EP0668342B1 - Procédé de préparation d'une huile lubrifiante de base - Google Patents

Procédé de préparation d'une huile lubrifiante de base Download PDF

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Publication number
EP0668342B1
EP0668342B1 EP19950200281 EP95200281A EP0668342B1 EP 0668342 B1 EP0668342 B1 EP 0668342B1 EP 19950200281 EP19950200281 EP 19950200281 EP 95200281 A EP95200281 A EP 95200281A EP 0668342 B1 EP0668342 B1 EP 0668342B1
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Prior art keywords
catalyst
alumina
silica
hydrogen
hydroconversion
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English (en)
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EP0668342A1 (fr
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Jacobus C/O Shell Nederland Raffin. B.V. Eilers
Jean-Pierre Gilson
Arend Hoek
Sytze Abel Posthuma
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Shell Internationale Research Maatschappij BV
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Shell Internationale Research Maatschappij BV
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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
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/12—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G65/00—Treatment of hydrocarbon oils by two or more hydrotreatment processes only
    • C10G65/02—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only
    • C10G65/04—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps
    • C10G65/043—Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including only refining steps at least one step being a change in the structural skeleton

Definitions

  • the present invention relates to a process for the preparation of lubricating base oils, in particular the preparation of very high viscosity index lubricating base oils from a mixture of carbon monoxide and hydrogen.
  • very high viscosity index refers to a viscosity index (VI) above 135, as determined by ASTM-D-2270.
  • Fischer-Tropsch synthesis The preparation of hydrocarbons from a mixture comprising carbon monoxide and hydrogen by contacting the mixture with a suitable synthesis catalyst at elevated temperatures and pressures is known in the art as the Fischer-Tropsch synthesis. It is known in the art to apply Fischer-Tropsch synthesis processes in the preparation of a range of principally aliphatic hydrocarbons having a wide range of molecular weights.
  • US patent specification No. 4 478 955 discloses a process scheme comprising contacting the effluent of a Fischer-Tropsch synthesis process with hydrogen in the presence of a suitable hydrogenation catalyst.
  • the effluent of the Fischer-Tropsch synthesis is described in this US patent specification as comprising pre-dominantly olefins and carboxylic acids.
  • useful fuel components comprising alkanes, alcohols and esters are produced.
  • European patent application No. 0 583 836 discloses a process for the preparation of hydrocarbon fuels from carbon monoxide and hydrogen.
  • Fischer-Tropsch synthesis is the use of the Fischer-Tropsch synthesis to prepare hydrocarbons suitable for use as lubricating base oil or lubricating base oil precursor, such as a Fischer-Tropsch wax.
  • European patent application No. 0 515 256 describes a process for the hydroisomerisation (hydroconversion) of Fischer-Tropsch waxes, using a catalyst containing zeolite Y. Upon solvent dewaxing of a fraction boiling above 380 °C a lubricating base oil is obtained having a VI of at least 130 and a pour point of at least -12 °C.
  • the hydroisomerisation treatment can be preceded by a hydrogenation treatment to remove any unsaturated hydrocarbons and oxygenates from the Fischer-Tropsch wax.
  • European patent application No. 0 321 303 discloses the preparation of middle distillate products from Fischer-Tropsch wax by a hydroisomerisation (hydroconversion) treatment. At least a portion of the bottoms fraction from the hydroisomerisation zone is either (a) further processed in a second hydroisomerisation zone or (b) fractionated and/or dewaxed for the production of a lubricating oil fraction boiling in the range of 343.3 °C to 510 °C. If desired, oxygenates may be removed from the Fischer-Tropsch wax by distillation.
  • the hydroisomerisation catalyst to be used in the first hydroisomerisation (hydroconversion) treatment is a platinum on fluorided alumina catalyst which is particularly effective (selective) at converting paraffinic Fischer-Tropsch wax to middle distillate material.
  • this catalyst is reported to be more effective than a catalyst containing a zeolite, in particular zeolite beta, as described in Example 3 of this patent application.
  • Example 3 describes in Example 3 that a zeolite Y catalyst can be as effective (selective) in the preparation of middle distillates from Fischer-Tropsch wax as a platinum on silica-alumina catalyst, but that a zeolite Y catalyst is much more active.
  • the zeolite Y catalyst required a reactor temperature of 260 °C, whilst the platinum on silica-alumina catalyst required a reactor temperature of 340 °C.
  • a hydroisomerisation (or hydroconversion) process involves both hydrocracking of paraffinic hydrocarbons and isomerisation of linear paraffinic hydrocarbons to branched paraffinic hydrocarbons. If it is desired to prepare lubricating base oils, it is advantageous to minimise the hydrocracking activity and to maximise the hydroisomerisation activity. Nevertheless, some hydrocracking activity is still required to crack the heaviest wax molecules to lower boiling products.
  • a disadvantage of a highly active catalyst, such as a zeolitic catalyst like zeolite Y, is that normally the hydrocracking activity is still too high and the hydroisomerisation activity too low.
  • molecular sieve catalysts such as silicoaluminophosphates and other zeolitic catalysts wherein the activity (expressed in terms of acidity) has been reduced to an alpha-value below 20 or even below 10 or 5.
  • these catalysts normally do not have sufficient hydrocracking activity.
  • European patent application No. 0 464 547 describes a process for the preparation of high viscosity index lubricants from slack wax by a two-step process wherein the first step the slack wax is hydrocracked under mild conditions using an amorphous catalyst, in particular a catalyst comprising Ni and W on a fluorided alumina carrier, and in the second step hydroisomerised using a low acidity zeolite beta catalyst, preferably having an alpha value of not greater than 5.
  • the alpha value is an approximate indication of the catalytic cracking activity of the catalyst compared to a standard catalyst.
  • the alpha test is described in United States patent specification No. 3 354 078 and in J. Catalysis, 4, 527 (1965); 6, 278 (1966); and 61, 395 (1980) and discussed in European patent application No. 0 464 547.
  • the alpha value is determined on the catalyst carrier not containing any catalytically active metals.
  • European patent application No. 0 323 092 discloses a process to prepare lubricating base oils starting from a Fischer Tropsch wax, by first hydrogenating the wax at a temperature of 343 to 412 °C and a pressure of between 70 and 100 bars in the presence of a catalyst having an alumina containing carrier. According to this publication a significant conversion of high boiling products occurs during hydrogenation. The hydrogenation step is followed by a hydrocracking/hydroisomerisation step and a pour point reducing treatment. A disadvantage of this process are the severe conditions employed in the hydrogenation step.
  • hydroconversion process refers to a process in which hydrocracking reactions and hydroisomerisation reactions occur and which is carried out in the presence of a catalyst comprising a refractory oxide carrier.
  • hydroisomerisation process refers to a process in which hydroisomerisation reactions and hydrocracking reactions occur, but which is carried out after a hydroconversion treatment and in which process generally less hydrocracking occurs than in the hydroconversion process.
  • a disadvantage of hydroconversion catalysts comprising a refractory oxide carrier is the high operating temperature which is required, in particular if the catalyst has been used for a prolonged time such as more than 2 years. In order to compensate for any catalyst deactivation generally the reaction temperature is increased. Above 350 °C and in particular above 400 °C at least part of the Fischer-Tropsch wax is converted into undesired aromatic compounds. Accordingly, it would be desirable to be able to provide a process which allows a hydroconversion process to be carried out at an operating temperature well below 400 °C and preferably below 350 °C, whilst using a catalyst containing a refractory oxide carrier and a catalytically active metal having hydrogenation/dehydrogenation activity.
  • the hydroconversion process can be operated at a reaction temperature below 400 °C, and even below 350 °C, even after the hydroconversion catalyst has been used for a prolonged time, that is for example more than 2 years.
  • the reaction temperature can be at least 5 °C, preferably at least 10 °C lower.
  • the hydroconversion catalyst deactivates much slower in a process which involves a preceding hydrogenation step.
  • the rate of reaction temperature increase required to compensate for any loss of catalyst activity can be much slower.
  • the present invention relates to a process for the preparation of lubricating base oils comprising subjecting a waxy raffinate to a pour point reducing treatment, and recovering a lubricating base oil therefrom, which waxy raffinate has been prepared by contacting a hydrocarbon product with hydrogen in the presence of a hydroconversion catalyst, comprising a catalytically active metal having hydrogenation/dehydrogenation activity supported on a refractory oxide carrier, under conditions such that hydrocracking and hydroisomerisation of the hydrocarbon product occur to yield the waxy raffinate, wherein the hydrocarbon product has been prepared by:
  • conditions such that substantially no hydrocracking or hydroisomerisation occurs in step (b) of the process of the present invention are defined as such conditions that the conversion in step (b) of the fraction of the feed boiling above 370 °C in % by weight, to a fraction boiling below 370 °C, is less than 10%.
  • hydroconversion step conditions such that hydrocracking and hydroisomerisation of the hydrocarbon product occur are defined as such conditions that the conversion as defined hereinabove is at least 15%.
  • substantially paraffinic when used in connection with hydrocarbon wax refers to a hydrocarbon mixture comprising at least 70 %wt (% by weight) paraffins, preferably at least 80 %wt paraffins.
  • Hydrocarbon wax produced by the process of this invention typically comprises at least 90 %wt paraffins, more typically at least 95 %wt paraffins.
  • a feed comprising a mixture of carbon monoxide and hydrogen is contacted at elevated temperature and pressure with a catalyst active in the synthesis of paraffinic hydrocarbons.
  • Suitable processes for the preparation of the mixture of carbon monoxide and hydrogen are well known in the art and include such processes as the partial oxidation of methane, typically in the form of natural gas, and the steam reforming of methane.
  • the relative amounts of carbon monoxide and hydrogen present in the feed may vary over a wide range and may be selected according to the precise catalyst and process operating conditions being employed.
  • the feed contacting the catalyst comprises carbon monoxide and hydrogen in a hydrogen/carbon monoxide molar ratio of below 2.5, preferably below 1.75. More preferably, the hydrogen/carbon monoxide ratio is in the range of from 0.4 to 1.5, especially from 0.9 to 1.3.
  • Unconverted carbon monoxide and/or hydrogen may be separated from the synthesis product and recycled to the inlet of the synthesis reactor.
  • the catalyst comprises, as the catalytically active component, a metal from Group VIII of the Periodic Table of the Elements.
  • a metal from Group VIII include ruthenium, iron, cobalt and nickel.
  • a catalyst comprising cobalt as the catalytically active metal is preferred.
  • the catalytically active metal is preferably supported on a porous carrier.
  • the porous carrier may be selected from any suitable refractory metal oxide or silicate or mixture thereof. Particular examples of preferred carriers include silica, alumina, titania, zirconia and mixtures thereof. Carriers comprising silica and/or alumina are especially preferred.
  • the catalytically active metal may be applied to the carrier by any of the techniques known in the art, for example comulling, impregnation or precipitation. Impregnation is a particularly preferred technique, in which the carrier is contacted with a compound of the catalytically active metal in the presence of a liquid, most conveniently in the form of a solution of the metal compound.
  • the compound of the active metal may be inorganic or organic, with inorganic compounds being preferred, in particular nitrates.
  • the liquid employed may also be either organic or inorganic. Water is a most convenient liquid.
  • the amount of catalytically active metal present on the carrier is typically in the range of from 1 to 100 parts by weight, preferably 10 to 50 parts by weight, per 100 parts by weight of carrier material.
  • the catalytically active metal may be present in the catalyst together with one or more metal promoters or co-catalysts.
  • the promoters may be present as metals or as the metal oxide, depending upon the particular promoter concerned. Suitable metal oxide promoters include oxides of metals from Groups IIA, IIIB, IVB, VB or VIB of the Periodic Table, oxides of the lanthanides and/or the actinides.
  • the catalyst comprises an oxide of an element in Group IVB of the Periodic Table, in particular titanium or zirconium. Catalysts comprising zirconium are especially preferred.
  • the catalyst may comprise a metal promoter selected from Groups VIIB and/or VIII of the Periodic Table.
  • Preferred metal promoters include platinum and palladium.
  • a most suitable catalyst comprises cobalt as the catalytically active metal and zirconium as a promoter.
  • the promoter may be incorporated in the catalyst using any of the methods discussed hereinbefore with respect to the catalytically active component.
  • the promoter if present in the catalyst, is typically present in an amount of from 1 to 60 parts by weight, preferably from 2 to 40 parts by weight, per 100 parts by weight of carrier material.
  • the hydrocarbon synthesis is conducted under conditions of elevated temperature and pressure. Typically, the synthesis is effected at a temperature in the range of from 125 to 300 °C, preferably from 175 to 250 °C.
  • the reaction pressure is typically in the range of from 5 to 100 bar, preferably from 12 to 50 bar.
  • the synthesis may be conducted using a variety of reactor types and reaction regimes, for example in a fixed bed regime, a slurry phase regime or an ebullating bed regime.
  • the hydrocarbon wax of the synthesis step (a) is subjected to a hydrogenation treatment in step (b) of the process of the present invention.
  • the entire effluent of the synthesis stage may be led directly to the hydrogenation step.
  • the low molecular weight products of the synthesis stage in particular the C 4 - fraction, for example methane, ethane and propane, may also be removed prior to the hydrogenation treatment.
  • the separation is conveniently effected using distillation techniques well known in the art.
  • the hydrocarbon wax can be separated into a low boiling fraction, boiling for example below 330 °C or below 370 °C and at least one high boiling fraction, boiling above 330 °C or above 370 °C and treat the high boiling fraction in the process of the present invention. Separation may be effected using vacuum distillation or alternatively short path distillation such as vacuum film distillation (using wiped film evaporators).
  • the hydrocarbon product is contacted with hydrogen in the presence of a hydrogenation catalyst.
  • a hydrogenation catalyst Suitable catalysts for use in this stage are known in the art.
  • the catalyst comprises as catalytically active component one or more metals selected from Groups VIB and VIII of the Periodic Table of Elements, in particular one or more metals selected from molybdenum, tungsten, cobalt, nickel, ruthenium, iridium, osmium, platinum and palladium.
  • the catalyst comprises on or more metals selected from nickel, platinum and palladium as the catalytically active component.
  • a particularly suitable catalyst comprises nickel as a catalytically active component.
  • Catalysts for use in the hydrogenation stage typically comprise a refractory metal oxide or silicate as a carrier.
  • Suitable carrier materials include silica, alumina, silica-alumina, zirconia, titania and mixtures thereof.
  • Preferred carrier materials for inclusion in the catalyst for use in the process of this invention are silica, alumina, silica-alumina, and diatomaceous earth (kieselguhr).
  • the catalyst may comprise the catalytically active component in an amount of from 0.05 to 80 parts by weight, preferably from 0.1 to 70 parts by weight, per 100 parts by weight of carrier material.
  • the amount of catalytically active metal present in the catalyst will vary according to the specific metal concerned.
  • One particularly suitable catalyst for use in the hydrogenation stage comprises nickel in an amount in the range of from 30 to 70 parts by weight per 100 parts by weight of carrier material.
  • a second particularly suitable catalyst comprises platinum in an amount in the range of from 0.05 to 2.0 parts by weight per 100 parts by weight of carrier material.
  • Suitable catalysts for use in the hydrogenation stage of the process of this invention are available commercially, or may be prepared by methods well known in the art, for example the methods discussed hereinbefore with reference to the preparation of the hydrocarbon synthesis catalyst.
  • the hydrocarbon wax is contacted with hydrogen at elevated temperature and pressure.
  • the operating temperature may typically range from 100 to 300 °C, more preferably from 150 to 275 °C, in particular from 175 to 250 °C.
  • the operating pressure ranges from 5 to 150 bars, preferably from 10 to 50 bars.
  • Hydrogen may be supplied to the hydrogenation stage at a gas hourly space velocity in the range of from 100 to 10000 Nl/l/hr, more preferably from 250 to 5000 Nl/l/hr.
  • the hydrocarbon wax being treated is typically supplied to the hydrogenation stage at a weight hourly space velocity in the range of from 0.1 to 5 kg/l/hr, more preferably from 0.25 to 2.5 kg/l/hr.
  • the ratio of hydrogen to hydrocarbon wax may range from 100 to 5000 Nl/kg and is preferably from 250 to 3000 Nl/kg.
  • the hydrogenation stage is operated under conditions such that substantially no isomerisation or hydrocracking of the feed occurs.
  • the precise operating conditions required to achieve the desired degree of hydrogenation without substantial hydrocracking or hydroisomerisation occurring will vary according to the composition of the hydrocarbon wax being fed to the hydrogenation stage and the particular catalyst being employed.
  • the degree of conversion of the feed hydrocarbon may be determined. In this respect, conversion, in percent, is defined as the percent weight of the fraction of the feed boiling above 370 °C which is converted during the hydrogenation to a fraction boiling below 370 °C.
  • the conversion of the hydrogenation stage is below 10%, preferably below 8%, more preferably below 5%.
  • the hydrocarbon product leaving the hydrogenation stage substantially consists of high molecular weight, paraffinic hydrocarbons having a boiling point range within and above that of lubricating base oils.
  • Lubricating base oils typically have a 5% by weight boiling point of at least 330 °C, preferably at least 370 °C.
  • the boiling point range of lubricating base oils may range up to 650 °C, preferably up to 600 °C. It will be appreciated that the above boiling points and boiling point ranges refer to boiling point (ranges) at atmospheric pressure. At least a part of this hydrocarbon product is subjected to the hydroconversion step of the process of this invention, to yield the waxy raffinate.
  • the entire effluent of the hydrogenation stage may be led directly to the hydroconversion stage.
  • the separation may be conveniently achieved using distillation techniques well known in the art. At least a part of the remaining C 5 + fraction of the hydrocarbon product is then used as feed for the hydroconversion stage.
  • waxy raffinate is prepared from the hydrocarbon product of the hydrogenation stage by hydrocracking and hydroisomerising the product with hydrogen in the presence of a suitable catalyst.
  • the catalyst comprises as catalytically active component one or more metals selected from Groups VIB and VIII of the Periodic Table of Elements, in particular one or more metals selected from molybdenum, tungsten, cobalt, nickel, ruthenium, iridium, osmium, platinum and palladium.
  • the catalyst comprises one or more metals selected from nickel, platinum and palladium as the catalytically active component. Catalysts comprising platinum as the catalytically active component have been found to be particularly suitable for use in the hydroconversion stage.
  • Catalysts for use in the hydroconversion stage typically comprise a refractory metal oxide as a carrier.
  • Suitable carrier materials include silica, alumina, silica-alumina, zirconia, titania and mixtures thereof.
  • Preferred carrier materials for inclusion in the catalyst for use in the process of this invention are silica, alumina and silica-alumina.
  • a particularly preferred catalyst comprises platinum supported on a silica-alumina carrier.
  • the acidity of the catalyst carrier may be enhanced by applying a halogen moiety, in particular fluorine, or a phosphorous moiety to the carrier. This may be especially preferred if the catalyst carrier itself is not acidic, for example if the catalyst carrier contains alumina or silica.
  • the catalyst may comprise the catalytically active component in an amount of from 0.05 to 80 parts by weight, preferably from 0.1 to 70 parts by weight, per 100 parts by weight of carrier material.
  • the amount of catalytically active metal present in the catalyst will vary according to the specific metal concerned.
  • a particularly preferred catalyst for use in the hydroconversion stage comprises platinum in an amount in the range of from 0.05 to 2 parts by weight, more preferably from 0.1 to 1 parts by weight, per 100 parts by weight of carrier material.
  • Suitable catalysts for use in the hydroconversion stage of the process of this invention are available commercially, or may be prepared by methods well known in the art, for example the methods discussed hereinbefore with reference to the preparation of the hydrocarbon synthesis catalyst.
  • the hydrocarbon product of the hydrogenation stage is contacted with hydrogen in the presence of the catalyst at elevated temperature and pressure.
  • the temperatures necessary to yield the waxy raffinate will lie in the range of from 175 to 380 °C, preferably from 250 to 350 °C, more preferably from 250 to 330 °C.
  • the pressure typically applied ranges from 10 to 250 bars, more preferably from 25 to 250 bars.
  • Hydrogen may be supplied at a gas hourly space velocity of from 100 to 10000 Nl/l/hr, preferably from 500 to 5000 Nl/l/hr.
  • the hydrocarbon feed may be provided at a weight hourly space velocity of from 0.1 to 5 kg/l/hr, preferably from 0.25 to 2 kg/l/hr.
  • the ratio of hydrogen to hydrocarbon feed may range from 100 to 5000 Nl/kg and is preferably from 250 to 2500 Nl/kg.
  • the degree of hydrocracking and isomerisation occurring in the hydroconversion stage may be measured by determining the degree of conversion of the fraction boiling above 370 °C, as hereinbefore defined.
  • the hydroconversion stage is operated at a conversion of at least 20%, preferably at least 25%, but preferably not more than 50%, more preferably not more than 45%.
  • the hydrogen required for the operation of both the hydrogenation and the hydroconversion stages may be generated by processes well known in the art, for example by the steam reforming of a refinery fuel gas.
  • the waxy raffinate is then subjected to a pour point reducing treatment to reduce the pour point to at least -12 °C, preferably at least -18 °C, more preferably at least -24 °C.
  • Pour point reducing treatments are well known to those skilled in the art and include solvent dewaxing, catalytic dewaxing, (hydro) isomerisation (dewaxing) and/or addition of pour point depressing agents.
  • solvent dewaxing catalytic dewaxing
  • hydro isomerisation
  • pour point depressing agents addition of pour point depressing agents.
  • the latter treatment is generally not preferred in the preparation of lubricating base oils as additives contained in a base oil may deteriorate rather quickly and blending of different base oils and additive packages to prepare a finished base oil may become a problem.
  • Catalytic dewaxing is well known to those skilled in the art. In a catalytic dewaxing process straight chain paraffins and slightly branched paraffins are cracked to products boiling below the lubricating base oil boiling point range. However, the catalysts which are employed are not fully selective to wax molecules only. In fact also branched paraffins having a very high VI and a sufficiently low pour point are cracked to lower boiling products. Thus, cracking of those compounds to products boiling below the lubricating base oil range results in lubricating base oils having a lower VI than lubricating base oils which have been prepared by a solvent dewaxing process. Further, as compared with solvent dewaxing, lubricating base oils are prepared in lower yield. Nevertheless, catalytic dewaxing is being applied commercially as generally the operation of the process is cheaper than operation of a solvent dewaxing process.
  • Catalysts which can be used in a catalytic dewaxing process include zeolites having a constraint index from 1 to 12, in particular of the MFI structure type, such as ZSM-5, -11, -22, -23, -35 as well as Ferrierite and composite crystalline silicates described in European patent application Nos. 0 100 115, 0 178 699 and 0 380 180.
  • Another suitable catalytic dewaxing catalyst comprises mordenite. If desired, waxy raffinate feed can be separated into various fractions and the various fraction can then be treated separately using different dewaxing catalysts, as disclosed in European patent application No. 0 237 655 and also European patent application No. 0 161 833.
  • the catalysts typically contain at least one catalytically active metal chosen from Groups VIb, VIIb and VIII of the Periodic Table of the Elements.
  • the catalytic dewaxing process is typically carried out at a temperature from 200 °C to 500 °C, a hydrogen pressure from 5 to 100 bar, a space velocity from 0.1 to 5 kg/l/h and a hydrogen/oil ratio from 100 to 2500 Nl/kg.
  • Solvent dewaxing is well known to those skilled in the art and involves admixture of one or more solvents and/or wax precipitating agents with waxy raffinate and cooling the mixture to a temperature in the range of from -10 °C to -40 °C, preferably in the range of from -20 °C to -35 °C, to separate the wax from the oil.
  • the oil containing the wax is usually filtered through a filter cloth which can be made of textile fibres, such as cotton; porous metal cloth; or cloth made of synthetic materials.
  • the solvents may be recovered from the wax and the lubricating base oil by filtration and recirculation of the solvents into the process. It will be appreciated that although solvents are recirculated the process is still rather expensive as a large amount of solvents is required and cooling of the waxy raffinate/solvent mixture requires much energy.
  • the wax that is separated in the solvent dewaxing process may be recycled to the hydroconversion stage, or alternatively, may be sent to a hydroisomerisation stage if for example, the pour point reducing treatment involves both a solvent dewaxing stage and a hydroisomerisation stage.
  • the wax may be subjected to a deoiling treatment prior to recycling. Another possibility is to fractionate the wax and sell one or more of the fractions on the wax market. Fractionation is typically effected using short path distillation.
  • a very suitable pour point reducing treatment comprises a hydroisomerisation treatment, in the art sometimes referred to as isomerisation dewaxing or iso-dewaxing.
  • the hydroisomerisation treatment typically comprises contacting the waxy raffinate with hydrogen in the presence of a hydroisomerisation catalyst.
  • the hydroisomerisation treatment is cheaper to operate and the hydroisomerisation treatment does substantially not suffer from the disadvantages of catalytic dewaxing, that is a lower VI and a lower yield as compared with solvent dewaxing.
  • a hydroisomerisation catalyst having a high activity for catalysing hydroisomerisation reactions, but a low activity for catalysing hydrocracking reactions. It has been found that in order to achieve this the acidity of the catalyst, as expressed by the alpha value, should be below 20.
  • the catalyst comprises a molecular sieve.
  • the hydroisomerisation catalyst comprises a molecular sieve having an alpha value below 20, more preferably below 10, even more preferably below 5.
  • the experimental conditions of the alpha test to be used to determine the alpha values referred to in this specification include a constant temperature of 538 °C and a variable flow rate as described in detail in J. Catalysis, 61, 395 (1980).
  • the molecular sieve operating in hydroisomerisation duty is a zeolite, preferably having a silica/alumina molar ratio of at least 10, more preferably at least 30.
  • a zeolite having a high silica/alumina ratio generally has a lower acidity than a zeolite having a low silica/alumina ratio.
  • a high silica/alumina ratio may be obtained by synthesis of the zeolite at a high silica/alumina ratio and/or by a dealumination treatment such as steaming. Both methods are well known to those skilled in the art.
  • framework aluminium may be replaced by another trivalent element such as boron which results in a lower level of acidity.
  • the molecular sieve is chosen from the group of ZSM-12, mordenite and zeolite beta, more preferably zeolite beta.
  • the low acidity forms of zeolite beta may be obtained by synthesis of a highly siliceous form of the zeolite, e.g. with a silica/alumina ratio above 50 or by steaming zeolites of lower silica-alumina ratio to the requisite acidity level.
  • Another method is by replacement of a portion of the framework aluminium of the zeolite with another trivalent element such as boron.
  • the zeolite contains framework boron, typically at least 0.1% by weight, preferably, at least 0.5% by weight.
  • the zeolite also may contain material in the pores of the structure which do not form part of the framework constituting the characteristic structure of the zeolite.
  • framework boron refers to boron that is actually present in the framework of the zeolite. As opposed to material present in the pores of the zeolite, framework boron contributes to the ion exchange capacity of the zeolite.
  • zeolite beta to be used in the process of the present invention contains at least 0.1% by weight.
  • the boron content will usually be not more than 5% by weight, preferably not more than 2% by weight.
  • the silica/alumina ratio of the as-synthesized zeolite is typically below 30.
  • the boron containing zeolite is steamed to reduce the alpha value to not more than 10, preferably not more than 5. Typical steaming conditions are known and have been described in European patent application No. 0 464 547.
  • the zeolite will usually be composited with a matrix material (binder) to form the finished catalyst.
  • a matrix material binder
  • Non-acidic refractory oxide binder materials like silica, titania or alumina are preferred. Silica is especially preferred.
  • the zeolite is usually composited with the matrix in amounts from 20 to 80% by weight, preferably from 50 to 80% by weight. Methods for extruding zeolite with the binder are known to those skilled in the art.
  • the molecular sieve is an aluminophosphate.
  • Aluminophosphates are well known in the art and have been described in, for example, United States patent Nos. 4 310 440, 4 440 871, 4 567 029, and 4 793 984.
  • Aluminophosphates have the advantage of an intrinsically lower acidity as compared with zeolites.
  • aluminophosphates are to be understood as reference to the class of aluminophosphates, that is including metallo-aluminophosphates, silico-aluminophosphates, metallo-silico-aluminophosphates as well as non-metal substituted aluminophosphates and silico-aluminophosphates.
  • the molecular sieve has at least some intrinsic acidity and therefore the aluminophosphate is chosen from the group of metallo-aluminophosphates, wherein the further metal present in the framework of the aluminophosphate is not a trivalent metal, silico-aluminophosphates or metallo-silico-aluminophosphates.
  • the aluminophosphate is a silico-aluminophosphate.
  • the process is preferably carried out with a hydroisomerisation catalyst comprising an aluminophosphate, in particular a silico-aluminophosphate, chosen from the group of structure types 11, 31 and 41, more preferably structure type 11. Silico-aluminophosphates of structure types 11, 31 and 41 have been described in international patent application No. WO 90/09362.
  • the hydroisomerisation catalyst comprises a silico-aluminophosphate of structure type 11, and having a special silica/alumina distribution over the crystalline particle.
  • the silico-aluminophosphate molecular sieve is characterised by an X-ray diffraction pattern according to Table I.
  • X-ray powder diffraction patterns can be determined by standard techniques, using K-alpha/doublet copper radiation.
  • the silico-aluminophosphate is further characterised by a P 2 O 5 to alumina molar ratio at the surface of 0.80 or less and a P 2 O 5 to alumina ratio of the bulk of the silico-aluminophosphate is 0.96 or greater, and the silica to alumina mole ratio at the surface is greater than in the bulk of the silico-aluminophosphate.
  • This silico-aluminophosphate is known in the art as SM-3. Preparation of SM-3 has been disclosed in international patent application No. WO 91/13132.
  • the isomerisation catalyst comprises an inorganic, non-layered, porous, crystalline phase material as described in international patent application No. WO 93/02161.
  • the hydroisomerisation catalyst typically comprises a catalytically active metal having hydrogenation/dehydrogenation activity, such as those of Groups VIb and VIII.
  • the hydroisomerisation catalyst comprises a Group VIII metal, in particular a Group VIII noble metal such as platinum and/or palladium.
  • Means for incorporating the metal into the catalyst carrier, comprising a molecular sieve as described hereinbefore, are well known to those skilled in the art and have been described hereinbefore.
  • the amount of noble metal is typically in the range of from 0.5 to 5% by weight of the total catalyst, preferably in the range of from 0.5 to 2% by weight.
  • the waxy raffinate is contacted with hydrogen in the presence of a catalyst as described hereinabove at elevated temperature and pressure.
  • the temperatures necessary to yield the lubricating base oil will lie in the range of from 175 to 380 °C, preferably from 200 to 350 °C.
  • the pressure typically applied ranges from 10 to 250 bars, more preferably from 25 to 250 bars.
  • the waxy raffinate may be provided at a weight hourly space velocity of from 0.1 to 20 kg/l/hr, preferably from 0.1 to 5 kg/l/hr.
  • the finished lubricating base oil preferably has a pour point of less than -15 °C, more preferably less than -20 °C and a VI of more than 135, preferably more than 140.

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Claims (29)

  1. Procédé de préparation d'huiles de base lubrifiantes consistant à soumettre un raffinat cireux à un traitement de réduction du point d'écoulement et à récupérer une huile de base lubrifiante de celui-ci, lequel raffinat cireux a été préparé par la mise en contact d'un produit hydrocarboné avec de l'hydrogène en présence d'un catalyseur d'hydroconversion, comprenant un métal catalytiquement actif ayant une activité d'hydrogénation/déshydrogénation fixé sur un support d'oxyde réfractaire, sous des conditions telles qu'un hydrocraquage et une hydroisomérisation du produit hydrocarboné se produisent pour donner le raffinat cireux, dans lequel le produit hydrocarboné a été préparé par:
    (a) la mise en contact d'un mélange de monoxyde de carbone et d'hydrogène avec un catalyseur de synthèse d'hydrocarbure à température et pression élevées pour préparer une cire hydrocarbonée essentiellement paraffinique; et
    (b) la mise en contact de la cire hydrocarbonée ainsi obtenue avec de l'hydrogène en présence d'un catalyseur d'hydrogénation à une température entre 100 et 300°C et sous des conditions telles que la fraction en pour-cent en poids de l'alimentation bouillant au-dessus de 370°C qui est convertie en une fraction bouillant en dessous de 370°C est en dessous de 10% pour donner le produit hydrocarboné.
  2. Procédé suivant la revendication 1, caractérisé en ce que le mélange de monoxyde de carbone et d'hydrogène en contact avec le catalyseur dans l'étape (a) a un rapport hydrogène/monoxyde de carbone inférieur à 2,5, avantageusement inférieur à 1,75, plus avantageusement de 0,4 à 1,5.
  3. Procédé suivant l'une ou l'autre des revendications 1 et 2, caractérisé en ce que le catalyseur de synthèse d'hydrocarbure dans l'étape (a) comprend du ruthénium, du fer, du nickel ou du cobalt, comme métal catalytiquement actif, avantageusement du cobalt.
  4. Procédé suivant l'une quelconque des revendications précéentes, caractérisé en ce que le catalyseur de synthèse d'hydrocarbure dans l'étape (a) comprend un support, avantageusement choisi parmi la silice, l'alumine, l'oxyde de titane, la zircone et leurs mélanges, plus avantageusement la silice ou l'alumine.
  5. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le catalyseur de synthèse d'hydroarbure dans l'étape (a) comprend comme promoteur un oxyde d'un métal choisi dans le Groupe IVB du Tableau Périodique des Eléments, avantaeusement le titane ou le zirconium.
  6. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le mélange de monoxyde de carbone et d'hydrogène est mis en contact avec le catalyseur dans l'étape (a) à une température de 175 à 250°C.
  7. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le mélange de monoxyde de carbone et d'hydrogène est mis en contact avec le catalyseur dans l'étape (a) à une pression de 12 à 50 bars.
  8. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le catalyseur d'hydrogénation de l'étape (b) comprend du molybdène, du tungstène, du cobalt, du nickel, du ruthénium, de l'iridium, de l'osmium, du platine ou du palladium comme métal catalytiquement actif, avantageusement un ou plusieurs métaux choisis parmi le nickel, le platine et le palladium.
  9. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le catalyseur d'hydrogénation de l'étape (b) comprend un support, avantageusement choisi parmi la silice, l'alumine, la silice-alumine, l'oxyde de titane, la zircone et leurs mélanges, avantageusement la silice, l'alumine ou la silice-alumine.
  10. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que dans l'étape (b), le produit hydrocarboné est mis en contact avec le catalyseur d'hydrogénation à une température de 150 à 275°C.
  11. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que dans l'étape (b), le produit hydrocarboné est mis en contact avec le catalyseur d'hydrogénation à une pression de 10 à 50 bars.
  12. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que dans l'étape (b), l'hydrogène est amené à une vitesse spatiale horaire gazeuse de 100 à 10000 Nl/l/h, avantageusement de 250 à 5000 Nl/l/h.
  13. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que dans l'étape (b), la fraction en pour-cent en poids de l'alimentation bouillant au-dessus de 370°C qui est convertie en une fraction bouillant en dessous de 370°C est inférieure à 5%.
  14. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le catalyseur d'hydroconversion comrend du molybdène, du tungstène, du cobalt, du nickel, du ruthénium, de l'iridium, de l'osmium, du platine ou du palladium comme métal catalyiquement actif, avantageusement un ou plusieurs métaux choisis parmi le nickel, le platine et le palladium.
  15. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le catalyseur d'hydroconversion comprend un support, avantageusement choisi parmi la silice, l'alumine, la silice-alumine, l'oxyde de titane, la zircone et leurs mélanges, avantaeusement la silice, l'alumine ou la silice-alumine.
  16. Procédé suivant la revendication 15, caractérisé en ce que le catalyseur d'hydroconversion comprend un support contenant de l'halogène.
  17. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le produit hydrocarboné est mis en contact avec le catalyseur d'hydroconversion à une température de 175 à 380°C, avantageusement de 250 à 350°C.
  18. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le produit hydrocarboné est mis en contact avec le catalyseur d'hydroconversion à une pression de 10 à 250 bars, avantageusement de 25 à 250 bars.
  19. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que dans l'étape d'hydroconversion, l'hydrogène est amené à une vitesse spatiale horaire gazeuse de 100 à 10000 Nl/l/h, avantageusement de 500 à 5000 Nl/l/h.
  20. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que dans l'étape d'hydroconversion, la fraction en pour-cent en poids de l'alimentation bouillant au-dessus de 370°C qui est convertie en une fraction bouillant en dessous de 370°C est d'au moins 20%.
  21. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le traitement de réduction du point d'écoulement comprend la mise en contact du raffinat cireux avec de l'hydrogène en présence d'un catalyseur d'hydroisomérisation.
  22. Procédé suivant la revendication 21, caractérisé en ce que le catalyseur d'hydroisomérisation comprend un tamis moléculaire et le catalyseur a une valeur alpha en dessous de 20, avantageusement en dessous de 10.
  23. Procédé suivant la revendication 22, caractérisé en ce que le tamis moléculaire est une zéolite, avantageusement ayant un rapport molaire silice/alumine d'au moins 10.
  24. Procédé suivant l'une et l'autre des revendications 22 et 23, caractérisé en ce que le tamis moléculaire est choisi dans le groupe comprenant la ZSM-12, la mordénite et la zéolite bêta, avantageusement le zéolite bêta.
  25. Procédé suivant la revendication 22, caractérisé en ce que le tamis moléculaire est un aluminophosphate.
  26. Procédé suivant la revendication 25, caractérisé en ce que l'aluminophosphate est un silicoaluminophosphate.
  27. Procédé suivant l'une et l'autre des revendications 25 et 26, caractérisé en ce que l'aluminophosphate est choisi dans le groupe comprenant les types de structure 11, 31 et 41, avantageusement le type de structure 11.
  28. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le catalyseur d'hydroisomérisation comprend un métal catalytiquement actif choisi dans les Groupes VIB et/ou VIII du Tableau Périodique des Eléments, avantageusement un ou plusieurs métaux nobles du Groupe VIII.
  29. Procédé suivant l'une quelconque des revendications précédentes, caractérisé en ce que le traitement de réduction du point d'écoulement comprend un traitement de déparaffinage au solvant ou un traitement de déparaffinage catalytique.
EP19950200281 1994-02-08 1995-02-06 Procédé de préparation d'une huile lubrifiante de base Revoked EP0668342B1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6669743B2 (en) 1997-02-07 2003-12-30 Exxonmobil Research And Engineering Company Synthetic jet fuel and process for its production (law724)
WO2004033595A1 (fr) 2002-10-08 2004-04-22 Exxonmobil Research And Engineering Company Huile lubrifiante lourde formee a partir de cire fischer-tropsch
EP1272592B1 (fr) * 2000-04-04 2004-09-29 ExxonMobil Research and Engineering Company Procede pour adapter la durete de la cire de fischer-tropsch par malaxage
US6846778B2 (en) 2002-10-08 2005-01-25 Exxonmobil Research And Engineering Company Synthetic isoparaffinic premium heavy lubricant base stock
EP1626080A2 (fr) 2001-03-05 2006-02-15 Shell Internationale Researchmaatschappij B.V. Composition de fluide hydraulique
US7018525B2 (en) 2003-10-14 2006-03-28 Chevron U.S.A. Inc. Processes for producing lubricant base oils with optimized branching
EP1686164A2 (fr) 2002-02-25 2006-08-02 Shell Internationale Researchmaatschappij B.V. Gazole ou composant de mélange de gazole
US7132042B2 (en) 2002-10-08 2006-11-07 Exxonmobil Research And Engineering Company Production of fuels and lube oils from fischer-tropsch wax
WO2006132964A2 (fr) 2005-06-03 2006-12-14 Exxonmobil Research And Engineering Company Detergents sans cendre et huile lubrifiante formulee les contenant
US7201838B2 (en) 2002-10-08 2007-04-10 Exxonmobil Research And Engineering Company Oxygenate treatment of dewaxing catalyst for greater yield of dewaxed product
WO2007050352A1 (fr) 2005-10-21 2007-05-03 Exxonmobil Research And Engineering Company Huiles de lubrification ameliorees destinees a des moteurs a deux temps
US7252753B2 (en) 2004-12-01 2007-08-07 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
WO2007133554A2 (fr) 2006-05-09 2007-11-22 Exxonmobil Research And Engineering Company Composition d'huile de graissage
WO2008002425A1 (fr) 2006-06-23 2008-01-03 Exxonmobil Research And Engineering Company Compositions lubrifiantes
US7335802B2 (en) 2003-10-15 2008-02-26 Shell Oil Company Methods of preparing branched aliphatic alcohols
US7344631B2 (en) 2002-10-08 2008-03-18 Exxonmobil Research And Engineering Company Oxygenate treatment of dewaxing catalyst for greater yield of dewaxed product
US7510674B2 (en) 2004-12-01 2009-03-31 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
EP1268712B2 (fr) † 2000-04-04 2009-06-10 ExxonMobil Research and Engineering Company Procede d'adoucissement de cires de fischer-tropsch par hydrotraitement doux
US7655605B2 (en) 2005-03-11 2010-02-02 Chevron U.S.A. Inc. Processes for producing extra light hydrocarbon liquids
US7763161B2 (en) 2003-12-23 2010-07-27 Chevron U.S.A. Inc. Process for making lubricating base oils with high ratio of monocycloparaffins to multicycloparaffins
WO2012143550A1 (fr) 2011-04-21 2012-10-26 Shell Internationale Research Maatschappij B.V. Procédé de transformation d'un matériau de biomasse solide
EP2746367A1 (fr) 2012-12-18 2014-06-25 Shell Internationale Research Maatschappij B.V. Procédé pour préparer une huile de base et du gazole
US10364403B2 (en) 2013-11-06 2019-07-30 Chevron Oronite Technology B.V. Marine diesel cylinder lubricant oil compositions
US10669506B2 (en) 2013-11-06 2020-06-02 Chevron Oronite Technology B.V. Marine diesel cylinder lubricant oil compositions

Families Citing this family (204)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0782608A4 (fr) * 1994-09-08 1998-08-05 Mobil Oil Corp Procede d'hydro-isomerisation de la cire
US6296757B1 (en) 1995-10-17 2001-10-02 Exxon Research And Engineering Company Synthetic diesel fuel and process for its production
US5689031A (en) 1995-10-17 1997-11-18 Exxon Research & Engineering Company Synthetic diesel fuel and process for its production
EP1365005B1 (fr) * 1995-11-28 2005-10-19 Shell Internationale Researchmaatschappij B.V. Procédé pour la production d'huiles lubrifiantes
DZ2129A1 (fr) * 1995-11-28 2002-07-23 Shell Int Research Procédé pour produire des huiles lubrifiantes de base.
CA2237068C (fr) † 1995-12-08 2005-07-26 Exxon Research And Engineering Company Huiles de base hydrocarbonees biodegradables et extremement efficaces
US6475960B1 (en) 1998-09-04 2002-11-05 Exxonmobil Research And Engineering Co. Premium synthetic lubricants
US6165949A (en) * 1998-09-04 2000-12-26 Exxon Research And Engineering Company Premium wear resistant lubricant
US6080301A (en) 1998-09-04 2000-06-27 Exxonmobil Research And Engineering Company Premium synthetic lubricant base stock having at least 95% non-cyclic isoparaffins
US6179994B1 (en) * 1998-09-04 2001-01-30 Exxon Research And Engineering Company Isoparaffinic base stocks by dewaxing fischer-tropsch wax hydroisomerate over Pt/H-mordenite
US6332974B1 (en) 1998-09-11 2001-12-25 Exxon Research And Engineering Co. Wide-cut synthetic isoparaffinic lubricating oils
WO2001007538A1 (fr) * 1999-07-26 2001-02-01 Shell Internationale Research Maatschappij B.V. Procede de preparation d'huile minerale lubrifiante
US6497812B1 (en) 1999-12-22 2002-12-24 Chevron U.S.A. Inc. Conversion of C1-C3 alkanes and fischer-tropsch products to normal alpha olefins and other liquid hydrocarbons
US6773578B1 (en) 2000-12-05 2004-08-10 Chevron U.S.A. Inc. Process for preparing lubes with high viscosity index values
US6635171B2 (en) 2001-01-11 2003-10-21 Chevron U.S.A. Inc. Process for upgrading of Fischer-Tropsch products
AU2002249198B2 (en) 2001-02-13 2006-10-12 Shell Internationale Research Maatschappij B.V. Lubricant composition
AR032941A1 (es) 2001-03-05 2003-12-03 Shell Int Research Un procedimiento para preparar un aceite base lubricante y aceite base obtenido, con sus diversas utilizaciones
AR032930A1 (es) 2001-03-05 2003-12-03 Shell Int Research Procedimiento para preparar un aceite de base lubricante y gas oil
DE10126516A1 (de) 2001-05-30 2002-12-05 Schuemann Sasol Gmbh Verfahren zur Herstellung von mikrokristallinen Paraffinen
US6709569B2 (en) 2001-12-21 2004-03-23 Chevron U.S.A. Inc. Methods for pre-conditioning fischer-tropsch light products preceding upgrading
DE10256431A1 (de) * 2002-05-31 2004-01-15 SCHÜMANN SASOL GmbH Mikrokristallines Paraffin, Verfahren zur Herstellung von mikrokristallinen Paraffine und Verwendung der mikrokristallinen Paraffine
EP1666569B1 (fr) 2002-07-12 2018-12-26 Shell International Research Maatschappij B.V. Composition lubrifiante et son utilisation
AU2003255058A1 (en) 2002-07-18 2004-02-09 Shell Internationale Research Maatschappij B.V. Process to prepare a microcrystalline wax and a middle distillate fuel
WO2004009699A1 (fr) 2002-07-19 2004-01-29 Shell Internationale Research Maatschappij B.V. Composition comprenant un caoutchouc ethylene-propylene-diene (epdm) et de l'huile paraffinique
AU2003250109A1 (en) 2002-07-19 2004-02-09 Shell Internationale Research Maatschappij B.V. Silicon rubber comprising an extender oil and process to prepare said extender oil
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BRPI0408151A (pt) * 2003-03-10 2006-03-01 Shell Int Research composição lubrificante
US20080028680A1 (en) 2003-04-15 2008-02-07 Wouter Detlof Berggren Process to Prepare Synthesis Gas
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US7727378B2 (en) 2003-07-04 2010-06-01 Shell Oil Company Process to prepare a Fischer-Tropsch product
EP1548088A1 (fr) 2003-12-23 2005-06-29 Shell Internationale Researchmaatschappij B.V. Procédé de préparation d'une huile de base non-trouble
US7195706B2 (en) 2003-12-23 2007-03-27 Chevron U.S.A. Inc. Finished lubricating comprising lubricating base oil with high monocycloparaffins and low multicycloparaffins
US7282134B2 (en) 2003-12-23 2007-10-16 Chevron Usa, Inc. Process for manufacturing lubricating base oil with high monocycloparaffins and low multicycloparaffins
US7083713B2 (en) 2003-12-23 2006-08-01 Chevron U.S.A. Inc. Composition of lubricating base oil with high monocycloparaffins and low multicycloparaffins
AU2005254733B2 (en) 2004-06-18 2008-05-29 Shell Internationale Research Maatschappij B.V. Lubricating oil composition
US7345211B2 (en) 2004-07-08 2008-03-18 Conocophillips Company Synthetic hydrocarbon products
WO2006037805A2 (fr) 2004-10-08 2006-04-13 Shell Internationale Research Maatschappij B.V. Procede de preparation d'olefines inferieures d'une matiere de base contenant du carbone
CN101068907A (zh) 2004-11-18 2007-11-07 国际壳牌研究有限公司 制备基油的方法
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US7550415B2 (en) 2004-12-10 2009-06-23 Shell Oil Company Lubricating oil composition
WO2006067104A1 (fr) 2004-12-20 2006-06-29 Shell Internationale Research Maatschappij B.V. Craquage de l'essence
US7837853B2 (en) 2005-04-11 2010-11-23 Shell Oil Company Process to blend a mineral and a Fischer-Tropsch derived product onboard a marine vessel
WO2006122585A1 (fr) 2005-05-19 2006-11-23 Shell Internationale Research Maatschappij B.V. Liquide de trempe
WO2006122979A2 (fr) 2005-05-20 2006-11-23 Shell Internationale Research Maatschappij B.V. Utilisation d'huile blanche obtenue par procede fischer-tropsch dans des applications de contact alimentaire
TR201908546T4 (tr) 2005-06-23 2019-07-22 Shell Int Research Elektriksel yağ formülasyonu.
EP1927643A4 (fr) * 2005-09-22 2015-05-27 Japan Oil Gas & Metals Jogmec Procede d'hydrogenation
WO2007096361A1 (fr) 2006-02-21 2007-08-30 Shell Internationale Research Maatschappij B.V. Composition d'huile lubrifiante
US8747650B2 (en) 2006-12-21 2014-06-10 Chevron Oronite Technology B.V. Engine lubricant with enhanced thermal stability
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EP2072610A1 (fr) 2007-12-11 2009-06-24 Shell Internationale Research Maatschappij B.V. Composition d'huile support
WO2009080673A2 (fr) 2007-12-20 2009-07-02 Shell Internationale Research Maatschappij B.V. Compositions de carburant
WO2009080672A1 (fr) 2007-12-20 2009-07-02 Shell Internationale Research Maatschappij B.V. Compositions de caburant
EP2078743A1 (fr) 2008-01-10 2009-07-15 Shell Internationale Researchmaatschappij B.V. Composition de carburant
AR070686A1 (es) 2008-01-16 2010-04-28 Shell Int Research Un metodo para preparar una composicion de lubricante
CN105154177A (zh) 2008-06-19 2015-12-16 国际壳牌研究有限公司 润滑脂组合物
RU2499036C2 (ru) 2008-06-24 2013-11-20 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Применение смазочной композиции
US20100024286A1 (en) 2008-07-31 2010-02-04 Smith Susan Jane Liquid fuel compositions
EP2100946A1 (fr) 2008-09-08 2009-09-16 Shell Internationale Researchmaatschappij B.V. Formules de pétrole
US20100162693A1 (en) 2008-12-31 2010-07-01 Michael Paul W Method of reducing torque ripple in hydraulic motors
EP2382290A1 (fr) 2009-01-28 2011-11-02 Shell Internationale Research Maatschappij B.V. Composition lubrifiante
EP2186871A1 (fr) 2009-02-11 2010-05-19 Shell Internationale Research Maatschappij B.V. Composition de lubrification
EP2398872B1 (fr) 2009-02-18 2013-11-13 Shell Internationale Research Maatschappij B.V. Utilisation d'une composition lubrifiante avec de l'huile de base gtl pour réduire les émissions d'hydrocarbure
EP2248878A1 (fr) 2009-05-01 2010-11-10 Shell Internationale Research Maatschappij B.V. Composition de lubrification
PL2432752T3 (pl) 2009-05-20 2019-07-31 Shell Internationale Research Maatschappij B.V. Produkt z cementu siarkowego
CN102803446A (zh) 2009-06-24 2012-11-28 国际壳牌研究有限公司 润滑组合物
WO2010149712A1 (fr) 2009-06-25 2010-12-29 Shell Internationale Research Maatschappij B.V. Composition lubrifiante
CN102575189B (zh) 2009-08-18 2016-10-19 国际壳牌研究有限公司 润滑脂组合物
EP2298855A1 (fr) 2009-08-27 2011-03-23 Castrol Limited Procédé pour lubrifier un moteur diesel avec une composition lubrifiante comprenant polyisobutylene
WO2011023766A1 (fr) 2009-08-28 2011-03-03 Shell Internationale Research Maatschappij B.V. Composition d’huile de traitement
US8349776B2 (en) 2009-09-29 2013-01-08 Chevron Oronite Company Llc Trunk piston engine lubricating oil compositions
WO2011042552A1 (fr) 2009-10-09 2011-04-14 Shell Internationale Research Maatschappij B.V. Composition lubrifiante
EP2159275A3 (fr) 2009-10-14 2010-04-28 Shell Internationale Research Maatschappij B.V. Composition de lubrification
US20120214719A1 (en) 2009-10-26 2012-08-23 Jose Luis Garcia Ojeda Lubricating composition
EP2189515A1 (fr) 2009-11-05 2010-05-26 Shell Internationale Research Maatschappij B.V. Composition liquide fonctionnelle
EP2186872A1 (fr) 2009-12-16 2010-05-19 Shell Internationale Research Maatschappij B.V. Composition de lubrification
PH12012501309A1 (en) 2009-12-24 2013-01-21 Shell Internationalale Res Maatschappij B V Liquid fuel compositions
US20130000584A1 (en) 2009-12-29 2013-01-03 Shell International Research Maatschappij B.V. Liquid fuel compositions
WO2011110551A1 (fr) 2010-03-10 2011-09-15 Shell Internationale Research Maatschappij B.V. Procédé de réduction de la toxicité de compositions lubrifiantes usagées
WO2011113851A1 (fr) 2010-03-17 2011-09-22 Shell Internationale Research Maatschappij B.V. Composition de lubrification
EP2194114A3 (fr) 2010-03-19 2010-10-27 Shell Internationale Research Maatschappij B.V. Schmiermittelzusammensetzung
EP2385097A1 (fr) 2010-05-03 2011-11-09 Shell Internationale Research Maatschappij B.V. Composition lubrifiante
CN102869755A (zh) 2010-05-03 2013-01-09 国际壳牌研究有限公司 用过的润滑组合物
WO2012004198A1 (fr) 2010-07-05 2012-01-12 Shell Internationale Research Maatschappij B.V. Procédé pour la fabrication d'une composition de graisse
WO2012017023A1 (fr) 2010-08-03 2012-02-09 Shell Internationale Research Maatschappij B.V. Composition lubrifiante
EP2441818A1 (fr) 2010-10-12 2012-04-18 Shell Internationale Research Maatschappij B.V. Composition de lubrification
US8455406B2 (en) 2010-10-28 2013-06-04 Chevron U.S.A. Inc. Compressor oils having improved oxidation resistance
RU2582677C2 (ru) 2010-12-17 2016-04-27 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Смазывающая композиция
WO2012138733A2 (fr) 2011-04-05 2012-10-11 Chevron Oronite Company Llc Compositions d'huile de graissage de cylindre de moteur marin de faible viscosité
CA2833085A1 (fr) 2011-04-21 2012-10-26 Shell Internationale Research Maatschappij B.V. Procede de conversion d'une biomasse solide
JP2014511937A (ja) 2011-04-21 2014-05-19 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイ 液体燃料組成物
WO2012143564A1 (fr) 2011-04-21 2012-10-26 Shell Internationale Research Maatschappij B.V. Procédé de conversion d'une biomasse solide
CN103547660A (zh) 2011-05-05 2014-01-29 国际壳牌研究有限公司 包含费-托衍生基油的润滑油组合物
US20120304531A1 (en) 2011-05-30 2012-12-06 Shell Oil Company Liquid fuel compositions
EP2395068A1 (fr) 2011-06-14 2011-12-14 Shell Internationale Research Maatschappij B.V. Composition de lubrification
US9206374B2 (en) 2011-12-16 2015-12-08 Chevron Oronite Sas Trunk piston engine lubricating oil compositions
US9593267B2 (en) 2011-12-20 2017-03-14 Shell Oil Company Adhesive compositions and methods of using the same
RU2014130105A (ru) 2011-12-22 2016-02-10 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Усовершенствования, касающиеся смазки компрессора высокого давления
JP5976836B2 (ja) 2011-12-22 2016-08-24 昭和シェル石油株式会社 潤滑組成物
EP2626405B1 (fr) 2012-02-10 2015-05-27 Ab Nanol Technologies Oy Composition lubrifiante
CN104508095B (zh) 2012-06-21 2018-09-28 国际壳牌研究有限公司 包含重质费-托衍生和烷基化芳族基油的润滑油组合物
BR112014031498A2 (pt) 2012-06-21 2017-06-27 Shell Int Research composição lubrificante, e, uso de uma composição lubrificante
BR112015002105B1 (pt) 2012-08-01 2021-05-04 Shell Internationale Research Maatschappij B.V. cabo de fibra óptica
WO2014020535A2 (fr) 2012-08-02 2014-02-06 Sasol Technology (Proprietary) Limited Traitement de la cire
EP2695932A1 (fr) 2012-08-08 2014-02-12 Ab Nanol Technologies Oy Composition de graisse
EP2816098A1 (fr) 2013-06-18 2014-12-24 Shell Internationale Research Maatschappij B.V. Utilisation d'un composé à soufre pour améliorer la stabilité oxidante d'une composition d'huile de lubrification
EP2816097A1 (fr) 2013-06-18 2014-12-24 Shell Internationale Research Maatschappij B.V. Composition d'huile de lubrification
FR3013357B1 (fr) 2013-11-18 2016-09-16 Total Marketing Services Procede de production de fluides hydrocarbures a basse teneur en aromatiques
US20170009180A1 (en) 2013-12-24 2017-01-12 Shell Oil Company Lubricating composition
CN106133006B (zh) 2014-03-28 2018-04-03 三井化学株式会社 乙烯/α‑烯烃共聚物及润滑油
US8968592B1 (en) 2014-04-10 2015-03-03 Soilworks, LLC Dust suppression composition and method of controlling dust
US9068106B1 (en) 2014-04-10 2015-06-30 Soilworks, LLC Dust suppression composition and method of controlling dust
WO2015172846A1 (fr) 2014-05-16 2015-11-19 Ab Nanol Technologies Oy Composition d'additif pour lubrifiants
RU2692794C2 (ru) 2014-06-19 2019-06-27 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Смазывающая композиция
WO2016032782A1 (fr) 2014-08-27 2016-03-03 Shell Oil Company Procédés de lubrification d'une surface revêtue de carbone de type diamant, compositions d'huile lubrifiante associées et procédés de criblage associés
EP3192856B1 (fr) 2014-09-10 2020-12-23 Mitsui Chemicals, Inc. Composition lubrifiante
US10913916B2 (en) 2014-11-04 2021-02-09 Shell Oil Company Lubricating composition
MY188310A (en) 2014-11-12 2021-11-27 Shell Int Research Use of a fuel composition
RU2683646C2 (ru) 2014-12-17 2019-04-01 Шелл Интернэшнл Рисерч Маатсхаппий Б.В. Композиция смазочного масла
EP3040404A1 (fr) 2014-12-31 2016-07-06 Shell Internationale Research Maatschappij B.V. Procédé de préparation de naphta et de fractions de distillat moyen
JP6674472B2 (ja) 2015-02-06 2020-04-01 シエル・インターナシヨネイル・リサーチ・マーチヤツピイ・ベー・ウイＳｈｅｌｌ Ｉｎｔｅｒｎａｔｉｏｎａｌｅ Ｒｅｓｅａｒｃｈ Ｍａａｔｓｃｈａｐｐｉｊ Ｂｅｓｌｏｔｅｎ Ｖｅｎｎｏｏｔｓｈａｐ グリース組成物
WO2016135036A1 (fr) 2015-02-27 2016-09-01 Shell Internationale Research Maatschappij B.V. Utilisation d'une composition de graissage
WO2016156328A1 (fr) 2015-03-31 2016-10-06 Shell Internationale Research Maatschappij B.V. Utilisation d'une composition lubrifiante comprenant un photostabilisant de type amine encombrée pour une meilleure propreté d'un piston dans un moteur à combustion interne
WO2016166135A1 (fr) 2015-04-15 2016-10-20 Shell Internationale Research Maatschappij B.V. Procédé permettant de détecter la présence d'hydrocarbures obtenus à partir du méthane dans un mélange
WO2016184842A1 (fr) 2015-05-18 2016-11-24 Shell Internationale Research Maatschappij B.V. Composition lubrifiante
EP3095842A1 (fr) 2015-05-20 2016-11-23 Total Marketing Services Procédé pour la production de fluides hydrocarbonés biodégradables basé sur un gaz de synthèse
CN107849481B (zh) 2015-07-22 2021-09-03 雪佛龙奥伦耐技术有限责任公司 船用柴油机汽缸润滑油组合物
US9434881B1 (en) 2015-08-25 2016-09-06 Soilworks, LLC Synthetic fluids as compaction aids
US10808195B2 (en) 2015-09-22 2020-10-20 Shell Oil Company Fuel compositions
WO2017093203A1 (fr) 2015-11-30 2017-06-08 Shell Internationale Research Maatschappij B.V. Composition de carburant
US10385288B1 (en) 2016-05-13 2019-08-20 Evonik Oil Additives Gmbh Graft copolymers based on polyolefin backbone and methacrylate side chains
SG11201901183RA (en) 2016-08-15 2019-03-28 Evonik Oil Additives Gmbh Functional polyalkyl (meth)acrylates with enhanced demulsibility performance
SG11201901623TA (en) 2016-08-31 2019-03-28 Evonik Oil Additives Gmbh Comb polymers for improving noack evaporation loss of engine oil formulations
EP3315592A1 (fr) 2016-10-27 2018-05-02 Total Marketing Services Utilisation de fluides hydrocarbonés biodégradables en tant que fluides de forage
EP3315586A1 (fr) 2016-10-27 2018-05-02 Total Marketing Services Utilisation de fluides d'hydrocarbures biodégradables servant d'agents caloporteurs
EP3315590A1 (fr) 2016-10-27 2018-05-02 Total Marketing Services Utilisation de fluides d'hydrocarbure dans des véhicules électriques
EP3336162A1 (fr) 2016-12-16 2018-06-20 Shell International Research Maatschappij B.V. Composition de lubrification
RU2019121715A (ru) 2016-12-19 2021-01-19 Эвоник Оперейшнс Гмбх Комопозиция смазочного масла, содержащая диспергирующие гребенчатые полимеры
EP3342842A1 (fr) 2017-01-03 2018-07-04 Total Marketing Services Procédé de déparaffinage et désaromatisation d'hydrocarbure dans un bioréacteur à boues liquides
EP3569678B1 (fr) 2017-01-16 2023-10-18 Mitsui Chemicals, Inc. Composition d'huile lubrifiante pour engrenages d'automobile
US20180305633A1 (en) 2017-04-19 2018-10-25 Shell Oil Company Lubricating compositions comprising a volatility reducing additive
WO2018197312A1 (fr) 2017-04-27 2018-11-01 Shell Internationale Research Maatschappij B.V. Composition lubrifiante
JP7143395B2 (ja) 2017-07-14 2022-09-28 エボニック オペレーションズ ゲーエムベーハー イミド官能性を有するくし型ポリマー
EP3450527B1 (fr) 2017-09-04 2020-12-02 Evonik Operations GmbH Nouveaux améliorants l'indice de viscosité ayant des répartitions de poids moléculaire définies
EP3498808B1 (fr) 2017-12-13 2020-05-13 Evonik Operations GmbH Agent améliorant l'indice de viscosité présentant une meilleure résistance au cisaillement et une meilleure solubilité après cisaillement
KR102587267B1 (ko) 2018-01-23 2023-10-11 에보닉 오퍼레이션스 게엠베하 중합체-무기 나노입자 조성물, 이의 제조 방법 및 윤활제 첨가제로서의 이들의 용도
WO2019145287A1 (fr) 2018-01-23 2019-08-01 Evonik Oil Additives Gmbh Compositions nanoparticulaires polymères inorganiques, leur procédé de fabrication et leur utilisation en tant qu'additifs pour lubrifiants
ES2893267T3 (es) 2018-01-23 2022-02-08 Evonik Operations Gmbh Composiciones de nanopartículas poliméricas-inorgánicas, proceso de fabricación de las mismas y su uso como aditivos para lubricantes
CN112004918B (zh) 2018-04-26 2023-10-03 国际壳牌研究有限公司 润滑剂组合物及其作为管道涂料的用途
WO2020007945A1 (fr) 2018-07-05 2020-01-09 Shell Internationale Research Maatschappij B.V. Composition lubrifiante
WO2020011948A1 (fr) 2018-07-13 2020-01-16 Shell Internationale Research Maatschappij B.V. Composition lubrifiante
WO2020064619A1 (fr) 2018-09-24 2020-04-02 Evonik Operations Gmbh Utilisation de composés à base de trialcoxysilane pour lubrifiants
WO2020099078A1 (fr) 2018-11-13 2020-05-22 Evonik Operations Gmbh Copolymères statistiques destinés à être utilisés comme huiles de base ou additifs lubrifiants
WO2020126494A1 (fr) 2018-12-19 2020-06-25 Evonik Operations Gmbh Utilisation de copolymères triséquencés associatifs en tant qu'agents d'amélioration de l'indice de viscosité
EP3898721B1 (fr) 2018-12-19 2023-05-03 Evonik Operations GmbH Dispositifs d'amélioration de l'indice de viscosité basés sur des copolymères séquencés
SG10202002189PA (en) 2019-03-11 2020-10-29 Evonik Operations Gmbh Novel Viscosity Index Improvers
CN113597463B (zh) 2019-03-20 2022-08-02 赢创运营有限公司 用于改进燃料经济性、分散性和沉积物性能的聚(甲基)丙烯酸烷基酯
US20220186133A1 (en) 2019-03-26 2022-06-16 Mitsui Chemicals, Inc. Lubricating oil composition for industrial gears and method for producing the same
KR20210139402A (ko) 2019-03-26 2021-11-22 미쓰이 가가쿠 가부시키가이샤 내연 기관용 윤활유 조성물 및 그의 제조 방법
CN113574147A (zh) 2019-03-26 2021-10-29 三井化学株式会社 汽车齿轮用润滑油组合物及其制造方法
EP3950892A4 (fr) 2019-03-26 2022-08-10 Mitsui Chemicals, Inc. Composition de graisse, et procédé de fabrication de celle-ci
EP3950900A4 (fr) 2019-03-26 2022-08-10 Mitsui Chemicals, Inc. Composition d'huile lubrifiante pour moteur à combustion interne, et procédé de fabrication de celle-ci
WO2020194545A1 (fr) 2019-03-26 2020-10-01 三井化学株式会社 Composition d'huile lubrifiante pour huile de fonctionnement, et procédé de fabrication de celle-ci
CN113574145A (zh) 2019-03-26 2021-10-29 三井化学株式会社 压缩机油用润滑油组合物及其制造方法
KR20210141610A (ko) 2019-03-26 2021-11-23 미쓰이 가가쿠 가부시키가이샤 자동차 변속기유용 윤활유 조성물 및 그의 제조 방법
EP3778839B1 (fr) 2019-08-13 2021-08-04 Evonik Operations GmbH Agent améliorant l'indice de viscosité présentant une meilleure résistance au cisaillement
JP7408344B2 (ja) 2019-10-23 2024-01-05 シェルルブリカンツジャパン株式会社 潤滑油組成物
BR112022019578A2 (pt) 2020-03-30 2022-11-16 Shell Int Research Sistema de gerencimento térmico
BR112022019587A2 (pt) 2020-03-30 2022-11-16 Shell Int Research Gerenciamento de fuga térmica
MX2022013305A (es) 2020-04-30 2022-11-14 Evonik Operations Gmbh Procedimiento de preparacion de polimeros de (met)acrilato de polialquilo.
JP2023523755A (ja) 2020-04-30 2023-06-07 エボニック オペレーションズ ゲーエムベーハー 分散剤ポリアルキル（メタ）アクリレートポリマーを製造する方法
ES2950909T3 (es) 2020-05-05 2023-10-16 Evonik Operations Gmbh Copolímeros de polidieno lineales hidrogenados como material base o aditivos lubricantes para composiciones lubricantes
WO2022003088A1 (fr) 2020-07-03 2022-01-06 Evonik Operations Gmbh Fluides de base à viscosité élevée à base de polyesters compatibles avec l'huile préparés à partir d'époxydes à longue chaîne
JP2023532930A (ja) 2020-07-03 2023-08-01 エボニック オペレーションズ ゲーエムベーハー 親油性ポリエステルをベースとする高粘度ベースフルード
BR112023003513A2 (pt) 2020-09-01 2023-04-11 Shell Int Research Composição de óleo de motor
KR20230070242A (ko) 2020-09-18 2023-05-22 에보닉 오퍼레이션스 게엠베하 윤활제 첨가제로서 그래핀계 물질을 포함하는 조성물
KR20230107653A (ko) 2020-11-18 2023-07-17 에보니크 오퍼레이션즈 게엠베하 높은 점도 지수를 갖는 압축기 오일
CA3202022A1 (fr) 2020-12-18 2022-06-23 Evonik Operations Gmbh Procede de preparation d'homo polymeres et de copolymeres de (meth)acrylates d'alkyle ayant une faible teneur en monomeres residuels
EP4060009B1 (fr) 2021-03-19 2023-05-03 Evonik Operations GmbH Un agent améliorant l'indice de viscosité et composition lubrifiante
EP4119640B1 (fr) 2021-07-16 2023-06-14 Evonik Operations GmbH Composition d'additif lubrifiant contenant des polyalkyl méthacrylates
WO2023002947A1 (fr) 2021-07-20 2023-01-26 三井化学株式会社 Modificateur de viscosité pour huile lubrifiante, et composition d'huile lubrifiante pour huile hydraulique
WO2023099635A1 (fr) 2021-12-03 2023-06-08 Totalenergies Onetech Compositions lubrifiantes
EP4441176B1 (fr) 2021-12-03 2025-10-01 Evonik Operations GmbH Polymères de poly(méth)acrylate d'alkyle modifiés par des esters boroniques
EP4441178B1 (fr) 2021-12-03 2025-05-14 TotalEnergies OneTech Compositions lubrifiantes
EP4441175B1 (fr) 2021-12-03 2025-08-27 Evonik Operations GmbH Polymères de poly(méth)acrylate d'alkyle modifiés par des esters boroniques
EP4441180A1 (fr) 2021-12-03 2024-10-09 TotalEnergies OneTech Compositions lubrifiantes
EP4441177B1 (fr) 2021-12-03 2025-08-06 Evonik Operations GmbH Polymères de poly(méth)acrylate d'alkyle modifiés par des esters boroniques
JPWO2023167307A1 (fr) 2022-03-03 2023-09-07
CN119213095A (zh) 2022-05-19 2024-12-27 国际壳牌研究有限公司 热管理系统
CN119630768A (zh) 2022-08-08 2025-03-14 赢创运营有限公司 具有改进的低温性质的聚(甲基)丙烯酸烷基酯基聚合物
EP4321602B1 (fr) 2022-08-10 2024-09-11 Evonik Operations GmbH Copolymères de poly(méth)acrylate d'alkyle sans soufre utilisés comme améliorants d'indice de viscosité dans des lubrifiants
EP4630521A1 (fr) 2022-12-07 2025-10-15 Evonik Operations GmbH Polymères dispersants exempts de soufre pour applications industrielles
WO2025008274A1 (fr) 2023-07-03 2025-01-09 Shell Internationale Research Maatschappij B.V. Composition d'huile lubrifiante
WO2025201962A1 (fr) 2024-03-27 2025-10-02 Shell Internationale Research Maatschappij B.V. Composition d'huile lubrifiante
WO2025252603A1 (fr) 2024-06-04 2025-12-11 Shell Internationale Research Maatschappij B.V. Composition d'huile lubrifiante
EP4682207A1 (fr) 2024-12-13 2026-01-21 TotalEnergies OneTech Composition biosourcée pour le traitement de fibres textiles

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CA1310287C (fr) * 1987-12-18 1992-11-17 Exxon Research And Engineering Company Procede pour l'hydroisomerisation de cire fischer-tropsch pour la production d'huile lubrifiante
AU638336B2 (en) * 1990-07-05 1993-06-24 Mobil Oil Corporation Production of high viscosity index lubricants
DK0583836T4 (da) * 1992-08-18 2002-03-11 Shell Int Research Fremgangsmåde til fremstilling af carbonhydridbrændstoffer

Cited By (34)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6669743B2 (en) 1997-02-07 2003-12-30 Exxonmobil Research And Engineering Company Synthetic jet fuel and process for its production (law724)
EP1268712B2 (fr) † 2000-04-04 2009-06-10 ExxonMobil Research and Engineering Company Procede d'adoucissement de cires de fischer-tropsch par hydrotraitement doux
EP1272592B1 (fr) * 2000-04-04 2004-09-29 ExxonMobil Research and Engineering Company Procede pour adapter la durete de la cire de fischer-tropsch par malaxage
EP1630222A1 (fr) 2001-03-05 2006-03-01 Shell Internationale Researchmaatschappij B.V. Fluid pour turbines comprenant une huile de base préparé d'un produit sorti d'un procédé de Fischer-Tropsch
EP1630221A1 (fr) 2001-03-05 2006-03-01 Shell Internationale Researchmaatschappij B.V. Graisse de lubrification comprenant une huile de base préparé d'un produit sorti d'un procédé de Fischer-Tropsch
EP1626080A2 (fr) 2001-03-05 2006-02-15 Shell Internationale Researchmaatschappij B.V. Composition de fluide hydraulique
EP1686164A2 (fr) 2002-02-25 2006-08-02 Shell Internationale Researchmaatschappij B.V. Gazole ou composant de mélange de gazole
US7670983B2 (en) 2002-10-08 2010-03-02 Exxonmobil Research And Engineering Company Oxygenate treatment of dewaxing catalyst for greater yield of dewaxed product
US7132042B2 (en) 2002-10-08 2006-11-07 Exxonmobil Research And Engineering Company Production of fuels and lube oils from fischer-tropsch wax
WO2004033595A1 (fr) 2002-10-08 2004-04-22 Exxonmobil Research And Engineering Company Huile lubrifiante lourde formee a partir de cire fischer-tropsch
US7201838B2 (en) 2002-10-08 2007-04-10 Exxonmobil Research And Engineering Company Oxygenate treatment of dewaxing catalyst for greater yield of dewaxed product
US7241375B2 (en) 2002-10-08 2007-07-10 Exxonmobil Research And Engineering Company Heavy hydrocarbon composition with utility as a heavy lubricant base stock
US7344631B2 (en) 2002-10-08 2008-03-18 Exxonmobil Research And Engineering Company Oxygenate treatment of dewaxing catalyst for greater yield of dewaxed product
US6846778B2 (en) 2002-10-08 2005-01-25 Exxonmobil Research And Engineering Company Synthetic isoparaffinic premium heavy lubricant base stock
US7018525B2 (en) 2003-10-14 2006-03-28 Chevron U.S.A. Inc. Processes for producing lubricant base oils with optimized branching
US7335802B2 (en) 2003-10-15 2008-02-26 Shell Oil Company Methods of preparing branched aliphatic alcohols
US8882989B2 (en) 2003-12-23 2014-11-11 Chevron U.S.A. Inc. Lubricating base oil manufacturing plant for producing base oils having desired cycloparafinic functionality
US7763161B2 (en) 2003-12-23 2010-07-27 Chevron U.S.A. Inc. Process for making lubricating base oils with high ratio of monocycloparaffins to multicycloparaffins
US9809760B2 (en) 2003-12-23 2017-11-07 Chevron U.S.A. Inc. Method for producing a base oil having high weight percent total molecules with cycloparaffinic functionality and low weight percent molecules with multicycloparaffinic functionality
US7252753B2 (en) 2004-12-01 2007-08-07 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
US7510674B2 (en) 2004-12-01 2009-03-31 Chevron U.S.A. Inc. Dielectric fluids and processes for making same
US7981270B2 (en) 2005-03-11 2011-07-19 Chevron U.S.A. Inc. Extra light hydrocarbon liquids
US7655605B2 (en) 2005-03-11 2010-02-02 Chevron U.S.A. Inc. Processes for producing extra light hydrocarbon liquids
EP2363453A1 (fr) 2005-06-03 2011-09-07 ExxonMobil Research and Engineering Company Detergents sans cendre et huile lubrifiante les contenant
EP2366764A1 (fr) 2005-06-03 2011-09-21 ExxonMobil Research and Engineering Company Détergents sans cendre et huile lubrifiante les contenant
EP2366763A1 (fr) 2005-06-03 2011-09-21 ExxonMobil Research and Engineering Company Detergents sans cendre et huile lubrifiante les contenant
WO2006132964A2 (fr) 2005-06-03 2006-12-14 Exxonmobil Research And Engineering Company Detergents sans cendre et huile lubrifiante formulee les contenant
WO2007050352A1 (fr) 2005-10-21 2007-05-03 Exxonmobil Research And Engineering Company Huiles de lubrification ameliorees destinees a des moteurs a deux temps
WO2007133554A2 (fr) 2006-05-09 2007-11-22 Exxonmobil Research And Engineering Company Composition d'huile de graissage
WO2008002425A1 (fr) 2006-06-23 2008-01-03 Exxonmobil Research And Engineering Company Compositions lubrifiantes
WO2012143550A1 (fr) 2011-04-21 2012-10-26 Shell Internationale Research Maatschappij B.V. Procédé de transformation d'un matériau de biomasse solide
EP2746367A1 (fr) 2012-12-18 2014-06-25 Shell Internationale Research Maatschappij B.V. Procédé pour préparer une huile de base et du gazole
US10364403B2 (en) 2013-11-06 2019-07-30 Chevron Oronite Technology B.V. Marine diesel cylinder lubricant oil compositions
US10669506B2 (en) 2013-11-06 2020-06-02 Chevron Oronite Technology B.V. Marine diesel cylinder lubricant oil compositions

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