CN100469858C - Fuels and lubricants using layered bed catalysts in hydrotreating waxy feeds, including fischer-tropsch wax - Google Patents
Fuels and lubricants using layered bed catalysts in hydrotreating waxy feeds, including fischer-tropsch wax Download PDFInfo
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- CN100469858C CN100469858C CNB2004800234564A CN200480023456A CN100469858C CN 100469858 C CN100469858 C CN 100469858C CN B2004800234564 A CNB2004800234564 A CN B2004800234564A CN 200480023456 A CN200480023456 A CN 200480023456A CN 100469858 C CN100469858 C CN 100469858C
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- China
- Prior art keywords
- hydrocracking
- base oil
- lubricant base
- hydrocarbon feed
- wax shape
- Prior art date
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- 239000003054 catalyst Substances 0.000 title claims abstract description 81
- 239000000314 lubricant Substances 0.000 title claims abstract description 61
- 239000000446 fuel Substances 0.000 title claims abstract description 32
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 86
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 68
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 67
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 66
- 239000002199 base oil Substances 0.000 claims abstract description 58
- 239000002808 molecular sieve Substances 0.000 claims abstract description 38
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 38
- 238000000034 method Methods 0.000 claims description 108
- 239000002994 raw material Substances 0.000 claims description 53
- 230000008569 process Effects 0.000 claims description 28
- 238000006243 chemical reaction Methods 0.000 claims description 27
- 238000005194 fractionation Methods 0.000 claims description 13
- 238000013517 stratification Methods 0.000 claims description 9
- 230000008859 change Effects 0.000 claims description 8
- 239000011148 porous material Substances 0.000 abstract description 7
- 239000001993 wax Substances 0.000 description 83
- 239000000047 product Substances 0.000 description 59
- 238000009835 boiling Methods 0.000 description 30
- 229910052739 hydrogen Inorganic materials 0.000 description 21
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 20
- 239000001257 hydrogen Substances 0.000 description 20
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 17
- 238000005336 cracking Methods 0.000 description 16
- 239000007789 gas Substances 0.000 description 16
- 238000005984 hydrogenation reaction Methods 0.000 description 16
- 239000010457 zeolite Substances 0.000 description 15
- 229910021536 Zeolite Inorganic materials 0.000 description 14
- 239000002283 diesel fuel Substances 0.000 description 14
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 14
- 239000003921 oil Substances 0.000 description 11
- 230000009466 transformation Effects 0.000 description 11
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 10
- 239000007795 chemical reaction product Substances 0.000 description 10
- 238000002360 preparation method Methods 0.000 description 10
- 238000004088 simulation Methods 0.000 description 10
- 239000000463 material Substances 0.000 description 9
- 239000000203 mixture Substances 0.000 description 9
- 239000012188 paraffin wax Substances 0.000 description 9
- 229910052697 platinum Inorganic materials 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical group N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 238000006317 isomerization reaction Methods 0.000 description 8
- 229910052751 metal Inorganic materials 0.000 description 8
- 239000002184 metal Substances 0.000 description 8
- 150000001335 aliphatic alkanes Chemical class 0.000 description 7
- 150000001336 alkenes Chemical class 0.000 description 7
- -1 aviation spirit Substances 0.000 description 7
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 6
- CIWBSHSKHKDKBQ-JLAZNSOCSA-N Ascorbic acid Chemical compound OC[C@H](O)[C@H]1OC(=O)C(O)=C1O CIWBSHSKHKDKBQ-JLAZNSOCSA-N 0.000 description 6
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 239000008186 active pharmaceutical agent Substances 0.000 description 6
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 5
- 230000015572 biosynthetic process Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 229910052763 palladium Inorganic materials 0.000 description 5
- 238000003786 synthesis reaction Methods 0.000 description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 4
- 239000005864 Sulphur Chemical group 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 230000003197 catalytic effect Effects 0.000 description 4
- 150000001875 compounds Chemical class 0.000 description 4
- DCAYPVUWAIABOU-UHFFFAOYSA-N hexadecane Chemical compound CCCCCCCCCCCCCCCC DCAYPVUWAIABOU-UHFFFAOYSA-N 0.000 description 4
- 239000010687 lubricating oil Substances 0.000 description 4
- 229910052987 metal hydride Inorganic materials 0.000 description 4
- 150000004681 metal hydrides Chemical class 0.000 description 4
- 229910052757 nitrogen Chemical group 0.000 description 4
- 239000010703 silicon Substances 0.000 description 4
- 229910052710 silicon Inorganic materials 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical group [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- ILRRQNADMUWWFW-UHFFFAOYSA-K aluminium phosphate Chemical compound O1[Al]2OP1(=O)O2 ILRRQNADMUWWFW-UHFFFAOYSA-K 0.000 description 3
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 3
- 229910017052 cobalt Inorganic materials 0.000 description 3
- 239000010941 cobalt Substances 0.000 description 3
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 3
- 238000002050 diffraction method Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000011159 matrix material Substances 0.000 description 3
- 229910044991 metal oxide Inorganic materials 0.000 description 3
- 150000004706 metal oxides Chemical class 0.000 description 3
- 229910052750 molybdenum Inorganic materials 0.000 description 3
- 239000011733 molybdenum Substances 0.000 description 3
- 229910052759 nickel Inorganic materials 0.000 description 3
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 3
- 239000012169 petroleum derived wax Substances 0.000 description 3
- 235000019381 petroleum wax Nutrition 0.000 description 3
- 229910052814 silicon oxide Inorganic materials 0.000 description 3
- 238000010561 standard procedure Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 3
- 229910052721 tungsten Inorganic materials 0.000 description 3
- 239000010937 tungsten Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 229940001007 aluminium phosphate Drugs 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical group [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 235000011089 carbon dioxide Nutrition 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000011651 chromium Substances 0.000 description 2
- 239000004927 clay Substances 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 238000002290 gas chromatography-mass spectrometry Methods 0.000 description 2
- 125000005842 heteroatom Chemical group 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000000395 magnesium oxide Substances 0.000 description 2
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- MOWMLACGTDMJRV-UHFFFAOYSA-N nickel tungsten Chemical compound [Ni].[W] MOWMLACGTDMJRV-UHFFFAOYSA-N 0.000 description 2
- 229910000510 noble metal Inorganic materials 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000002310 reflectometry Methods 0.000 description 2
- 239000013557 residual solvent Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000005303 weighing Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 239000005069 Extreme pressure additive Substances 0.000 description 1
- 102220500397 Neutral and basic amino acid transport protein rBAT_M41T_mutation Human genes 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- BUGBHKTXTAQXES-UHFFFAOYSA-N Selenium Chemical compound [Se] BUGBHKTXTAQXES-UHFFFAOYSA-N 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 1
- YIFVJYNWLCNYGB-UHFFFAOYSA-N [Si]=O.[Zr] Chemical compound [Si]=O.[Zr] YIFVJYNWLCNYGB-UHFFFAOYSA-N 0.000 description 1
- YNKHQQXFHLJHHA-UHFFFAOYSA-N [Zr+4].[O-2].[Mg+2].[Si+2]=O.[O-2].[O-2].[O-2] Chemical compound [Zr+4].[O-2].[Mg+2].[Si+2]=O.[O-2].[O-2].[O-2] YNKHQQXFHLJHHA-UHFFFAOYSA-N 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000001464 adherent effect Effects 0.000 description 1
- 150000001299 aldehydes Chemical class 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 239000011959 amorphous silica alumina Substances 0.000 description 1
- 239000003963 antioxidant agent Substances 0.000 description 1
- 230000003078 antioxidant effect Effects 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- 239000010953 base metal Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- LTPBRCUWZOMYOC-UHFFFAOYSA-N beryllium oxide Inorganic materials O=[Be] LTPBRCUWZOMYOC-UHFFFAOYSA-N 0.000 description 1
- 150000001721 carbon Chemical group 0.000 description 1
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 1
- 239000000969 carrier Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000007385 chemical modification Methods 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- GUJOJGAPFQRJSV-UHFFFAOYSA-N dialuminum;dioxosilane;oxygen(2-);hydrate Chemical compound O.[O-2].[O-2].[O-2].[Al+3].[Al+3].O=[Si]=O.O=[Si]=O.O=[Si]=O.O=[Si]=O GUJOJGAPFQRJSV-UHFFFAOYSA-N 0.000 description 1
- 238000007598 dipping method Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 229910001657 ferrierite group Inorganic materials 0.000 description 1
- 210000002683 foot Anatomy 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 150000004678 hydrides Chemical class 0.000 description 1
- 230000001771 impaired effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 229910052809 inorganic oxide Inorganic materials 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical group O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- OTUXRAAQAFDEQT-UHFFFAOYSA-N magnesium oxosilicon(2+) oxygen(2-) Chemical compound [O-2].[Mg+2].[Si+2]=O.[O-2] OTUXRAAQAFDEQT-UHFFFAOYSA-N 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 229910052914 metal silicate Inorganic materials 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 239000004200 microcrystalline wax Substances 0.000 description 1
- 235000019808 microcrystalline wax Nutrition 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 229910052901 montmorillonite Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- FMLYSTGQBVZCGN-UHFFFAOYSA-N oxosilicon(2+) oxygen(2-) titanium(4+) Chemical compound [O-2].[Ti+4].[Si+2]=O.[O-2].[O-2] FMLYSTGQBVZCGN-UHFFFAOYSA-N 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229920013639 polyalphaolefin Polymers 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 150000003138 primary alcohols Chemical class 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 150000003333 secondary alcohols Chemical class 0.000 description 1
- 229910052711 selenium Inorganic materials 0.000 description 1
- 239000011669 selenium Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000012265 solid product Substances 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 229910052719 titanium Inorganic materials 0.000 description 1
- 239000010936 titanium Substances 0.000 description 1
- OGIDPMRJRNCKJF-UHFFFAOYSA-N titanium oxide Inorganic materials [Ti]=O OGIDPMRJRNCKJF-UHFFFAOYSA-N 0.000 description 1
- 229910052723 transition metal Inorganic materials 0.000 description 1
- 150000003624 transition metals Chemical class 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- GPPXJZIENCGNKB-UHFFFAOYSA-N vanadium Chemical compound [V]#[V] GPPXJZIENCGNKB-UHFFFAOYSA-N 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 238000004018 waxing Methods 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
- 239000004711 α-olefin Substances 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
- 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
-
- 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
- C10G2400/10—Lubricating oil
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Lubricants (AREA)
Abstract
Wary hydrocarbon feedstocks are contacted with a hydrocracking catalyst and the effluent then contacted with an intermediate pore size molecular sieve hydroisomerization catalyst. The effluent from the hydroisomerization is fractionated to provide a heavy fraction and a middle distillate fuel. A high quality lubricant base oil with a high viscosity index and a low pour point is isolated from the heavy fraction.
Description
Invention field
The present invention relates to make wax shape hydrocarbon feed to change into the method for best-selling product.More specifically, the present invention relates to make fischer-tropsch derived wax shape feedstock conversion become in the method for distillate fuel and lubricant base oil.
Background of invention
Available Fischer-Tropsch synthesis makes under catalytic condition mainly by CO and H
2The gas of forming (being commonly referred to synthetic gas) changes into various gaseous states, liquid state and solid hydrocarbons product.These liquid and many waxy substances of forming by high molecular weight alkane that all contain of solid product.These paraffin are crystallizable when cooling, and the product that comprises these paraffin has unacceptable high pour point and high cloud point usually.Pour point is that sample begins the mobile temperature under the condition of careful control, can measure by ASTM D5950-96.Cloud point is that sample begins to form muddy temperature under controlled conditions, can measure by ASTMD5773-95.
The low boiling hydrocarbon that wax shape alkane in the hydrocarbon feed is catalytically converted in middle cut product scope is known.This conversion can be by hydrotreatment technology such as hydrocracking and hydroisomerization realization.Hydrocracking changes into bigger molecule and introduces some side chain than small molecules and in cracked product.Hydroisomerization is mainly introduced side chain in alkane molecule, thereby improves such as character such as pour point and cloud points.The unreacted components of hydrocracking and/or hydroisomerization is not capable of circulation as yet in the hydrocarbon feed is used for further handling the other products that boiling range is provided to provide.
Among the EP 0544766B1 instruction by hydrotreatment and hydroisomerization combined treatment paraffinic hydrocarbon raw material with cut hydrocarbon in producing.EP 0544766B1 instruction is a kind of to make the method for cut hydrocarbon in hydrocarbon feed and macropore hydrogenation cracking catalyst and the catalyzer contact preparation low pour point that comprises mesopore silicoaluminophosphamolecular molecular sieves and hydrogenation component.
US5,935,414 relate to a kind of wax content that reduces the waxy hydrocarbon raw material produce in the method for cut product, this product comprises the diesel oil fuel and the heater oil of low freezing point jet fuel and/or low pour point and low cloud point.In this method, raw material is being contacted under increasing temperature and pressure in the presence of the hydrogen at hydrocracking zone with hydrocracking catalyst, and hydrocracking catalyst comprises hydrogenation metal component and the large pore zeolite such as the y-type zeolite of carrier, at least a group vib and group VIII metal.Whole effluents from hydrocracking zone are contacting under increasing temperature and pressure in the presence of the hydrogen in the Hydrodewaxing district with dewaxing catalyst, and catalyst for hydrogenation de-waxing comprises the crystallization mesoporous molecular sieve that is selected from metal silicate and silicon aluminium phosphate.
US5,139,647 relate to a kind of by hydrocracking and isomerization method by cut in the hydrocarbon feed preparation.In this method, raw material is contacted with the catalyzer that comprises mesopore silicoaluminophosphamolecular molecular sieves and hydrogenation component.
US4,859,312 relate to the method for cut in a kind of preparation.This method makes heavy oil experience hydrocracking and isomerization reaction simultaneously with the catalyzer that comprises silicoaluminophosphamolecular molecular sieves such as SAPO-11 and SAPO-41 and platinum or palladium (hydrogenation component).This method is with the well middle cut that reduces of pour point and viscosity especially of optionally production cryogen of high yield characteristic.
EP 0323092 A2 and US 4,943,672 relate to a kind ofly to be changed into fischer-tropsch wax to have the method for the lubricating oil of high viscosity index (HVI) and low pour point.In this method earlier than under the exacting terms wax being carried out hydrogen treatment, then in the presence of the hydrogen at the wax hydroisomerization that on the group VIII metal/alumina catalyzer hydrogen treatment is crossed of fluoridizing of particular type.Make the dewaxing of hydroisomerization product produce the high-quality lube base stock then.
US4,080,397 discloses the method for the quality of 177 ℃ of a kind of raising fischer-tropsch synthetic+(350 ℉+) product.In this method, fischer-tropsch synthesis product is carried out hydrogen treatment, make the hydrogen treatment material optionally cracking of boiling point below about 316 ℃ (600 ℉) then.
EP 0583836 A1 discloses a kind of preparation method of hydrocarbon fuel.In this method, preparation is essentially the product of alkane, and this hydrocarbon product is being contacted under the condition of isomerization that hydrocarbon product does not take place basically or hydrocracking in the presence of the hydrogenation conversion catalyst with hydrogen.At least a portion hydrocarbon product that makes process since then and hydrogen produce the fuel that is essentially alkane causing in the presence of the hydrogenation conversion catalyst contacting under hydrocarbon feed generation hydrocracking and the isomerized condition.
EP 0147873 A1 discloses a kind of preparation method of middle cut.By the two-stage series connection method by cut in the synthesis gas preparation.This method is included in that to carry out fischer-tropsch on special Zr, Ti or the promoted promotor of Cr synthetic, makes fischer-tropsch synthetic all prods hydrocracking on loaded noble metal catalyst then.
Need under the situation of not sacrificing the desirable properties of paraffins in the raw material, make wax shape paraffin raw material change into the cost-effective method of middle distillate fuel and lubricant base oil with high yield.The main products of expecting this method is the lubricant base oil with good cryogenic properties (being cloud point, pour point, cold filter clogging temperature etc. and high viscosity).
Summary of the invention
The present invention relates to a kind of treatment process of wax shape hydrocarbon feed.This method comprises that raw material and hydrocracking catalyst are contacted at hydrocracking zone produces the hydrocracking effluent, and makes hydrocracking effluent and molecular sieve hydroisomerisation catalysts contact generation hydroisomerization effluent in the hydroisomerization district.Make the fractionation of hydroisomerization effluent obtain last running and middle distillate fuel.From last running, isolate the lubricant base oil cut, the viscosity index of this lubricant base oil greater than 130, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 3cSt.
The invention still further relates to the treatment process of a kind of 343 ℃+(650 ℉+) wax shape hydrocarbon feed.This method comprises that raw material and hydrocracking catalyst are contacted at hydrocracking zone produces the hydrocracking effluent, and makes hydrocracking effluent and molecular sieve hydroisomerisation catalysts contact generation hydroisomerization effluent in the hydroisomerization district.Make the fractionation of hydroisomerization effluent obtain last running and middle distillate fuel; With from last running, isolate the lubricant base oil cut.The viscosity index of this lubricant base oil greater than 130, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 3cSt.343 ℃+(650 ℉+) component in the preferred feedstock is lower than 60% (weight) and changes into 343 ℃-(650 ℉-) product.
In another embodiment, the present invention relates to the treatment process of a kind of 343 ℃+(650 ℉+) wax shape hydrocarbon feed again.In this method, raw material and hydrocracking catalyst are contacted at hydrocracking zone produce the hydrocracking effluent, and make hydrocracking effluent and molecular sieve hydroisomerisation catalysts contact generation hydroisomerization effluent in the hydroisomerization district.Make the fractionation of hydroisomerization effluent obtain last running and middle distillate fuel; With from last running, isolate the lubricant base oil cut.The lubricant base oil viscosity index of producing by this method greater than 130, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 3cSt, described 343 ℃+(650 ℉+) wax shape hydrocarbon feed comprises 482 ℃+(900 ℉+) component more than 20% (weight).
The accompanying drawing summary
Accompanying drawing is the synoptic diagram of a kind of embodiment of the inventive method.
Embodiment
The present invention relates to the method for producing the high quality lubricant base oil with high yield by wax shape hydrocarbon feed.Found that the wax shape hydrocarbon feed that can be easy to and make economically the initial boiling point height and contain a large amount of paraffin such as fischer-tropsch wax changes into high-quality middle distillate fuel and high-quality lubricant base oil, wherein lubricant base oil is a main products.In the inventive method, these wax shape hydrocarbon feeds are contacted with hydrocracking catalyst again contact, cut product and last running in being separated into hydroisomerisation catalysts.From last running, isolate lubricant base oil.This method makes high boiling wax shape hydrocarbon feed change into distillate fuel and the low high quality lubricant base oil of viscosity index height, pour point and cloud point in the low high quality of pour point and cloud point.The inventive method causes the cracking of high boiling point end in the high boiling point wax shape raw material less (the high boiling point end that is raw material changes into lacking than light product).Thereby generation viscosity index height, pour point and the low high quality lubricant base oil of cloud point.
Definition
The following term that uses in this specification sheets has following implication, except as otherwise noted.
" last running " is that hydrocarbon feed hydrocracking of wax shape and hydroisomerization are afterwards isolated than last running.The initial boiling point of described last running in the scope of 316 to 399 ℃ (600 to 750 ℉), full boiling point 510 to scope greater than 649 ℃ (950 to greater than 1200 ℉).Described last running comprises lubricant base oil and wax.The wax content of this last running can be between 0.1 and 5% (weight).Thereby but last running also fractionation obtain tower bottom distillate.
" tower bottom distillate " is non-volatile (the being residual oil) cut that comprises in the described last running.
" synthetic from fischer-tropsch " means described fuel or product and comes from Fischer-Tropsch process or produced by a certain stage of Fischer-Tropsch process.
" the wax shape hydrocarbon feed " that is applicable to method disclosed herein can be synthetic wax shape raw material such as fischer-tropsch wax shape hydrocarbon, perhaps can be from natural source such as petroleum wax.This wax shape hydrocarbon feed comprises wax greater than 50% (weight), more preferably greater than the wax of about 80% (weight), most preferably greater than the wax of about 90% (weight).Wax content used herein is measured by solvent dewaxing process.Solvent dewaxing process is standard method, for known in this field.In this method, with 300g wax shape product with being cooled to-20 ℃ methylethylketone and the 4:1 mixture of toluene dilutes by 50/50 (volume).Make this mixture evenly to be cooled to-15 ℃ at a slow speed in about 0.5 to 4.5 ℃/min scope, filter by the Coors funnel with Whatman3 filter paper down at-15 ℃ then.Wax is taken out from strainer, be placed in tarry 2 liters of flasks.On hot plate, remove residual solvent in the dewax, the weight of weighing wax.
The initial boiling point of " 343 ℃+(650 ℉+) wax shape hydrocarbon feed " is 343 ℃ (650 ℉), wherein at least 70% (weight), preferably the raw material boiling point of at least 85% (weight) is higher than 343 ℃ (650 ℉).
" middle distillate fuel " or " middle distillate fuel cut " is isolated lighting end behind hydrocarbon feed hydrocracking of wax shape and the hydroisomerization.It is the material that comprises the hydrocarbon of boiling point between about 149 to 343 ℃ (300 to 650 ℉).It should be to be produced by the overhead gas stream that crude distillation obtains that term " cut " means this type of traditional fuel.Concrete fuel in the big class of distillate fuel comprises petroleum naphtha, jet fuel, diesel oil fuel, kerosene, aviation spirit, fuel oil and tempered oil thereof.
" lubricant base oil " means the cut of the technical requirements of satisfying lubricant base oil.The lubricant base oil cut is isolating from last running by the inventive method.The character of lubricant base oil provided by the invention comprises that initial boiling point is in the scope of 316 to 399 ℃ (600 to 750 ℉), full boiling point 482 to scope greater than 649 ℃ (900 to greater than 1200 ℉), 100 ℃ of following viscosity are in 3 to 15cSt scope, viscosity index in 115 to 160 scope, preferably in 130 to 180 scope, more preferably in 140 to 180 scope, pour point is lower than-9 ℃, preferably in-10 to-24 ℃ scope, cloud point is in 0 to-20 ℃ scope.
" hydrocarbon or hydrocarbon matter " means the compound or the material that contain hydrogen and carbon atom, can also comprise heteroatoms such as oxygen, sulphur or nitrogen.
In the inventive method, by raw material contact with hydrocracking catalyst contact with hydroisomerisation catalysts again make wax shape hydrocarbon feed change in distillate fuel product and lubricant base oil products.The inventive method provides viscosity index height and pour point and cloud point low lubricant base oil products.The inventive method causes the cracking of high boiling point end in the high boiling point wax shape raw material less (the high boiling point end that is raw material changes into lacking than light product).Thereby generation viscosity index height and pour point and the low high quality lubricant base oil of cloud point.
Methods described herein can make this pyroparaffine shape feedstock conversion become high-quality middle cut product and high-quality lubricant base oil products.The initial boiling point of this wax shape hydrocarbon feed be lower than 371 ℃+(700 ℉+).The full boiling point of this wax shape hydrocarbon feed 538 to scope greater than 649 ℃ (1000 to greater than 1200 ℉).The wax shape hydrocarbon feed of preferred methods described herein comprises greater than 343 ℃+(the 650 ℉+) material of 70% (weight) even more preferably greater than 343 ℃+(the 650 ℉+) material of 85% (weight).This raw material preferably comprises 482 ℃+(900 ℉+) material greater than 20% (weight).
The wax shape raw material of the inventive method comprises wax greater than 80% (weight), is preferably greater than the wax of 95% (weight).Wax content used herein is measured by solvent dewaxing process.Solvent dewaxing process is standard method, for known in this field.In this method, with 300g wax shape product with being cooled to-20 ℃ methylethylketone and the 4:1 mixture of toluene dilutes by 50/50 (volume).Make this mixture evenly to be cooled to-15 ℃ at a slow speed in about 0.5 to 4.5 ℃/min scope, filter by the Coors funnel with Whatman3 filter paper down at-15 ℃ then.Wax is taken out from strainer, be placed in tarry 2 liters of flasks.On hot plate, remove residual solvent in the dewax, the weight of weighing wax.
The wax shape hydrocarbon feed that is applicable to method disclosed herein can be synthetic wax shape raw material such as fischer-tropsch wax shape hydrocarbon, perhaps can be from natural source such as petroleum wax.Therefore, the wax shape raw material of this method can comprise fischer-tropsch derived wax shape raw material, petroleum wax, wax shape cut oil plant such as gasoline, lube stock, high pour point poly-alpha olefins, garbage grease, positive alpha-olefin wax, waxy stone, dewaxed oil and Microcrystalline Wax, and composition thereof.Preferred described wax shape raw material is from fischer-tropsch wax shape raw material.
Can before methods described herein, carry out hydrogen treatment as required to wax shape hydrocarbon feed.But for fischer-tropsch derived wax shape raw material, do not need hydrogen treatment usually.
The preferred wax shape of the present invention raw material is fischer-tropsch derived wax shape raw material.In the fischer-tropsch chemistry, make synthetic gas change into liquid hydrocarbon by under reaction conditions, contacting with Fischer-Tropsch catalyst.Typically, methane can be sent into conventional synthetic gas generator with optional heavier hydrocarbon (ethane and heavier) synthetic gas is provided.Synthetic gas generally contains hydrogen and carbon monoxide, can comprise a spot of carbonic acid gas and/or water.It is undesirable having sulphur, nitrogen, halogen, selenium, phosphorus and arsenic impurities in the synthetic gas.For this reason, according to the quality of synthetic gas, preferably before carrying out the fischer-tropsch chemistry, from raw material, remove desulfuration and other pollutent.The method that removes these pollutents is as well known to those skilled in the art.For example, preferably remove sulphur impurity with ZnO protection bed.The method that removes other pollutent is as well known to those skilled in the art.Any other sulphur compound that the carbonic acid gas Buddhist monk that may wish also that the synthetic gas purifying is removed and produce in the synthesis gas reaction process does not remove.This can contact realization with weakly alkaline solution (for example wet chemical) by for example making synthetic gas in packed tower.
In Fischer-Tropsch process, comprise H
2Under the temperature and pressure reaction conditions that is fit to, contact the liquid gentle attitude hydrocarbon of generation with the synthetic gas of CO mixture with Fischer-Tropsch catalyst.Fischer-Tropsch reaction generally can be carried out under the following conditions: temperature about 149 to 371 ℃ (300 to 700 ℉), preferred about 204 to 228 ℃ (400 to 550 ℉); About 10 to 600psia (0.7-41bar) of pressure, preferred about 30 to 300psia (2-21bar); With catalyzer air speed about 100 to about 10 000cc/g/hr, preferred 300 to 3 000cc/g/hr.The example that carries out the condition of fischer-tropsch type reaction is as well known to those skilled in the art.
The product of Fischer-Tropsch synthesis can be at C
1To C
200+Scope in, great majority at C
5-C
100+Scope in.This reaction can be carried out in various type of reactor for example have the combination of fixed-bed reactor, slurry-phase reactor, fluidized-bed reactor or dissimilar reactors of one or more catalyst bed.This reaction process and reactor are known, and be open in the literature.
Usually, Fischer-Tropsch catalyst comprises the group VIII transition metal that supports on metal oxide carrier.This catalyzer can also comprise noble metal promoted agent and/or crystalline molecular sieve.Known some catalyzer provides and is low to moderate medium chainpropagation probability, and reaction product comprises the lower molecular weight (C of higher proportion
2-8) high molecular (C of alkene and low ratio
30+) wax.Known other catalyzer provide higher chainpropagation probability, and reaction product comprises the lower molecular weight (C of low ratio
2-8) high molecular (C of alkene and higher proportion
30+) wax.This type of catalyzer is as well known to those skilled in the art, is easy to obtain and/or preparation.
Product from Fischer-Tropsch process mainly comprises paraffins; But may also comprise C
2+Alkene, oxygenatedchemicals and heteroatom contaminants.The oxygenatedchemicals that is rich in most in the fischer-tropsch products is an alcohol, is straight chain primary alcohol mostly.The less oxygenatedchemicals of content comprises alcohol such as secondary alcohol, acid, ester, aldehyde and the ketone of other type in the fischer-tropsch products.Product from Fischer-Tropsch reaction generally comprises light reaction product and wax shape reaction product.Light reaction product (being condensate fraction) comprises that boiling point is lower than the hydrocarbon of about 371 ℃ (700 ℉) (for example tail gas is to middle distillate fuel), mostly at C
5-C
20In the scope, with decrement to about C
30Wax shape reaction product (being wax slop) comprises that boiling point is higher than the hydrocarbon (for example vacuum gas oil is to heavy paraffin) of about 316 ℃ (600 ℉), mainly at C
20+In the scope, with decrement to C
10
Described light reaction product and wax shape product all are that alkane belongs to basically.Wax shape product generally comprises more than the n-paraffin of 70% (weight), usually more than the n-paraffin of 80% (weight).Light reaction product comprises paraffin wax product, and very a high proportion of pure and mild alkene is arranged.Under some situation, light reaction product can comprise nearly 50% (weight) even higher pure and mild alkene.It is the wax shape reaction product (being wax slop) that can be used as the inventive method raw material.
According to the present invention, wax shape hydrocarbon feed is contacted at hydrocracking zone with hydrocracking catalyst produce the hydrocracking effluent, hydrocracking effluent and molecular sieve hydroisomerisation catalysts are contacted in the hydroisomerization district produce the hydroisomerization effluent.Hydrocracking catalyst and hydroisomerisation catalysts can be in various design option scopes, as long as all feed the hydroisomerization district from the effluent of hydrocracking zone.Therefore, hydrocracking and hydroisomerisation catalysts can the single reaction district in single reaction vessel in stratification, perhaps hydrocracking and hydroisomerisation catalysts can be in the tandem reactor of close-coupled stratification, do not have heating, products export or feed(raw material)inlet between the reactor.Preferred catalyst system is the multi-layer catalyst system, and hydrocracking catalyst is stratification on hydroisomerisation catalysts, and ratio is preferably about 1:1 to 15:1.
The hydrocracking zone of this technology comprises hydrocracking catalyst.In the hydrocracking process, high-molecular weight wax molecule is cracked into the boiling range of requirement.In the cracking process, at least some cracking molecules may be also by isomerization.The gained crackate mainly comprises the mixture of alkane and isoalkane, and boiling point is in the scope of want fuel or lube product.According to the inventive method, expectation reduces the cracking of raw material to produce the light product of less amount.
Hydrocracking catalyst is as well known to those skilled in the art.Conventional hydrocracking catalyst generally comprises cracking component, hydrogenation component and tackiness agent or matrix.This type of catalyzer is known in this field.
Matrix component can be many types, includes the more active matrixes of acidic catalyst.There is acid active matrix to comprise the amorphous silica-alumina.Described catalyzer can also comprise large pore zeolite or non-zeolitic crystalline molecular sieve, and wherein macropore is defined as the aperture greater than 7.1 dusts.The example that is fit to molecular sieve comprises Y zeolite, X zeolite and so-called overstable Y zeolite and high structure silica alumina ratio Y zeolite such as US4,401,556,4,820,402 and 5,059, and described in 567.Also can use the Y zeolite of small crystalline size, as US5, described in 073,530.Spendable non-zeolite molecular sieve comprises for example silicon aluminium phosphate (SAPO), phosphoric acid ferro-aluminum, phosphorus titanium aluminate and US4, and 913,799 reach the various ELAPO molecular sieves of describing in the reference of wherein quoting.The details of the preparation of relevant various non-zeolite molecular sieves can be referring to US5,114,563 (SAPO); The reference of quoting in 4,913,799 and US4,913,799.Also can use mesoporous molecular sieve, for example M41S family material (J.Am.Chem.Soc., 114:10834-10843 (1992)), MCM-41 (US5,246,689; 5,198,203; 5,334,368) and MCM-48 (Kresge et al., Nature 359:710 (1992)).The content of above mentioned each patent and public publication all is incorporated herein for reference.The molecular sieve content of preferred hydrocracking catalyst is lower than 2% (weight).
The body material that is fit to also can comprise synthetic or crude substance and inorganic materials such as clay, silicon oxide and/or metal oxide such as silica-alumina, silicon oxide-magnesium oxide, silicon oxide-zirconium white, silicon oxide-Thorotrast, silicon oxide-beryllium oxide, silicon oxide-titanium oxide and ternary composition such as silica-alumina-Thorotrast, silica-alumina-zirconium white, silica-alumina-magnesium oxide and silicon oxide-magnesium oxide-zirconium white.The latter can be natural existence or gelatinous precipitate or comprise silicon oxide and the gel form of metal oxide mixture.Can comprise montmorillonite and kaolin group with catalyzer compound naturally occurring clay.These clays can virgin state such as form use original exploitation or that pass through dealuminzation, acid treatment or chemical modification at first.
Hydrogenation component is VI family, VII family or group VIII metal or its oxide compound or sulfide, one or more of preferred molybdenum, tungsten, cobalt or nickel or its sulfide or oxide compound.If be present in the catalyzer, these hydrogenation component generally account for catalyzer about 5 to about 40% (weight).Perhaps, can exist the platinum metals especially platinum and/or palladium as hydrogenation component, perhaps Individual existence or with base metal hydrogenation component such as molybdenum, tungsten, cobalt or nickel combination.If exist, the platinum metals generally account for catalyzer about 0.1 to about 2% (weight).Can in catalyzer, add hydrogenation component by being total to methods such as grinding, dipping or ion-exchange.
Typical hydrocracking condition comprises: temperature of reaction about 204 to 510 ℃ (400 to 950 ℉), preferred 316 to 399 ℃ (600 to 750 ℉); About 300 to 5000psig (2.1-34.5MPa) of reaction pressure, preferred 500 to 2000psig (5.2-13.8MPa); Liquid hourly space velocity (LHSV) about 0.1 is to 15hr
-1, preferred 0.25 to 2.5hr
-1With about 500 to 5000 standard cubic foots (SCF) of hydrogen recycle speed/bucket liquid hydrocarbon feeds (89.1-890m
3H
2/ m
3Raw material).
Effluent from hydrocracking zone is contacted in the hydroisomerization district with the mesoporous molecular sieve hydroisomerisation catalysts.
When word used herein " mesopore " means porous inorganic oxide and is in calcined form the effective pore radius about 4.8 to the scope of about 7.1 dusts.
The hydroisomerization dewaxing is will be by optionally add the cold flowability that side chain improves lubricating base oil in molecular structure.The hydroisomerization dewaxing realizes the high conversion of wax shape raw material to the non-waxy isoparaffin ideally when reducing by the cracking conversion.
Being applicable to that hydroisomerization dewaxing catalyst of the present invention comprises selects the shape mesoporous molecular sieve and optionally supports catalytically-active metals hydrogenation component on the refractory oxide carrier.Be applicable to that implementing the shape mesoporous molecular sieve of selecting of the present invention generally is one dimension 10-, 11-or 12-unit toroidal molecule sieve.The preferred molecular sieve of the present invention is an one dimension 10-unit ring, and wherein the first toroidal molecule sieve of 10-(or 11-or 12-) has the individual tetrahedral coordination atoms in 10 (or 11 or 12) (T-atom) that connect by oxygen.In the one dimension molecular sieve, the hole of 10-unit's ring (or bigger) is parallel to each other, and does not interconnect.The zeolite inner duct is divided into one dimension, two and three dimensions is that R.M.Barrer is at Zeolites, Science and Technology, edited by F.R.Rodrigues, L.D.Rollmanand C.Naccache, NATO ASI Series, propose in 1984, this classification is incorporated herein (especially referring to 75 pages) for reference.
The shape mesoporous molecular sieve of selecting that is preferred for hydroisomerization dewaxing is based on aluminum phosphate, as SAPO-11, SAPO-31 and SAPO-41.SAPO-11 and SAPO-31 are preferred, and SAPO-11 is most preferred.SM-3 is the particularly preferred shape mesopore SAPO that selects, and the crystalline structure that falls in the SAPO-11 molecular sieve scope is arranged.The preparation of SM-3 and characteristic description thereof be at US4, in 943,424 and 5,158,665.The shape mesoporous molecular sieve of selecting that also is preferred for the hydroisomerization dewaxing is a zeolite, as ZSM-22, ZSM-23, ZSM-35, ZSM-48, ZSM-57, SSZ-32, offretite and ferrierite.SSZ-32 and ZSM-23 are preferred.
The mesoporous molecular sieve that is particularly preferred for the inventive method is described in for example US5, in 135,638 and 5,282,958, all is incorporated herein for reference.At US5, in 282,958, mesoporous molecular sieve has and is not more than the hole that about 0.5 micron crystalline size and minimum diameter are at least about 4.8 dusts, about 7.1 dusts of maximum diameter.This catalyzer has enough acid so that under 370 ℃, pressure 1200psig, hydrogen flowing quantity 160ml/min and input speed 1ml/hr at least 50% of n-Hexadecane is transformed when placing 0.5g in tubular reactor.When this catalyzer uses under the n-hexadecane (n-C16) that makes 96% changes into the condition of other material, also demonstrate 40 or bigger isomerization selectivity (definition of isomerization selectivity is as follows: 100 * (wt% of side chain C16 in the product)/(in the product in the wt%+ product of side chain C16 the wt% of C13-).
This particularly preferred molecular sieve also can have about 4.0 to about 7.1 dust scopes, preferably the free diameter of the crystallography in 4.0 to 6.5 dust scopes characterizes by hole or duct.The free diameter of the crystallography of molecular sieve pore passage is disclosed in ＂ Atlas of Zeolite Framework Types ＂, Fifth Revised Edition, 2001, by Ch.Baerlocher, W.M.Meier, and D.H.Olson, Elsevier among the pp 10-15, is incorporated herein for reference.
If the free diameter of the crystallography of molecular sieve pore passage is unknown, the hydrocarbon compound of available standards adsorption technology and known minimum power diameter is measured the effective pore radius of molecular sieve.Referring to Breck, Zeolite Molecular Sieves, 1974 (especially Chapter 8); Anderson et al.J.Catalysis 58,114 (1979) and US4,440,871, its relative section is incorporated herein for reference.Adsorb measurement to determine adopting standard technique in the aperture.Be convenient to get rid of and be less than about 10 minutes (p/po=0.5; 25 ℃) with interior at least 95% the molecule that does not reach its equilibrium adsorption value on molecular sieve.It is the molecule of 5.3 to 6.5 dusts that the common receivability of mesoporous molecular sieve does not almost have the sterically hindered kinetic diameter.
Be applicable to that hydroisomerization dewaxing catalyst of the present invention comprises the metal hydride of catalytic activity alternatively.Exist the metal hydride of catalytic activity to cause producing improvement, especially VI and stability.The metal hydride of typical catalytic activity comprises chromium, molybdenum, nickel, vanadium, cobalt, tungsten, zinc, platinum and palladium.Especially preferable alloy platinum and palladium, most preferably platinum.If use platinum and/or palladium, the total amount of active metal hydride typically in the scope of 0.1 to 5% (weight) of total catalyst, be generally 0.1 to 2% (weight) and be no more than 10% (weight).
The refractory oxide carrier can be selected from those oxide carriers that are usually used in catalyzer, comprises silicon oxide, aluminum oxide, silica-alumina, magnesium oxide, titanium oxide and combination thereof.
The mesoporous molecular sieve hydroisomerisation catalysts is specially adapted to make the production of n-paraffin hydroisomerization to hang down the product of cloud point, low pour point.Therefore, the distillate fuel that reclaims from hydroisomerisation step has the cloud point of reduction.In addition, hydroisomerisation step makes the depression of pour point of last running, and recyclable at least a portion last running is used for lubricating oil.Transform though estimate also will take place some crackings on hydroisomerisation catalysts, hydroisomerisation step keeps such condition that hygrogenating isomerization reaction is preponderated.
Found to use the cloud point of former hydroisomerization method gained lubricant base oil may very high (more than 0 ℃).Though other isomerization can reduce cloud point, because of cracking and excessive branching cause yield, viscosity index and the viscosity of base oil impaired.
Adopt this hydrocracking/hydroisomerization method, make cracking transform minimizing and in lubricant base oil and middle distillate fuel product, realize low pour point simultaneously.The inventive method causes the cracking of high boiling point end in the high boiling point wax shape raw material less (the high boiling point end that is raw material changes into lacking than light product).Thereby produce viscosity index height, pour point is low and viscosity is higher high quality lubricant base oil.According to the inventive method, preferably make 60% (weight) that be lower than of 343 ℃+(650 ℉+) product in the raw material change into 650 ℉-product.Thereby, adopt this method to make cracking transform minimizing and in product, realize low pour point simultaneously.In addition, because cracking is few, cause the yield height of high quality lubricant base oil products.
Make the product fractionation of this hydrocracking/hydroisomerization method that middle distillate fuel and last running are provided at least by ordinary method.Can by have be fit to separate in the conventional distillating method of fractionation cut point of distillate fuel and last running realize fractionation.
From last running, isolate lubricant base oil.Can comprise that vacuum distilling makes the last running fractionation that the lubricant base oil cut is provided by ordinary method, also separablely alternatively go out tower bottom distillate.Capable of circulation time hydrocracking reaction district of tower bottom distillate.The all or part of circulation time of tower bottom distillate, can make tower bottom distillate separately experience hydrocracking step of the present invention or can with other wax shape hydrocarbon feed combination.The all or part of circulation of tower bottom distillate improves the yield of this technology.
According to the present invention, under the situation that need not add the dewaxing step, from last running, isolate high-quality lubricant base oil.The inventive method provides full-bodied lubricant base oil because of the cracking of high boiling point end in the wax shape raw material is less.60% (weight) that be lower than of 343 ℃+(650 ℉+) product changes into 343 ℃-(650 ℉-) product in the preferred feedstock.The lubricant base oil viscosity index that reclaims by the inventive method greater than 130, be preferably greater than 140, more preferably greater than 150.The lubricant base oil that is provided is lower than-15 ℃ pour point in addition.The viscosity of this lubricant base oil under 100 ℃ greater than 3cSt, preferably under 100 ℃ greater than 4cSt, more preferably under 100 ℃ greater than 5cSt.
The lubricating oil that is reclaimed can be randomly with relax hydride process through hydrofining to improve its heat and oxidative stability.Hydrofining can be carried out in the presence of metal hydrogenation catalyst such as platinum/aluminum oxide traditionally.Hydrofining can be about 190 to about 340 ℃ temperature, about 300 pressure to about 3000psig (2.76-20.7MPa), carry out under the hydrogen recycle speed of the LHSV between about 0.1 and 20 and about 400 to about 1500SCF/bb1.
The lubricant base oil that is reclaimed by the inventive method can be used as for example lubricant, perhaps can with have the refining lubricant oil plant blending of another kind of different nature.Alternatively, described lubricant base oil as before the lubricant can with for example blendings such as antioxidant, extreme-pressure additive and viscosity index improver of one or more additive.
Exemplary
Accompanying drawing is schematic illustration of one embodiment of the invention.With reference to the accompanying drawings, wax shape hydrocarbon feed (10) infeeds at hydrocracking zone (110) and hydrocracking catalyst is housed and is equipped with in the single reaction vessel (100) of hydroisomerisation catalysts in hydroisomerization district (120), and wherein hydrocracking zone (110) is positioned on the hydroisomerization district (120).Wax shape hydrocarbon feed (10) contacts with hydrocracking catalyst in the hydrocracking zone (110) earlier, contacts with hydroisomerization district (120) interior hydroisomerisation catalysts from the effluent of hydrocracking zone (110) again.From whole effluents (20) fractionation in fractionator (200) of hydroisomerization district (120), obtain last running (30), middle distillate fuel (50) and light product (70) then.Obtain lubricant base oil (60) and obtain tower bottom distillate (40) alternatively by last running (30).The viscosity index of this lubricant base oil greater than 130, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 3cSt.Alternatively, the hydrocracking zone (110) in the capable of circulation time reactor of tower bottom distillate (40) (100).Except that lubricant base oil (60), cut product (50) during described fractionation also produces.At last, can randomly in hydro-refining unit (300), provide hydrorefined lubricating oil (70) with lubricant base oil (60) hydrofining.
Now by the full and clear the present invention of following examples, these embodiment will illustrate and restriction anything but.
Embodiment
Embodiment 1
Go up at 1.2hr at nickel-tungsten/silica-alumina hydrocracking catalyst (catalyst A)
-1371 ℃+(700 ℉+) transformation efficiency with 68% under LHSV and the 1800psig makes the hydrocracking of 232 ℃+(450 ℉+) Arab Heavy VGO first class product, and the pour point of described 371 ℃+(700 ℉+) tower bottom distillate is+21 ℃, and VI is 125.On the contrary, using the multi-compartment bed of 2:1 catalyst A/PtSAPO-11 hydroisomerisation catalysts (catalyst B) to obtain pour point under the same conditions is 385 ℃+(725 ℉+) product (100 ℃ of following 4cSt) of 127 for-20 ℃ and VI.Compare with the situation with catalyst A only, the cloud point of this diesel oil distillate descends and the cetane value index improves.In the cut total amount be 56.9% (weight), and be 53.1% (weight) during only with catalyst A, partly cause is that the diesel oil end points is extended to 385 ℃ (725 ℉) from 371 ℃ (700 ℉).
Embodiment 2
On sulfurized nickel-tungsten/silica-alumina catalyzer at 1hr
-1Make light fischer-tropsch wax (Table I) hydrocracking under LHSV, 1000psig, 363 ℃ (685 ℉) and the 6300SCF/Bb1.Under these conditions, 343 ℃ (650 ℉) following transformation efficiency is 80.4% (weight).Cut the liquid product cut at about 177 ℃ (350 ℉) and about 357 ℃ (675 ℉) and obtain diesel oil distillate.The yield and the character of diesel oil distillate and 357 ℃+(675 ℉+) tower bottom distillate are shown in the Table II.Not preferred in the cloud point of tower bottom distillate (+29 ℃) Tai Gao so that the lubricant applications.
Table I
| Describe | Light fischer-tropsch wax |
| Proportion, API | 42.5 |
| Nitrogen, ppm | 3.2 |
| Sim.Dist.，LV％，℉ | |
| ST/5 | 728/771 |
| 10/30 | 789/811 |
| 50 | 839 |
| 70/90 | 858/885 |
| 95/EP | 898/943 |
Table II
| Transformation efficiency＜343 ℃, wt% | 80.4 |
| Yield, wt% | |
| C 1-C 2 | 0.03 |
| C 3-C 4 | 5.06 |
| C 5-82℃ | 17.77 |
| 82-177℃(180-350℉) | 20.85 |
| 177-343℃(350-650℉) | 37.51 |
| 343℃+(650℉+) | 19.71 |
| C 5+ | 95.49 |
| 177-357℃(350-675℉) | |
| The wt% of raw material | 52.9 |
| Proportion, API | 50.7 |
| Viscosity, 40 ℃, cSt | 2.631 |
| Cloud point, ℃ | -26 |
| Aromatic hydrocarbons, (SFC), wt% | |
| Total amount | <0.5 |
| PNA | Do not detect |
| The cetane value index | 75.9 |
| Refractive index | 1.4342 |
| Density, g/ml | 0.7745 |
| Molecular weight | 253 |
| P/N/A carbon | 100/0/0 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 288/342 |
| 10/30 | 368/448 |
| 50 | 523 |
| 70/90 | 594/673 |
| 95/EP | 697/743 |
| 357℃+(675℉+) | |
| The wt% of raw material | 14.1 |
| Cloud point, ℃ | +29 |
| Viscosity, 100 ℃, cSt | 3.364 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 700/722 |
| 10/30 | 732/777 |
| 50 | 808 |
| 70/90 | 829/857 |
| 95/EP | 871/900 |
Embodiment 3
On the catalyzer identical of sulfurized 3/1 bed/, make with 15% (weight) aluminum oxide adherent Pt/SAPO-11 catalyzer with embodiment 2 with embodiment 2 in identical raw material hydrocracking.Identical among condition and the embodiment 2, promptly total LHSV 1.0hr
-1, 1000psig, 363 ℃ (685 ℉) and 6.3MSCF/Bbl H
2343 ℃ of (650 ℉) following transformation efficiencys are 74.6% (weight).Cut the product cut at about 177 ℃ (350 ℉) and about 343 ℃ (650 ℉) and obtain diesel oil distillate.The yield and the character of diesel oil distillate and 343 ℃+(650 ℉+) tower bottom distillate are shown in the Table III.As measuring by ASTMD6468, this diesel oil is high-temperature stable.Aromatic hydrocarbons is less than 0.5% (weight) in this diesel oil.Cetane value index high (73.8), cloud point extremely low (57 ℃).Record these 343 ℃+(650 ℉+) stripping tower tower bottom distillate and be pour point and cloud point is low and 3cSt (under 100 ℃) oil that VI is high.
Table III
| Transformation efficiency＜343 ℃ (650 ℉), wt% | 74.6 |
| Yield, wt% | |
| C 1-C 2 | 0.08 |
| C 3-C 4 | 5.16 |
| C 5-82℃(180℉) | 13.02 |
| 82-177℃(180-350℉) | 15.70 |
| 177-343℃(350-650℉) | 40.97 |
| 343℃+(650℉+) | 25.59 |
| C 5+ | 95.36 |
| 177-343℃(350-650℉) | |
| The wt% of raw material | 43.1 |
| Proportion, API | 51.3 |
| Viscosity, 40 ℃, cSt | 2.206 |
| Cloud point, ℃ | -57 |
| Alkene, wt% (GC-MS) | Do not detect |
| Aromatic hydrocarbons (SFC), wt% | |
| Total amount | <0.5 |
| PNA | Do not detect |
| High-temperature stability, 150 ℃, % reflectivity, ASTM D6468 | |
| 1.5hr | 99.7 |
| 3.0hr | 99.8 |
| The cetane value index | 73.8 |
| Refractive index | 1.4318 |
| Density, g/ml | 0.7699 |
| Molecular weight | 239 |
| P/N/A carbon | 100/0/0 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 314/352 |
| 10/30 | 370/433 |
| 50 | 496 |
| 70/90 | 549/606 |
| 95/EP | 629/676 |
| 343℃+(650℉+) | |
| The wt% of raw material | 29.7 |
| Pour point, ℃ | -39 |
| Cloud point, ℃ | -26 |
| Viscosity, 40 ℃, cSt | 10.69 |
| 100℃，cSt | 2.849 |
| VI | 114 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 602/627 |
| 10/30 | 641/690 |
| 50 | 736 |
| 70/90 | 798/837 |
| 95/EP | 851/880 |
Embodiment 4
Continue operation embodiment 3, but catalyst temperature is 354 ℃ (670 ℉).Under this temperature, 343 ℃ of (650 ℉) following transformation efficiencys are 40.1% (weight).The yield and the character of 343 ℃+(650 ℉+) stripping tower tower bottom distillate are shown in the Table IV.Record the 3.4cSt that this is high VI (under 100 ℃) oil.
Table IV
| Transformation efficiency＜343 ℃ (650 ℉), wt% | 40.1 |
| Yield, wt% | |
| C 1-C 2 | 0.08 |
| C 3-C 4 | 5.69 |
| C 5-82℃(180℉) | 7.36 |
| 82-177℃(180-350℉) | 6.60 |
| 177-343℃(350-650℉) | 20.61 |
| 343℃+(650℉+) | 60.25 |
| C 5+ | 94.83 |
| 343℃+(650℉+) | |
| The wt% of raw material | 64.4 |
| Pour point, ℃ | -8 |
| Cloud point, ℃ | 0 |
| Viscosity, 40 ℃, cSt | 13.33 |
| 100℃，cSt | 3.433 |
| VI | 138 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 587/639 |
| 10/30 | 678/775 |
| 50 | 817 |
| 70/90 | 840/869 |
| 95/EP | 881/911 |
Embodiment 5
Fasten FT wax (Table V) hydrocracking that 371-538 ℃ of (700-1000 ℉) hydrogen treatment crossed at many beds catalyst body identical with embodiment 3.Condition comprises total LHSV1.0hr
-1, reactor pressure 300psig, top catalyzer 360 ℃ (680 ℉), following catalyzer 366 ℃ of (690 ℉) and 6.3MSCF/Bbl H
2343 ℃ of (650 ℉) following transformation efficiencys are 58.2% (weight).Cut the product cut at about 149 ℃ (300 ℉) and about 343 ℃ (650 ℉) and obtain diesel oil distillate.The yield and the character of diesel oil distillate and 343 ℃+(650 ℉+) tower bottom distillate are shown in the Table VI.Measuring this diesel oil by ASTM D6468 is high-temperature stable.Aromatic hydrocarbons accounts for 6.1% (weight) in this diesel oil.Cetane value index height (67.6), cloud point are-44 ℃.Record these 343 ℃+(650 ℉+) stripping tower tower bottom distillate and be pour point and cloud point is low and 5cSt (under 100 ℃) oil that VI is high.
Table V
| Describe | The 371-538 ℃ of fischer-tropsch wax that (700-1000 ℉) hydrogen treatment is crossed |
| Proportion, API | 42.3 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 691/804 |
| 10/30 | 824/884 |
| 50 | 919 |
| 70/90 | 940/974 |
| 95/EP | 991/1031 |
Table VI
| Transformation efficiency＜343 ℃ (650 ℉), wt% | 58.2 |
| Yield, wt% | |
| C 1-C 2 | 0 |
| C 3-C 4 | 4.78 |
| C 5-82℃(180℉) | 14.93 |
| 82-177℃(180-350℉) | 15.53 |
| 177-343℃(350-650℉) | 23.22 |
| 343℃+(650℉+) | 41.92 |
| C 5+ | 95.7 |
| 177-343℃(350-650℉) | |
| The wt% of raw material | 31.1 |
| Proportion, API | 50.1 |
| Viscosity, 40 ℃, cSt | 2.027 |
| Cloud point, ℃ | -44 |
| Alkene, wt% (GC-MS) | Do not detect |
| Aromatic hydrocarbons (SFC), wt% | |
| Total amount | 6.1 |
| PNA | 0.5 |
| High-temperature stability, 150 ℃, % reflectivity, ASTM D6468 | |
| 1.5hr | 99.2 |
| 3.0hr | 99.2 |
| The cetane value index | 67.6 |
| Refractive index | 1.4348 |
| Density, g/ml | 0.7741 |
| Molecular weight | I96 |
| P/N/A carbon | 92.40/5.01/2.59 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 266/300 |
| 10/30 | 325/396 |
| 50 | 472 |
| 70/90 | 561/645 |
| 95/EP | 667/698 |
| 343℃+(650℉+) | |
| The wt% of raw material | 41.0 |
| Pour point, ℃ | -26 |
| Cloud point, ℃ | -5 |
| Viscosity, 40 ℃, cSt | 22.04 |
| 100℃，cSt | 4.882 |
| VI | 151 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 681/710 |
| 10/30 | 732/803 |
| 50 | 856 |
| 70/90 | 896/937 |
| 95/EP | 954/990 |
Embodiment 6
Fasten fischer-tropsch wax (Table VII) (raw material of Table V the is prepared therefrom) hydrocracking that full boiling range hydrogen treatment is crossed at many beds catalyst body identical with embodiment 3.Condition comprises total LHSV 1.0hr
-1, reactor pressure 1000psig, top catalyzer 360 ℃ (680 ℉), following catalyzer 366 ℃ of (691 ℉) and 6.3MSCF/Bbl H
2343 ℃ of (650 ℉) following transformation efficiencys are 45.9% (weight).The yield and the character of 343 ℃+(650 ℉+) tower bottom distillate are shown in the Table VIII.Record this and be that pour point is low and 5.5cSt (under 100 ℃) oil that VI is high.
Table VII
| Describe | The fischer-tropsch wax that full boiling range hydrogen treatment is crossed |
| Proportion, API | 38.2 |
| Nitrogen, ppm | 1.9 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 791/856 |
| 10/30 | 876/942 |
| 50 | 995 |
| 70/90 | 1031/1085 |
| 95/EP | 1107/1133 |
Table VIII
| Transformation efficiency＜343 ℃ (650 ℉), wt% | 45.9 |
| Yield, wt% | |
| C 1-C 2 | 0.06 |
| C 3-C 4 | 3.99 |
| C 5-82℃(180℉) | 5.76 |
| 82-177℃(180-350℉) | 8.21 |
| 177-343℃(350-650℉) | 27.91 |
| 343℃+(650℉+) | 54.34 |
| C 5+ | 96.44 |
| 343℃+(650℉+) | |
| The wt% of raw material | 52.5 |
| Pour point, ℃ | -18 |
| Cloud point, ℃ | +10 |
| Viscosity, 40 ℃, cSt | 26.58 |
| 100℃，cSt | 5.529 |
| VI | 152 |
| Simulation distil, LV% ， ℉ | |
| ST/5 | 666/706 |
| 10/30 | 739/847 |
| 50 | 909 |
| 70/90 | 966/1056 |
| 95/EP | 1083/1138 |
Various modifications of the present invention without departing from the scope and spirit of the present invention and change apparent to those skilled in the art.According to above description, other purpose and advantage are apparent to those skilled in the art.
Claims (32)
1. the treatment process of a wax shape hydrocarbon feed may further comprise the steps:
A) raw material is contacted with hydrocracking catalyst at hydrocracking zone and produce the hydrocracking effluent;
B) hydrocracking effluent and mesoporous molecular sieve hydroisomerisation catalysts are contacted in the hydroisomerization district and produce the hydroisomerization effluent;
C) make the fractionation of hydroisomerization effluent obtain last running and middle distillate fuel; With
D) from last running, isolate the lubricant base oil cut, the viscosity index of this lubricant base oil greater than 130, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 3cSt.
2. the process of claim 1 wherein the viscosity index of lubricant base oil greater than 140, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 4cSt.
3. the process of claim 1 wherein the viscosity index of lubricant base oil greater than 150, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 5cSt.
4. the process of claim 1 wherein whole hydrocracking effluents are contacted in the hydroisomerization district with hydroisomerisation catalysts.
5. the process of claim 1 wherein hydrocracking catalyst and the hydroisomerisation catalysts single reaction district stratification in single reaction vessel.
6. the process of claim 1 wherein and hydrocracking catalyst and hydroisomerisation catalysts stratification in the tandem reactor of close-coupled do not have products export or feed(raw material)inlet between the reactor.
7. the method for claim 1 also comprises making the heavy tower bottom distillate loop back hydrocracking zone.
8. the process of claim 1 wherein that wax shape hydrocarbon feed comprises 343 ℃ fischer-tropsch derived+(650 ℉+) raw material.
9. the process of claim 1 wherein that wax shape hydrocarbon feed comprises 482 ℃+(900 ℉+) component more than 20wt%.
10. the process of claim 1 wherein that wax shape hydrocarbon feed comprises 343 ℃+(650 ℉+) component more than 85wt%, 343 ℃+(the 650 ℉+) component that wherein is lower than 60wt% changes into 343 ℃-(650 ℉-) product.
11. the treatment process of one kind 343 ℃+(650 ℉+) wax shape hydrocarbon feed may further comprise the steps:
A) raw material is contacted with hydrocracking catalyst at hydrocracking zone and produce the hydrocracking effluent;
B) hydrocracking effluent and mesoporous molecular sieve hydroisomerisation catalysts are contacted in the hydroisomerization district and produce the hydroisomerization effluent;
C) make the fractionation of hydroisomerization effluent obtain last running and middle distillate fuel; With
D) from last running, isolate the lubricant base oil cut, the viscosity index of this lubricant base oil greater than 130, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 3cSt, 343 ℃+(the 650 ℉+) component that wherein is lower than 60wt% changes into 343 ℃-(650 ℉-) product.
12. the method for claim 11, wherein the viscosity index of lubricant base oil greater than 140, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 4cSt.
13. the method for claim 11, wherein the viscosity index of lubricant base oil greater than 150, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 5cSt.
14. the method for claim 11, wherein hydrocracking catalyst and the hydroisomerisation catalysts single reaction district stratification in single reaction vessel.
15. the method for claim 11, wherein 343 ℃+(650 ℉+) wax shape hydrocarbon feed is from Fischer-Tropsch process.
16. the method for claim 15, wherein 343 ℃+(650 ℉+) wax shape hydrocarbon feed unhydrogenation before hydrocracking is handled.
17. the method for claim 11, wherein 343 ℃+(650 ℉+) wax shape hydrocarbon feed comprises 482 ℃+(900 ℉+) component more than 20wt%.
18. the method for claim 11, wherein 343 ℃+(650 ℉+) wax shape hydrocarbon feed comprises 343 ℃+(650 ℉+) component more than 85wt%.
19. the method for claim 11, wherein hydrocracking catalyst and hydroisomerisation catalysts stratification in the tandem reactor of close-coupled does not have products export or feed(raw material)inlet between the reactor.
20. the method for claim 11 also comprises making the heavy tower bottom distillate loop back hydrocracking zone.
21. the treatment process of one kind 343 ℃+(650 ℉+) wax shape hydrocarbon feed may further comprise the steps:
A) raw material is contacted with hydrocracking catalyst at hydrocracking zone and produce the hydrocracking effluent;
B) hydrocracking effluent and mesoporous molecular sieve hydroisomerisation catalysts are contacted in the hydroisomerization district and produce the hydroisomerization effluent;
C) make the fractionation of hydroisomerization effluent obtain last running and middle distillate fuel; With
D) from last running, isolate the lubricant base oil cut, the viscosity index of this lubricant base oil greater than 130, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 4cSt, wherein 343 ℃+(650 ℉+) wax shape hydrocarbon feed comprises 482 ℃+(900 ℉+) component more than 20wt%.
22. the method for claim 21, wherein 343 ℃+(650 ℉+) wax shape hydrocarbon feed comprises 482 ℃+(900 ℉+) component more than 40wt%.
23. the method for claim 21, wherein 343 ℃+(650 ℉+) wax shape hydrocarbon feed comprises 482 ℃+(900 ℉+) component more than 60wt%.
24. the method for claim 21, wherein the viscosity index of lubricant base oil greater than 140, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 4cSt.
25. the method for claim 21, wherein the viscosity index of lubricant base oil greater than 150, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 5cSt.
26. the method for claim 21, wherein hydrocracking catalyst and the hydroisomerisation catalysts single reaction district stratification in single reaction vessel.
27. the method for claim 21, wherein 343 ℃+(650 ℉+) wax shape hydrocarbon feed is from Fischer-Tropsch process.
28. the method for claim 21, wherein hydrocracking catalyst and hydroisomerisation catalysts stratification in the tandem reactor of close-coupled does not have products export or feed(raw material)inlet between the reactor.
29. the method for claim 21 also comprises and isolates tower bottom distillate and make the heavy tower bottom distillate loop back hydrocracking zone from last running.
30. the method for claim 23, wherein the viscosity index of lubricant base oil greater than 140, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 4cSt.
31. the method for claim 23, wherein the viscosity index of lubricant base oil greater than 150, pour point is lower than-15 ℃ and 100 ℃ of following viscosity greater than 5cSt.
32. the method for claim 21,343 ℃+(650 ℉+) component of wherein 343 ℃+(650 ℉+) wax shape hydrocarbon feed are lower than 60wt% and change into 343 ℃-(650 ℉-) product.
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| US10/464,566 | 2003-06-19 | ||
| US10/464,566 US20040256286A1 (en) | 2003-06-19 | 2003-06-19 | Fuels and lubricants using layered bed catalysts in hydrotreating waxy feeds, including Fischer-Tropsch wax |
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- 2003-06-19 US US10/464,566 patent/US20040256286A1/en not_active Abandoned
-
2004
- 2004-06-16 CN CNB2004800234564A patent/CN100469858C/en not_active Expired - Fee Related
- 2004-06-16 BR BRPI0411616-0A patent/BRPI0411616A/en not_active Application Discontinuation
- 2004-06-16 AU AU2004252511A patent/AU2004252511B2/en not_active Expired
- 2004-06-16 ZA ZA200600303A patent/ZA200600303B/en unknown
- 2004-06-16 GB GB0600805A patent/GB2418673B/en not_active Expired - Fee Related
- 2004-06-16 JP JP2006517326A patent/JP5481014B2/en not_active Expired - Lifetime
- 2004-06-16 WO PCT/US2004/019253 patent/WO2005001006A2/en active Application Filing
- 2004-06-18 NL NL1026464A patent/NL1026464C2/en not_active IP Right Cessation
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5288395A (en) * | 1991-07-24 | 1994-02-22 | Mobil Oil Corporation | Production of high viscosity index lubricants |
Also Published As
| Publication number | Publication date |
|---|---|
| AU2004252511B2 (en) | 2010-02-25 |
| AU2004252511A1 (en) | 2005-01-06 |
| NL1026464C2 (en) | 2005-08-09 |
| GB2418673A (en) | 2006-04-05 |
| JP2007520580A (en) | 2007-07-26 |
| WO2005001006A2 (en) | 2005-01-06 |
| CN1836028A (en) | 2006-09-20 |
| NL1026464A1 (en) | 2004-12-21 |
| GB0600805D0 (en) | 2006-02-22 |
| WO2005001006A3 (en) | 2005-04-28 |
| JP5481014B2 (en) | 2014-04-23 |
| BRPI0411616A (en) | 2006-08-08 |
| US20040256286A1 (en) | 2004-12-23 |
| ZA200600303B (en) | 2007-11-28 |
| GB2418673B (en) | 2008-05-28 |
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