US3896025A - Production of improved lubricating oils - Google Patents
Production of improved lubricating oils Download PDFInfo
- Publication number
- US3896025A US3896025A US370246A US37024673A US3896025A US 3896025 A US3896025 A US 3896025A US 370246 A US370246 A US 370246A US 37024673 A US37024673 A US 37024673A US 3896025 A US3896025 A US 3896025A
- Authority
- US
- United States
- Prior art keywords
- lubricating oil
- hydrocracking
- viscosity
- solvent
- oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
- 239000010687 lubricating oil Substances 0.000 title claims abstract description 32
- 238000004519 manufacturing process Methods 0.000 title claims description 8
- 238000004517 catalytic hydrocracking Methods 0.000 claims abstract description 29
- 238000000034 method Methods 0.000 claims description 30
- 239000003054 catalyst Substances 0.000 claims description 17
- 239000002904 solvent Substances 0.000 claims description 13
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 12
- 238000009835 boiling Methods 0.000 claims description 11
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical group O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 claims description 10
- 229910052751 metal Inorganic materials 0.000 claims description 9
- 239000002184 metal Substances 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 9
- 239000011148 porous material Substances 0.000 claims description 9
- 239000000463 material Substances 0.000 claims description 8
- 229910052809 inorganic oxide Inorganic materials 0.000 claims description 7
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical group CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 claims description 6
- 239000000377 silicon dioxide Substances 0.000 claims description 6
- 238000004821 distillation Methods 0.000 claims description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 4
- 150000001875 compounds Chemical class 0.000 claims description 4
- 238000000638 solvent extraction Methods 0.000 claims description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims description 2
- 238000004064 recycling Methods 0.000 abstract 1
- 239000001257 hydrogen Substances 0.000 description 21
- 229910052739 hydrogen Inorganic materials 0.000 description 21
- 239000003921 oil Substances 0.000 description 21
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 20
- 239000000047 product Substances 0.000 description 14
- 238000006243 chemical reaction Methods 0.000 description 8
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- 238000007670 refining Methods 0.000 description 6
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 239000007789 gas Substances 0.000 description 4
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 3
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000004927 clay Substances 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 2
- ZOKXTWBITQBERF-UHFFFAOYSA-N Molybdenum Chemical compound [Mo] ZOKXTWBITQBERF-UHFFFAOYSA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 2
- MCMNRKCIXSYSNV-UHFFFAOYSA-N Zirconium dioxide Chemical compound O=[Zr]=O MCMNRKCIXSYSNV-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 125000003118 aryl group Chemical group 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000010941 cobalt Substances 0.000 description 2
- 229910017052 cobalt Inorganic materials 0.000 description 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 229910052750 molybdenum Inorganic materials 0.000 description 2
- 239000011733 molybdenum Substances 0.000 description 2
- 239000008188 pellet Substances 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- VYZAMTAEIAYCRO-UHFFFAOYSA-N Chromium Chemical compound [Cr] VYZAMTAEIAYCRO-UHFFFAOYSA-N 0.000 description 1
- 244000304337 Cuminum cyminum Species 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 239000010426 asphalt Substances 0.000 description 1
- 239000002199 base oil Substances 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 229910052810 boron oxide Inorganic materials 0.000 description 1
- 239000001273 butane Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 239000011651 chromium Substances 0.000 description 1
- WHDPTDWLEKQKKX-UHFFFAOYSA-N cobalt molybdenum Chemical compound [Co].[Co].[Mo] WHDPTDWLEKQKKX-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- JKWMSGQKBLHBQQ-UHFFFAOYSA-N diboron trioxide Chemical compound O=BOB=O JKWMSGQKBLHBQQ-UHFFFAOYSA-N 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- -1 distillation Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229910052736 halogen Inorganic materials 0.000 description 1
- 150000002367 halogens Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000001050 lubricating effect Effects 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910052976 metal sulfide Inorganic materials 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- DDTIGTPWGISMKL-UHFFFAOYSA-N molybdenum nickel Chemical compound [Ni].[Mo] DDTIGTPWGISMKL-UHFFFAOYSA-N 0.000 description 1
- 239000010707 multi-grade lubricating oil Substances 0.000 description 1
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 1
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 1
- 229910052759 nickel Inorganic materials 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
- 239000001294 propane Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000005486 sulfidation Methods 0.000 description 1
- 125000000101 thioether group Chemical group 0.000 description 1
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 description 1
- 229910052721 tungsten Inorganic materials 0.000 description 1
- 239000010937 tungsten Substances 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 239000010457 zeolite 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
- 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
- C10G67/0409—Extraction of unsaturated hydrocarbons
- C10G67/0445—The hydrotreatment being a hydrocracking
-
- 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
Definitions
- This invention relates to the production of improved petroleum oils. More particularly it is concerned with the production of base oils of high viscosity index suitable for blending into multigrade lubricating oils, automatic transmission fluids and other specialty oils requiring high viscosity index. In one of its more specific aspects, it is concerned with the production of high viscosity index lubricating oils in good yield from lubricating oil charge stocks using a process sequence which includes in a preferred embodiment hydrocracking, selective fractionation and dewaxing.
- distillation is employed as a means of separating a crude oil into fractions of various viscosities
- solvent refining with, for example, furfural, sulfur dioxide or N-methyl-2- pyrrolidone is ordinarily used as a means of removing aromatic compounds and thereby improving the viscosity index
- solvent dewaxing using for example a mixture of methyl ethyl ketone and toluene is used to improve low temperature properties by lowering the pour point of the oil and clay contacting is used generally as a final step to further improve the color and to neutralize the oil, after it has been acid treated to improve color, oxidation and heat stability.
- a crude oil is topped under atmospheric pressure to produce light distillates such as naphtha, kerosene and atmospheric gas oils and an atmospheric reduced crude which is then vacuum distilled to produce lube oil distillates with the residue from the vacuum distillation being deasphalted to yield residual lubricating stocks.
- light distillates such as naphtha, kerosene and atmospheric gas oils
- an atmospheric reduced crude which is then vacuum distilled to produce lube oil distillates with the residue from the vacuum distillation being deasphalted to yield residual lubricating stocks.
- the various lube oil fractions are then further processed by solvent refining and dewaxing. With the advent of mild hydrogenation, acid treating and clay contacting have more or less fallen into disuse.
- a crude petroleum lubricating oil is subjected to hydrocracking to improve its viscosity index, the hydrocraclted product is subjected to selective fractionation, the desired fraction is dewaxed and that portion boiling above the desired fraction is recycled to the hydrocracking zone.
- the process of the invention may be applied to a variety of petroleum feedstocks.
- the feed may be obtained by subjecting a vacuum residuum to deasphalting with a low molecular weight hydrocarbon such as propane or butane.
- the deasphalted residuum can then be hydrocracked.
- a wax distillate as feed to the hydrocracking stage.
- the feed whether obtained by distillation or by deasphalting a vacuum residuum may be subjected to hydrocracking.
- a lubricating oil fraction which has been obtained from a residuum such as an atmospheric residuum or vacuum residuum by a simultaneous deasphalting-solvent refining procedure in which the residuum is treated not with the conventional low molecular weight hydrocarbon deasphalting agents but with a solvent such as furfural or N-methyl- 2-pyrrolidone and the raffinate of reduced aromatic and asphalt content is charged to the hydrocracking zone.
- the reaction conditions for the hydrocracking may be varied depending on the product desired and on the charge stock. Typical reaction conditions include a temperature of about 700-900F., preferably 750-850F.
- the hydrogen partial pressure may range between about 500 and 5000 psig. a preferred range being from 1500 to 3000 psig.
- Space velocities may vary between about 0.1 and 3.0 v/v/hr. with a preferred range being 0.2-1.0 Hydrogen rates of from l000l0,000 SCFB have been found satisfactory al though rates of 3000-7000 SCFB are preferred.
- Hydrogen from any suitable source such as electrolytic hydrogen, hydrogen obtained from the partial combustion of hydrocarbonaceous material followed by shift conversion and purification or catalytic reformer by-product hydrogen may be used.
- the hydrogen should have a purity of between about 50 and 100% with hydrogen purities of at least 65 volume being preferred, a particularly preferred range being -95% purity.
- the oil and hydrogen ordinarily are preheated and brought into contact with a particulate catalyst.
- the catalyst may be in the form of a fixed bed, a moving bed, a fluidized bed or may be slurried with the oil.
- hydrogen flow may be upward or downward through the reactor as may be the flow of the oil.
- both the oil and a portion of the hydrogen are introduced at the top of a reactor containing a fixed bed of the catalyst, the balance of the hydrogen being introduced at intermediate points in the reactor for cooling purposes.
- the catalyst for the hydrocracking step preferably comprises as a hydrogenating component a compound of a Group VI metal such as molybdenum, chromium or tungsten or a compound of a Group VIII metal such as cobalt, iron or nickel and mixtures thereof.
- a Group VI metal such as molybdenum, chromium or tungsten
- a Group VIII metal such as cobalt, iron or nickel and mixtures thereof.
- the catalyst is charged to the reactor in oxide form although it can be expected that some reduction and some sulfidation take place during the course of the process so that after being on stream for some time, the catalyst is probably a mixture of the metal, the metal sulfide and perhaps the oxide.
- the catalyst after being charged to the reactor but prior to the institution of the on-stream period may be converted at least in part to the sulfide form for example by contact with a gas such as a mixture of hydrogen and sulfiding agent, e.g. hydrogen sulfide, methyl mercaptan or carbon disulfide at an elevated temperature, eg 400F.
- a gas such as a mixture of hydrogen and sulfiding agent, e.g. hydrogen sulfide, methyl mercaptan or carbon disulfide at an elevated temperature, eg 400F.
- the group VIII metal may be present in an amount varying from I to 20% by weight of the total catalyst composite, preferably 2-l5% and the group VI metal may be present in an amount ranging from about 540%, preferably 7-25%.
- Preferred combinations are nickel-tungsten, nickel-molybdenum and cobaltmolybdenum.
- the hydrogenating component is supported on a refractory inorganic oxide such as hydrogen form or decationized zeolite Y, alumina, zirconia, silica or magnesia and mixtures thereof optionally promoted with an acidic material such as boron oxide or a halogen.
- a refractory inorganic oxide such as hydrogen form or decationized zeolite Y, alumina, zirconia, silica or magnesia and mixtures thereof optionally promoted with an acidic material such as boron oxide or a halogen.
- the catalyst has a surface area of at least 150 m lg, a pore volume of at least 0.5 cc/g a major portion of the pore volume being made up of pores having an average pore diameter between 50 and I A.
- the upper limit of the surface area and pore volume is governed. by the hardness and ruggedness of the catalyst. As a practical matter, for commercial installations where the catalyst is used in units capable of processing several thousand barrels of charge per day, the surface area probably should not exceed about 600 mlg and the pore volume should not exceed about 0.8 cc/g.
- the catalyst which may be in the shape of pellets, extrudates or spheres, may be prepared by any of the methods well known in the art, such as by impregnating the support with a solution of a salt of one of the metals, filtering, drying and then if desired impregnating with a solution of a salt of another metal, filtering, drying and calcining in a manner well known in the art.
- the effluent from the hydrocracking zone is cooled and, in one embodiment of the invention, hydrogenrich gas is separated therefrom and recylced to the hydrocracking zone.
- the hydrogen-rich stream is treated to remove any hydrogen sulfide and ammonia contained therein or a portion thereof may be bled from the system to prevent the build-up of hydrogen sulfide, ammonia and/or low molecular weight hydrocarbons.
- Hydrogen is added to the recycle stream to replace that consumed by the hydrocracking and if necessary to replace any hydrogen purged from the system.
- the balance of the hydrocracking zone effluent then is passed to a low pressure separator for the removal of low molecular weight hydrocarbons and then to a fractionator for removal of hydrocarbons boiling below about 600F.
- the 600F+ material may be sent to a second fractionator to obtain a lube oil fraction of the desired flash point and viscosity or the low pressure separator bottoms may be fractionated to produce suitable flash point and viscosity material in the initial frac' tionator.
- the desired flash point is obtained by removing the light ends and an oil of the desired viscosity may be removed from the fractionator as a side stream or heart cut.
- the high viscosity bottoms may then be returned to the hydrocracking zone.
- the oil should be subjected to a solvent extraction treatment using a selective solvent such 'as furfural or N-methyl-Z- pyrrolidone in any conventional liquid-liquid contacting apparatus such as a packed'column, a centrifugal contactor, a rotating disc contactor or the like.
- a selective solvent such 'as furfural or N-methyl-Z- pyrrolidone
- any conventional liquid-liquid contacting apparatus such as a packed'column, a centrifugal contactor, a rotating disc contactor or the like.
- the solvent extraction is carried out at any stage of the process after the hydrocracking, preferably immediately prior to dewaxing.
- the charge is a deasphalted residuum l-Iydrocracking of the charge oil is effected by passing it downwardly with hydrogen through a bed of catalyst pellets containing 2.3 wt. cobalt, I03 wt. molybdenum, 3.9 wt. silica and 79.7 wt. alumina having a pore volume of 0.63 cc/g and a surface area of 290 m /g at a temperature of 805F., a pressure of 1500 psig, 5000 SCFB of purity hydrogen at an hourly space velocity of 0.5 volumes of charge oil per volume of catalyst per hour.
- the 600F.+ portion of the prodnot, obtained in 63.8 volume per cent basis charge to the hydrocracker has the following characteristics:
- Example II follows the procedure of our invention in which a high viscosity oil having substantially the same flash point as that obtained in Example I is produced without incurring a loss in viscosity index.
- the flow differs from that of Example I in that the charge includes a recycle fraction obtained by fractionating the hydrocracked product to produce a heart cut having a suitable flash point and the desired (pre-dewaxed) viscosity. This is accomplished by topping the 600F.+ hydrocracked fraction to obtain an oil of suitable flash point and cutting out an intermediate fraction which,
- the fractionator is operated at an average vacuum of 29.2 inches of mercury and a maximum temperature of 680F.
- the charge, including recycle, has the following characteristics:
- Example I By way of comparison, by the procedure of Example I, a dewaxed oil having a viscosity SUS at 100F. of I49 would have a viscosity index of less than 108.
- a process for the production of a lubricating oil of specified flash point and viscosity which comprises subl5 jecting a crude lubricating oil to catalytic hydrocraclting, distilling the hydrocraclced product to remove material boiling up to about 600F., subjecting the hydrocracked fraction boiling above about 600F. to additional distillation to obtain a lubricating oil having a predetermined flash point, distilling said lubricating oil of predetermined flash point until a heart out is obtained having substantially the same viscosity as said fraction boiling above about 600F., returning the remainder of the hydrocracked fraction boiling above said heart cut to the hydrocracking zone and dewaxing said heart cut.
- the hydrocracking catalyst comprises a Group Vlll metal or compound thereof supported on an amorphous inorganic oxide having a surface area of at least 250 mlg and a pore volume of at least 0.5 cc/g.
- amorphous inorganic oxide comprises a mixture of silica and alumina.
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
Lube oils of improved viscosity index are produced by subjecting a crude lubricating oil to hydrocracking, selectively fractionating the hydrocracked product to yield a product having the desired flash point and viscosity and recycling the fractionator bottoms to the hydrocracking zone.
Description
Ultited States Patent Coleman et al.
PRODUCTION or IMPRovEd warucxrmo OILS Inventors: Richard L. Coleman, Port Arthur;
Billy H. Cummins, Nederland; Ambrose J. Startz, Groves, all of Tex.
Assignee: Texaco, Inc., New York. NY.
Filed: June 15, 1973 Appl. No.: 370,246
U.S. Cl. 208/95; 208/18; 208/96 Int. Cl Cl0g 13/04 Field of Search 208/l8, 111, 112, 95
References Cited UNlTED STATES PATENTS 4/1957 Watkins et a1 208/58 451 July 22, 1975 3,l42,634 7/]964 Ireland et al 208/95 3,l42,635 7/l964 Coonradt et al i 208/l l l 3.242068 3/1966 Peterson i r i 208/] l I 3,285,848 ll/l966 Donaldson et al 208/110 3308,055 3 /l9 67 Kozlowski 208/] ll 3.562,l49 2/197! Bryson et al..... 208/l43 3.660.273 5/1972 Cummins 208/96 Primary Exarii'irir-Hflbmt Levine Attorney. Agent. or FirmT. H. Whaley; C. G. Ries; Robert Knox 9 Claims, No Drawings PRODUCTION OI" IMPROVED LUBRICATING OILS This invention relates to the production of improved petroleum oils. More particularly it is concerned with the production of base oils of high viscosity index suitable for blending into multigrade lubricating oils, automatic transmission fluids and other specialty oils requiring high viscosity index. In one of its more specific aspects, it is concerned with the production of high viscosity index lubricating oils in good yield from lubricating oil charge stocks using a process sequence which includes in a preferred embodiment hydrocracking, selective fractionation and dewaxing.
Various steps for the refining of lubricating oils such as distillation, solvent refining, solvent dewaxing, acid treating and clay contacting are well known. When residual type oils are being processed, a preliminary step of deasphalting is also generally required.
[n the processing steps listed above, distillation is employed as a means of separating a crude oil into fractions of various viscosities, solvent refining with, for example, furfural, sulfur dioxide or N-methyl-2- pyrrolidone is ordinarily used as a means of removing aromatic compounds and thereby improving the viscosity index, solvent dewaxing using for example a mixture of methyl ethyl ketone and toluene is used to improve low temperature properties by lowering the pour point of the oil and clay contacting is used generally as a final step to further improve the color and to neutralize the oil, after it has been acid treated to improve color, oxidation and heat stability.
In a typical operation, a crude oil is topped under atmospheric pressure to produce light distillates such as naphtha, kerosene and atmospheric gas oils and an atmospheric reduced crude which is then vacuum distilled to produce lube oil distillates with the residue from the vacuum distillation being deasphalted to yield residual lubricating stocks. Conventionally, the various lube oil fractions are then further processed by solvent refining and dewaxing. With the advent of mild hydrogenation, acid treating and clay contacting have more or less fallen into disuse.
Because of the increasing demand for the lighter grade lubricating oils it has been found advantageous to convert the heavier oils to the more valuable lighter products by hydrocracking, or severe hydrotreating. Not only does this result in an increase in yield of desired lube oil fractions but because of the high hydrogen pressures involved which result in a reduction in the aromatic content of the oil, hydrocracking and hydrotreating have been proposed as replacements for solvent refining.
Conventionally, when a crude lubricating oil is hydrocracked, the effluent from the hydrocracking zone is passed through a high pressure separator for removal of a hydrogen-rich gas then through a low pressure separator for removal of low molecular weight normally gaseous hydrocarbons. The balance of the effluent is then sent to a fractionator where, to obtain a hydrocracked lube oil having a satisfactory flash point, the material boiling below about 600F. is removed. The 600F+ material is then considered as product. One drawback to this method of operation is that if it is desired to change the product viscosity it is necessary to change the reaction conditions or to use a charge stock from a different source or both. However, a change in the reaction conditions also produces change in the product viscosity index.
it is an object of the present invention to produce lubricating oils of specified flash point and viscosity without changing the hydrocracking reaction conditions or conversely, to change the hydrocracking reaction conditions while continuing to produce a product of constant specifications.
According to our invention a crude petroleum lubricating oil is subjected to hydrocracking to improve its viscosity index, the hydrocraclted product is subjected to selective fractionation, the desired fraction is dewaxed and that portion boiling above the desired fraction is recycled to the hydrocracking zone.
The process of the invention may be applied to a variety of petroleum feedstocks. For example, the feed may be obtained by subjecting a vacuum residuum to deasphalting with a low molecular weight hydrocarbon such as propane or butane. The deasphalted residuum can then be hydrocracked. It is also possible to use a wax distillate as feed to the hydrocracking stage. The feed whether obtained by distillation or by deasphalting a vacuum residuum may be subjected to hydrocracking. It is also possible to use as the feed a lubricating oil fraction which has been obtained from a residuum such as an atmospheric residuum or vacuum residuum by a simultaneous deasphalting-solvent refining procedure in which the residuum is treated not with the conventional low molecular weight hydrocarbon deasphalting agents but with a solvent such as furfural or N-methyl- 2-pyrrolidone and the raffinate of reduced aromatic and asphalt content is charged to the hydrocracking zone.
The reaction conditions for the hydrocracking may be varied depending on the product desired and on the charge stock. Typical reaction conditions include a temperature of about 700-900F., preferably 750-850F. The hydrogen partial pressure may range between about 500 and 5000 psig. a preferred range being from 1500 to 3000 psig. Space velocities may vary between about 0.1 and 3.0 v/v/hr. with a preferred range being 0.2-1.0 Hydrogen rates of from l000l0,000 SCFB have been found satisfactory al though rates of 3000-7000 SCFB are preferred.
Hydrogen from any suitable source such as electrolytic hydrogen, hydrogen obtained from the partial combustion of hydrocarbonaceous material followed by shift conversion and purification or catalytic reformer by-product hydrogen may be used. The hydrogen should have a purity of between about 50 and 100% with hydrogen purities of at least 65 volume being preferred, a particularly preferred range being -95% purity.
The oil and hydrogen ordinarily are preheated and brought into contact with a particulate catalyst. The catalyst may be in the form of a fixed bed, a moving bed, a fluidized bed or may be slurried with the oil. In the case of a fixed bed, hydrogen flow may be upward or downward through the reactor as may be the flow of the oil. In a specific embodiment, both the oil and a portion of the hydrogen are introduced at the top of a reactor containing a fixed bed of the catalyst, the balance of the hydrogen being introduced at intermediate points in the reactor for cooling purposes.
The catalyst for the hydrocracking step preferably comprises as a hydrogenating component a compound of a Group VI metal such as molybdenum, chromium or tungsten or a compound of a Group VIII metal such as cobalt, iron or nickel and mixtures thereof. Ordinarily the catalyst is charged to the reactor in oxide form although it can be expected that some reduction and some sulfidation take place during the course of the process so that after being on stream for some time, the catalyst is probably a mixture of the metal, the metal sulfide and perhaps the oxide. If desired, the catalyst after being charged to the reactor but prior to the institution of the on-stream period may be converted at least in part to the sulfide form for example by contact with a gas such as a mixture of hydrogen and sulfiding agent, e.g. hydrogen sulfide, methyl mercaptan or carbon disulfide at an elevated temperature, eg 400F. The group VIII metal may be present in an amount varying from I to 20% by weight of the total catalyst composite, preferably 2-l5% and the group VI metal may be present in an amount ranging from about 540%, preferably 7-25%. Preferred combinations are nickel-tungsten, nickel-molybdenum and cobaltmolybdenum.
The hydrogenating component is supported on a refractory inorganic oxide such as hydrogen form or decationized zeolite Y, alumina, zirconia, silica or magnesia and mixtures thereof optionally promoted with an acidic material such as boron oxide or a halogen.
' Advantageously, the catalyst has a surface area of at least 150 m lg, a pore volume of at least 0.5 cc/g a major portion of the pore volume being made up of pores having an average pore diameter between 50 and I A. The upper limit of the surface area and pore volume is governed. by the hardness and ruggedness of the catalyst. As a practical matter, for commercial installations where the catalyst is used in units capable of processing several thousand barrels of charge per day, the surface area probably should not exceed about 600 mlg and the pore volume should not exceed about 0.8 cc/g.
The catalyst which may be in the shape of pellets, extrudates or spheres, may be prepared by any of the methods well known in the art, such as by impregnating the support with a solution of a salt of one of the metals, filtering, drying and then if desired impregnating with a solution of a salt of another metal, filtering, drying and calcining in a manner well known in the art.
7 The effluent from the hydrocracking zone is cooled and, in one embodiment of the invention, hydrogenrich gas is separated therefrom and recylced to the hydrocracking zone. Optionally, the hydrogen-rich stream is treated to remove any hydrogen sulfide and ammonia contained therein or a portion thereof may be bled from the system to prevent the build-up of hydrogen sulfide, ammonia and/or low molecular weight hydrocarbons. Hydrogen is added to the recycle stream to replace that consumed by the hydrocracking and if necessary to replace any hydrogen purged from the system. The balance of the hydrocracking zone effluent then is passed to a low pressure separator for the removal of low molecular weight hydrocarbons and then to a fractionator for removal of hydrocarbons boiling below about 600F. The 600F+ material may be sent to a second fractionator to obtain a lube oil fraction of the desired flash point and viscosity or the low pressure separator bottoms may be fractionated to produce suitable flash point and viscosity material in the initial frac' tionator. The desired flash point is obtained by removing the light ends and an oil of the desired viscosity may be removed from the fractionator as a side stream or heart cut. The high viscosity bottoms may then be returned to the hydrocracking zone.
By following the procedure outlined above, the deficiencies of the prior art are overcome. In conventional processing, if it were desired to adjust a lube oil hydrocracking process to produce a product oil of higher viscosity the severity of the hydrocracking reaction conditions would be reduced resulting in the higher viscosity product but the product viscosity index would be lower. However, by the procedure of our invention it is possible to produce higher viscosity lube oils without sustaining any loss in the viscosity index of the product.
Advantageously, if it is desired to produce a lube oil having stability to ultraviolet light, the oil should be subjected to a solvent extraction treatment using a selective solvent such 'as furfural or N-methyl-Z- pyrrolidone in any conventional liquid-liquid contacting apparatus such as a packed'column, a centrifugal contactor, a rotating disc contactor or the like. The solvent extraction is carried out at any stage of the process after the hydrocracking, preferably immediately prior to dewaxing.
The following examples are submitted for comparative and illustrative purposes only.
EXAMPLE I In this example, which is representative of conventional processing, the charge is a deasphalted residuum l-Iydrocracking of the charge oil is effected by passing it downwardly with hydrogen through a bed of catalyst pellets containing 2.3 wt. cobalt, I03 wt. molybdenum, 3.9 wt. silica and 79.7 wt. alumina having a pore volume of 0.63 cc/g and a surface area of 290 m /g at a temperature of 805F., a pressure of 1500 psig, 5000 SCFB of purity hydrogen at an hourly space velocity of 0.5 volumes of charge oil per volume of catalyst per hour. The 600F.+ portion of the prodnot, obtained in 63.8 volume per cent basis charge to the hydrocracker has the following characteristics:
This example follows the procedure of our invention in which a high viscosity oil having substantially the same flash point as that obtained in Example I is produced without incurring a loss in viscosity index. The flow differs from that of Example I in that the charge includes a recycle fraction obtained by fractionating the hydrocracked product to produce a heart cut having a suitable flash point and the desired (pre-dewaxed) viscosity. This is accomplished by topping the 600F.+ hydrocracked fraction to obtain an oil of suitable flash point and cutting out an intermediate fraction which,
when dewaxed will have the desired viscosity leaving 5 still bottoms which are recycled and introduced with fresh feed to the hydrocracking zone. The fractionator is operated at an average vacuum of 29.2 inches of mercury and a maximum temperature of 680F. The charge, including recycle, has the following characteristics:
TABLE 3 Gravity, IAPI 23.2 Viscosity, sus, IF. 3034 2l0F. l64.0 Viscosity index 92 Hydrocraclting conditions, using the same catalyst as in Example I, are a temperature of 8l9F., a pressure of 1500 psig a space velocity of 0.5 v/v/hr. and a hydrogen rate of 5000 SCFB. The 600F.+ portion of the product, obtained in a yield of 72.4 vol. has the following characteristics:
TABLE 4 Gravity, API 3L2 Viscosity, SUS, IOOF. 162.7 2IO'F. 46.5 Viscosity index 14] TABLE 5 heart out dewaxed Gravity. APl 31.7 28.1 Viscosity, SUS, 100F. B2 149 ZIO'F 43.1 43.8 Viscosity Index 12 I 13 Flash point, P. 375F.
Pour point, F. +3
By way of comparison, by the procedure of Example I, a dewaxed oil having a viscosity SUS at 100F. of I49 would have a viscosity index of less than 108.
Obviously, various modifications of the invention as hereinbefore set forth may be made without departing from the spirit and scope thereof, and therefore, only such limitations should be made as are indicated in the appended claims.
We claim:
1. A process for the production of a lubricating oil of specified flash point and viscosity which comprises subl5 jecting a crude lubricating oil to catalytic hydrocraclting, distilling the hydrocraclced product to remove material boiling up to about 600F., subjecting the hydrocracked fraction boiling above about 600F. to additional distillation to obtain a lubricating oil having a predetermined flash point, distilling said lubricating oil of predetermined flash point until a heart out is obtained having substantially the same viscosity as said fraction boiling above about 600F., returning the remainder of the hydrocracked fraction boiling above said heart cut to the hydrocracking zone and dewaxing said heart cut.
2. The process of claim 1 in which the heart out is subjected to solvent extraction for the removal of aromatic hydrocarbons prior to being dewaxed.
3. The process of claim 1 in which the crude lubricating oil is a wax distillate.
4. The process of claim 1 in which the crude lubricating oil is a deasphalted residuum.
5. The process of claim 1 in which the hydrocracking catalyst comprises a Group Vlll metal or compound thereof supported on an amorphous inorganic oxide having a surface area of at least 250 mlg and a pore volume of at least 0.5 cc/g.
6. The process of claim 5 in which the amorphous inorganic oxide comprises a mixture of silica and alumina.
7. The process of claim 6 in which the mixture of amorphous inorganic oxide comprises between 2 and 15 wt. silica.
8. The process of claim 2 in which the solvent is furfural.
9. The process of claim 2 in which the solvent is N-methyl-Z-pyrrolidone.
Claims (9)
1. A PROCESS FOR THE PRODUCTION OF A LUBRICATING OIL OF SPECIFIED LASH POINT AND VISCOSITY WHICH COMPRISES SUBJECTING A CRUDE LUBRICATING OIL TO CATALYTIC HYDROCRACKING, DISTILLING THE HYDROCRACKED PRODUCT TO REMOVE MATERIAL BOILING UP TO ABOUT 600*F. SUBSJECTING THE HYDROCRACKED FRACTION BOILING UP TO ABOUT ABOUT 600*F. TO ADDITIONAL DISTILLATION TO OBTAIN A LUBRICATING OIL HAVING A PREDETERMINED FLASH POINT, DISTILLING SAID LUBRICATING OIL OF PREDETERMINED FLASH POINT UNTIL A HEART CUT IS OBTAINED HAVING SUBSTANTIALLY THE SAME VISCOSITY AS SAID FRACTION BOILING ABOVE ABOUT 600*F., RETURNING THE REMAINDER OF THE DROCRACKED FRACTION BOILING ABOVE SAID HEART CUT TO THE HYDROCRACKING ZONE AND DEWAXING SAID HEART CUT.
2. The process of claim 1 in which the heart cut is subjected to solvent extraction for the removal of aromatic hydrocarbons prior to being dewaxed.
3. The process of claim 1 in which the crude lubricating oil is a wax distillate.
4. The process of claim 1 in which the crude lubricating oil is a deasphalted residuum.
5. The process of claim 1 in which the hydrocracking catalyst comprises a Group VIII metal or compound thereof supported on an amorphous inorganic oxide having a surface area of at least 250 m2/g and a pore volume of at least 0.5 cc/g.
6. The process of claim 5 in which the amorphous inorganic oxide comprises a mixture of silica and alumina.
7. The process of claim 6 in which the mixture of amorphous inorganic oxide comprises between 2 and 15 wt. % silica.
8. The process of claim 2 in which the solvent is furfural.
9. The process of claim 2 in which the solvent is N-methyl-2-pyrrolidone.
Priority Applications (9)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US370246A US3896025A (en) | 1973-06-15 | 1973-06-15 | Production of improved lubricating oils |
JP1553774A JPS5419882B2 (en) | 1973-06-15 | 1974-02-08 | |
GB611274A GB1465975A (en) | 1973-06-15 | 1974-02-11 | Production of lubricating oils |
FR7407740A FR2233385B3 (en) | 1973-06-15 | 1974-03-07 | |
FI866/74A FI86674A (en) | 1973-06-15 | 1974-03-21 | |
DE2424295A DE2424295A1 (en) | 1973-06-15 | 1974-05-18 | PROCESS FOR MANUFACTURING LUBRICATING OILS WITH IMPROVED VISCOSITY INDEX |
CA202,118A CA1030886A (en) | 1973-06-15 | 1974-06-11 | Production of improved lubricating oils |
IT23918/74A IT1015023B (en) | 1973-06-15 | 1974-06-12 | PROCEDURE FOR THE PRODUCTION OF A LUBRICATING OIL |
ES427273A ES427273A1 (en) | 1973-06-15 | 1974-06-14 | Production of improved lubricating oils |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US370246A US3896025A (en) | 1973-06-15 | 1973-06-15 | Production of improved lubricating oils |
Publications (1)
Publication Number | Publication Date |
---|---|
US3896025A true US3896025A (en) | 1975-07-22 |
Family
ID=23458839
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US370246A Expired - Lifetime US3896025A (en) | 1973-06-15 | 1973-06-15 | Production of improved lubricating oils |
Country Status (9)
Country | Link |
---|---|
US (1) | US3896025A (en) |
JP (1) | JPS5419882B2 (en) |
CA (1) | CA1030886A (en) |
DE (1) | DE2424295A1 (en) |
ES (1) | ES427273A1 (en) |
FI (1) | FI86674A (en) |
FR (1) | FR2233385B3 (en) |
GB (1) | GB1465975A (en) |
IT (1) | IT1015023B (en) |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5167847A (en) * | 1990-05-21 | 1992-12-01 | Exxon Research And Engineering Company | Process for producing transformer oil from a hydrocracked stock |
US5370788A (en) * | 1992-12-18 | 1994-12-06 | Texaco Inc. | Wax conversion process |
US20140202924A1 (en) * | 2008-10-01 | 2014-07-24 | Chevron U.S.A. Inc. | Process To Manufacture A Base Stock |
Families Citing this family (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA1090275A (en) * | 1975-12-16 | 1980-11-25 | Jacobus H. Breuker | Base-oil compositions |
JPS5565295A (en) * | 1978-11-11 | 1980-05-16 | Idemitsu Kosan Co Ltd | Preparation of base oil for light lubricant |
JP4496647B2 (en) * | 1998-11-06 | 2010-07-07 | アンスティテュ フランセ デュ ペトロール | An adaptable (flexible) production method of very high quality base oils and possibly middle distillates |
FR2785617B1 (en) * | 1998-11-06 | 2001-01-05 | Inst Francais Du Petrole | FLEXIBLE PROCESS FOR THE PRODUCTION OF OIL BASES AND POSSIBLY MEDIUM DISTILLATES OF VERY HIGH QUALITY |
FR2797270B1 (en) * | 1999-08-02 | 2003-03-07 | Inst Francais Du Petrole | PROCESS AND FLEXIBLE PRODUCTION OF OIL BASES AND POSSIBLY MEDIUM DISTILLATES OF VERY HIGH QUALITY |
Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2787582A (en) * | 1955-04-12 | 1957-04-02 | Universal Oil Prod Co | Production of lubricating oils |
US3142634A (en) * | 1961-12-14 | 1964-07-28 | Socony Mobil Oil Co Inc | Preparation of multi-grade lubricating oil |
US3142635A (en) * | 1961-10-27 | 1964-07-28 | Socony Mobil Oil Co Inc | Production of lubricating oils |
US3242068A (en) * | 1962-12-24 | 1966-03-22 | Chevron Res | Production of lubricating oil |
US3285848A (en) * | 1963-09-03 | 1966-11-15 | Gulf Research Development Co | Preparing dissimilar oils by hydrocracking |
US3308055A (en) * | 1964-04-13 | 1967-03-07 | Chevron Res | Hydrocracking process producing lubricating oil |
US3562149A (en) * | 1969-08-19 | 1971-02-09 | Gulf Research Development Co | Process for producing lubricating oil by hydrogen treatment |
US3660273A (en) * | 1969-11-12 | 1972-05-02 | Texaco Inc | Production of improved lubricating oils by hydrocracking and solvent extraction |
-
1973
- 1973-06-15 US US370246A patent/US3896025A/en not_active Expired - Lifetime
-
1974
- 1974-02-08 JP JP1553774A patent/JPS5419882B2/ja not_active Expired
- 1974-02-11 GB GB611274A patent/GB1465975A/en not_active Expired
- 1974-03-07 FR FR7407740A patent/FR2233385B3/fr not_active Expired
- 1974-03-21 FI FI866/74A patent/FI86674A/fi unknown
- 1974-05-18 DE DE2424295A patent/DE2424295A1/en active Pending
- 1974-06-11 CA CA202,118A patent/CA1030886A/en not_active Expired
- 1974-06-12 IT IT23918/74A patent/IT1015023B/en active
- 1974-06-14 ES ES427273A patent/ES427273A1/en not_active Expired
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2787582A (en) * | 1955-04-12 | 1957-04-02 | Universal Oil Prod Co | Production of lubricating oils |
US3142635A (en) * | 1961-10-27 | 1964-07-28 | Socony Mobil Oil Co Inc | Production of lubricating oils |
US3142634A (en) * | 1961-12-14 | 1964-07-28 | Socony Mobil Oil Co Inc | Preparation of multi-grade lubricating oil |
US3242068A (en) * | 1962-12-24 | 1966-03-22 | Chevron Res | Production of lubricating oil |
US3285848A (en) * | 1963-09-03 | 1966-11-15 | Gulf Research Development Co | Preparing dissimilar oils by hydrocracking |
US3308055A (en) * | 1964-04-13 | 1967-03-07 | Chevron Res | Hydrocracking process producing lubricating oil |
US3562149A (en) * | 1969-08-19 | 1971-02-09 | Gulf Research Development Co | Process for producing lubricating oil by hydrogen treatment |
US3660273A (en) * | 1969-11-12 | 1972-05-02 | Texaco Inc | Production of improved lubricating oils by hydrocracking and solvent extraction |
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5167847A (en) * | 1990-05-21 | 1992-12-01 | Exxon Research And Engineering Company | Process for producing transformer oil from a hydrocracked stock |
US5370788A (en) * | 1992-12-18 | 1994-12-06 | Texaco Inc. | Wax conversion process |
US20140202924A1 (en) * | 2008-10-01 | 2014-07-24 | Chevron U.S.A. Inc. | Process To Manufacture A Base Stock |
US9732287B2 (en) * | 2008-10-01 | 2017-08-15 | Chevron U.S.A. Inc. | Process to manufacture a base stock |
Also Published As
Publication number | Publication date |
---|---|
JPS5054602A (en) | 1975-05-14 |
FR2233385B3 (en) | 1976-12-17 |
JPS5419882B2 (en) | 1979-07-18 |
IT1015023B (en) | 1977-05-10 |
FR2233385A1 (en) | 1975-01-10 |
ES427273A1 (en) | 1976-11-16 |
CA1030886A (en) | 1978-05-09 |
FI86674A (en) | 1974-12-16 |
DE2424295A1 (en) | 1975-01-09 |
GB1465975A (en) | 1977-03-02 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US3923636A (en) | Production of lubricating oils | |
JP3065816B2 (en) | Production method of high viscosity index low viscosity lubricating base oil | |
US3883417A (en) | Two-stage synthesis of lubricating oil | |
US2917448A (en) | Hydrogenation and distillation of lubricating oils | |
US3915843A (en) | Hydrocracking process and catalyst for producing multigrade oil of improved quality | |
US3779896A (en) | Lube oil manufacture | |
JPS62101689A (en) | Stabilization of lubricant base stock | |
JPH06116572A (en) | Production of low-viscosity base oil having high viscosity index for lubricating oil | |
US4853104A (en) | Process for catalytic conversion of lube oil bas stocks | |
US3702817A (en) | Production of lubricating oils including hydrofining an extract | |
US3660273A (en) | Production of improved lubricating oils by hydrocracking and solvent extraction | |
US20040245147A1 (en) | Process to manufacture high viscosity hydrocracked base oils | |
US3816295A (en) | Production of lubricating oils | |
US3896025A (en) | Production of improved lubricating oils | |
US5098551A (en) | Process for the manufacture of lubricating base oils | |
US3870622A (en) | Hydrogenation of a hydrocracked lubricating oil | |
RU2675852C1 (en) | Method of obtaining high-index components of base oils of group iii/iii+ | |
US3684684A (en) | Production of oils stable to ultra-violet light | |
US3652448A (en) | Production of improved lubricating oils | |
US4085036A (en) | Process of hydrodesulfurization and separate solvent extraction of distillate and deasphalted residual lubricating oil fractions | |
US3691067A (en) | Production of lubricating oils by hydrotreating and distillation | |
US4163707A (en) | Asphalt conversion | |
US3790470A (en) | Production of lubricating oils | |
US3671423A (en) | Stabilizing hydrocracked lubricating oils | |
US3725245A (en) | Production of lubricating oils |