EP0104807B1 - Emploi de haute pression pour l'amélioration de la qualité de produit et l'augmentation de la longueur du cycle dans le déparaffinage catalytique des lubrifiants - Google Patents

Emploi de haute pression pour l'amélioration de la qualité de produit et l'augmentation de la longueur du cycle dans le déparaffinage catalytique des lubrifiants Download PDF

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Publication number
EP0104807B1
EP0104807B1 EP19830305125 EP83305125A EP0104807B1 EP 0104807 B1 EP0104807 B1 EP 0104807B1 EP 19830305125 EP19830305125 EP 19830305125 EP 83305125 A EP83305125 A EP 83305125A EP 0104807 B1 EP0104807 B1 EP 0104807B1
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Prior art keywords
raffinate
dewaxing
catalyst
process according
zeolite
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EP19830305125
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German (de)
English (en)
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EP0104807A3 (en
EP0104807A2 (fr
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Samuel Allen Tabak
Stuart Shan-San Shih
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ExxonMobil Oil Corp
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Mobil Oil Corp
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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins
    • C10G45/60—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used
    • C10G45/64—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to change the structural skeleton of some of the hydrocarbon content without cracking the other hydrocarbons present, e.g. lowering pour point; Selective hydrocracking of normal paraffins characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves
    • 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 manufacture of high grade viscous oil products from crude petroleum fractions, particularly high quality lube base stock oils from crude stocks of high wax content, commonly classified as “wax base” as compared with the “naphthenic base” crudes.
  • the latter crudes are relatively lean in straight chain paraffins and yield viscous fractions which inherently possess low pour points.
  • High quality lube base stock oils are conventionally prepared by refining distillate fractions or the residuum prepared by vacuum distilling a suitable crude oil from which the lighter portion has been removed by distillation in an atmospheric tower.
  • the charge to the vacuum tower is commonly referred to as a "long residuum” and the residuum from the vacuum tower is distinguished from the starting material by referring to it as the “short residuum".
  • the vacuum distillate fractions are upgraded by a sequence of unit operations, the first of which is solvent extraction with a solvent selective for aromatic hydrocarbons.
  • This step serves to remove aromatic hydrocarbons of low viscosity index and provides a raffinate of improved viscosity index and quality.
  • Various processes have been used in this extraction stage, and these employ solvents such as furfural, phenol, sulfur dioxide and others.
  • the short residuum because it contains most of the asphaltenes of the crude oil, is conventionally treated to remove these asphalt-like constituents prior to solvent extraction to increase the viscosity index.
  • the raffinate from the solvent extraction steps contains paraffins which adversely affect the pour point.
  • the waxy raffinate regardless of whether prepared from a distillate fraction or from the short residuum, must be dewaxed.
  • Various dewaxing procedures have been used and the art has gone in the direction of treatment with a solvent such as methyl ethyl ketone (MEK)/toluene mixtures to remove the wax and prepare a dewaxed raffinate.
  • MEK methyl ethyl ketone
  • the dewaxed raffinate may then be finished by any of a number of sorption or catalytic processes to improve color and oxidation stability.
  • the quality of the lube base stock oil prepared by the sequence of operations outlined above depends on the particular crude chosen as well as the severity of treatment for each of the treatment steps. Additionally, the yield of high quality lube base stock oil also depends on these factors and, as a rule, the higher the quality sought, the less the yield. In general, naphthenic crudes are favored because less loss is encountered, particularly in the dewaxing step. In many cases, however, waxy crudes are more readily available and it would be desirable to provide a process for preparing high quality lube base stock oils in good yields from such waxy crude oils.
  • That fraction is solvent refined by counter current extraction with at least an equal volume of a selective solvent such as furfural.
  • the furfural raffinate is subjected to catalytic dewaxing by mixing with hydrogen and contacting at 260°-357°C (500°-675°F) with a catalyst containing a hydrogenation metal and zeolite ZSM-5 or other aluminosilicate zeolite having a silica/alumina ratio above 12 and a constraint index of 1 to 12 and space velocity (LHSV) of 0.1 to 2.0 volumes of charge oil per volume of catalyst per hour.
  • LHSV space velocity
  • the effluent of catalytic dewaxing is then cascaded into a hydrotreater containing, as catalyst, a hydrogenation component on a non-acidic support, such as cobalt-molybdate or nickel-molybdate on alumina.
  • the hydrotreater operates at 218° to 316°C (425° to 600°F), preferably 246° to 288°C (475° to 550°F), and space velocity like that of the catalytic dewaxing reactor.
  • the reactions are carried out at hydrogen partial pressures of 1035-10350 kPa (150-1500 psia), at the reactor inlets, and preferably at 1725-3450 kPa (250-500 psia), with 89 to 890 I/I (500 to 5000 standard cubic feet) of hydrogen per barrel of feed (SCF/B), preferably 267 to 445 I/I (1500 to 2500 SCF/B).
  • a configuration similar to that of U.S. 4,137,148, including cascading the dewaxer effluent to the hydrotreater, is described in G.B. 2,010,3212, and the hydrogen partial pressure exemplified therein (Example 1) is 400 psig for both the catalytic dewaxer and hydrotreater.
  • the hydrotreating step of the process of U.S. Patent No. 4,137,148 is essential if a lube base stock oil possessing adequate oxidation stability is to be obtained.
  • the present process results in a significant lowering of the line-out temperature thereby extending catalyst life and reducing the frequency with which the dewaxing catalyst must be regenerated.
  • this invention provides a process for preparing a high quality lube base stock oil having a pour point not higher than -1°C (+30°F) from a waxy crude oil, which process comprises extracting distillate fraction that boils within the range of at least 232°C (450°F) to less than 566°C (1050°F) with a solvent selective for aromatic hydrocarbons to yield a raffinate; mixing the raffinate with hydrogen at pressure and contacting the mixture at a temperature of 260° to 385°C (500° to 725°F) with a dewaxing catalyst comprising a hydrogenation metal and an aluminosilicate zeolite having a silica/alumina ratio of at least about 12 and a constraint index of 1 to 12, thereby converting the wax contained in the raffinate to lower boiling hydrocarbons; and topping the dewaxed hydrotreated raffinate thereby recovering the high quality lube base stock oil, characterized in that the dewaxing is e
  • the wax base crudes (sometimes called “paraffin base") from which the charge stock is derived by distillation constitute a well recognized class of crude petroleums.
  • Many scales have been devised for classification of crude, some of which are described in Chapter VII Evaluation of Oil Stocks of "Petroleum Refinery Engineering," W. L. Nelson, McGraw-Hill, 1941.
  • a convenient scale identified by Nelson at page 69 involves determination of the cloud point of the Bureau of Mines "Key Fraction No. 2" which boils between 275°C and 300°C (527°F and 572°F) at 40 mm pressure. If the cloud point of this fraction is above -15°C (5°F), the crude is considered to be wax base.
  • a propane deasphalted short residuum fraction or a fraction having an initial boiling point of at least 232°C (450°F) and a final boiling point less than 566°C (1050°F) is prepared by distillation of such wax base crude. That fraction is solvent refined by counter current extraction with at least an equal volume (100 vol.%) of a selective solvent such as furfural. It is preferred to use from 1.5 to 3.0 volumes of solvent per volume of oil.
  • the furfural raffinate is subjected to catalytic dewaxing by mixing with hydrogen and contacting at 260°-385°C (500°-725°F) and a hydrogen partial pressure of above 10350 kPa (1,500 psia) and preferably at least 13800 kPa (2,000 psia) with a catalyst containing a hydrogenation metal and zeolite ZSM-5 or other aluminosilicate zeolite having a silicalalumina ratio above 12 and a constraint index of 1 to 12 and preferably a hydrogenation component, using a liquid hourly space velocity (LHSV) of 0.1 to 2.0 volumes of charge oil per volume of catalyst per hour.
  • the preferred space velocity is 0.5 to 1.0 LHSV.
  • the higher melting point waxes so removed are those of higher market value than the waxes removed in conventionally taking the product to a still lower pour point below -12°C (10°F).
  • cracked (and hydrogenated) fragments from cracking wax molecules in the catalytic dewaxer will have adverse effects on flash and fire points of the dewaxed raffinate product and are therefore removed by distillation of the product to meet flash and fire point specifications.
  • the catalyst employed in the catalytic dewaxing reactor and the temperature in that reactor are important to success in obtaining good yields and very low pour point product.
  • the hydrotreater catalyst may be any of the catalysts commercially available for that purpose but the temperature should be held within narrow limits for best results.
  • the solvent extraction technique is well understood in the art and needs no detailed review here.
  • the severity of extraction is adjusted to the composition of the charge stock to meet specifications for the particular lube base stock and the contemplated end-use. This severity will be determined in practice of this invention in accordance with well established practices.
  • the dewaxing catalyst is a composite of hydrogenation metal, preferably a metal of Group VIII of the Periodic Table, associated with the acid form of a novel class of aluminosilicate zeolite having a silica/alumina ratio of at least about 12 and a constrained access to the intracrystalline free space, as more fully described hereinbelow.
  • zeolites An important characteristic of the crystal structure of this class of zeolites is that it provides constrained access to, and egress from the intracrystalline free space by virtue of having a pore dimension greater than 5 Angstroms and pore windows of about a size such as would be provided by 10-membered rings of oxygen atoms. It is to be understood, of course, that these rings are those formed by the regular disposition of the tetrahedra making up the anionic framework of the crystalline aluminosilicate, the oxygen atoms themselves being bonded to the silicon or aluminum atoms at the centers of the tetrahedra.
  • the preferred type zeolites useful in this invention possess, in combination: a silica to alumina mole ratio of at least 12; and a structure providing constrained access to the crystalline free space.
  • the silica to alumina ratio referred to may be determined by conventional analysis. This ratio is meant to represent, as closely as possible, the ratio in the rigid anionic framework of the zeolite crystal and to exclude aluminum in the binder or in cationic or other form within the channels.
  • zeolites with a silica to alumina ratio of at least 12 are useful, it is preferred to use zeolites having higher ratios of at least 30. Such zeolites, after activation, acquire an intracrystalline sorption capacity for normal hexane which is greater than that for water, i.e., they exhibit "hydrophobic" properties. It is believed that this hydrophobic character is advantageous in the present invention.
  • the type zeolites useful in this invention freely sorb normal hexane and have a pore dimension greater than about 5 Angstroms.
  • the structure must provide constrained access to larger molecules. It is sometimes possible to judge from a known crystal structure whether such constrained access exists. For example, if the only pore windows in a crystal are formed by 8-membered rings of oxygen atoms, then access by molecules of larger cross-section than normal hexane is excluded and the zeolite is not of the desired type. Windows of 10-membered rings are preferred, although, in some instances, excessive puckering or pore blockage may render these zeolites ineffective.
  • a simple determination of the "constraint index" may be made by passing continuously a mixture of an equal weight of normal hexane and 3-methylpentane over a small sample, approximately 1 gram or less, of catalyst at atmospheric pressure according to the following procedure.
  • a sample of the zeolite, in the form of pellets or extrudate, is crushed to a particle size about that of coarse sand and mounted in a glass tube.
  • the zeolite Prior to testing, the zeolite is treated with a stream of air at 538°C (1000°F) for at least 15 minutes.
  • the zeolite is then flushed with helium and the temperature adjusted between 288°C and 510°C (550°F and 950°F) to give an overall conversion between 10% and 60%.
  • the mixture of hydrocarbons is passed at 1 liquid hourly space velocity (i.e., 1 volume of liquid hydrocarbon per volume of zeolite per hour) over the zeolite with a helium dilution to give a helium to total hydrocarbon mole ratio of 4:1.
  • a sample of the effluent is taken and analyzed, most conveniently by gas chromotography, to determine the fraction remaining unchanged for each of the two hydrocarbons.
  • the "constraint index” is calculated as follows:
  • the constraint index approximates the ratio of the cracking rate constants for the two hydrocarbons.
  • Zeolites suitable for the present invention are those having a constraint index in the approximate range of 1 to 12.
  • Constraint Index (CI) values for some typical zeolites are:
  • the above constraint index values typically characterize the specified zeolites but that such are the cumulative result of several variables used in determination and calculation thereof.
  • the constraint index may vary within the indicated approximate range of 1 to 12.
  • other variables such as the crystal size of the zeolite, the presence of possible occluded contaminants and binders intimately combined with the zeolite may affect the constraint index.
  • the constraint index while affording a highly useful means for characterizing the zeolites of interest is approximate, taking into consideration the manner of its determination, with probability, in some instances, of compounding variable extremes. However, in all instances, at a temperature within the above-specified range of 288° to 510°C (550°F to 950°F), the constraint index will have a value for any given zeolite of interest herein within the approximate range of 1 to 12.
  • the class of zeolites defined herein is exemplified by ZSM-5, ZSM-11, ZSM-12, ZSM-35, ZSM-38, and other similar materials.
  • U.S. Patent No. 3,702,886 describes ZSM-5
  • ZSM-11 is described in U.S. Patent No. 3,709,979
  • ZSM-12 is described in U.S. Patent No. 3,832,449
  • ZSM-35 is described in U.S. Patent No. 4,016,245,
  • ZSM-38 is described in U.S. Patent No. 4,046,859.
  • the specific zeolites described, when prepared in use presence of organic cations, are catalytically inactive, possibly because the intracrystalline free space is occupied by organic cations from the forming solution. They may be activated by heating in an inert atmosphere at 538°C (1000°F) for one hour, for example, followed by base exchange with ammonium salts followed by calcination at 38°C (100°F) in air.
  • the presence of organic cations in the forming solution may not be absolutely essential to the formation of this type zeolite; however, the presence of these cations does appear to favor the formation of this special type of zeolite. More generally, it is desirable to activate this type catalyst by base exchange with ammonium salts followed by calcination in air at about 538°C (1000°F) for from 15 minutes to 24 hours.
  • Natural zeolites may sometimes be converted to this type zeolite catalyst by various activation procedures and other treatments such as base exchange, steaming, alumina extraction and calcination, in combinations.
  • Natural minerals which may be so treated include ferrierite, brewsterite, stilbite, dachiardite, epistilbite, heulandite, and clinoptilolite.
  • the preferred crystalline aluminosilicates are ZSM-5, ZSM-11, ZSM-12, ZSM-38 and ZSM-35, with ZSM-5 particularly preferred.
  • the zeolites hereof are selected as those having a crystal framework density, in the dry hydrogen form, of not substantially below 1.6 grams per cubic centimeter. It has been found that zeolites which satisfy all three of these criteria are most desired. Therefore, the preferred zeolites of this invention are those having a constraint index as defined above of from 1 to 12, a silica to alumina ratio of at least about 12 and a dried crystal density of not less than about 1.6 grams per cubic centimeter.
  • the dry density for known structures may be calculated from the number of silicon plus aluminum atoms per 1000 cubic Angstroms, as given, e.g., on page 19 of the article on Zeolite Structure by W. M.
  • the crystal framework density may be determined by classical pycnometer techniques. For example, it may be determined by immersing the dry hydrogen form of the zeolite in an organic solvent which is not sorbed by the crystal. It is possible that the unusual sustained activity and stability of this class of zeolites is associated with its high crystal anionic framework density of not less than about 1.6 grams per cubic centimeter. This high density, of course, must be associated with a relatively small amount of free space within the crystal, which might be expected to result in more stable structures. This free space, however, is important as the locus of catalytic activity.
  • Crystal framework densities of some typical zeolites are:
  • the zeolite When synthesized in the alkali metal form, the zeolite is conveniently converted to the hydrogen form, generally by intermediate formation of the ammonium form as a result of ammonium ion exchange and calcination of the ammonium form to yield the hydrogen form.
  • the hydrogen form In addition to the hydrogen form, other forms of the zeolite wherein the original alkali metal has been reduced to less than about 1.5 percent by weight may be used.
  • the original alkali metal of the zeolite may be replaced by ion exchange with other suitable ions of Groups IB to VIII of the Periodic Table, including, for example, nickel, copper, zinc, palladium, calcium or rare earth metals.
  • Such matrix materials include synthetic or naturally occurring substances as well as inorganic materials such as clay, silica and/or metal oxides.
  • the latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides.
  • Naturally occurring clays which can be composited with the zeolite include those of the montmorillonite and kaolin families, which families include the sub-bentonites and the kaolins commonly known as Dixie, McNamee-Georgia and Florida clays or others in which the main mineral constituent is haloysite, kaolinite, dickite, nacrite or anauxite. Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment or chemical modification.
  • the zeolites employed herein may be composited with a porous matrix material such as alumina, silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania as well as ternary compositions, such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia.
  • the matrix may be in the form of a cogel.
  • the relative proportions of zeolite component and inorganic oxide gel matrix may vary widely with the zeolite content ranging from 1 to 99 percent by weight and more usually in the range of from 5 to 80 percent by weight of the composite.
  • the effluent of the dewaxing unit is topped by distillation, i.e., the most volatile components are removed, to meet flash and fire point specifications.
  • a hydrotreating step such as that described in U.S. Patent No. 4,137,148, supra, is ordinarily not required to provide a lube base stock oil having a suitable level of oxidation stability, in some cases it may be desirable to conduct such a step herein.
  • the catalytic dewaxing effluent is introduced into a hydrotreater containing, as catalyst, a hydrogenation component on a non-acidic support, such as cobalt-molybdate or nickel-molybdate on alumina.
  • Hydrotreating is effected therein at a temperature of from about 218° to 316°C (425° to 600°F), hydrogen partial pressures of 1035-10350 kPa (150-1500 psia), at the reactor inlets, and preferably 1725-3450 kPa (250-500 psia), with 89 to 890 I/I (500 to 5000 standard cubic feet) of hydrogen per barrel of feed (SCF/B), preferably 267 to 445 I/I (1500 to 2500 SCF/B).
  • Examples 1 to 4 illustrate of the high-pressure catalytic dewaxing process of the present invention carried out upon two heavy neutral lube stocks, designated Raffinate A and Raffinate B, and
  • Example 5 illustrates a low-pressure combined catalytic dewaxing/hydrotreating process such as. described in U.S. Patent No. 4,137,148.
  • a nickel-containing HZSM-5 catalyst was employed.

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  • Chemical & Material Sciences (AREA)
  • Crystallography & Structural Chemistry (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)

Claims (6)

1. Un procédé pour préparer une huile servant de charge de base pour des lubrifiants de haute qualité ayant un point de coulée ne dépassant pas -1°C (+30°F) à partir d'un pétrole brut paraffinique, lequel procédé comprend l'extraction d'une fraction de distillat qui bout dans la gamme d'au moins 232°C à moins de 566°C (450-1050°F) avec un solvant sélectif pour des hydrocarbures aromatiques afin de fournir un raffinat; le mélange du raffinat avec de l'hydrogène, sous pression, et la mise en contact du mélange à une température de 260°C à 385°C (500 à 725°F) avec un catalyseur de déparaffinage comprenant un métal d'hydrogénation et une zéolite de type aluminosilicate ayant un rapport silice/alumine d'au moins environ 12 et un indice de contrainte de 1 à 12, de façon à convertir les paraffines contenues dans le raffinat en hydrocarbures de point d'ébullition inférieur; et l'enlèvement des têtes du raffinat hydrotraité déparaffiné pour récupérer l'huile servant de charge de base pour des lubrifiants de haute qualité, caractérisé en ce que le déparaffinage est effectué par mise en contact du raffinat avec le catalyseur de déparaffinage à une pression partielle d'hydrogène d'au moins 10.350 kPa (1500 psia), si bien que la longueur du cycle du catalyseur est améliorée.
2. Un procédé suivant la revendication 1, caractérisé en ce que l'enlèvement des têtes est effectué directement sur le raffinat déparaffiné, éliminant ainsi l'hydrotraitement.
3. Un procédé suivant la revendication 1 ou la revendication 2, caractérisé en ce que la pression partielle d'hydrogène est de 13.800 (2000 psia).
4. Un procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que la zéolite de type aluminosilicate comprend la ZSM-5.
5. Un procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le métal d'hydrogénation comprend du nickel.
6. Un procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le raffinat est partiellement déparaffiné au cours d'un déparaffinage par solvant effectué avant l'étape de déparaffinage catalytique.
EP19830305125 1982-09-28 1983-09-05 Emploi de haute pression pour l'amélioration de la qualité de produit et l'augmentation de la longueur du cycle dans le déparaffinage catalytique des lubrifiants Expired EP0104807B1 (fr)

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US42584282A 1982-09-28 1982-09-28
US425842 1982-09-28

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EP0104807A3 EP0104807A3 (en) 1986-08-13
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EP (1) EP0104807B1 (fr)
JP (1) JPS5980491A (fr)
AU (1) AU561968B2 (fr)
BR (1) BR8305306A (fr)
CA (1) CA1228563A (fr)
DE (1) DE3381413D1 (fr)

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EP0161833B1 (fr) * 1984-05-03 1994-08-03 Mobil Oil Corporation Déparaffinage catalytique d'huiles légères et lourdes dans deux réacteurs parallèles
JPH06916B2 (ja) * 1984-06-01 1994-01-05 東燃株式会社 低流動点潤滑油基油の製造方法
US5098551A (en) * 1989-05-30 1992-03-24 Bertaux Jean Marie A Process for the manufacture of lubricating base oils
FR2797270B1 (fr) * 1999-08-02 2003-03-07 Inst Francais Du Petrole Procede et flexible de production de bases huiles et eventuellement de distillats moyens de tres haute qualite
KR100603225B1 (ko) * 1998-11-06 2006-07-24 앵스띠뛰 프랑세 뒤 뻬뜨롤 의약용 오일 및 임의로 중간 증류물의 융통적인 제조 방법
FR2785617B1 (fr) * 1998-11-06 2001-01-05 Inst Francais Du Petrole Procede flexible de production de bases huiles et eventuellement de distillats moyens de tres haute qualite
JP5737981B2 (ja) 2011-02-04 2015-06-17 独立行政法人石油天然ガス・金属鉱物資源機構 炭化水素油の製造方法
US9796936B2 (en) * 2015-09-09 2017-10-24 Chevron U.S.A. Inc. Production of heavy API group II base oil

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US4137148A (en) * 1977-07-20 1979-01-30 Mobil Oil Corporation Manufacture of specialty oils
CA1117455A (fr) * 1977-12-20 1982-02-02 Mobil Oil Corporation Fabrication d'une huile lubrifiante
US4357232A (en) * 1981-01-15 1982-11-02 Mobil Oil Corporation Method for enhancing catalytic activity

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EP0104807A3 (en) 1986-08-13
CA1228563A (fr) 1987-10-27
AU1910983A (en) 1984-04-05
JPS5980491A (ja) 1984-05-09
BR8305306A (pt) 1984-05-08
AU561968B2 (en) 1987-05-21
DE3381413D1 (de) 1990-05-10
EP0104807A2 (fr) 1984-04-04

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