發明之範圍。
具有沸點300～380℃之輕循環油餾分從流體化裂煤(FCC)流出物中分離出來，接著提供至氫化處理單元。
該氫化處理過程係使用鎳鉬催化劑作為氫化處理催化劑來進行，其操作條件為：流體每小時空間流速(LHSV)0.1~3h-1
，氫與原料之體積比500~2500Nm3
/m3
，反應壓力30~220kg/cm2
，以及反應溫度280~430℃。
氫化處理過程後，得到之中間油餾分具有硫含量少於200ppm，氮含量少於100ppm，以及芳香族含量少於70wt%。根據一較佳實施態樣，此油餾分具有硫含量少於100ppm，氮含量少於100ppm，以及芳香族含量少於50wt%。
在脫蠟過程中使用鎳鉬(NiMo)/沸石催化劑，而加氫精製過程中係使用PtPd/Al2
O3
催化劑。這些過程係在以下操作條件下進行：流體每小時空間流速(LHSV)0.1~3h-1
，氫與原料之體積比300~1000Nm3
/m3
，以及反應壓力10~200kg/cm2
。如此，脫蠟之反應溫度設置在250~430℃，以及加氫精製設置在150~400℃。在本實施例中，此經過氫化精製後之油餾分可全部用做為產物，無須額外再分離。
下面表2顯示本實施例之原料(LCO)以及經由氫化處理與脫蠟原料所得之環烷基油(產物：N9)之性質。如表2所示，經由本發明之方法可生產高品質之環烷基油，且所製得之環烷基油具有環烷含量約57.7%，因此可增進環烷的含量，其運動黏度(kinetic viscosity)在40℃約9.314cSt，且其硫、氮、以及芳香族成分之含量遠較原料之含量為低。
本實施例係關於將一經由溶劑脫瀝青油漿得到之脫瀝青油用來製備環烷基油之方法，其中由於油漿係利用一丙烷作為溶劑進行溶劑萃取，因此所得到之脫瀝青油可接著作為實際原料來製備環烷基油。
溶劑脫瀝青(用於油漿前處理)之操作條件包括：瀝青質分離器之壓力40~50kg/cm2
，脫瀝青油與瀝青之分離溫度40~180℃，以及溶劑與油之比(L/kg)為4:1~12:1。
氫化處理過程使用如實施例1之鎳鉬催化劑，操作條件包括：流體每小時空間流速(LHSV)0.1~3h-1
，基於氫/油之氫消耗500~2500 Nm3
/m3
，反應壓力30~220kg/cm2
，以及反應溫度280~430℃。
脫蠟過程使用鎳鉬(NiMo)/沸石催化劑，以及加氫精製過程使用PtPd/Al2
O3
催化劑。這些過程之操作條件包括：流體每小時空間流速(LHSV)0.1~3h-1
，基於氫/油之氫消耗300~1000Nm3
/m3
，以及反應壓力10~200kg/cm2
。如此，脫蠟之反應溫度設置在250~430℃，以及加氫精製設置在150~400℃。
下面表3顯示第一原料(SLO)、實際原料(DAO)、以及脫蠟(DW)(利用分餾器分離之前)後之油餾分之性質。
經由溶劑脫瀝青得到之脫瀝青油，相較於用作第一原料之油漿，硫減少約16.67%，氮減少約50.77%。另外，總芳香族含量減少約15.85%。雖然脫蠟油餾分在那種狀態下可用做為產物，為了確保可得到各種產物，其須在氫化精製過程中使用分餾器分離。而最終產物之性質係總結於下表4。
在N9產物之案例中，其氣體吸收性能經測得為+14.96。由此可知，做為評估產物標準值之氣體吸收性能可藉由利用加氫精製控制芳香族含量而被調整。
在本實施例中，脫瀝青油中不純物與芳香族類之含量遠較輕油漿中來得低。因此，氫化處理的極端狀態可被緩和。最終油餾分係利用加氫精製過程的分餾器而被分離成各種產物，包括N9/46/110/540。
更進一步，在脫蠟過程中，使用鎳鉬(NiMo)/沸石催化劑，因此可防止單芳香族成分之過飽和，以使芳香族含量在接下來的加氫精製過程中維持適當的含量。當芳香族飽和程度被控制在一受要求之等級時，相當於產物標準值之氣體吸收性能與氧化穩定性可被適當地調整。
本實施例中，環烷基油產自經由溶劑脫瀝青油漿得到之輕循環油與脫瀝青油之混合物。
如此，溶劑脫瀝青過程使用丙烷做為溶劑，並於以下操作條件中進行，包括：瀝青質分離器之壓力40~50kg/cm2
，脫瀝青油與瀝青之分離溫度為40~180℃，以及溶劑與油之比為(L/kg)4:1~12:1。
脫瀝青油(DAO)與輕循環油以大約1：1質量比混合。
氫化處理過程係使用如實施例2中相同之鎳鉬催化劑，於以下操作條件中進行，包括：流體每小時空間流速(LHSV)0.1~3h-1
，基於氫/油之氫消耗500~2500Nm3
/m3
，反應壓力30~220kg/cm2
，以及反應溫度280~430℃。
脫蠟過程使用鎳鉬(NiMo)/沸石催化劑，以及加氫精製過程使用PtPd/Al2
O3
催化劑，這些過程係在以下操作條件下進行，包括：流體每小時空間流速(LHSV)0.1~3h-1
，基於氫/油之氫消耗300~1000Nm3
/m3
，以及反應壓力10~200kg/cm2
。如此，脫蠟之反應溫度設置在250~430℃，以及加氫精製設置在150~400℃。
下表5顯示第一原料(LCO/SLO)與實際原料(LCO+DAO)之性質。
根據黏度不同，可將脫蠟單元之流出物分離出最終產物。產物之性質總結於下表6。
本實施例中，雖然最終油餾分在那種狀態下可直接用作為產物，然而考慮到環烷基油之各種不同應用，必須根據在40℃時之運動黏度利用分餾器將其分離為四種產物。因此，產物具有各種黏度標準，且其中硫、氮等等的含量相較於原料急遽減少，而則可產生環烷含量高且具有優異低溫性能之產物。
如上文中所述，本發明提供一種製備高品質環烷基油之方法。在本發明中，經由溶劑脫瀝青油漿，此油漿為流體化裂媒(FCC)的流出物做為原料而得到脫瀝青油。利用溶劑萃取分離使脫瀝青油，相較於經由簡單蒸餾所得到之油漿，具有較少量之不純物(硫、氮、多環芳香族化合物與各種金屬化合物)，且因此可緩和下游氫化處理單元之極端操作條件，且延長催化劑之使用壽命。更進一步，被穩定處理之油漿餾分之產量增加，因此總產量可得到提升。
雖然本發明之較佳實施例為舉例之目的而揭露，熟習此領域技術之人將領會在本發明之技術範疇中之各種修飾、增加與替代均為可能。
圖1係根據本發明顯示製備環烷基油程序之流程圖。
(該圖為一流程圖故無元件代表符號)
Claims (14)
- 一種製備環烷基油之方法，其係製備自一具有高於汽油之沸點及含有雜原子類與芳香族類之碳氫原料，包括：(a)將一經由流體化裂媒得到之油餾分分離出一輕循環油與一油漿；(b)將自步驟(a)中分離得到之該油漿經由溶劑脫瀝青分離，以分離出一脫瀝青油與一瀝青；(c)使用一氫化處理催化劑來氫化處理分離自步驟(a)之該輕循環油、分離自步驟(b)之該脫瀝青油、或其混合物，以產生具有減少雜原子類之含量的一氫化油餾分；(d)使用一脫蠟催化劑將自步驟(c)得到之全部氫化油餾分進行脫蠟以產生具有降低傾點之一脫蠟油餾分，該脫蠟催化劑係包括一支承，係選自由分子篩、氧化鋁、與矽鋁所組成之群組，以及(i)Ni或Co、及(ii)Mo或W之組合作為具有氫化活性之金屬成分；(e)使用一加氫精製催化劑來加氫精製自步驟(d)得到之該脫蠟油餾分，以產生一加氫精製油餾分，調整其芳香族類之含量而符合一產物標準值；以及(f)根據一黏度範圍將自步驟(e)得到之該加氫精製油餾分進行分離，其中，分離自步驟(a)的該輕循環油、分離自步驟(b)的該脫瀝青油、或其混合物具有芳香族含量60wt%或更多，其中，步驟(c)中的該氫化油餾分具有芳香族含量小於60wt%且多環芳烴含量不大於5wt%，以及 其中，該環烷基油具有黏度指數指數85或更少，根據ASTM D-2140方法檢測，該環烷基油之至少30%的碳鍵為環烷型，以及具有環烷含量40%或更多。
- 如申請專利範圍第1項所述之方法，其中，該輕循環油、該脫瀝青油、或其混合物，具有硫含量0.5wt%或更多，以及氮含量1000ppm或更多。
- 如申請專利範圍第1項所述之方法，其中，步驟(b)中之該分離之操作條件係包括：瀝青分離器之壓力在40至50kg/cm2 ，脫瀝青油與瀝青之分離溫度在40至180℃，以及溶劑與油之比(L/kg)為4：1至12：1。
- 如申請專利範圍第1項所述之方法，其中，步驟(c)中之該氫化處理之操作條件係包括：溫度280至430℃，壓力30至220kg/cm2 ，流體每小時空間流速0.1至3.0h-1 ，氫與原料之體積比500至2500Nm3 /m3 。
- 如申請專利範圍第1項所述之方法，其中，步驟(c)中使用之該氫化處理催化劑係包括選自週期表第6、9、及第10金屬族類之金屬。
- 如申請專利範圍第5項所述之方法，其中，步驟(c)中使用之該氫化處理催化劑包括一或以上選自由鈷鉬(CoMo)、鎳鉬(NiMo)、以及鈷鉬(CoMo)及鎳鉬(NiMo)之組合所組成之群組。
- 如申請專利範圍第1項所述之方法，其中，步驟(d)中之脫蠟之操作條件係包括：溫度250至430℃，壓力10至 200kg/cm2 ，流體每小時空間流速0.1至3h-1 ，氫與原料之體積比300至1000Nm3 /m3 。
- 如申請專利範圍第1項所述之方法，其中，該脫蠟催化劑之支承是至少一分子篩，係選自由SAPO-11、SAPO-41、ZSM-5、ZSM-11、ZSM-22、ZSM-23、ZSM-35、ZSM-48、FAU、Beta、以及MOR所組成之群組。
- 如申請專利範圍第1項所述之方法，其中，步驟(e)中之加氫精製之操作條件係包括：溫度150至400℃，壓力10至200kg/cm2 ，流體每小時空間流速0.1至3.0h-1 ，氫與供給之油餾分之體積比300至1000Nm3 /m3 。
- 如申請專利範圍第1項所述之方法，其中，步驟(e)中使用之該加氫精製催化劑包括一或以上選自週期表第6、8、9、10、及第11金屬族類之金屬。
- 如申請專利範圍第10項所述之方法，其中，步驟(e)中使用之該一或以上加氫精製催化劑之金屬係包括一或以上之金屬係選自由鉑、鈀、鎳、鈷、鉬、以及鎢所組成之群組。
- 如申請專利範圍第1項所述之方法，其中，步驟(f)中之分離係依據40℃之運動黏度來進行，使加氫精製油餾分分離出環烷基油產物，且該環烷基油產物係於40℃具有運動黏度3至5cSt、8至10cSt、18至28cSt、43至57cSt、90至120cSt、200至240cSt、及500cSt或更多。
- 如申請專利範圍第1項至第12項之任一項所述之方法，其中，該環烷基油係具有硫含量200ppm或更少。
- 如申請專利範圍第12項之方法，其中，該環烷基油產物具有總芳香族含量21.09至51.54wt%。
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| KR100877004B1 (ko) * | 2002-03-16 | 2008-12-31 | 에스케이에너지 주식회사 | 연료유 수소화 분해공정의 미전환유 및 이의 감압증류분획 유분으로부터 질소화합물을 제거하는 방법 |
| US7282137B2 (en) * | 2002-10-08 | 2007-10-16 | Exxonmobil Research And Engineering Company | Process for preparing basestocks having high VI |
| US7179365B2 (en) * | 2003-04-23 | 2007-02-20 | Exxonmobil Research And Engineering Company | Process for producing lubricant base oils |
| US7279090B2 (en) | 2004-12-06 | 2007-10-09 | Institut Francais Du Pe'trole | Integrated SDA and ebullated-bed process |
| WO2007003708A1 (en) * | 2005-07-04 | 2007-01-11 | Neste Oil Oyj | Process for the manufacture of diesel range hydrocarbons |
| KR100841804B1 (ko) * | 2007-07-13 | 2008-06-26 | 에스케이에너지 주식회사 | 유동층 촉매 반응 공정의 유출물로부터 나프텐계 베이스오일을 제조하는 방법 |
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2008
- 2008-06-17 KR KR1020080056855A patent/KR100934331B1/ko not_active IP Right Cessation
- 2008-08-07 JP JP2011514477A patent/JP5263634B2/ja not_active Expired - Fee Related
- 2008-08-07 WO PCT/KR2008/004594 patent/WO2009154324A1/en active Application Filing
- 2008-08-07 GB GB1100665.7A patent/GB2473992B/en not_active Expired - Fee Related
- 2008-08-07 US US12/999,415 patent/US8585889B2/en not_active Expired - Fee Related
- 2008-08-07 CN CN200880129955XA patent/CN102066530B/zh not_active Expired - Fee Related
- 2008-10-16 TW TW097139715A patent/TWI458819B/zh not_active IP Right Cessation
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2013
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020189972A1 (en) * | 2000-04-21 | 2002-12-19 | Eric Benazzi | Flexible method for producing oil bases with a zsm-48 zeolite |
| US20060018601A1 (en) * | 2002-01-17 | 2006-01-26 | Cornell Research Foundation, Inc. | High-index contrast waveguide coupler |
Also Published As
| Publication number | Publication date |
|---|---|
| US8585889B2 (en) | 2013-11-19 |
| JP5263634B2 (ja) | 2013-08-14 |
| JP2011530610A (ja) | 2011-12-22 |
| GB2473992B (en) | 2012-03-07 |
| GB201100665D0 (en) | 2011-03-02 |
| JP2013151685A (ja) | 2013-08-08 |
| CN102066530B (zh) | 2013-11-06 |
| KR100934331B1 (ko) | 2009-12-29 |
| GB2473992A (en) | 2011-03-30 |
| JP5692545B2 (ja) | 2015-04-01 |
| TW201000621A (en) | 2010-01-01 |
| US20110089080A1 (en) | 2011-04-21 |
| CN102066530A (zh) | 2011-05-18 |
| KR20090131072A (ko) | 2009-12-28 |
| WO2009154324A1 (en) | 2009-12-23 |
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