|Publication number||US3642610 A|
|Publication date||Feb 15, 1972|
|Filing date||Sep 5, 1969|
|Priority date||Sep 5, 1969|
|Also published as||CA1016485A, CA1016485A1, DE2043849A1|
|Publication number||US 3642610 A, US 3642610A, US-A-3642610, US3642610 A, US3642610A|
|Inventors||Joseph M Divijak Jr, Maurice K Rausch|
|Original Assignee||Atlantic Richfield Co|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (4), Referenced by (20), Classifications (9)|
|External Links: USPTO, USPTO Assignment, Espacenet|
United States Patent Divijak, Jr. et al.
[ Feb. 15,1972
 TWO-STAGE HYDROCRACKING- HYDROTREATING PROCESS TO MAKE LUBE OIL  inventors: Joseph M. Diviiak, Jr., Grifiith, lnd.; Maurice K. Rausch, South Holland, [11.
Atlantic Richfield Company, New York, N.Y.
Sept. 5, 1969  Appl.No.: 855,737
52] U.S.Cl ..260/s8,208/57,2o8/s8, 208/87, 208/144, 252/432 511 Int. Cl. ..Cl0g23/02,Cl0g13/06,Cl0g 37/00  FieldoiSearch ..208/l8,58,59,111,143,144, 208/87  References Cited UNITED STATES PATENTS 2,779,713 1/1957 Coleetal ..208/57 2,917,448 12/1959 Bewther etal ..208/57 3,506,565 4/1970 White eta]. ....208/58 3,444,071 5/1969 Van ZijllLanghout ..208/59 Primary Examiner -Delbert E. Gantz Assistant Examiner-G. E. Schmitkons AttorneyMcLean, Morton & Boustead  ABSTRACT 12-Claims, No Drawings tion of high quality mineral lubricating oils from feedstocks that are not normally used in present commercial processes to make such products. In addition to mineral lube oil distillates and deasphalted residuums of relatively high quality, stocks containing high percentages of sulfur, nitrogen and carbon residue, such as sour oils and more highly contaminated deasphalted oils, may be employed as feeds. Moreover, a wide range of products is possible. Lubricating oils with viscosity indexes up to about 150 or more (ASTM Designation: D-2270) with partial or even complete aromatic saturation are possible. The present process is also more economical than present methods for the production of high viscosity index oils involv- ,ing solvent treatment, dewaxing and finishing. The invention produces such oils by hydrocracking the mineral oil feed while in contact with a catalyst containing nickel, and tungsten or molybdenum along with boria on an alumina support, followed by hydrogenation of resulting hydrocracked materials of lubricating viscosity over a hydrogenation catalyst whereby a high viscosity index oil is produced.
Many of the present day refining techniques employed to produce high quality mineral lubricating oils having high viscosity indexes possess certain undesirable features. For example, the production of finished oils having a viscosity index of 95 by known methods of fractionation and solvent extraction of vacuum distillates or deasphalted residuums followed by dewaxing and finishing with acid, clay or hydrogen, normally results in yields of about 50 to 65 volume percent. The present invention, however, can produce 95 VI oils in yields of about 60 to 80 volume percent on a dewaxed basis and yields of about 40 volume percent or more on a dewaxed basis of oils having viscosity indexes of about 120 and higher.
The mineral lubricating oils treated by the process of the present invention are of lubricating viscosity at 210 F. and are principally stocks having at least about 90 weight percent boiling above about 600 F.; preferably the feed is a residuum at least about 90 weight percent of which boils above about 1,000 F. The feeds are usually oils of at least about 50 V1, e.g., about 50 to 80, or even about 70 to 80 V1, and can be derived from paraffinic or mixed base crude oils. The total or full range oil of lubricating viscosity obtained by the method of thepresent invention has a viscosity index in the range of at least about 90, say up to about 150 or more, with the increase in the viscosity index of the product being at least about 20, preferably at least about 30, over that of the feed. Both the initial hydrocarbonfeedstock and the product of lubricating viscosity from the hydrogenation reaction boil over a considerable temperature range, e.g., overa range of at least about 100 F., often at least about 200 F. The hydrocarbon feedstock preferably has a specific dispersion (ASTM Designation: D-l218) in the range of about 105-165 while the specific dispersion of the product of lubricating viscosity is preferably in the range of about 100-1 10. The method of the present invention is particularly suitable for treating feedstocks having a specific dispersion in the range of about 135-165, such stocks being the highly contaminated stocks,
containing larger amounts of aromatics and frequently having been subjected only to fractionation and deasphalting. Thus the present method can utilize these economically cheaper feedstocks to produce high quality lubricating oils in high yields.
Hydrocracking of the feedstock which includes ring opening and usually desulfurization and denitrogenation, is carried out in contact with a catalyst containing nickel and one or both of molybdenum or tungsten supported, along with boria, on a catalytically active alumina base. The metals of the catalyst may be present in the form of free metals or in combined form such as the oxides and sulfides, the sulfides being the preferred form. Examples of such mixtures or compounds are nickel molybdate or tungstate (or thiomolybdate or thiotungstate). These catalytic ingredients, along with boria, are employed while disposed on a catalytically-active alumina.
The catalyst is composed of minor, catalytically effective amounts of nickel, tungsten and/or molybdenum and boria on the alumina base. Nickel may often comprise about l-40 weight percent of the catalyst, preferably about 2-10 percent, with the total amount of tungsten and molybdenum being about 5-30 weight percent, preferably about 10-20 percent, of the catalyst on a metal oxide basis. Preferably the boria is present in an amount of about 2 to 10 weight percent, based on the total weight of the catalyst while the alumina is the major component of the catalyst, e.g., the essential balance of the composition.
The catalyst composition used in the hydrocracking stage of the present invention can be prepared by adding the nickel, tungsten, molybdenum and boria components to the alumina by the various methods known to the art, for example by impregnation or precipitation and coprecipitation using suitable compounds of the metals and boron. For example, alumina particles containing boria or a material which upon heating yields boria, can be mixed with aqueous ammonia solutions containing nickel and tungsten, and/or molybdenum, or other aqueous solutions of water-soluble compounds of nickel and tungsten and/or molybdenum, so that the metal components are absorbed on the base. Alternatively, the promoting materials can be precipitated on the boria-containing alumina base through suitable reaction of an aqueous slurry of the support containing water-insoluble salts of the promoting metals. The boria-containing particles can be formed into macrosize either before or after being mixed with the nickel and tungsten and/or molybdenum components. The catalyst can be dried and calcined, e.g., at temperatures of about 800 to 1,200 F. or somewhat more. Prior to use the catalyst is preferably sulfided at elevated temperature.
The hydrocracking step is carried out under conditions designed to selectively crack the feed so that opening of aromatic and naphthenic rings is favored, rather than the splitting of chains into lower molecular weight compounds. Such conditions include a temperature of about 725to 875 F., preferably about 750to 850 F. The other reaction conditions often include a hydrogen partial pressure of about 1,000 to 5,000 p.s.i.g., preferably about 1,500 to 3,000 p.s.i.g. In the production of VI oils by the method of this invention, cracking may take place to the extent that from about 5 to 10 percent by volume of the product of the hydrocracking stage is material boiling below about 600 F. In the production of VI oils, about 30 to 40 percent by volume of the product of the hydrocracking stage may be comprised of such materials. The amount of free hydrogen employed during hydrocracking can be generally about 1,000 to 5,000 standard cubic feet per barrel of hydrocarbon feed,,preferably about 1,500 to 3,000 standard cubic feet per barrel. The weight hourly space velocity (WHSV), weight units of feed in'-. troduced into the reaction zone per weight unit of catalyst per hour, will often be in the range of about 0.3 to 3, preferably about 0.5 to 2. The reactor effluent from the first or hydrocracking stage can be flashed to prevent hydrogen sul tide and ammonia from going to the hydrogenation stage, but this is not necessary, especially if nonprecious metal hydrogenation catalysts are used in the hydrogenation stage. Also, if desired any light hydrocarbons can be removed from the feed to the hydrogenation stage.
Lubricating oil from the hydrocracking stage is subjected to a hydrogenation operation which involves contacting lubricating oil, preferably the essentially full range lube oil, from the hydrocracking stage in the presence of hydrogen with a solid hydrogenation catalyst at a temperature of about 550to 825 F., preferably about 600 to 800 F. It is preferred that the temperature employed in the second stage he at least about 50 F. less than the temperature of the first stage for optimum decolorization and saturation. The other reactionconditions often include pressures of about 1,000 to 5,000 p.s.i.g., preferably about 1,500 to 3,000 p.s.i.g.; space velocities (WHSV) of about 0.3 to 5, preferably about 0.5 to 3; and
molecular hydrogen to feed ratios of about500 to 3,500 standard cubic feet of hydrogen per barrel of hydrocarbon feed, preferably about 1,500 to 2,500 standard cubic feet of hydrogen per barrel of hydrocarbon feed.
The solid catalyst employed in the hydrogenation operation is preferably a sulfur-resistant, nonprecious metal hydrogenation catalyst, such as those conventionally employed in the hydrogenation of heavy petroleum oils. Examples of suitable catalytic ingredients are tin, vanadium, members of Group VIB in the periodic table, i.e., chromium, molybdenum and tungsten and metals of the iron group, i.e., iron, cobalt and nickel. These metals are present in minor, catalytically effective amounts, for instances, about 2 to 30 weight percent of the catalyst, and may be present in the elemental form or in combined form such as the oxides or sulfides, the sulfide form being preferred. Mixtures of these materials or compounds of two or more of the oxides or sulfides can be employed, for example, mixtures or compounds of the iron group metal oxides or sulfides with the oxides or sulfides of Group VIB constitute very satisfactory catalysts. Examples of such mixtures or compounds are nickel molybdate, tungstate or chromate (or thiomolybdate, thio-tungstate or thiochromate) or mixtures of nickel or cobalt oxides with molybdenum, tungsten or chromium oxides. As the art is aware and as the specific examples below illustrate, these catalytic ingredients are generally employed while disposed upon a suitable carrier of the solid oxide refractory type, e.g., a predominantly calcined or activated alumina. To avoid undue cracking the catalyst base and other components have little, if any, hydrocarbon cracking activity. Usually not more than about 5 volume percent, preferably not more than about 2 volume percent, of the feed is cracked in the second or hydrogenation stage to produce materials boiling below about 600 F. Commonly employed catalysts have about 1 to weight percent of an iron group metal and about 5 to 25 percent ofa Group VIB metal (calculated as the oxide). Advantageously, the catalyst is nickel molybdate or cobalt molybdate, supported on alumina. Such preferred catalysts can be prepared by the method described in US. Pat. No. 2,938,002.
Other suitable hydrogenation catalysts which can be employed in the method of this invention include the platinum group metal types. Such catalysts often have a minor catalytically effective amount, say about 0.05 to 2 weight percent, preferably about 0.1 to 1 weight percent of one or more platinum group metals carried on a solid support, especially an active alumina. Suitable platinum group metals include platinum, rhodium and ruthenium with platinum being preferred.
The catalysts employed in both the hydrocracking and hydrogenation stages of the method of this invention are preferably disposed in the reaction zones as fixed beds. Such fixed bed catalysts are usually particles of macrosize, e.g., about one sixty-fourth to one-fourth inch, preferably about one-sixteenth to one-eighth inch, in diameter, and, about one sixty-fourth to 1 inch or more, preferably about one-eighth to one-half inch in length. These catalysts can be made by extrusion, tableting or other suitable procedures.
The hydrogenation operation provides additional aromatic saturation, color improvement and stability towards oxidation and corrosion. Additional color improvement can be provided by subjecting the effluent from the hydrogenation operation to treatment with ultraviolet light. The treatment was found to lighten considerably the color of the darker oils, a surprising result since such treatment usually produces the opposite effect. The reactor effluent from the hydrogenation stage may be flashed to recover hydrogen for possible recycle and fed to a steam stripper to remove excess light hydrogenated components. The oil can then be fractionated and the lube fractions dewaxed. This dewaxing step can be carried out, for example, by pressing or by solvent dewaxing using methyl ethyl ketone and toluene as the solvent system. Dewaxing may be carried out prior to the initial hydrocracking step but it is preferred to conduct dewaxing after hydrogenation has been completed. No additional finishing is required. Yields of about 60 to volume percent, based on the raw stock, of V1 oils are not uncommon and finished base oils having viscosity indexes of and higher are obtained in economical yields, e. g., in the range of about 40 volume percent and higher.
The following example is illustrative of the method of this invention:
Deasphalted petroleum residuum was fed to an isothermal reactor unit having a nickel-tungstate on boria-aluminia catalyst in the first or hydrocracking stage and nickel-molybdate on alumina catalyst in the second or hydrogenation stage. The catalysts were macrosize and presulfided. The feedstock employed had the following specifications:
Vl (D-2270) (dewaxed basis) 76 Gravity, AP1 23.1
' Flash, F. 555
Viscosity, SUS/210F. 154.4 Pour, F. 1 20+ ASTM color Dark Carbon residue (Con.), wt.% 1.58 10% boiling point 1,000F.
Table I lists operating conditions and dewaxed oil inspections for nominal 100 and V1 operations.
The catalysts employed in the successive stages analyzed as follows:
TABLE 11 NiW on NiMo on Boria-Alumina Alumina Nickel, wt.% 5.35 2.30 Tungsten Oxide, wt.% 12.15 Molybdenum Oxide, wt.% 15.60 Silicon Dioxide, wt.% 0.29 Boria, wt.% 5.06 Volatile matter at 1,200 F. 3.95 (at 1,000 F.) 0.86 Apparent Density, g./rn1. 0.75 0.765
It is claimed:
1. A process of preparing a mineral hydrocarbon lubricating oil having a viscosity index of at least about 90 on a dewaxed basis which comprises:
a. Contacting a mineral hydrocarbon oil feedstock of lubricating viscosity at 210 F., at least about 90 weight percent of which boils above about 600 F. and having a viscosity index of about 50 to 80, with molecular hydrogen under hydrocracking conditions including a temperature of about 725 to 875 F., in the presence of a catalyst having minor, catalytically effective amounts of each of nickel, a member selected from the group consisting of tungsten and molybdenum, and boria on an active alumina support; and
b. Contacting hydrocarbon oil of lubricating viscosity from step (a) with molecular hydrogen under hydrogenation conditions including a temperature of about 550 to 825 F. in the presence of a solid hydrogenation catalyst at a hydrotreating severity such that not more than about 5 volume percent of the feed to step (b) boiling above 600 F. is cracked to material boiling below about 600 F. to produce oil of lubricating viscosity having a viscosity index of at least about 90 and at least about 20 viscosity index number greater than the hydrocarbon oil feedstock passing to step (a).
2. The process of claim 1 wherein said hydrocracking conditions include a hydrogen partial pressure of about 1,000 to 5,000 p.s.i.g., a weight hourly space velocity of about 0.3 to 3 WHSV and a molecular hydrogen to hydrocarbon feed ratio of about 1 ,000 to 5,000 standard cubic feet per barrel of feed.
3. The process of claim 2 wherein the catalysts are in sulfide form.
4. The process of claim 3 wherein the hydrocracking catalyst contains about 2 to 10 weight percent nickel, about 10 to 20 percent of the member selected from the group consisting of tungsten and molybdenum on an oxide basis, and about 2 to 10 percent boria.
5. The process of claim 4 wherein the selected member of the catalyst employed in the hydrocracking stage is tungsten.
6. The process of claim 2 wherein said hydrogenation conditions include a temperature of about 550to 825 F., a hydrogen partial pressure of about 1,000 to 5,000 p.s.i.g., a weight hourly space velocity of about 0.3 to 5 WHSV and a molecular hydrogen to hydrocarbon feed ratio of about 500 to 3,500 standard cubic feet per barrel of feed.
7. The process of claim 6 wherein the catalyst employed in the hydrogenation stage contains minor, catalytically-effective amounts of a member selected from the group consisting of nickel and cobalt, and molybdenum on alumina.
8. The process of claim 7 wherein the catalyst is in sulfide form.
9. The process of claim 8 wherein the hydrocracking catalyst contains about 2 to l weight percent nickel, about 10 to 20 percent of the member selected from the group consisting of tungsten and molybdenum on an oxide basis, and about 2 to 10 percent boria.
10. A process of preparing a mineral hydrocarbon lubricating oil having a viscosity index of at least about on a dewaxed basis which comprises:
a. Contacting a mineral hydrocarbon oil feedstock of lubricating viscosity at 210 F., at least 90 weight percent of which boils above about l,000 F. and having a viscosity index of about 50 to 80, with molecular hydrogen under hydrocracking conditions including a temperature of about 750 to 850 F., a hydrogen partial pressureof about 1,500 to 3,000 p.s.i.g., a weight hourly space velocity of about 0.5 to 2 WHSV and a molecular hydrogen to hydrocarbon feed ratio of about 1,500 to 3,000 standard cubic feet per barrel of feed, in the presence of a catalyst containing about 2 to 10 weight percent nickel, about 10 to 20 percent tungsten on an oxide basis and about 2 to 10 percent boria on an active alumina support, the metals of the catalyst being present in the sulfide form; and Contacting hydrocarbon oil of lubricating viscosity from step (a) with molecular hydrogen under hydrogenation conditions, including a temperature of about 600 to 800 F., a hydrogen partial pressure of about 1,500 to 3,000 p.s.i.g., a weight hourly space velocity of about 0.5 to 3 WHSV and a molecular hydrogen to hydrocarbon feed ratio of about 1,500 to 2,500 standard cubic feet per barrel of feed in the presence of a solid hydrogenation catalyst containing minor, catalytically effective amounts of a member selected from the group consisting of nickel and cobalt, and molybdenum on alumina, the metals of the catalyst being present in the sulfide form, to produce oil of lubricating viscosity having a viscosity index of at least about 90 and at least about 30 viscosity index numbers greater than the hydrocarbon oil feedstock passing to step (a).
11. The process of claim 1 wherein the product from step (b) is fractionated to separate oil of lubricating viscosity and the lubricating oil fraction is dewaxed.
12. The process of claim 10 wherein the product from step (b) is fractionated to separate oil of lubricating viscosity and the lubricating oil fraction is dewaxed.
|Cited Patent||Filing date||Publication date||Applicant||Title|
|US2779713 *||Oct 10, 1955||Jan 29, 1957||Texas Co||Process for improving lubricating oils by hydro-refining in a first stage and then hydrofinishing under milder conditions|
|US2917448 *||Nov 15, 1956||Dec 15, 1959||Gulf Research Development Co||Hydrogenation and distillation of lubricating oils|
|US3444071 *||Mar 18, 1966||May 13, 1969||Shell Oil Co||Process for the hydrogenative cracking of a hydrocarbon oil to produce lubricating oil|
|US3506565 *||Jul 31, 1968||Apr 14, 1970||Chevron Res||Process for the production of high viscosity index lubricating oils|
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US3870622 *||Jun 25, 1973||Mar 11, 1975||Texaco Inc||Hydrogenation of a hydrocracked lubricating oil|
|US3993557 *||Oct 9, 1975||Nov 23, 1976||Pine Lloyd A||Hydrocarbon conversion process employing boria-alumina compositions|
|US4082866 *||Sep 25, 1975||Apr 4, 1978||Rte Corporation||Method of use and electrical equipment utilizing insulating oil consisting of a saturated hydrocarbon oil|
|US4196408 *||Jul 28, 1975||Apr 1, 1980||Rte Corporation||High temperature transformer assembly|
|US4234434 *||Feb 14, 1979||Nov 18, 1980||Atlantic Richfield Company||Stabilization of hydrocracked oils with certain nitrogen-containing aromatic components|
|US4238316 *||Jul 6, 1978||Dec 9, 1980||Atlantic Richfield Company||Two-stage catalytic process to produce lubricating oils|
|US4263127 *||Jan 7, 1980||Apr 21, 1981||Atlantic Richfield Company||White oil process|
|US4264461 *||Sep 26, 1979||Apr 28, 1981||Atlantic Richfield Company||Stabilization of hydrocracked oils with aliphatic amine components|
|US4294687 *||Dec 26, 1979||Oct 13, 1981||Atlantic Richfield Company||Lubricating oil process|
|US4306985 *||Jun 30, 1980||Dec 22, 1981||Atlantic Richfield Company||Stabilization of hydrocracked oils with certain nitrogen containing aromatic components and phenolic components|
|US4325804 *||Nov 17, 1980||Apr 20, 1982||Atlantic Richfield Company||Process for producing lubricating oils and white oils|
|US4627908 *||Oct 24, 1985||Dec 9, 1986||Chevron Research Company||Process for stabilizing lube base stocks derived from bright stock|
|US4699707 *||Sep 25, 1985||Oct 13, 1987||Union Oil Company Of California||Process for producing lubrication oil of high viscosity index from shale oils|
|US4744884 *||May 28, 1986||May 17, 1988||Union Oil Company Of California||Process for producing lubrication oil of high viscosity index|
|US5026472 *||Dec 29, 1989||Jun 25, 1991||Uop||Hydrocracking process with integrated distillate product hydrogenation reactor|
|US5122257 *||Mar 18, 1991||Jun 16, 1992||Shell Internationale Research Maatschappij B.V.||Process for the manufacture of kerosene and/or gas oils|
|US8927796 *||Sep 13, 2012||Jan 6, 2015||Chevron U.S.A. Inc.||Base oil upgrading by co-feeding a ketone or beta-keto-ester feedstock|
|US9115327 *||Dec 4, 2014||Aug 25, 2015||Chevron U.S.A. Inc.||Base oil upgrading by co-feeding a ketone or beta-keto-ester feedstock|
|US20140073826 *||Sep 13, 2012||Mar 13, 2014||Chevron U.S.A. Inc.||Base oil upgrading by co-feeding a ketone or beta-keto-ester feedstock|
|US20150087872 *||Dec 4, 2014||Mar 26, 2015||Chevron U.S.A. Inc.||Base Oil Upgrading by Co-Feeding a Ketone or Beta-Keto-Ester Feedstock|
|U.S. Classification||208/58, 208/57, 208/144, 208/87|
|International Classification||C10G65/12, C10G47/12|
|Cooperative Classification||C10G2400/10, C10G47/12|