EP0140468B1 - Procédé combiné pour la production d'huiles lubrifiantes à partir de pétroles bruts marginaux - Google Patents

Procédé combiné pour la production d'huiles lubrifiantes à partir de pétroles bruts marginaux Download PDF

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Publication number
EP0140468B1
EP0140468B1 EP84304382A EP84304382A EP0140468B1 EP 0140468 B1 EP0140468 B1 EP 0140468B1 EP 84304382 A EP84304382 A EP 84304382A EP 84304382 A EP84304382 A EP 84304382A EP 0140468 B1 EP0140468 B1 EP 0140468B1
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Prior art keywords
raffinate
zsm
catalyst
dewaxing
hydrotreating
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EP84304382A
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German (de)
English (en)
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EP0140468A1 (fr
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William Everett Garwood
Murray Robert Silk
John Wesley Walker
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ExxonMobil Oil Corp
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Mobil Oil Corp
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/58—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
    • 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

Definitions

  • This invention is concerned with manufacture of high grade viscous oil products from crude petroleum fractions. It is particularly directed to the manufacture of high quality lube basestock 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 and straight chain paraffins and yield viscous fractions which inherently possess low pour points. More specifically, the invention is concerned with improving the viscosity index of lube basestock oils obtained from marginal lube crudes.
  • High quality lube basestock 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 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 conveniently treated to remove these asphalt-like constituents prior to solvent extraction to increase the viscosity index.
  • the raffinate from the solvent extraction step 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/toluene mixtures to remove the wax and prepare a dewaxed raffinate.
  • the dewaxed raffinate may then be finished by any number of sorption or catalytic processes to improve color and oxidation stability.
  • the quality of the lube basestock 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.
  • crudes such as Arab Heavy have been found previously to be unsatisfactory crudes for making lubes having a viscosity index (V.I.) of 100 using conventional furfural extraction and solvent dewaxing processing steps and are thus characterized as giving marginal quality lubricating oils.
  • V.I. viscosity index
  • the yield of high quality lube basestock oil also depends on these factors, and as a rule, the higher quality sought, the less the yield.
  • naphthenic crudes are favored because less loss is encountered, particularly in the dewaxing step.
  • waxy crudes are more readily available, and it would be desirable to provide a process for preparing high quality lube basestock oils in good yields from such waxy crude oils to broaden the crude sources for making lubes.
  • a stabilized lubricating oil stock resistant to oxidation and sludge formation upon exposure to a highly oxidative environment is formed by contacting a high viscosity lubricating oil stock with hydrogen in the presence of a catalyst of low acidity comprised of a platinum- group metal on a solid refractory inorganic oxide support.
  • a stabilized lube oil product obtained by hydrocracking is produced by contacting a lube oil product before or after dewaxing with a catalyst having hydrogenation-dehydrogenation activity and hydrogen at pressure in the range from atmospheric up to about 100 psig (791 kPa) under conditions of temperature in the range of 204°C (400°F) to about 427°C (800°F).
  • a two-stage process for preparing a high quality lube basestock oil is disclosed in US-A-4,181,598 in which a raffinate is mixed with hydrogen and the mixture contacted with a dewaxing catalyst comprising a ZSM-5 type catalyst to convert the wax contained in the raffinate to low boiling hydrocarbons and subsequently, contacting the dewaxed raffinate in the presence of hydrogen at a temperature of 218-316°C (425-600°F) with a hydrotreating catalyst comprising a hydrogenation component on a non-acid support such as cobalt-molybdate or nickel-molybdate on alumina. Hydrotreating the dewaxed raffinate is limited to saturate olefins and reduce product colour without causing appreciable desulfurization.
  • EP-A-134637 discloses a process for preparing a high quality lube basestock oil from waxy crude oil, which process comprises:
  • Another object of the invention is to produce light and air stable lubricating oils with V.I. in the order of 100 from marginal crude feedstocks.
  • the present invention provides a process for preparing a high quality lube basestock oil from waxy crude oil.
  • Such a process comprises (A) extracting a waxy crude oil distillate fraction that boils within the range of from 316°C to 593°C (600°F to 1100°F), or a deasphalted short residuum fraction of such a waxy crude oil, with an aromatic hydrocarbon solvent in order to yield a wax-containing raffinate from which undesirable compounds have been removed; (B) mixing the wax-containing raffinate with hydrogen and contacting this mixture under particular temperature conditions with a particular type of dewaxing catalyst to thereby convert wax contained in the raffinate to lower boiling hydrocarbons; and (C) cascading this dewaxed raffinate to a hydrotreating zone wherein the dewaxed raffinate is contacted in the presence of hydrogen with a particular type of hydrotreating catalyst under particular reaction conditions to hydrotreat the dewaxed raffinate to substantialy complete
  • the dewaxing catalyst employed in the dewaxing step is a catalyst comprising an aluminosilicate zeolite having a silica/alumina ratio of at least 12 and a constraint index of from 1 to 12. Temperature in the dewaxing step ranges from 260°C to 357°C (500°F to 675°F).
  • the hydrotreating catalyst employed in the hydrotreating zone comprises a strong hydrogenation component on a non-acidic support.
  • Conditions in the hydrotreating zone include a hydrogen partial pressure of from about 6996 kPa to 20786 kPa (1000 psig to 3000 psig), a temperature of from about 260°C to 357°C (500°F to 675°F) and a liquid hourly space velocity of from about 0.1 to 2.0.
  • the present invention is thus based on the discovery that the obtainable light and air stability and high viscosity index of the resulting product coincides with essentially complete desulfurization of this dewaxed lube product.
  • Light and air stable lubricating oils with a viscosity index in the order or 100 can thus be produced from marginal crude feedstocks.
  • the wax base crudes (sometimes called "paraffin base") from which the chargestock 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 U.S. Bureau of Mines (key fraction #2) which boils between 527°F (275°C) and 572°F (300°C) at 40 mm (5333 Pa) pressure. If the cloud point of this fraction is above 5°F (-15°C), the crude is considered to be wax base.
  • a suitable chargestock such as propane deasphalted short residuum fraction or a fraction having an initial boiling point of at least about 450°F (232°C), and preferably at least about 600°F (316°C), and a final boiling point less than about 1100°F (593°C) is prepared by distillation of such wax base crude.
  • Such fraction can then be solvent refined by counter current extraction with at least an equal volume (100 volume percent) of a selective solvent such as furfural. It is preferred to use about 1.5-3.0 volumes of solvent per volume of oil.
  • the solvent e.g., furfural, raffinate can be subjected to catalytic dewaxing by mixing with hydrogen and contacting at 500-675°F (260-357°C) with a catalyst containing a hydrogenation metal and zeolite ZSM-5 or other related silicate zeolites having a silicalalumina ratio of at least 1 and a Constraint Index of 1-12 using a liquid hourly space velocity (LHSV) of 0.1-2.0 volumes of charge oil per volume of catalyst per hour.
  • LHSV liquid hourly space velocity
  • the preferred space velocity is 0.5-1.0 LHSV.
  • the effluent of catalytic dewaxing can then be cascaded into a hydrotreater containing, as catalyst, a strong hydrogenation component on a non-acid support, such as supported nickel- tungsten or platinum on alumina.
  • a hydrotreater operates at temperatures of 500-675°F (260-357°C) and at elevated pressures within the range of 1000-3000 psig (6996-20786 kPa), preferably 1200-2500 psig (8375-17338 kPa) and a space velocity like that of the catalytic dewaxing reactor.
  • the catalytic dewaxing reaction can be carried out at hydrogen partial pressures of 150-3000 psia (1034-20684 kPa), at the reactor inlet, and preferably at 250-1500 psia (1724-10342 kPa).
  • Dewaxing and hydrotreating operate at 500 to 5000 standard cubic feet of hydrogen per barrel of feed (SCF/bbi) (89 to 890 nl of H z /I of feed), preferably 1500-2500 SCF/bbl (267-445 nl/I). It is preferred to dewax at the same pressure as the hydrotreat stage.
  • the dewaxed effluent is converted over the strong hydrogenating catalyst to a material having a viscosity index (V.I.) of approximately 100, e.g., from 95 to 105.
  • V.I. viscosity index
  • the viscosity inded is an empirical number indicating the effect of change of temperature on the viscosity of an oil.
  • a low viscosity index signifies a relatively large change of viscosity with temperature, and vice versa.
  • the steepness of the viscosity-temperature curve of the sample is interpolated between that of a Pennsylvania Oil (denoted as 100 VI) and that of a Texas Coastal Oil (denoted 0 VI), both of which reference oils have the same viscosity as the sample at 210°F (99°C).
  • the high viscosity index of the lube obtained coincides with substantially complete desulfurization. While further cracking increases V.I., loss of yield increases and both light and air stability suffer.
  • 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 10°F (-12°C).
  • 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 flash and fire point specifications.
  • the catalyst employed in the catalytic dewaxing reaction zone and the temperature in that reaction zone are important to success in obtaining good yields and very low pour point product.
  • the strong hydrotreater catalyst may be any of the catalysts commercially available for that purpose but the temperature should be held within narrow limits for the desired cracking (desulfurization).
  • the solvent extraction technique is well understood in the art and needs no detailed review here.
  • the severity of extraction is adjusted to composition of the chargestock to meet specifications for the particular lube basestock and the contemplated end-use; this severity will be determined in practice of this invention in accordance with well established practices.
  • the catalytic dewaxing step can be conducted at temperatures of 500-675°F (260-357°C). At temperatures above about 675°F (357°C), bromine number of the product generally increases significantly and the oxidation stability decreases.
  • the dewaxing catalyst is preferably a composite of hydrogenation metal, preferably a metal of Group VIII of the Periodic Table, associated with the acid form of an aluminosilicate zeolite having a silica/alumina ratio of at least about 12, and a constrained access to the intracrystalline free space as measured by having a Constraint Index of from about 1 to 12.
  • Zeolite materials of silica/alumina molar ratio greater than 12 and Constraint Index of 1 to 12 are used in the dewaxing catalyst employed in the present invention.
  • Such zeolites, also known as ZSM-5 type zeolites, are well known. This use as dewaxing catalysts has, for example been described in US-A-4,358,363.
  • Crystalline zeolites of the type useful in the dewaxing catalysts of the present invention include ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 and zeolite beta, with ZSM-5 being particularly preferred.
  • ZSM-5 is described in greater detail in US-A-3,702,886 and US-E-29,948, which patents provide the X-ray diffraction pattern of the therein disclosed ZSM-5.
  • ZSM-11 is described in US-A-3,709,979, which discloses in particular the X-ray diffraction pattern of ZSM-11.
  • ZSM-12 is described in US-A-3,832,449, which discloses in particular the X-ray diffraction pattern of ZSM-12.
  • ZSM-23 is described in US-A-4,076,842, which discloses in particular the X-ray diffraction pattern of ZSM-23.
  • ZSM-35 is described in US-A-4,016,245, which discloses in particular the X-ray diffraction pattern of ZSM-35.
  • ZSM-38 is described in US-A-4,046,859, which discloses in particular the X-ray diffraction pattern of ZSM-38.
  • ZSM-48 is described in US-A-4,375,573 and European Patent Publication EP-A-0015132, which discloses in particular the X-ray diffraction pattern of ZSM-48.
  • Zeolite beta is described in greater detail in US-A-3,308,069 and US-E-28,341, which patents disclose in particular the X-ray diffraction pattern of zeolite beta.
  • a ZSM-5 type zeolite also useful herein includes the highly siliceous ZSM-5 described in US-A-4,067,724 and referred to in that patent as "silicalite.”
  • the specific zeolites described, when prepared in the 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 1000°F(538°C) for 1 hour, for example, followed by base exchange with ammonium salts followed by calcination at 1000°F (538°C) 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 1000°F (538°C) for from 15 minutes to 24 hours.
  • the zeolite when synthesized in the alkali metal form, is conveniently converted to the hydrogen form, generally by intermediate formation of the ammonium form as a result of ammonium form to yield 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, by way of example, nickel, copper, zinc, palladium, calcium or rare earth metals.
  • crystalline aluminosilicate zeolite in another material resistant to the temperature and other conditions employed in the process.
  • 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 halloysite, 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 composed with a porous matrix material, such as alumina, silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-berylia, silica-titania as well as ternary compositions, such as silica-alumina-thoria, silica- alumina-magnesia and silica-magne1;ia-zirconia.
  • the matrix may be in the-form of a cogel.
  • the relative proportions of zeolite component and matrix may vary widely with the zeolite content ranging from between 1 to 99 percent by weight and more usually.in the range of 5 to 80 percent by weight of the composite.
  • the total effluent of the catalytic dewaxing step including the hydrogen, is cascaded into a hydrotreating reactor of the type now generally employed for finishing of lubricating oil stocks.
  • the hydrotreater is sized to handle the total dewaxer effluent.
  • some modification of the cascade operation is contemplated, such as interstage recovery of gasoline boiling range by-product, it is to be understood that such modification contemplates no substantial interruption or substantial delay in passing the dewaxed raffinate to the hydrotreater.
  • “cascading” means passing the dewaxed raffinate plus hydrogen to hydrotreating without storage of the dewaxer effluent.
  • any of the known hydrotreating catalysts consisting of a strong hydrogenation component on a non-acidic support may be employed in the hydrotreating step.
  • Such catalysts include, for example, nickel- tungsten on silica-alumina or platinum on alumina.
  • temperature control is required for production of high quality products having the desired desulfurization and thus high V.I. as well as light and air stability.
  • the effluent of the hydrotreater is topped by distillation, i.e., the most volatile components are removed, to meet flash and fire point specifications.
  • the crude source of this Example is Arab. Heavy. Distillation of the crude yielded 9.1 % volume vacuum distillate, above a 27.3% volume vacuum resid.
  • the vacuum distillate had the properties as set forth in Table 1.
  • the vacuum distillate was furfural extracted at 91°C (195°F) using a solvent/oil ratio of 200.
  • the yield of raffinate was 53.3 wt.% and had the following properties: Kinematic Viscosity.
  • the raffinate obtained above was processed under dewaxing conditions to a pour point of -4°C (+25°F) using a dual catalyst bed of Ni/ZSM-5 followed by Co/Mo/AI.
  • the dewaxing conditions are as follows:
  • the viscosity index of the oil is too low to be of commercial value as is that obtained by conventional solvent dewaxing of the raffinate (about 90).
  • the viscosity of the catalytically dewaxed oil is undesirably high.
  • the catalytically dewaxed oil of Example 1 having the properties set forth in Table 2 was hydrotreated over a commercial catalyst Ni/W/Ti/SiAI (ICR-106 - Trademark from Chevron).
  • the catalyst samples contained 19.7 wt.% W, 6.5 wt.% Ni, 4.5 wt.% Ti, 0.04 wt.% CoO, 0.03 wt.% MoO 3 , and the remainder is silica-alumina.
  • the catalyst was sulfided before use. Conditions of the hydrotreating were as follows:
  • Figures 1-5 are obtained from the data set forth in Table 3.
  • lube yield is about 80 wt.%, and at 110 V.I. yield drops sharply to 55 wt.%.
  • the V.I. at 100 matches that obtained from premium lube stocks, such as Arab Light using conventional solvent dewaxing technology.
  • the haze in the 91 V.I. sample was a very fine divided white material as opposed to the reddish-brown coarse floc characteristic of hydrocracked oils. Warming of the oil by direct sunlight reduced the haze considerably. An alcohol thermometer taped to the window read 115°F (46°C) while the temperature was 78°F (26°C). Late in the day, as the oil cooled, the haze returned. This reversibility of the haze would fit wax formation. The charge oil containing all its aromatic sulfur compounds does not form haze, which suggests that the addition of sulfur compounds normally used in the additive package could inhibit the haze.

Claims (7)

1. Un procédé de préparation d'une huile de base lubrifiante à partir d'une huile brute paraffinique, ce procédé comprenant les étapes suivantes:
a) on extrait une fraction de distillat d'huile brute paraffinique bouillant dans un intervalle compris entre 316 et 593°C (600 à 1100°F), ou une fraction de résidu court désasphalté de cette huile brute paraffinique, à l'aide d'un solvant hydrocarboné aromatique pour obtenir un raffinat paraffinique dont les composants indésirables ont été éliminés;
b) on mélange le raffinat paraffinique avec de l'hydrogène et on met mélange, à une température de 260 à 357°C (500 à 675°F) au contact d'un catalyseur de déparaffinage comprenant une zéolite à base d'aluminosilicate dont le rapport silice/alumine est au moins égal à 12 et l'indice de contrainte est compris entre 1 et 12 pour convertir ainsi les paraffines contenues dans la raffinat en hydrocarbures de plus faible point d'ébullition, et
c) on fait passer en cascade le raffinat déparaffiné vers une zone d'hydrotraitement dans laquelle on met le raffinat déparaffiné en contact, en présence d'hydrogène, avec un catalyseur d'hydrotraitement comprenant un composant d'hydrogénation intense sur un support non acide, à une pression partielle d'hydrogène comprise entre 6996 kPa et 20786 kPa (1000 psig et 3000 psig) à une température de 260 à 357°C (500 à 675°F) et à une vitesse spatiale horaire liquide comprise entre 0,1 et 2,0 pour hydrotraiter ainsi ce raffinat déparaffiné et obtenir une huile de base lubrifiante dont l'indice de viscosité est approximativement égal à 100.
2. Un procédé selon la revendication 1, dans lequel on prépare le raffinat par extraction d'une fraction de résidu court désasphalté et dans lequel on fait passer en cascade la totalité de l'effluent de l'étape de déparaffinage catalytique vers la zone d'hydrotraitement.
3. Un procédé selon la revendication 1 ou la revendication 2, dans lequel le catalyseur de déparaffinage comprend une zéolite à base d'aluminosilicate choisie parmi les suivantes: ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 ou la zéolite béta.
4. Un procédé selon la revendication 1 ou la revendication 2, dans lequel le catalyseur de déparaffinage comprend de la ZSM-5 et un métal d'hydrogénation.
5. Un procédé selon l'une quelconque des revendications 1 à 4, dans lequel le raffinat est partiellement déparaffiné par déparaffinage au solvant avant que l'on ne mette le raffinat déparaffiné au contact du catalyseur d'hydrotraitement.
6. Un procédé selon l'une quelconque des revendications 1 à 5, dans lequel le catalyseur d'hydrotraitement est du nickel-tungstène ou du platine supporté sur alumine.
7. Un procédé selon la revendication 4, dans lequel le métal d'hydrogénation du catalyseur de déparaffinage est le nickel.
EP84304382A 1983-08-31 1984-06-28 Procédé combiné pour la production d'huiles lubrifiantes à partir de pétroles bruts marginaux Expired EP0140468B1 (fr)

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JP (1) JPS6055083A (fr)
AU (1) AU574688B2 (fr)
BR (1) BR8403436A (fr)
CA (1) CA1252410A (fr)
DE (1) DE3476080D1 (fr)
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US7670983B2 (en) 2002-10-08 2010-03-02 Exxonmobil Research And Engineering Company Oxygenate treatment of dewaxing catalyst for greater yield of dewaxed product

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GB8425837D0 (en) * 1984-10-12 1984-11-21 Shell Int Research Manufacture of lubricating base oils
EP0271265A1 (fr) * 1986-12-04 1988-06-15 Mobil Oil Corporation Procédé pour réduire les points d'écoulement et de trouble d'huiles lubrifiantes d'hydrocraquage
JPH07116453B2 (ja) * 1987-06-06 1995-12-13 出光興産株式会社 流動パラフィンの製造方法
US7087152B2 (en) 2002-10-08 2006-08-08 Exxonmobil Research And Engineering Company Wax isomerate yield enhancement by oxygenate pretreatment of feed
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US7077947B2 (en) 2002-10-08 2006-07-18 Exxonmobil Research And Engineering Company Process for preparing basestocks having high VI using oxygenated dewaxing catalyst
US20040108250A1 (en) * 2002-10-08 2004-06-10 Murphy William J. Integrated process for catalytic dewaxing
US7282137B2 (en) 2002-10-08 2007-10-16 Exxonmobil Research And Engineering Company Process for preparing basestocks having high VI
US6951605B2 (en) 2002-10-08 2005-10-04 Exxonmobil Research And Engineering Company Method for making lube basestocks
US7704379B2 (en) 2002-10-08 2010-04-27 Exxonmobil Research And Engineering Company Dual catalyst system for hydroisomerization of Fischer-Tropsch wax and waxy raffinate
US7125818B2 (en) 2002-10-08 2006-10-24 Exxonmobil Research & Engineering Co. Catalyst for wax isomerate yield enhancement by oxygenate pretreatment

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US4181598A (en) * 1977-07-20 1980-01-01 Mobil Oil Corporation Manufacture of lube base stock oil
US4137148A (en) * 1977-07-20 1979-01-30 Mobil Oil Corporation Manufacture of specialty oils

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7670983B2 (en) 2002-10-08 2010-03-02 Exxonmobil Research And Engineering Company Oxygenate treatment of dewaxing catalyst for greater yield of dewaxed product

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AU574688B2 (en) 1988-07-14
BR8403436A (pt) 1985-06-25
CA1252410A (fr) 1989-04-11
AU2990084A (en) 1985-03-07
DE3476080D1 (en) 1989-02-16
IN161436B (fr) 1987-12-05
ZA845040B (en) 1986-02-26
JPS6055083A (ja) 1985-03-29
EP0140468A1 (fr) 1985-05-08

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