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    • 专利摘要:
    The invention relates to a low viscosity oil comprising more than 50% by weight of 9-methyl-11,13-dioctyltricosane and a lubricating composition comprising this base oil and optionally another base oil or an additive. This oil according to the invention has a kinematic viscosity at 100 ° C, measured according to ASTM D445, ranging from 4 to 8 mm2.s-1. The invention also relates to such a low viscosity oil prepared according to a particular method employing a metallocene catalyst and the use of this oil as a high performance lubricant for lubrication in the fields of engines, hydraulic fluids, gears, in particular bridges and transmissions.
    公开号:FR3037949A1
    申请号:FR1556039
    申请日:2015-06-29
    公开日:2016-12-30
    发明作者:Marion Courtiade；Julien Sanson；Alexandre Welle；Martine Slawinski；Jeroen Wassenaar
    申请人:Total Marketing Services SA；
    IPC主号:
    专利说明:

    [0001] The invention relates to a low-viscosity oil comprising more than 50% by weight of 9-methyl-11,13-dioctyltricosane and a lubricating composition comprising this base oil and optionally another oil. base or additive. This oil according to the invention has a kinematic viscosity at 100 ° C, measured according to ASTM D445, ranging from 4 to 8 mm2.s-1. The invention also relates to such a low viscosity oil prepared according to a particular process employing a metallocene catalyst and the use of this oil as a high performance lubricant for lubrication in the fields of engines, hydraulic fluids, gears, in particular bridges and transmissions.
    [0002] In the API classification of base oils, polyalphaolefins (PAO) are referenced as Group IV base oils. Thanks to a good compromise between the viscosity, the volatility and the cold properties, these PAO are more and more used in the high performance lubricating formulas. In particular, this better compromise is very advantageous compared to Group III mineral bases.
    [0003] In general, PAOs are synthesized from different olefinic monomers, in particular from C 6 -C 14 monomers, by acid catalysis or in the presence of a metallocene catalyst. In general, to prepare PAO products of low viscosity, in particular kinematic viscosity at 100 ° C. ranging from 2 to 10 mes-1, measured according to ASTM D445 (grades 2 to 10), catalysts are used. acids. Processes for the preparation of PAO by metallocene catalysis are known, generally making it possible to produce high viscosity products whose kinematic viscosity at 100 ° C., measured according to the ASTM D445 standard, ranges from 40 to 150 mm 2 .s-1 (40 grades). at 150).
    [0004] In addition, the need for high performance lubricants is increasing. In particular, because of conditions of use whose severity increases, for example because of very high temperatures or mechanical stresses. The spacing of the oil changes and the reduction in the size of the lubrication systems also increase the need for high performance lubricants.
    [0005] The energy efficiency and in particular the improvement of the Fuel Eco (FE) lubricants or the reduction of the fuel consumption of the engines, in particular the engines of 3037949 2 vehicle, are objectives more and more important and lead to the increasing use of high performance lubricants. High performance lubricants must therefore have improved properties, particularly with regard to kinematic viscosity, viscosity index, volatility, dynamic viscosity or cold pour point. Thermal stability and oxidation resistance are also properties to be improved for high performance lubricants. Reduced toxicity and good miscibility with other lubricants or other materials are also properties to look for high performance lubricants. Furthermore, improved PAO preparation methods must also be developed, in particular to improve the yield or selectivity of these processes. The improvement of the catalytic activity must also be aimed at.
    [0006] The processes for preparing PAO should also make it possible to control the molecular weight as well as the polydispersity index and the distribution of the PAOs formed. The improvement of the characterization techniques of the different products formed during the synthesis of PAO is also to be sought, in particular during the qualitative or quantitative analysis of the products formed.
    [0007] There is therefore a need for high performance lubricants to provide a solution to all or some of the problems of the lubricants of the state of the art. Thus, the invention provides a kinematic viscosity oil at 100.degree. C., measured according to ASTM D445, ranging from 4 to 8 mm.sup.2.sup.-1, and comprising more than 50% by weight of 1-decene tetramer of The oil according to the invention has a particularly advantageous viscosity ranging from 4 to 8 mm.sup.-2. More advantageously, the kinematic viscosity of the oil according to the invention ranges from 5 to 7 mm 2 s -1. Preferably, the kinematic viscosity of the oil according to the invention ranges from 5.4 to 6.5 mm.sup.2.s -1. More preferably, the kinematic viscosity of the oil according to the invention is 5.4 mm 2 s -1, 5.5 mm 2 s -1, 5.6 mm 2 s -1, 5.7 mm 2. s-1 or 5.8 mm2s-1. Also advantageously, the oil according to the invention has a viscosity index greater than 130 or greater than or equal to 140. Preferably, the viscosity index of the oil according to the invention is between 130 and 180 or between 140 and 160. Generally according to the invention, the viscosity index is calculated according to ASTM D2270. Also advantageously, the oil according to the invention has a volatility measured according to the CEC L-40-93 standard of less than 6% by weight or even less than 5% by weight. Preferably, the volatility of the oil according to the invention is between 4 and 6% by weight or between 4.5 and 6% by weight. Also advantageously, the oil according to the invention has a dynamic viscosity (CCS) at -35 ° C, measured according to ASTM D5293, of less than 4000 mPa.s. Preferably, the dynamic viscosity of the oil according to the invention is less than 3500 mPa.s or less than 3000 mPa.s. According to the invention, the dynamic viscosity of the oil is measured on a rotary dynamic viscometer (CCS cold cranking simulator).
    [0008] Also advantageously, the oil according to the invention has an average molecular weight ranging from 300 to 1000 g / mol, preferably from 400 to 600 g / mol. In general, according to the invention, the average molecular weight is calculated according to the ASTM D2502 standard.
    [0009] Also advantageously, the oil according to the invention has a pour point of less than or equal to -50 ° C, preferably less than or equal to -55 ° C or less than or equal to -57 ° C. In general, according to the invention, the pour point is measured according to EN ISO 3016.
    [0010] Advantageously, the invention provides an oil combining (a) a kinematic viscosity at 100 ° C, measured in accordance with ASTM D445 ranging from 5 to 7 mm 2 s -1, preferably from 5.4 to 6 , 5 mm2.s-1, or 5.4 mm2.s-1, 5.5 mm2s1, 5.6 mm2.s-1, 5.7 mm2.s-1 or 5.8 mm2 .s-1; (B) a viscosity number greater than 130 or greater than or equal to 140 or 130 to 180 or 140 to 160; (c) a volatility measured according to CEC L-40-93 below 6% by mass or less than 5% by mass; and (d) a dynamic viscosity (CCS) at -35 ° C, measured according to ASTM D5293 less than 3,500 mPa.s or less than 3,000 mPa.s. Also advantageously, the invention provides an oil combining these properties (a) and (b); (a) and (c); (a) and (d); (b) and (c); (b) and (d); (c) and (d); (a), (b) and (c); (a), (b) and (d); (a), (c) and (d); (b), (c) and (d).
    [0011] Preferably, the invention provides an oil combining (a) a kinematic viscosity at 100 ° C, measured in accordance with ASTM D445 ranging from 5.4 to 6.5 mm 2 · s, or 5.4 mm 2. s-1, 5.5 mm2s-1, 5.8 mm2s-1, 5.7 mm2s-, or 5.8 mm2s- ,; (b) a viscosity number of 130 to 180 or 140 to 160; (C) a volatility measured according to the CEC standard L-40-93 of less than 5% by weight; and (d) a dynamic viscosity (CCS) at -35 ° C, measured according to ASTM D5293 below 3000 mPa.s. Also preferably, the invention provides an oil combining these properties (a) and (b); (a) and (c); (a) and (d); (b) and (c); (b) and (d); (c) and (d); (a), (b) and (c); (a), (b) and (d); (A), (c) and (d); (b), (c) and (d). Advantageously, the oil according to the invention comprises from 50 to 99% by weight of 1-decene tetramer of formula (I). Also advantageously, the oil according to the invention comprises 60 to 95% by weight or 70 to 90% by weight of 1-decene tetramer of formula (I). Preferably, the oil according to the invention comprises at least 65% by weight of 1-decene tetramer of formula (I) or at least 70% by weight of 1-decene tetramer of formula (I). More advantageously, the oil according to the invention comprises at least 80% by weight of 1-decene tetramer of formula (I) or at least 90% by weight of 1-decene tetramer of formula (I).
    [0012] In addition to the 1-decene tetramer of formula (I), the oil according to the invention may comprise other oligomers derived from the oligomerization of 1-decene, in particular saturated oligomers. Preferably, the oil according to the invention may comprise at least one other saturated oligomer of 1-decene chosen from the other saturated tetramers of 1-decene; or the other saturated tetramers of 1-decene, the saturated dimers of 1-decene, the saturated trimers of 1-decene, the saturated pentamers of 1-decene, the saturated hexamers of 1-decene. ; or the other saturated tetramers of 1-decene, the saturated pentamers of 1-decene, the saturated hexamers of 1-decene. Also advantageously, the oil according to the invention comprises from 51 to 94.8% by weight of 1-decene tetramer of formula (I); from 0.1 to 10% by weight of at least one other saturated tetramer of 1-decene; From 0.1 to 10% by weight of at least one saturated trimer of 1-decene; from 5 to 25% by weight of at least one pentamer saturated with 1-decene or at least one saturated hexamer of 1-decene. In particular, the oil according to the invention comprises from 51 to 94.7% by weight of 1-decene tetramer of formula (I); From 0.1 to 10% by weight of at least one other saturated tetramer of 1-decene; from 0.1 to 5% by weight of at least one saturated dimer of 1-decene; from 0.1 to 10% by weight of at least one saturated trimer of 1-decene; from 5 to 25% by weight of at least one pentamer saturated with 1-decene or at least one saturated hexamer of 1-decene.
    [0013] The oil according to the invention has the essential characteristic of comprising more than 50% by weight of 9-methyl-11,13-dioctyltricosane, 1-decene tetramer of formula (I). Preferably, the oil according to the invention comprising more than 50% by weight of 9-methyl-11,13-dioctyltricosane is prepared according to a process comprising the oligomerization of 1-decene in the presence of hydrogen (H2 ), a metallocene catalyst and an activator compound or in the presence of hydrogen (H2), a metallocene catalyst, an activator compound and a coactivator compound; catalytic hydrogenation of the oligomerization products in the presence of hydrogen (H2) and a catalyst selected from a hydrogenation catalyst and a hydrogenation catalyst comprising palladium; The separation by distillation at reduced pressure of the tetramer fraction comprising more than 50% by weight of 1-decene tetramer of formula (I) (I). Preferably, the oligomerization of 1-decene is carried out in the presence of a metallocene catalyst which is a racemic compound of formula (II) L (Q1) (Q2) MR1R2 (II) in which o M represents a transition metal selected from titanium, zirconium, hafnium, and vanadium or represents zirconium; O1 and Q2, substituted or unsubstituted, independently represent a tetrahydroindenyl cyclic group or Q1 and Q2 independently represent a tetrahydroindenyl cyclic group and are linked to form a polycyclic structure; L represents a Cl-C20-divalent bridging alkyl group Q1 and Q2 where L represents a group chosen from methylene (-CH2-), ethylene (-CH2-CH2-), methylmethylene (-CH (CH3) -), methyl-ethylene (- CH (CH3) -CH2-), n-propylene (-CH2-CH2-CH2-), 2-methylpropylene (-CH2-CH (CH3) -CH2-), 3-methylpropylene (-CH2 -CH2-CH (CH3) -), n-butylene (-CH2-CH2-CH2-CH2-), 2-methylbutylene (-CH2-CH (CH3) -CH2-CH2-), 4-methylbutylene (-CH2-CH2- CH2-CH (CH3) -), pentylene and its isomers, hexylene and isomers thereof, heptylene and isomers thereof, octylene and isomers thereof, nonylene and isomers thereof, decylene and isomers thereof, undecylene and isomers thereof, dodecylene and isomers thereof; R 1 and R 2, substituted or unsubstituted, independently represent an atom or a group chosen from hydrogen, halogens (such as Cl and I), alkyl (such as Me, Et, nPr, iPr), alkenyl, alkynyl, haloalkyl, Haloalkenyl, haloalkynyl, silylalkyl, silylalkenyls, silylalkynyls, germylalkyl, germylalkenyl, germylalkynyl; or R1 and R2 together with M form a metallocycle comprising from 3 to 20 carbon atoms. More preferably, the metallocene catalyst is a racemic compound of formula (II) wherein M represents zirconium; O1 and Q2, substituted or unsubstituted, independently represent a tetrahydroindenyl cyclic group; L represents a group selected from methylene (-CH2-), ethylene (-CH2-CH2-), methylmethylene (-CH (CH3) -), 1-methyl-ethylene (- CH (CH3) -CH2-), n-propylene (-CH2-CH2-CH2-), 2-methylpropylene (-CH2-CH (CH3) -CH2-), 3-methylpropylene (-CH2-CH2-CH (CH3) -), nbutylene (-CH2- CH2-CH2-CH2-), 2-methylbutylene (-CH2-CH (CH3) -CH2-CH2-), 4-methylbutylene (-CH2-CH2-CH2-CH (CH3) -), pentylene and its isomers, hexylene and its isomers, heptylene and isomers thereof, octylene and isomers thereof, nonylene and isomers thereof, decylene and isomers thereof, undecylene and isomers thereof, dodecylene and isomers thereof; R 1 and R 2, substituted or unsubstituted, independently represent a halogen atom, such as Cl and I, or an alkyl group, such as Me, Et, nPr, iPr.
    [0014] Even more preferably, the metallocene catalyst is selected from rac-ethylene bis (tetrahydroindenyl) zirconium dimethyl and rac-ethylene bis (tetrahydroindenyl) zirconium dichloride, in particular rac-ethylene bis (tetrahydroindenyl) zirconium dimethyl. For the process according to the invention, the catalyst is used in an activated form for the oligomerization of 1-decene. Thus, the process according to the invention uses an activator compound during the oligomerization of 1-decene. Advantageously, the activator compound is chosen from an alumoxane, an ionic activator and their mixtures. Preferably for the process according to the invention, the alumoxane is an oligomeric compound comprising residues of the formula -Al (R) -O- in which R independently represents a Cl-C20 alkyl, cyclic or linear group. Preferably, the alumoxane is chosen from methylalumoxane, modified methylalumoxane, ethylalumoxane, isobutylalumoxane and mixtures thereof.
    [0015] Also preferably, the alumoxane is used in an alumoxane / catalyst molar ratio ranging from 1 to 10,000, preferably from 10 to 3,000 and more preferably from 100 to 1,500. According to the invention, the activator compound is an ionic activator. The ionic activator may be selected from dimethylanilinium tetrakis- (perfluorophenyl) borate (DMAB), triphenylcarbonium tetrakis- (perfluorophenyl) borate, dimethylanilinium tetrakis- (perfluorophenyl) aluminate and mixtures thereof. More preferably, the ionic activator is dimethylanilinium tetrakis- (perfluorophenyl) borate (DMAB).
    [0016] Also preferably, the ionic activator is carried out at an ionic activator / catalyst molar ratio of from 0.5 to 4, preferably from 0.8 to 1.2. During the oligomerization of 1-decene, the process according to the invention uses an activator compound. It may also be advantageous to use a coactivator compound, particularly when using an ionic activator. Preferably, the coactivator compound is a trialkylaluminium derivative. More preferably, the coactivator compound is chosen from triethyl aluminum (TEAL), triisobutylaluminum (TIBAL) and triethyl aluminum (TMA). ), tri-n-octyl aluminum and methyl-methyl-ethyl aluminum (MMEAL). Advantageously, tri-iso-butyl aluminum (TIBAL) is used in the form of a dispersion ranging from 10 to 60% by weight. Also preferably, the coactivator compound is used in a co-activator / catalyst compound molar ratio ranging from 10 to 1,000, preferably from 20 to 200.
    [0017] Advantageously, the metallocene catalyst and the activator compound, optionally in the presence of a coactivator compound, are contacted at a pressure of 1 bar and a temperature of 20 ° C. Advantageously, the oligomerization of 1-decene is carried out in a time ranging from 2 to 300 min. Preferably, the duration of the oligomerization is from 5 to 180 min, in particular from 30 to 140 min. Also advantageously, the oligomerization of 1-decene is carried out in the presence of hydrogen (H2) at a partial pressure ranging from 0.1 to 20 bar. Preferably, the hydrogen partial pressure (H2) is from 1 to 6 bar.
    [0018] Advantageously, the oligomerization is carried out at a mass ratio hydrogen / 1-decene greater than 100 ppm or less than 600 ppm. Preferably, this ratio is between 100 and 600 ppm.
    [0019] Also advantageously, the oligomerization of 1-decene is carried out at a temperature of from 50 to 200 ° C, preferably from 70 to 160 ° C. More preferably, the temperature during the oligomerization of 1-decene is from 80 to 150 ° C and even more preferably from 90 to 140 ° C or from 100 to 130 ° C.
    [0020] The oligomerization of 1-decene can be carried out in 1-decene which then serves as a support for the reaction. The reaction is then advantageously carried out in the absence of a solvent. The oligomerization of 1-decene can also be carried out in a solvent. Preferably, the solvent may be selected from a linear or branched hydrocarbon, a cyclic or non-cyclic hydrocarbon, an alkyl aromatic compound and mixtures thereof. As preferred solvents for the oligomerization of 1-decene, it is preferred to use a solvent selected from butanes, pentanes, hexanes, heptanes, octanes, cyclopentane, cyclohexane, methylcyclopentane, methylcyclohexane, methylcycloheptane, toluene, xylene and mixtures thereof.
    [0021] After the oligomerization of 1-decene, the process according to the invention implements the catalytic hydrogenation of the oligomerization products. The catalytic hydrogenation of the oligomerization products is carried out in the presence of hydrogen (H2) and a hydrogenation catalyst.
    [0022] Preferably, the hydrogenation catalyst is chosen from a palladium derivative, a supported palladium derivative, a palladium derivative supported on alumina (for example on gamma-alumina), a nickel derivative or a supported nickel derivative. , a kieselguhr supported nickel derivative, a platinum derivative, a supported platinum derivative, a cobalt-molybdenum derivative, a supported cobalt-molybdenum derivative. More preferably, the hydrogenation catalyst comprises palladium. A particularly preferred hydrogenation catalyst comprises palladium supported on alumina (for example on gamma-alumina).
    [0023] Also preferably, the hydrogen pressure (H2) during the catalytic hydrogenation of the oligomerization products ranges from 5 to 50 bar, more preferably from 10 to 40 bar, in particular from 15 to 25 bar. .
    [0024] After the oligomerization of 1-decene and the catalytic hydrogenation of the oligomerization products, the process according to the invention comprises the separation by distillation at reduced pressure of the fraction of tetramers comprising more than 50% by weight of tetramer of 1 -ecene of formula (I). The separation by distillation is carried out under reduced pressure. Advantageously, the distillation separation is carried out according to ASTM D5236. Preferably, during the separation by distillation according to ASTM D5236, the initial boiling point (IBP or initial boiling point) is between 450 and 520 ° C, preferably between 475 and 495 ° C. The partial pressure is advantageously less than 0.67 mbar.
    [0025] Preferably, the separation by distillation according to ASTM D5236 makes it possible to separate the fraction of tetramers comprising more than 50% by weight of 1-decene tetramer of formula (I). Thus, separation by distillation at reduced pressure makes it possible to separate the fraction of tetramers resulting from the oligomerization of 1-decene and then from the hydrogenation of the oligomerization products. This fraction of tetramers comprises more than 50% by weight of 1-decene tetramer of formula (I). In addition to the oligomerization steps of 1-decene, catalytic hydrogenation of the oligomerization products and separation by distillation at reduced pressure of the fraction of tetramers comprising more than 50% by weight of 1-decene tetramer of formula ( I), the method according to the invention may advantageously comprise other steps. Thus, the process according to the invention can also combine all or part of the following steps: the prior preparation of 1-decene by catalytic oligomerization of ethylene; deactivation of the catalyst after oligomerization of 1-decene or after catalytic hydrogenation of the oligomerization products; recycling of a dimer fraction of 1-decene (for example 9-methyl nonadecane), separated by distillation at reduced pressure and oligomerization with 1-decene of this recycled 1-decene dimer fraction, in the presence of hydrogen (H2), a metallocene catalyst and an activator compound or the presence of hydrogen (H2), a metallocene catalyst, an activator compound and a co-activator compound ; a final hydrogenation step of the tetramer fraction comprising more than 50% by weight of 1-decene tetramer of formula (I) in the presence of hydrogen (H 2) and a catalyst selected from a catalyst of hydrogenation and a hydrogenation catalyst comprising palladium. The prior preparation of 1-decene by catalytic oligomerization of ethylene is known as such. It can be particularly advantageous in combination with the other steps of the process according to the invention. This prior preparation of 1-decene by catalytic oligomerization of ethylene makes it possible in particular to use more abundant sources of starting substrate. Furthermore, and preferably, once the oligomerization of 1-decene has been carried out, the process according to the invention may comprise the deactivation of the catalyst. The deactivation of the oligomerization catalyst can be carried out after the oligomerization of 1-decene or after the catalytic hydrogenation of the oligomerization products. Preferably, the deactivation of the oligomerization catalyst is carried out after the oligomerization of 1-decene and before the catalytic hydrogenation of the oligomerization products. Advantageously, the deactivation of the catalyst is carried out by the action of air or water or by means of at least one alcohol or a solution of deactivating agent. Preferably, the deactivation of the catalyst is carried out using at least one alcohol, for example isopropanol.
    [0026] Also preferably, the process according to the invention may comprise a final hydrogenation step of the tetramer fraction comprising more than 50% by weight of 1-decene tetramer of formula (I). This final hydrogenation is carried out in the presence of hydrogen (H2) and a hydrogenation catalyst.
    [0027] Preferably, the hydrogenation catalyst is chosen from a palladium derivative, a supported palladium derivative, a palladium derivative supported on alumina (for example on gamma-alumina), a nickel derivative or a supported nickel derivative. , a nickel derivative supported on kieselguhr, a platinum derivative, a supported platinum derivative, a cobalt-molybdenum derivative, a supported cobalt-molybdenum derivative. More preferably, the hydrogenation catalyst comprises palladium. A particularly preferred catalyst comprises palladium supported on alumina (for example on gamma-alumina). The hydrogenation catalyst is advantageously identical to the hydrogenation catalyst used during the hydrogenation following the oligomerization of 1-decene.
    [0028] Advantageously, during the final hydrogenation, the hydrogen pressure (H 2) is 5 to 50 bar or 10 to 40 bar, preferably 15 to 25 bar. Also advantageously, during the final hydrogenation, the duration of the hydrogenation is between 2 and 600 min, preferably between 30 and 300 min. Advantageously, during the final hydrogenation, the temperature ranges from 50 to 200 ° C or from 60 to 150 ° C. Preferably, the temperature is 70 to 140 ° C or 80 to 120 ° C. Preferably, the oil according to the invention is prepared according to a process for which the oligomerization of 1-decene is carried out in a time ranging from 2 to 300 min or from 5 to 180 min or from 30 to 140 min; or the oligomerization of 1-decene is carried out in the presence of hydrogen (H2) at a partial pressure ranging from 0.1 to 20 bar or from 1 to 6 bar; or the oligomerization is carried out in a weight ratio hydrogen / 1-decene greater than 100 ppm or less than 600 ppm or between 100 and 600 ppm; or the oligomerization of 1-decene is carried out at a temperature of 50 to 200 ° C or 70 to 160 ° C or 80 to 150 ° C or 9 (11140 ° C or 100 to 130 ° C) or the metallocene catalyst is a racemic compound of formula (II) L (Q1) (Q2) MR1R2 (II) in which o M represents a transition metal selected from titanium, zirconium, hafnium, and vanadium or represents zirconium and, (c) substituted or unsubstituted, independently represent a tetrahydroindenyl ring group or Q1 and Q2 independently represent a tetrahydroindenyl ring group and are bonded to form a polycyclic structure; L represents a bridging divalent Cl-C20-alkyl group Q1 and Q2 orL represents a group selected from methylene (-CH2-), ethylene (-CH2-CH2-), methylmethylene (-CH (CH3) -), 1-methylethylene (-CH (CH3) -CH2-), n-propylene (-CH2-CH2-CH2-), 2-methylpropylene (-CH2-CH (CH3) -CH2-), 3-methylpropylene (-CH2- CH2-CH (CH3) -), n-butylene (-CH2-CH2-CH2-CH2-), 2-methylbutylene (-CH2-CH (CH3) -CH2-CH2-), 4-methylbutylene (-CH2- CH2-CH2-CH (CH3) -), pentylene and its isomers, hexylene and isomers thereof, heptylene and isomers thereof, octylene and isomers thereof, nonylene and isomers thereof, decylene and isomers thereof, undecylene and isomers thereof, dodecylene and isomers thereof ; R 1 and R 2, substituted or unsubstituted, independently represent an atom or a group selected from hydrogen, halogens (such as Cl and I), alkyl (such as Me, Et, nPr, iPr), alkenyl, alkynyl, haloalkyl haloalkenyl, haloalkynyl, silylalkyl, silylalkenyls, silylalkynyls, germylalkyl, germylalkenyl, germylalkynyl; or R1 and R2 together with M form a metallocycle comprising from 3 to 20 carbon atoms; or the metallocene catalyst is selected from rac-ethylene bis (tetrahydroindenyl) zirconium dimethyl and rac-ethylene bis (tetrahydroindenyl) zirconium dichloride; or the oligomerization of 1-decene is carried out in a solvent selected from a linear or branched hydrocarbon, a cyclic or non-cyclic hydrocarbon, an alkyl aromatic compound and mixtures thereof or in a solvent selected from butanes, pentanes, hexanes, heptanes, octanes, cyclopentane, cyclohexane, methylcyclopentane, methylcyclohexane, methylcycloheptane, toluene, xylene and mixtures thereof; or the activator compound is selected from an ionic activator and an oligomeric compound comprising residues of the formula -Al (R) -O- wherein R is independently a cyclic or linear Cl-C20 alkyl group; or the activator compound is selected from methylalumoxane, modified methylalumoxane, ethylalumoxane, isobutylalumoxane and mixtures thereof; or the activator compound is selected from dimethylanilinium triphenylcarbonium tetrakis (perfluorophenyl) borate (DMAB), dimethylanilinium tetrakis (perfluorophenyl) borate, tetrakis (perfluorophenyl) aluminate and mixtures thereof; or the coactivator compound is a trialkylaluminum derivative or a compound selected from triethyl aluminum (TEAL), triisobutyl aluminum (TIBAL), tri-methyl aluminum (TMA), tri-n-octyl aluminum and methyl-methyl-ethyl aluminum (MMEAL); or deactivation of the catalyst is effected by the action of air or water or by means of at least one alcohol or a deactivating agent solution; or the hydrogen pressure (H2) during the catalytic hydrogenation of the oligomerization products is 5 to 50 bar or 10 to 40 bar or 15 to 25 bar; or the hydrogenation catalyst is selected from a palladium derivative, a supported palladium derivative, a palladium derivative supported on alumina (for example on gamma-alumina), a nickel derivative, a supported nickel derivative, a a nickel derivative supported on kieselguhr, a platinum derivative, a supported platinum derivative, a cobalt-molybdenum derivative, a supported cobalt-molybdenum derivative; or the hydrogen pressure (H2) during the final hydrogenation of the majority by weight fraction of 1-decene tetramer of formula (I) ranges from 5 to 50 bar or from 10 to 40 bar or from 15 to 15 bar. 25 bar; or the duration of the hydrogenation during the final hydrogenation is between 2 and 600 min or between 30 and 300 min; or the final hydrogenation is carried out at a temperature of 50 to 200 ° C or 60 to 150 ° C or 70 to 140 ° C or 80 to 120 ° C or the hydrogenation catalyst, at the final hydrogenation of the tetramer fraction comprising more than 50% by weight of 1-decene tetramer of formula (I) is selected from a palladium derivative, a supported palladium derivative, a palladium derivative supported on alumina (eg gamma-alumina), a nickel derivative, a supported nickel derivative, a kieselguhr supported nickel derivative, a platinum derivative, a supported platinum derivative, a cobalt-molybdenum derivative, a cobalt-molybdenum derivative supported. More preferably, the oil according to the invention is prepared according to a method combining all of these characteristics. Preferably, the oil according to the invention is prepared according to a process comprising the oligomerization of 1-decene in the presence of hydrogen (H2), a metallocene catalyst and an activator compound or in the presence of hydrogen (H2), a metallocene catalyst, an activator compound and a coactivator compound; catalytic hydrogenation of the oligomerization products in the presence of hydrogen (H2) and of a catalyst selected from a hydrogenation catalyst and a hydrogenation catalyst comprising palladium; separation by distillation at reduced pressure of the fraction of tetramers comprising more than 50% by weight of 1-decene tetramer of formula (I). More preferably, the oil according to the invention is prepared according to a process combining all of these characteristics.
    [0029] More preferably, the oil according to the invention is prepared according to a process for which the oligomerization of 1-decene is carried out in a time ranging from 2 to 300 min or from 5 to 180 min or from 30 to 140 min. min; The oligomerization of 1-decene is carried out in the presence of hydrogen (H2) at a partial pressure ranging from 0.1 to 20 bar or from 1 to 6 bar; the oligomerization of 1-decene is carried out in a weight ratio hydrogen / 1-decene greater than 100 ppm or less than 600 ppm or between 100 and 600 ppm; or the oligomerization of 1-decene is carried out at a temperature of 50 to 200 ° C or 70 to 160 ° C or 80 to 150 ° C or 9 (11140 ° C or 100 to 130 ° C) the metallocene catalyst is a racemic compound of formula (II) L (Q1) (Q2) MR1R2 (II) in which o M represents a transition metal selected from titanium, zirconium, hafnium, and vanadium or represents zirconium; and Q 2, O c), substituted or unsubstituted, independently represent a tetrahydroindenyl ring group or Q1 and Q2 independently represent a tetrahydroindenyl ring group and are bonded to form a polycyclic structure; L is a bridging C 1 -C 20 -alkyl group Q 1 and Q 2 where L is a group selected from methylene (-CH 2 -), ethylene (-CH 2 -CH 2 -), methylmethylene (-CH (CH 3) - ), 1-methylethylene (-CH (CH3) -CH2-), n-propylene (-CH2-CH2-CH2-), 2-methylpropylene (-CH2-CH (CH3) -CH2-), 3-methylpropylene (- CH2-CH2-CH (CH3) -), n-butylene (-CH2-CH2-CH2-CH2-), 2-methylbutylene (-CH2-CH (CH3) -CH2-CH2-), 4-methylbutylene (- CH2-CH2-CH2-CH (CH3) -), pentylene and its isomers, hexylene and isomers thereof, heptylene and isomers thereof, octylene and isomers thereof, nonylene and isomers thereof, decylene and isomers thereof, undecylene and isomers thereof, dodecylene and its isomers; R 1 and R 2, substituted or unsubstituted, independently represent an atom or a group selected from hydrogen, halogens (such as Cl and I), alkyl (such as Me, Et, nPr, iPr), alkenyl, alkynyl, haloalkyl haloalkenyl, haloalkynyl, silylalkyl, silylalkenyls, silylalkynyls, germylalkyl, germylalkenyl, germylalkynyl; or R1 and R2 together with M form a metallocycle comprising from 3 to 20 carbon atoms; or the metallocene catalyst is selected from rac-ethylene bis (tetrahydroindenyl) zirconium dimethyl and rac-ethylene bis (tetrahydroindenyl) zirconium dichloride; the oligomerization of 1-decene is carried out in a solvent selected from a linear or branched hydrocarbon, a cyclic or non-cyclic hydrocarbon, an alkyl aromatic compound and mixtures thereof or in a solvent selected from butanes, pentanes, hexanes, heptanes octanes, cyclopentane, cyclohexane, methylcyclopentane, methylcyclohexane, methylcycloheptane, toluene, xylene and mixtures thereof; The activator compound is selected from an ionic activator and an oligomeric compound comprising residues of the formula -Al (R) -O- wherein R independently represents a linear or cyclic Cl-C20 alkyl group; or the activator compound is selected from methylalumoxane, modified methylalumoxane, ethylalumoxane, isobutylalumoxane and mixtures thereof; or the activator compound is selected from dimethylanilinium tetrakis (perfluorophenyl) borate, triphenylcarbonium tetrakis (perfluorophenyl) borate, dimethylanilinium tetrakis (perfluorophenyl) aluminate, and mixtures thereof; the coactivator compound is a trialkylaluminum derivative or a compound selected from triethyl aluminum (TEAL), triisobutyl aluminum (TIBAL), tri-methyl aluminum (TMA), tri-n-octyl aluminum; and methyl-methyl-ethyl aluminum (MMEAL); the deactivation of the catalyst is carried out by the action of air or water or by means of at least one alcohol or a solution of deactivating agent; or the hydrogen pressure (H2) during the catalytic hydrogenation of the oligomerization products is 5 to 50 bar or 10 to 40 bar or 15 to 25 bar; the hydrogenation catalyst is selected from a palladium derivative, a supported palladium derivative, a palladium derivative supported on alumina (for example on gamma-alumina), a nickel derivative, a supported nickel derivative, a derivative nickel supported on kieselguhr, a platinum derivative, a supported platinum derivative, a cobalt-molybdenum derivative, a supported cobalt-molybdenum derivative; the hydrogen pressure (H2) during the final hydrogenation of the majority by weight fraction of 1-decene tetramer of formula (I) ranges from 5 to 50 bar or from 10 to 40 bar or from 15 to 25 bar; bar; the duration of the hydrogenation during the final hydrogenation is between 2 and 600 min or between 30 and 300 min; the final hydrogenation is carried out at a temperature ranging from 50 to 200 ° C or from 60 to 150 ° C or from 70 to 140 ° C or from 80 to 120 ° C the hydrogenation catalyst, at the final hydrogenation of the tetramer fraction comprising more than 50% by weight of 1-decene tetramer of formula (I) is chosen from a palladium derivative, a supported palladium derivative, a palladium derivative supported on alumina (for example on gamma-alumina), a nickel derivative, a supported nickel derivative, a kieselguhr supported nickel derivative, a platinum derivative, a supported platinum derivative, a cobalt-molybdenum derivative, a supported cobalt-molybdenum derivative. In addition to the oligomerization steps of 1-decene, catalytic hydrogenation of the oligomerization products and separation by distillation at reduced pressure of the tetramer fraction comprising more than 50% by weight of 1-decene tetramer of formula (I ), the method according to the invention may advantageously comprise other steps. Thus, the process according to the invention can also combine all or part of the following steps: the prior preparation of 1-decene by catalytic oligomerization of ethylene; or deactivation of the catalyst after oligomerization of 1-decene or after catalytic hydrogenation of the oligomerization products; or recycling a dimeric fraction of 1-decene (e.g., 9-methyl nonadecane) separated by reduced pressure distillation and oligomerization with 1-decene of this 1-decene dimer fraction recycled, in the presence of hydrogen (H2), a metallocene catalyst and an activator compound or in the presence of hydrogen (H2), a metallocene catalyst, an activator compound and a compound -activator; or a final hydrogenation step of the tetramer fraction comprising more than 50% by weight of 1-decene tetramer of formula (I) in the presence of hydrogen (H2) and a catalyst selected from a catalyst of hydrogenation and a hydrogenation catalyst comprising palladium. The invention also relates to the use as base oil or lubricating base oil of an oil according to the invention. This use therefore relates to a low viscosity oil comprising more than 50% by weight of 9-methyl-11,13-dioctyltricosane, 1-decene tetramer of formula (I). The invention also relates to the use of an oil according to the invention for improving the Fuel Eco (FE) of a lubricant. It also relates to its use to reduce the fuel consumption of an engine or to reduce the fuel consumption of a vehicle engine. These uses also relate to an oil according to the invention as defined by its advantageous, particular or preferred characteristics and by its preparation process. The invention also relates to a lubricating composition comprising an oil according to the invention. This lubricating composition therefore comprises an oil of low viscosity comprising more than 50% by weight of 9-methyl-11,13-dioctyltricosane, 1-decene tetramer of formula (I). Advantageously, the composition according to the invention comprises at least 10% by weight or at least 20% by weight of an oil according to the invention. Also advantageously, the composition according to the invention comprises at least 30, 40, 50 or 60% by weight of an oil according to the invention. Also advantageously, the composition according to the invention comprises from 10 to 50% by weight, preferably from 10 to 40% by weight or from 15 to 30% by weight of at least one base oil according to the invention.
    [0030] Also advantageously, the composition according to the invention comprises an oil according to the invention and at least one other base oil. It may also comprise an oil according to the invention and at least one additive or an oil according to the invention, at least one other base oil and at least one additive.
    [0031] The lubricating composition according to the invention may comprise an oil according to the invention as defined by its advantageous, particular or preferred characteristics as well as by its preparation process. As another oil-base base oil according to the invention, the composition according to the invention may comprise an oil chosen from a Group III oil, a Group IV oil, a Group V oil, especially the esters and polyalkylene glycols (PAG). The lubricant composition according to the invention is particularly advantageous for use as a high performance lubricant for lubrication in the fields of motors, hydraulic fluids, gears, in particular bridges and transmissions. The invention also relates to the use of a lubricant composition according to the invention for improving the Fuel Eco (FE) of a lubricant. It also relates to its use to reduce the fuel consumption of an engine or to reduce the fuel consumption of a vehicle engine.
    [0032] The various aspects of the invention will be the subject of the following examples, which are provided by way of illustration. EXAMPLES An autoclave reactor equipped with an agitator, a temperature control system and inlets was used to introduce nitrogen, hydrogen and 1-decene. 1-decene (product of the company ICI or the company Acros) is used at a purity higher than 94%. It is purified on 3 A and 13 X molecular sieves (Sigma-Aldrich company). Before use, the molecular sieves used are pre-dried at 200 ° C. for 16 hours. The products are characterized by 1H NMR and two-dimensional gas chromatography (GCxGC). For the NMR, the PAO samples were diluted in deuterated chloroform and the NMR spectra were carried out at 300 K on 400 MHz Bruker spectrometers: 1H, 130, 3037949 HMQC (heteronuclear multiple quantum coherence) and HMBC (heteronuclear). multiple bond coherence). Two-dimensional chromatography is carried out in continuous mode by means of two apolar and polar columns. The entire effluent from the first column is separated in the second dimension. The separation of the compounds is governed by the volatility on the first column and by specific interactions (rr-rr type, dipolar interactions, etc.) on the second dimension. Depending on their viscosity, the samples are usually diluted twice in heptane. The chromatographic conditions were optimized to elute the PAOs prepared according to the invention. The samples were analyzed by GCxGC with cryogenic modulation (liquid nitrogen), programming of the first oven from 45 ° C (5 min) to 320 ° C (20 min) with a ramp of 3 ° C / min, a secondary oven programming of 60 ° C (5 min) up to 330 ° C (20 min) with a ramp of 3 ° C / min and data used according to the following operating conditions: 15 o 1st dimension: HP1, 25 m, ID 0.32 mm, film thickness: 0.17 μm; o 2nd dimension: BPX-50, 1.5m, ID 0.1mm, film thickness: 0.1pm; o injector: split 100: 1, volume injected: 0.1 pl; o detector: FID, 320 ° C; o temperature of the hot jet: 320 ° C; 80 ° C cold jet programming (3/0): 4.8 s modulation period Example 1 An 8 L autoclave reactor was used. a flow of nitrogen for one hour and then cooled to 110 ° C. Then, it is filled with 3500 ml of 1-decene under a stream of nitrogen, the temperature of the reactor is maintained at 110 ° C. and hydrogen (It) is introduced at a m / m H2 / 1-decene ratio of 414 ppm The catalyst is rac-ethylene bis (tetrahydroindenyl) zirconium dimethyl activated with dimethylanilinium tetrakis (perfluorophenyl) borate (DMAB) in a molar ratio B / Zr 1.75. Triisobutyl aluminum (TiBAI) is used as a co-activating compound in an Al / Zr molar ratio of 200. It makes it possible to trap impurities present in the reactor. introduction of the activated catalyst in a concentration of 17 μM with respect to the oligomerization solution.
    [0033] After 120 min, 5 mL of isopropanol was introduced to deactivate the catalyst.
    [0034] Thereafter, the reaction products are hydrogenated using a palladium catalyst supported on alumina (5 g of 5% w / w palladium on gamma-alumina with respect to the alumina produced by Alfa Aesar) and hydrogen (H2) at 20 bar, at a temperature of 100 ° C, to hydrogenate bilaterally (followed by NMR to control the removal of unsaturation). The oligomerization products and the fraction of tetramers comprising more than 50% by weight of 9-methyl-11,13-dioctyltricosane are then separated by distillation at reduced pressure (0.67 mbar) according to the ASTM D5236 standard, by means of a 15-tray theoretical column with a maximum temperature of 495 ° C. This distillation according to ASTM D5236 allows to isolate products whose boiling point is 475 and 495 ° C. The oil according to the invention obtained has a content of 9-methyl-11,13-dioctyltricosane equal to 72.73%.
    [0035] This oil according to the invention comprising more than 50% by weight of 9-methyl-11,13-dioctyltricosane has a kinematic viscosity at 100 ° C, measured according to ASTM D445, of 5.823 mm 2 s -1. The viscosity index of this oil is 144. Its volatility measured according to the CEC L-40-93 standard is 4.6% by weight and its dynamic viscosity (CCS) at -35 ° C., measured according to the ASTM standard. D5293, is 2,950 mPa.s. Its average molecular weight is 479 g / mol, calculated according to ASTM D2502. The characteristics of the oil according to the invention make it possible to obtain excellent lubricating, rheological, in particular cold and oxidation resistance properties, as well as Fuel Eco.
    [0036] Comparative Example 2 Identical measurements and characterizations were made from a commercial reference oil. It is a PAO oil (product Ineos Durasyn 166) prepared from olefins by acid catalysis.
    [0037] This reference PAO oil has a kinematic viscosity at 100 ° C, measured according to ASTM D445, of 5,864 mm 2 s -1. Its viscosity index is 137. Its volatility measured according to the CEC L-40-93 standard is 6.8% by weight and its dynamic viscosity (CCS) at -35 ° C., measured according to the ASTM D5293 standard, is 3 870 mPa.s. Its average molecular weight is 473 g / mol, calculated according to ASTM D2502.
    [0038] Furthermore, the specifications of this commercial oil are as follows: kinematic viscosity at 100 ° C., measured according to ASTM D445, from 5.7 to 6.1 mm.sup.-2; volatility measured according to CEC L-40-93 below 7% by mass. The oligomers present in this oil were characterized by 1H NMR and two-dimensional gas phase chromatography (GCxGC). The oligomeric distribution of this PAO is 34% by weight of the various C30 oligomers, 42 by weight of the various C40 oligomers and 15% by weight of the various C50 oligomers, the rest being composed of other oligomers.
    [0039] The process according to the invention thus makes it possible to prepare an oil whose properties are equivalent to or better than commercial PAO oils, in particular the viscosity index, the volatility or the dynamic viscosity at cold, which are much better for oils according to US Pat. 'invention.
    [0040] EXAMPLE 3 Preparation of a Lubricating Composition According to the Invention (1) and a Comparative Lubricating Composition (1) The lubricating compositions are prepared by mixing the oil according to Example 1 or a known PAO oil. with another Group III base oil, viscosity index improvers and a mixture of additives (dispersants, detergents including sulfonate, friction modifier, antioxidant, pour point improver, antiwear agent) . The lubricating compositions thus prepared are described in Table 1 (% by weight). Composition (1) Composition according to the comparative invention (1) base oil group III (grade 4) 64.09 64.09 base oil group IV PAO 6 (Ineos Durasyn 166) 0 20 oil (1) according to the invention Additive mixture 9.51 9.51 polymers 6.4 6.4 Table 1 The characteristics of the lubricating compositions prepared are evaluated and the results obtained are shown in Table 2. Composition (1) Composition according to US Pat. comparative invention (1) kinematic viscosity at 100 ° C (NF EN ISO 3104) (mm2.s-1) 8.156 8.227 viscosity number (ISO 2909) 172 171 HTHS Ravenfield at 150 ° C (CEC L-36-A-90 / ASTM D4741) (mPa. $) 2.62 2.61 Noack volatility (CEC L-40-93) (% m / m) 9.6 10.5 Dynamic viscosity (CCS) at -35 ° C (ASTM D5293 The lubricating compositions comprising the oil (1) according to the invention have improved properties with respect to the lubricating composition comprising a known PAO base oil. The dynamic viscosity at cold is lower. Noack volatility is improved.
    [0041] EXAMPLE 4 Preparation of a Lubricating Composition According to the Invention (2) and a Comparative Lubricating Composition (2) The lubricating compositions are prepared by mixing the oil according to Example 1 or a known PAO oil. with another Group III base oil, viscosity index improvers and a mixture of additives (dispersants, friction modifier, detergents including sulfonate, antioxidant, pour point improver, antiwear agent) . The lubricating compositions thus prepared are described in Table 3 (% by weight). Composition (2) Composition according to the comparative invention (2) base oil group III (grade 4) 65.7 65.7 base oil group IV PAO 6 (Ineos Durasyn 166) 0 15 3037949 24 oil (1) according to the Additive mixture 15.9 15.9 polymer 3,4 3,4 The characteristics of the lubricating compositions prepared are evaluated and the results obtained are shown in Table 4. Composition (2) Composition according to the invention comparative invention (2) kinematic viscosity at 100 ° C (NF EN ISO 3104) (mm2.s-1) 7.801 7.801 viscosity number (ISO 2909) 178 176 HTHS Ravenfield at 150 ° C (CEC L-36-A-90 / ASTM D4741) (mPa. $) 2.60 2.63 Noack volatility (CEC L-40-93) (% w / w) 10.6 11.0 dynamic viscosity (CCS) at -35 ° C (ASTM D5293 (Table 4) The lubricating compositions comprising the oil (1) according to the invention have improved properties with respect to the lubricating composition comprising a known PAO base oil. The viscosity index is higher. The dynamic viscosity at cold is lower. Noack volatility is improved.
    [0042] EXAMPLE 5 Evaluation of Properties for the Lubrication of a Vehicle Engine of a Lubricating Composition According to the Invention (1) and of a Comparative Lubricating Composition LI1 An EB2 (PSA Peugeot Citroën) Engine of 1.2 L of displacement (maximum power of 60 kW), driven by an electric motor generator. The lubricant composition (1) according to the invention and the comparative lubricating composition (1) are compared with a reference lubricant composition (grade SAE OW-20).
    [0043] Each friction measurement is carried out for approximately 12 hours and makes it possible to establish a detailed map of the friction torque induced by each lubricant composition. The tests are carried out according to the following sequence: rinsing the engine with a rinsing oil supplemented with detergents and then rinsing with the reference composition, measuring the friction torque at 4 temperatures with the reference composition, rinsing the engine with a rinsing oil supplemented with detergents and then rinsing with the lubricating composition to be evaluated, measuring the friction torque at the four temperatures with the lubricating composition to be evaluated, rinsing the engine with a rinsing oil supplemented with detergents and then rinsing with the reference oil, measurement of the frictional torque at 4 temperatures with the reference lubricant composition. Regime ranges and temperature levels were selected to cover the most representative operating points of the NEDC and WLTC certification cycles. The 4 temperature levels chosen are consistent with the cycles considered. The instructions used are as follows: 20 ° water temperature at engine outlet: Ramp oil temperature: air temperature at intake: 28 ° C ± 2 ° C, exhaust pressure: 100 mbar at 5,000 rpm. The drive torque and the indicated operating torque of the motor are then measured over the selected speed and temperature ranges. For each temperature, a temperature conditioning phase of 90 min is respected. The measurement starts when the oil and water temperatures reach the set temperature +/- 0.5 ° C. For each operating point, 4 measurements are averaged over 250 revolutions and the measurement of the friction torque on this point corresponds to the average of these 4 values. A thermal stabilization time of 5 minutes is observed after each ramp of regime or temperature. The friction gain is evaluated for each lubricant composition as a function of the temperature and engine speed and then compared to the friction measured for the reference lubricant composition. Friction gains can be positive or negative, it is then a loss. The results in friction gains obtained between the composition 35 ° C / 50 ° C 80 ° C / 95 ° C ± 2 ° C, 35 ° C / 50 ° C / 80 ° C / 115 ° C ± 2 ° C, 3037949 26 lubricant (1) according to the invention and the comparative lubricating composition (1) are shown in Table 5. engine outlet water temperature / oil temperature of the ramp friction gain (%) 35 ° C / 35 ° C 1.86 50 ° C / 50 ° C 1.04 80 ° C / 80 ° C 0.58 95 ° C 115 ° C 0.81 Table 5 It is found that the lubricant composition (1) according to the invention allows a significant friction gain compared to the comparative lubricant composition (1) at different operating temperatures. From these friction gains and after treatment with a transfer function, the friction gains on the NEDC and WLTC standard approval cycles resulting from the use of the lubricating compositions are evaluated. This transfer function is based on a vehicle model developed on the SimulationX application (ITI GmbH). This model takes into account the trace of the driving cycle considered (speed and gear ratio as a function of time), the driving and resistive forces applying to the vehicle, the characteristics of the powertrain (engine characteristics, gear ratios, inertia , etc.) and the data from the tests (friction mapping, water temperature rise and oil on the running cycle considered). The results in friction gain obtained between the lubricant composition (1) according to the invention and the comparative lubricating composition (1) are presented in Table 6. NEDC cycle gain gain (%) 1.17 WLTC cycle gain (%) ) 0,97 Table 6 The lubricating composition according to the invention therefore allows a significant friction gain compared to the comparative lubricating composition and therefore allows to consider a significant reduction in CO2 emissions.
    [0044] EXAMPLE 6 Evaluation of the Properties for the Lubrication of a Vehicle Engine of a Lubricating Composition According to the Invention (2) and a Comparative Lubrication Composition A 2.0-liter N20 (BMW) engine is used. cubic capacity (maximum power of 180 kW), driven by an electric motor generator. The lubricating composition (2) according to the invention and the comparative lubricating composition (2) are compared with a reference lubricating composition (grade SAE OW-30). The conditions of the evaluations are adapted to the conditions of Example 5. The instructions implemented are the following: 10 ^ water temperature at the motor outlet: 40 ° C / 60 ° C90 ° C / 110 ° C ± 2 ° Ramp oil temperature: 40 ° C / 60 ° C / 90 ° / 110 ° C ± 2 ° C; inlet air temperature: 21 ° C ± 2 ° C; the exhaust: 40 mbar at 4,000 rpm The friction gain is evaluated for each lubricant composition according to the temperature and the engine speed and then compared to the friction measured for the reference lubricant composition. The results in friction gains obtained between the lubricant composition (2) according to the invention and the comparative lubricant composition (2) are shown in Table 7. engine outlet water temperature / oil temperature of the ramp gain friction coefficient (%) ° C / 40 ° C 1.25 60 ° C / 60 ° C 1.22 90 ° C / 90 ° C 0.86 110 ° C / 110 ° C 0.77 Table 7 20 It can be seen that the lubricant composition (2) according to the invention allows a significant increase in friction with respect to the comparative lubricating composition (2) at different operating temperatures. From these friction gains, a reduction in CO2 emissions can be expected.
    权利要求:
    Claims (15)
    [0001]
    REVENDICATIONS1. A kinematic viscosity oil at 100 ° C., measured according to ASTM D445, ranging from 4 to 8 mm2.s-1, comprising more than 50% by weight of 1-decene tetramer of formula (I) (I)
    [0002]
    2. Oil according to claim 1 comprising from 50 to 99% by weight of 1-decene tetramer of formula (I), preferably from 60 to 95% by weight of 1-decene tetramer of formula (I), more preferably from 70 to 90% by weight of 1-decene tetramer of formula (I).
    [0003]
    3. Oil according to one of claims 1 and 2 comprising at least 65% by weight of 1-decene tetramer of formula (I), preferably at least 70% by weight of 1-decene tetramer of formula (I), more preferably at least 80% by weight of 1-decene tetramer of formula (I), still more preferably at least 90% by weight of 1-decene tetramer of formula (I).
    [0004]
    4. The oil according to claim 1, also comprising at least one other saturated oligomer of 1-decene, chosen from among the other saturated 1-decene tetramers; or * selected from other 1-decene saturated tetramers, 1-decene saturated dimers, 1-decene saturated trimers, 1-decene saturated pentamers, 1-decene hexamers.
    [0005]
    5. An oil according to any one of claims 1 to 4 comprising from 51 to 94.8% by weight of 1-decene tetramer of formula (I); from 0.1 to 10% by weight of at least one other saturated tetramer of 1-decene; from 0.1 to 10% by weight of at least one saturated trimer of 1-decene; And 5 to 25% by weight of at least one pentamer saturated with 1-decene or at least one saturated hexamer of 1-decene.
    [0006]
    6. Oil according to one of claims 1 to 5, 5 (a) the kinematic viscosity at 100 ° C, measured according to ASTM D445 standard is 5 to 7 mm2.s-1, preferably 5.4 to 6 5 mm 2 S-1; or (b) the viscosity index is greater than 130, preferably greater than or equal to 140; or of which 10
    [0007]
    7. Oil according to one of claims 1 to 5, the volatility measured according to ASTM D6375 is less than 6% by weight, preferably less than 5 ° / 0 by mass.
    [0008]
    8. The oil according to one of claims 1 to 7 comprising 1-decene tetramer of formula (I) and prepared by a process comprising oligomerization of 1-decene in the presence of hydrogen (H2), a metallocene catalyst and an activator compound or in the presence of hydrogen (I-12), a metallocene catalyst, an activator compound and a coactivator compound; Catalytic hydrogenation of the oligomerization products in the presence of hydrogen (H2) and of a catalyst selected from a hydrogenation catalyst and a hydrogenation catalyst comprising palladium; separation by distillation at reduced pressure of the fraction of tetramers comprising more than 50% by weight of 1-decene tetramer of formula (I). 25
    [0009]
    9. An oil according to any one of claims 1 to 7 comprising 1-decene tetramer of formula (I) and prepared according to the process of claim 8 further comprising pre-preparing 1-decene by catalytic oligomerization of ethylene; or deactivation of the catalyst after oligomerization of 1-decene or after catalytic hydrogenation of the oligomerization products; or recycling a dimeric fraction of 1-decene (for example 9-methyl nonadecane) separated by distillation at reduced pressure and oligomerization with 1-decene of this dimeric fraction of recycled 1-decene, in the presence of hydrogen (H2), a metallocene catalyst and an activator compound or in the presence of hydrogen (H2), a metallocene catalyst, an activator compound and a co-compound activator; or a final hydrogenation step of the tetramer fraction comprising more than 50% by weight of 1-decene tetramer of formula (I) in the presence of hydrogen (H 2) and of a catalyst selected from a catalyst of hydrogenation and a hydrogenation catalyst comprising palladium.
    [0010]
    10. An oil according to one of claims 1 to 7 comprising 1-decene tetramer of formula (I) and prepared according to the process of claims 8 or 9 for which 10 ^ the oligomerization of 1-decene is carried out in the presence of hydrogen (H2) at a partial pressure of from 0.1 to 20 bar, preferably from 1 to 6 bar; or the oligomerization is carried out at a mass ratio hydrogen / 1-decene greater than 100 ppm or less than 600 ppm the metallocene catalyst is a racemic compound of formula (II) L (Q1) (Q2) MR1R2 (II) wherein o M represents a transition metal selected from titanium, zirconium, hafnium, and vanadium, preferentially zirconium; Wherein Q1 and Q2, substituted or unsubstituted, independently represent a tetrahydroindenyl ring group or Q1 and Q2 independently represent a tetrahydroindenyl ring group and are linked to form a polycyclic structure; L represents a bridging C1-C20-divalent alkyl group Q1 and Q2, preferably a group selected from methylene (-61-12-), ethylene (-CH2-CH2-), methylmethylene (-CH (CH3) -) 1-methylethylene (-CH (CH3) -CH2-), n-propylene (-CH2-CH2-CH2-), 2-methylpropylene (-CH2-CI-1 (C1-13) -CH2-), 3- methylpropylene (-CH2-CH2-CH (CH3) -), n-butylene (-CH2-CH2-CH2-CH2-), 2-methylbutylene (-CH2-CH (Cl-13) -C1-12-Cl- 12-), 4-methylbutylene (-CH2-CH2-CH2-CH (CH3) -), pentylene and its isomers, hexylene and isomers thereof, heptylene and isomers thereof, octyiene and isomers thereof, nonylene and isomers thereof, decylene and its isomers, undecylene and its isomers, dodecylene and isomers thereof; R 1 and R 2, substituted or unsubstituted, independently represent an atom or a group selected from hydrogen, halogen (such as Cl and I), alkyl (such as Me, Et, nPr, iPr), alkenyl, alkynyl, haloalkyl, haloalkenyl, haloalkynyl, silylalkyl, silylalkenyls, silylalkynyls, germylalkyl, germylalkenyl, germylalkynyl; or R1 and R2 together with M form a metallocycle comprising from 3 to 20 carbon atoms; or the activator compound is chosen from an ionic activator and an oligomeric compound comprising residues of formula -Al (R) -O- in which R 10 independently represents a linear or cyclic C1-C20 alkyl group, preferably chosen from methylalumoxane, modified methylalumoxane, ethylalumoxane, isobutylalumoxane and mixtures thereof; or the activator compound is selected from dimethylanilinium tetrakis (perfluorophenyl) borate (DMAB), triphenylcarbonium tetrakis (perfluorophenyl) borate, dimethylanilinium tetrakis (perfluorophenyl) aluminate, and mixtures thereof; or the co-activating compound is a trialkylaluminium derivative, preferably chosen from triethyl aluminum (TEAL), tri-iso-butyl aluminum (T1BAL), trimethyl aluminum (TMA), tri-n-octyl aluminum and methyl-methyl- ethyl aluminum (MMEAL). 20
    [0011]
    11. Use as a base oil or lubricating base oil of a defined oil according to one of claims 1 to 10.
    [0012]
    12. Use of an oil defined in any one of claims 1 to 10 for improving the Fuel Eco (FE) of a lubricant or for reducing the fuel consumption of an engine or for reducing fuel consumption. a vehicle engine.
    [0013]
    13. Lubricating composition comprising - at least one base oil defined according to one of claims 1 to 10; or at least one base oil defined according to one of claims 1 to 10 and at least one other base oil; or - at least one base oil defined according to one of claims 1 to 10 and at least one additive; or at least one base oil as defined in one of claims 1 to 10, at least one other base oil and at least one additive. 3037949 32
    [0014]
    A lubricating composition according to claim 13 comprising at least 10% by weight or at least 20% by weight or at least 30% by weight or at least 40% by weight or at least 50% by weight or at least 60% by weight. weight, of at least one base oil according to one of claims 1 5 to 10; or 10 to 50% by weight, preferably 10 to 40% by weight or 15 to 30% by weight of at least one base oil according to one of claims 1 to 10.
    [0015]
    15. Use of a lubricant composition according to one of claims 13 or 14 for improving the fuel Eco (FE) of a lubricant, for reducing the fuel consumption of an engine or for reducing fuel consumption. a motor vehicle.
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    同族专利:
    公开号 | 公开日
    WO2017001442A1|2017-01-05|
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    引用文献:
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    EP0283922A2|1987-03-23|1988-09-28|Dow Corning Corporation|Siloxane-polyalphaolefin hydraulic fluid|
    EP0468109A1|1990-07-24|1992-01-29|Ethyl Petroleum Additives Limited|Biodegradable lubricants and functional fluids|
    EP1950278A1|2005-11-15|2008-07-30|Idemitsu Kosan Co., Ltd.|Lubricant composition for internal combustion engine|
    MY139205A|2001-08-31|2009-08-28|Pennzoil Quaker State Co|Synthesis of poly-alpha olefin and use thereof|
    WO2013055483A1|2011-10-10|2013-04-18|Exxonmobil Chemical Patents Inc.|Poly alpha olefin compositions and process to produce poly alpha olefin compositions|
    FR3021664B1|2014-05-30|2020-12-04|Total Marketing Services|LOW VISCOSITY LUBRICATING POLYOLEFINS|
    FR3021665B1|2014-05-30|2018-02-16|Total Marketing Services|PROCESS FOR THE PREPARATION OF LOW VISCOSITY LUBRICATING POLYOLEFINS|US11180709B2|2018-02-19|2021-11-23|Exxonmobil Chemical Patents Inc.|Functional fluids comprising low-viscosity, low-volatility polyalpha-olefin base stock|
    WO2021015172A1|2019-07-25|2021-01-28|出光興産株式会社|Saturated aliphatic hydrocarbon compound composition, lubricant composition, and method for producing saturated aliphatic hydrocarbon compound composition|
    CN111205910A|2020-01-09|2020-05-29|辽宁汽众润滑油生产有限公司|AB type composite-effect engine lubricating oil composition|
    法律状态:
    2016-05-24| PLFP| Fee payment|Year of fee payment: 2 |
    2016-12-30| PLSC| Search report ready|Effective date: 20161230 |
    2017-05-23| PLFP| Fee payment|Year of fee payment: 3 |
    2018-05-25| PLFP| Fee payment|Year of fee payment: 4 |
    2020-05-20| PLFP| Fee payment|Year of fee payment: 6 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1556039A|FR3037949B1|2015-06-29|2015-06-29|LOW VISCOSITY LUBRICATING POLYOLEFINS|FR1556039A| FR3037949B1|2015-06-29|2015-06-29|LOW VISCOSITY LUBRICATING POLYOLEFINS|
    EP16732667.7A| EP3313963A1|2015-06-29|2016-06-29|Low viscosity lubricating polyolefins|
    CN201680037790.8A| CN107922866A|2015-06-29|2016-06-29|Low viscosity lubricates polyolefin|
    US15/740,735| US20180187117A1|2015-06-29|2016-06-29|Low viscosity lubricating polyolefins|
    JP2017567774A| JP2018519393A|2015-06-29|2016-06-29|Low viscosity lubricating polyolefin|
    PCT/EP2016/065077| WO2017001442A1|2015-06-29|2016-06-29|Low viscosity lubricating polyolefins|
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