DE202013012619U1 - Lubricant composition comprising polyester - Google Patents

Abstract

A lubricant composition comprising A) at least one base lubricating oil, B) at least one polyester comprising reacting an entire mixture comprising phthalic acid, optionally in the form of its esters or anhydrides, and an alcohol mixture comprising 1-nonanol, monomethyloctanols, dimethylheptanols and monoethylheptanols, and subsequent hydrogenation of the entire mixture is obtainable, wherein the polyester has a determined according to DIN 51562-1 dynamic viscosity at 20 ° C in the range of 40 to 62 mPa · s, and C) lubricating oil additives, characterized in that the alcohol mixture is a proportion of 6 wt .-% to 16 wt .-% 1-nonanol, 25 wt .-% to 55 wt .-% monomethyloctanols, 10 wt .-% to 30 wt .-% dimethyl heptanols and 7 wt .-% to 15 wt. % Monoethylheptanols, based on the total weight of the alcohol mixture.

Description

The present invention relates to the novel use of polyesters obtainable by reacting a mixture comprising cyclohexane-1,2-dicarboxylic acid and an alcohol mixture comprising 1-nonanol, monomethyloctanols, dimethylheptanols and monoethylheptanols, followed by hydrogenation of the entire mixture Lubricants and a lubricant composition comprising these polyesters.

The commercially available lubricant compositions are made from a variety of different natural or synthetic components. The lubricant compositions contain base oils and other additives. The base oils often consist of mineral oils, highly refined mineral oils, alkylated mineral oils, poly-alpha-olefins (PAO), polyalkylene glycols, phosphate esters, silicone oils, diesters and esters of polyhydric alcohols.

At present, as base oil in lubricant compositions, preferably, Group II and Group III hydrotreated paraffinic mineral oil, synthetic GTL oil and poly-α-olefin are used. However, these base oils have a detrimental effect on sealing materials that are part of engines and mechanical power transmission units. In particular, the use of these base oils leads to the shrinkage of sealing materials such as acrylonitrile-butadiene rubber.

However, polyester is known to accelerate the expansion of these sealants. Therefore, specific polyesters are used in lubricant compositions to counteract the shrinkage effect of modern base oils.

DIDA (diisodecyl adipate), DITA (diisotridecyl adipate) and TMTC (trimethylolpropanol caprylate) are currently used for this purpose. The cloud points of these esters are -30 ° C, -20 ° C and -10 ° C, respectively.

Given the properties of existing polyesters, there is still a need to provide novel polyesters which exhibit improved low temperature properties, as evidenced by low cloud points, and at the same time, when used as a component of a lubricant composition, have overall beneficial properties of lubricant formulations such as dimensions of sealants such as acrylonitrile. Retained butadiene rubber.

It is therefore an object of the present invention to provide polyesters which exhibit improved low temperature properties as evidenced by low cloud points and, when used as a component of a lubricant composition, result in a high degree of expansion of sealant materials such as acrylonitrile butadiene rubber.

The object is achieved by using a polyester which comprises reacting an entire mixture comprising phthalic acid, optionally in the form of their esters or their anhydrides, and an alcohol mixture comprising 1-nonanol, monomethyloctanols, dimethylheptanols and monoethylheptanols, and then hydrogenating the entire mixture is available, wherein the polyester according to DIN 51562-1 has certain dynamic viscosity at 20 ° C in the range of 40 to 64 mPa · s, as a lubricant.

The according to DIN 51562-1 certain dynamic viscosity of the polyester at 20 ° C is preferably 42 to 62 mPa · s, more preferably 44 to 60 mPa · s.

The polyesters of the invention preferably have densities at 20 ° C according to DIN 51757 from 0.85 to 1.00 g / cm ³ , more preferably 0.90 to 0.98 g / cm ^3, and most preferably 0.94 to 0.96 g / cm ³ . The refractive index n _D ²⁰ according to DIN 51423 is preferably 1.455 to 1.469, more preferably 1.456 to 1.468, and most preferably 1.460 to 1.466.

The alcohol mixture used according to the invention is particularly preferably obtainable in a multistage process starting from a hydrocarbon mixture containing butenes. In a first step, the butenes are dimerized to a mixture of isomeric octenes. The octene mixture is then hydroformylated to aldehydes ₉ C and then hydrogenated to give the alcohol mixture. In the case of this reaction sequence, specific, defined boundary conditions must be observed, at least in the butene dimerization, preferably in the butene dimerization and the hydroformylation.

Thus, it is preferred that the mixture of isomeric octenes be obtained by contacting a hydrocarbon mixture containing butenes with a nickel oxide-containing heterogeneous catalyst. Preferably, the isobutene content of the hydrocarbon mixture is 5 wt% or less, more preferably 3 wt% or less, more preferably 2 wt% or less, and most preferably 1.5 wt% or less, each based on the total net salary. A suitable hydrocarbon stream is the so-called C _{4 cut} , a mixture of butenes and butanes, available in large quantities from FCC plants or steam crackers. As a particularly preferred starting material, the so-called raffinate II is used, which is an isobutene-depleted C _{4 cut} .

A preferred feedstock contains from 50 to 100 wt%, preferably from 80 to 95 wt%, butenes and from 0 to 50 wt%, preferably from 5 to 20 wt%, of butanes. As a general quantitative framework, the following composition of the butene fraction can be cited: 1-butene From 1 to 98% by weight, cis-2-butene From 1 to 50% by weight, trans-2-butene 1 to 98 wt .-% and isobutene up to 5% by weight.

As a catalyst are known per se, nickel oxide catalysts, such as. B. from O'Connor et al. in Catalysis Today, 6, (1990) p. 329 are described. Supported nickel oxide catalysts can be used, suitable as support materials silica, alumina, aluminosilicates, aluminosilicates with layer structure and zeolites. Particularly suitable are precipitation catalysts obtained by mixing aqueous solutions of nickel salts and silicates, eg. Example of sodium silicate and sodium nitrate, and optionally other ingredients such as aluminum salts, for. As aluminum nitrate, and calcination are available.

Particular preference is given to catalysts which consist essentially of NiO, SiO ₂ , TiO ₂ and / or ZrO ₂ and optionally Al ₂ O ₃ . Most preferred is a catalyst containing as essential active ingredients 10 to 70% by weight of nickel oxide, 5 to 30% by weight of titanium dioxide and / or zirconium dioxide, 0 to 20% by weight of alumina and the remainder silica. Such a catalyst is obtainable by precipitating the catalyst mass at pH 5 to 9 by adding a nickel nitrate-containing aqueous solution to an alkali water glass solution containing titania and / or zirconia, filtering, drying and tempering at 350 to 650 ° C. For the preparation of these catalysts is in detail to the DE-A 4 339 713 directed. The disclosure of this document is incorporated by reference.

The contacting of the butene-containing hydrocarbon mixture with the catalyst is preferably carried out at temperatures of 30 to 280 ° C, in particular 30 to 140 ° C and particularly preferably from 40 to 130 ° C. It is preferably carried out at a pressure of 10 to 300 bar, in particular from 15 to 100 bar and particularly preferably from 20 to 80 bar. The pressure is expediently adjusted so that the olefin-rich hydrocarbon mixture is liquid or in the supercritical state at the selected temperature.

Suitable reaction apparatuses for contacting the hydrocarbon mixture with the heterogeneous catalyst are, for. B. tube bundle reactors or shaft furnaces. Due to the lower investment costs, shaft furnaces are preferred. The dimerization may be carried out in a single reactor, wherein the oligomerization catalyst may be disposed in one or more fixed beds in the reactor. Alternatively, a reactor cascade of several, preferably two reactors connected in series can be used, wherein the butene dimerization in the reaction mixture is only operated up to a partial conversion when passing the reactor or reactors connected upstream of the last reactor of the cascade and the desired final conversion only on passage of the reaction mixture is achieved by the last reactor of the cascade. The butene dimerization is preferably carried out in an adiabatic reactor or an adiabatic reactor cascade.

After leaving the reactor or the last reactor of a cascade, the octenes formed and optionally higher oligomers are separated from the unreacted butenes and butanes in the reactor discharge. The oligomers formed can be purified in a subsequent vacuum fractionation step to yield a pure octene fraction. To a small extent, dodecenes are usually also obtained in butene dimerization. These are preferably separated from the octenes before further reaction.

In a preferred embodiment, the reactor effluent freed from the oligomers formed, which consists essentially of unreacted butenes and butanes, is completely or partly recycled. It is preferred to choose the Rückführverhaltnis so that the concentration of oligomers in the reaction mixture 35 wt .-%, preferably 20 wt .-%, based on the reaction hydrocarbon mixture does not exceed. This measure increases the selectivity of butene dimerization with respect to such octenes, which after hydroformylation, hydrogenation and esterification provide a particularly preferred alcohol mixture.

The octenes obtained are converted in the second step in a conventional manner by hydroformylation with synthesis gas in a C atom extended aldehydes. The hydroformylation of olefins for the preparation of aldehydes is known per se and z. In J. Falbe (ed.): New Synthesis with Carbon Monoxides, Springer, Berlin, 1980 described. The hydroformylation takes place in the presence of catalysts homogeneously dissolved in the reaction medium. As catalysts, compounds or complexes of metals of VIII. Subgroup, especially Co, Rh, Ir, Pd, Pt or Ru compounds or complexes are generally used, the unmodified or z. B. may be modified with amine or with phosphine-containing compounds.

In the context of the present invention, the hydroformylation is preferably carried out in the presence of a cobalt catalyst, in particular dicobaltoctacarbonyl [Co ₂ (CO) ₈ ]. It is preferably carried out at temperatures of 120 to 240 ° C, in particular 160 to 200 ° C, and under a synthesis gas pressure of 150 to 400 bar, in particular 250 to 350 bar. The hydroformylation is preferably carried out in the presence of water. The mixing ratio of hydrogen to carbon monoxide in the synthesis gas used is preferably in the range of 70:30 to 50:50, in particular 65:35 to 55:45.

The cobalt-catalyzed hydroformylation process can be carried out as a multi-stage process comprising the following 4 stages: preparation of the catalyst (precarbonylation), catalyst extraction, olefin hydroformylation and removal of the catalyst from the reaction product (decobalting). In the first stage of the process, the precarbonylation, starting from an aqueous cobalt salt solution, for. As cobalt formate or cobalt acetate, prepared by reaction with carbon monoxide and hydrogen required for the hydroformylation catalyst complex. In the second stage of the process, the catalyst extraction, the cobalt catalyst prepared in the first process stage is extracted from the aqueous phase with an organic phase, preferably with the olefin to be hydroformylated. Sometimes it is expedient, in addition to the olefin, the reaction and by-products of the hydroformylation, if they are water-insoluble and liquid under the selected reaction conditions, to use for catalyst extraction. After the phase separation, the organic phase loaded with the cobalt catalyst is fed to the third process stage, hydroformylation. In the fourth stage of the process, decobalting, the organic phase of the reactor effluent is freed from the cobalt carbonyl complexes in the presence of process water, which may contain formic acid or acetic acid, by treatment with oxygen or air. In this case, the cobalt catalyst is oxidatively destroyed and the resulting cobalt salts are back-extracted into the aqueous phase. The resulting aqueous cobalt salt solution from the decobalting is recycled to the first process stage, the precarbonylation. The crude hydroformylation product obtained can be fed directly to the hydrogenation. Alternatively, it can in the usual way, for. B. by distillation, a C ₉ fraction are isolated, which is fed to the hydrogenation.

The formation of the cobalt catalyst, the extraction of the cobalt catalyst into the organic phase and the hydroformylation of the olefins can also be carried out in a one-step process in the hydroformylation reactor.

Useful cobalt compounds are, for example, cobalt (II) chloride, cobalt (II) nitrate, their amine or hydrate complexes, cobalt carboxylates such as cobalt formate, cobalt acetate, cobalt ethylhexanoate and cobalt naphthenate (co-salts of naphthenic acid), and the cobalt caprolactamate complex. Under the hydroformylation conditions, the catalytically active cobalt compounds in the form of cobalt carbonyls are formed in situ. It is also possible to use the carbonyl complexes of cobalt, such as dicobalt octacarbonyl, tetracobalt dodecacarbonyl and hexacobalt hexadecacarbonyl.

The aldehyde mixture obtained in the hydroformylation is reduced to primary alcohols. In general, partial reduction already occurs under the hydroformylation conditions, and the hydroformylation can also be controlled to provide substantially complete reduction. In general, however, the resulting hydroformylation product is hydrogenated in a further process step with hydrogen gas or a hydrogen-containing gas mixture. The hydrogenation usually takes place in Presence of a heterogeneous hydrogenation catalyst instead. As the hydrogenation catalyst, any suitable catalyst for hydrogenating aldehydes to primary alcohols can be used. Examples of suitable commercially available catalysts are copper chromite, cobalt, cobalt compounds, nickel, nickel compounds, optionally containing small amounts of chromium or other promoters, and mixtures of copper, nickel and / or chromium. The nickel compounds are generally supported on support materials such as alumina or diatomaceous earth. Furthermore, noble metals, such as platinum or palladium-containing catalysts can be used.

The hydrogenation can suitably be carried out in trickle mode, wherein the mixture to be hydrogenated and the hydrogen gas or the hydrogen-containing gas mixture z. B. are passed in cocurrent over a fixed bed of the hydrogenation catalyst.

The hydrogenation preferably takes place at a temperature of 50 to 250 ° C, in particular 100 to 150 ° C, and a hydrogen pressure of 50 to 350 bar, in particular 150 to 300 bar instead. From the reaction product obtained in the hydrogenation, the desired isononanol fraction can be separated by fractional distillation of the C ₈ hydrocarbons and higher-boiling products.

By gas chromatographic analysis of the alcohol mixture obtained, the relative amounts of the individual compounds can be obtained (where the percentages are area percent of the gas chromatogram):
the proportion of 1-nonanol in the alcohol mixture according to the invention is preferably 6 to 16 wt .-%, more preferably 8 to 14 wt .-%, based on the total weight of the alcohol mixture.

The proportion of monomethyloctanols is preferably 25 to 55 wt .-%, more preferably 35 to 55 wt .-%, with 6-methyl-1-octanol and 4-methyl-1-octanol together more preferably at least 25 wt .-% and most preferably at least 35 wt .-%, based on the total weight of the alcohol mixture make up.

The proportion of the dimethylheptanols and monoethylheptanols is preferably 15 to 60% by weight, more preferably 20 to 55% by weight, with 2,5-dimethyl-1-heptanol, 3-ethyl-1-heptanol and 4,5-dimethyl 1-heptanol together preferably at least 15 wt .-% and in particular 20 wt .-%, based on the total weight of the alcohol mixture make up. The proportion of hexanols is preferably 4 to 10 wt .-% and more preferably 5 to 10 wt .-%, based on the total weight of the alcohol mixture.

The alcohol mixture according to the invention preferably consists of 70 to 100%, more preferably 70 to 98%, most preferably 80 to 98% and even more preferably 85 to 95% of a mixture of 1-nonanol, monomethyloctanols, dimethylheptanols and monoethylheptanols, based on the Total weight of the alcohol mixture.

Preferably, the alcohol mixture contains a proportion of 6 wt .-% to 16 wt .-% 1-nonanol, 25 wt .-% to 55 wt .-% monomethyloctanols, 10 wt .-% to 30 wt .-% dimethyl heptanols and 7 wt .-% to 15 wt .-% monoethylheptanols, based on the total weight of the alcohol mixture.

Preferably, the alcohol mixture is in a molar ratio in the range of 1.1 to 2: 1, more preferably in a molar ratio in the range of 1: 1 to 1.3: 1, with respect to phthalic acid, optionally in the form of their esters or their anhydrides.

Preferably, the alcohol mixture contains a proportion of 6.0 to 16.0 wt .-%, preferably 7.0 to 15.0 wt .-%, particularly preferably 8.0 to 14.0 wt .-%, n-nonanol; From 12.8 to 28.8% by weight, preferably from 14.8 to 26.8% by weight, more preferably from 15.8 to 25.8% by weight, of 6-methyl-octanol; From 12.5 to 28.8% by weight, preferably from 14.5 to 26.5% by weight, more preferably from 15.5 to 25.5% by weight, of 4-methyl-octanol; From 3.3 to 7.3% by weight, preferably from 3.8 to 6.8% by weight, more preferably from 4.3 to 6.3% by weight, of 2-methyl-octanol; From 5.7 to 11.7% by weight, preferably from 6.3 to 11.3% by weight, particularly preferably from 6.7 to 10.7% by weight, of 3-ethylheptanol; From 1.9 to 3.9% by weight, preferably from 2.1 to 3.7% by weight, particularly preferably from 2.4 to 3.4% by weight, of 2-ethylheptanol; From 1.7 to 3.7% by weight, preferably from 1.9 to 3.5% by weight, more preferably from 2.2 to 3.2% by weight, of 2-propylhexanol; 3.2 to 9.2 wt .-%, preferably 3.7 to 8.7 wt .-%, particularly preferably 4.2 to 8.2 wt .-%, 3,5-dimethylheptanol; 6.0 to 16.0 wt.%, Preferably 7.0 to 15.0 wt.%, Particularly preferably 8.0 to 14.0 wt.%, 2,5-dimethylheptanol; From 1.8 to 3.8% by weight, preferably from 2.0 to 3.6% by weight, more preferably from 2.3 to 3.3% by weight, of 2,3-dimethylheptanol; 0.6 to 2.6% by weight, preferably 0.8 to 2.4% by weight, particularly preferably 1.1 to 2.1% by weight, of 3-ethyl-4-methylhexanol; 2.0 to 4.0% by weight, preferably 2.2 to 3.8% by weight %, more preferably 2.5 to 3.5% by weight, 2-ethyl-4-methylhexanol; 0.5 to 6.5% by weight, preferably 1.5 to 6% by weight, more preferably 1.5 to 5.5% by weight, of other alcohols having 9 carbon atoms; wherein the total sum of the components is 100% by weight.

The density of the alcohol mixture according to the invention at 20 ° C. is preferably 0.75 to 0.9 g / cm ³ , more preferably 0.8 to 0.88 g / cm ³ and most preferably 0.82 to 0.84 g / cm ³ . The refractive index n _D ²⁰ is preferably 1.425 to 1.445, more preferably 1.43 to 1.44, and most preferably 1.432 to 1.438. The boiling range at normal pressure is preferably 190 to 220 ° C, more preferably 195 to 215 ° C and most preferably 200 to 210 ° C.

The preparation of the polyesters according to the invention is carried out in a manner known per se (see, for example "Ullmann's Encyclopedia of Industrial Chemistry", 5th Edition, VCH Verlagsgesellschaft mbH, Weinheim, Volume A1, pp. 214 ff. And Volume A9, pp. 572-575 ). The chain length and average molecular weight of the polyesters can be adjusted in a targeted manner by adding the time and quantity of the alcohol mixture, which can easily be determined routinely by the person skilled in the art. Suitable catalysts are conventional esterification catalysts, in particular dialkyl titanates ((RO) ₂ TiO ₂ , where R is, for example, isopropyl, n-butyl or isobutyl), methanesulfonic acid and sulfuric acid; more preferably, the catalyst is isopropyl n-butyl titanate.

In a preferred embodiment, phthalic acid and the total amount of the alcohol mixture are initially charged in the reaction vessel. This reaction mixture is first heated to 100-140 ° C and homogenized by stirring. Thereafter, it is heated at normal pressure further to 160-190 ° C. The esterification with dehydration is preferably at about 150 ° C. The reaction water formed is separated by distillation through a column. If the alcohol mixture distils over, it is returned to the reaction vessel. Subsequently, the reaction vessel is heated to 200-250 ° C, and at a pressure of 150 to 300 mbar further reaction water is stripped by passing nitrogen through the reaction mixture. Residual water and excess alcohol mixture are stripped out by means of an increased nitrogen flow with stirring. Thereafter, the reaction mixture is filtered at 100-140 ° C.

The hydrogenation of the entire mixture is preferably carried out with a hydrogen-containing gas in the presence of a catalyst containing at least one metal of VIII. Subgroup of the Periodic Table as active metal alone or together with at least one metal of the I or VII. Subgroup of the Periodic Table, applied to a support , wherein the carrier has macropores.

In a preferred embodiment, the support has an average pore diameter of at least 50 nm and a BET surface area of at most 30 m ² / g, and the amount of the active metal is 0.01 to 30 wt .-%, based on the total weight of the catalyst ,

In a further embodiment, a catalyst is used wherein the amount of active metal is from 0.01 to 30% by weight based on the total weight of the catalyst, and from 10 to 50% of the pore volume of the support by macropores having a pore diameter in the range of 50 nm to 10,000 nm and 50 to 90% of the pore volume of the support are formed by mesopores having a pore diameter in the range of 2 to 50 nm, wherein the sum of the proportions of the pore volumes added to 100%.

In a further embodiment, the catalyst comprises 0.01 to 30 wt .-%, based on the total weight of the catalyst, of an active metal, supported on a support, wherein the carrier has an average pore diameter of at least 0.1 microns and a BET surface area of not more than 15 m ² / g. In principle, all carriers which have macropores, ie carriers which have exclusively macropores, as well as those which contain mesopores and / or micropores in addition to macropores, can be used as carriers.

In principle, all metals of subgroup VIII of the Periodic Table can be used as the active metal. The active metals used are preferably platinum, rhodium, palladium, cobalt, nickel or ruthenium or a mixture of two or more thereof, ruthenium in particular being used as the active metal. Among the metals of the I or VII subgroup or of the I and VII subgroups of the periodic table, all of which are also principally usable, preference is given to using copper and / or rhenium.

The terms "Macropores" and "mesopores" are used in the context of the present application as described in Pure Appl. Chem., 45, p. 79 (1976) are defined as pores whose diameter is above 50 nm (macropores), or whose diameter is between 2 nm and 50 nm (mesopores).

The content of the active metal is generally 0.01 to 30 wt .-%, preferably 0.01 to 5 wt .-%, particularly preferably 0.1 to 5 wt .-%, each based on the total weight of the catalyst used.

The polyester of the present invention can be used as a lubricant in industrial oils. The industrial oils can be selected from the group of light, medium and heavy duty engine oils, engine oils, marine engine oils, crankshaft oils, compressor oils, refrigeration oils, hydrocarbon compressor oils, cryogenic oils and greases, high temperature lubricating oils and greases, wire rope lubricants, textile machinery oils, refrigeration oils, lubricants for aerospace, aviation turbine oils, gear oils, gas turbine oils, spindle oils, centrifugal oils, traction fluids, gear oils, plastic gear oils, automotive gear oils, truck gear oils, engine oils, engine oils, insulating oils, instrument oils, brake fluids, power transmission fluids, shock absorber oils, heat distribution medium oils, transformer oils, Greases, chain oils, drilling detergents for soil exploration, hydraulic oils, chainsaw oil and gun, pistol and rifle lubricants are selected.

The engineering oil may preferably contain other additives such as polymer thickeners, viscosity index improvers, antioxidants, corrosion inhibitors, detergents, dispersants, demulsifiers, defoamers, dyes, antiwear additives, EP (exteme pressure) additives, AW (antiwear) additives and friction modifiers.

Further, the engineering oil may contain other base oils and / or cosolvents such as mineral oils (Group I, II or III oils), poly-alpha-olefins, alkylnaphthalenes, mineral oil-soluble polyalkylene glycols, silicone oils, phosphate esters and / or other carboxylic acid esters.

Typical additives that are found in hydraulic oils are u. a. Dispersants, detergents, corrosion inhibitors, anti-wear agents, anti-foaming agents, friction modifiers, seal swell agents, demulsifiers, VI improvers and pour point depressants.

Examples of dispersants are polyisobutylene succinimides, polyisobutylene succinate esters and ashless Mannich base dispersants.

Examples of detergents are metal alkyl phenates, sulfurized metal alkyl phenates, metal alkyl sulfonates and metal alkyl salicylates.

Examples of anti-wear additives are organoborates, organophosphites, organic sulfur compounds, zinc dialkyldithiophosphates, zinc diaryldithiophosphates and phospho-sulfurated hydrocarbons.

Examples of friction modifiers are fatty acid esters and amides, organomolybdenum compounds, molybdenum dialkylthiocarbamates and molybdenum dialkyldithiophosphates.

An example of an antifoam agent is polysiloxane. Examples of rust inhibitors are polyoxyalkylene polyols, carboxylic acids or triazole components. Examples of VI improvers are olefin copolymers, polyalkyl methacrylates and dispersing olefin copolymers. An example of a pour point depressant is polyalkylmethacrylate.

The polyester of the present invention can be used as a lubricant in metalworking fluids.

Depending on the applications, eg. Undiluted oils or soluble oils, the metalworking fluid may contain additives known in the art to improve the properties of the composition in amounts ranging from 0.10 to 40% by weight. These additives include metal deactivators; Corrosion inhibitors; antimicrobial agents; Anti-corrosion agents; emulsifiers; coupler; Extreme pressure agent; Anti friction means; Rust inhibitors; polymeric substances; anti-inflammatory agents; bactericides; antiseptics; antioxidants; chelating agents; pH regulators; Anti-wear agents including active sulfur-containing wear protection additive packages; wherein a metalworking fluid additive package contains at least one of the additives listed above.

Depending on the end uses, small amounts of additives such as anti-fogging agents may optionally be added in an amount ranging from 0.05 to 5.0% by volume in one embodiment and less than 1% by weight in other embodiments. Non-limiting examples thereof are rhamsan gum, hydrophobic and hydrophilic monomers, styrene or hydrocarbyl-substituted hydrophobic and hydrophilic styrenic monomers, oil-soluble organic polymers having a molecular weight (viscosity average molecular weight) in the range of about 0.3 to over 4 million, such as isobutylene, styrene, alkyl methacrylate, ethylene In one embodiment, polymethyl methacrylate or poly (ethylene, -propylene, -butylene or -isobutylene) in the molecular weight range of 1 to 3 million is used.

For certain applications, a small amount of prior art foam inhibitors may also be added to the composition in an amount in the range of 0.02 to 15.0 weight percent. Non-limiting examples of these are polydimethylsiloxanes, often trimethylsilyl terminated, alkylpolymethacrylates, polymethylsiloxanes, an N-acylamino acid having a long chain acyl group and / or a salt thereof, an N-alkylamino acid having a long chain alkyl group and / or a salt thereof, simultaneously used with an alkylalkylene oxide and / or an acylalkylene oxide, acetylenediols and ethoxylated acetylenediols, silicones, hydrophobic substances (eg silica), fatty amides, fatty acids, fatty acid esters and / or organic polymers, modified siloxanes, polyglycols, esterified or modified polyglycols, polyacrylates, fatty acids, fatty acid esters, fatty alcohols , Fatty alcohol esters, oxoalcohols, fluorosurfactants, waxes such as ethylenebisbeneamide wax, polyethylene wax, polypropylene wax, ethylenebisbeneamide wax and paraffin wax. The foam control agents can be used with suitable dispersants and emulsifiers. Other active foam control agents are found in "Foam Control Agents" by Henry T. Kemer (Noyes Data Corporation, 1976), pages 125-162 ,

The metalworking fluid further includes anti-friction agents including overbased sulfonates, sulfurized olefins, chlorinated paraffins and olefins, sulfurized esterolefins, amine terminated polyglycols, and sodium dioctyl phosphate salts. In yet another embodiment, the composition further comprises corrosion inhibitors including carboxylic acid / boric acid diamine salts, carboxylic acid amine salts, alkanolamines and alkanolamine borates.

The metalworking fluid further comprises oil-soluble metal deactivators in an amount of 0.01 to 0.5% by volume (based on the final volume of oil). Non-limiting examples of these are triazoles or thiadiazoles, especially aryltriazoles such as benzotriazole and tolyltriazole, alkyl derivatives of such triazoles, and benzothiadiazoles such as R (C ₆ H ₃ ) N ₂ S where R is H or C ₁ to C ₁₀ alkyl.

A small amount of at least one antioxidant may be added in the range of 0.01 to 1.0% by weight. Non-limiting examples of these are amine or phenolic type antioxidants or mixtures thereof, e.g. Butylhydroxytoluene (BHT), bis-2,6-di-t-butylphenol derivatives, sulfur-containing hindered phenols, and sulfur-containing hindered bisphenol.

The metalworking fluid further comprises 0.1 to 20 wt% of at least one extreme pressure agent. Non-limiting examples of these are zinc dithiophosphate, molybdenum oxide sulfide dithiophosphate, molybdenum amine compounds, sulfurized oils and fats, sulfurized fatty acids, sulfurized esters, sulfurized olefins, dihydrocarbyl polysulfides, thiocarbamates, thioterpenes and dialkyl thiodipropionates.

• A) mindestens ein Grundschmieröl,
• B) mindestens einen Polyester, der durch Umsetzung eines gesamten Gemischs, das Phthalsäure, gegebenenfalls in Form ihrer Ester oder ihrer Anhydride, und ein Alkoholgemisch, das 1-Nonanol, Monomethyloctanole, Dimethylheptanole und Monoethylheptanole umfasst, und anschließende Hydrierung des gesamten Gemischs erhältlich ist, wobei der Polyester eine gemäß DIN 51562-1 bestimmte dynamische Viskosität bei 20°C im Bereich von 40 bis 62 mPa·s aufweist, und
• C) Schmieröladditive.

In another embodiment, the present invention relates to a lubricant composition comprising

• A) at least one base lubricating oil,
• B) at least one polyester obtainable by reacting an entire mixture comprising phthalic acid, optionally in the form of their esters or their anhydrides, and an alcohol mixture comprising 1-nonanol, monomethyloctanols, dimethylheptanols and monoethylheptanols, followed by hydrogenation of the entire mixture, wherein the polyester according to DIN 51562-1 has certain dynamic viscosity at 20 ° C in the range of 40 to 62 mPa · s, and
• C) Lubricating Oil Additives.

For the sake of clarity, any preferred embodiment relating to the use of the claimed polyester according to the invention also relates to the lubricant composition itself.

Preferably, the lubricant composition comprises from 0.1% to 50% by weight of component A, from 50% to 90% by weight of component B, and from 0.1% to 40% by weight of component C).

In another embodiment, the lubricant composition preferably comprises from 30% to 90% by weight of component A), from 0.1% to 50% by weight of component B), and from 0.1% to 40% by weight .-% component C).

More preferably, the lubricant composition comprises 50% by weight to 90% by weight of component A), 3.5% by weight to 45% by weight of component B) and 1.0% by weight to 30% by weight. Component C).

Most preferably, the lubricant composition comprises 60% by weight to 90% by weight of component A), 10% by weight to 25% by weight of component B) and 2.0% by weight to 20% by weight of the component C).

The viscosity of the lubricant composition at 40 ° C is preferably 60 to 140 mm ² / s, more preferably 70 to 130 mm ² / s and most preferably 80 to 120 mm ² / s, determined according to DIN 51562-1 ,

Preferably, the base lubricating oil is hydrorefined mineral oil and / or synthetic hydrocarbon oil. Preferably, the hydrotreated mineral oil is selected from the group consisting of hydro-refined naphthenic mineral oil and hydrotreated paraffinic mineral oil of API Base Oil Classification Group II and Group III. Preferably, the synthetic hydrocarbon oil is selected from the group consisting of isoparaffinic synthetic oil, synthetic GTL oil and poly-α-olefin (PAO) of API Base Oil Classification Group IV.

Preferably, the lubricating oil additives are selected from the group consisting of lubricity improvers, viscosity improvers, combustion improvers, corrosion and / or antioxidant agents, pour point depressants, extreme pressure agents, antiwear agents, anti-foaming agents, detergents, dispersants, antioxidants, and metal passivators.

Typical lubricity improvers are commercially available acid-based lubricity enhancers with fatty acids as a major component and ester-based lubricity enhancers with glycerol monofatty acid esters as the major components. These compounds may be used singly or in combination of two or more kinds. The fatty acids used in these lubricity improvers are preferably those containing as their main ingredient a mixture of unsaturated fatty acids having from about 12 to 22 carbon atoms, but preferably about 18 carbon atoms, i. H. Oleic acid, linoleic acid and linolenic acid.

Viscosity improvers are u. a. Polyisobutenes, polymethyacrylic acid esters, polyacrylic acid esters, diene polymers, polyalkylstyrenes, copolymers of alkenylaryl compounds and conjugated dienes, polyolefins and multifunctional viscosity improvers.

Pour point depressants are a particularly useful type of additive that is commonly included in the lubricating oils described herein and typically includes such substances as polymethacrylates, styrene-based polymers, cross-linked alkylphenols, or alkylnaphthalenes. For example, see page 8 of "Lubricant Additives" by CV Smalheer and R. Kennedy Smith (Lesius-Hiles Company Publishers, Cleveland, Ohio, 1967 ).

Corrosion inhibitors, extreme pressure agents and wear protection agents are u. a. dithiophosphoric; chlorinated aliphatic hydrocarbons; Boron-containing compounds including borate esters and molybdenum compounds.

Antifoams used to reduce or prevent the formation of stable foam include silicones or organic polymers. Examples of these and other antifoam compositions can be found in "Foam Control Agents" by Henry T. Kerner (Noyes Data Corporation, 1976), pages 125-162 , Additional antioxidants may also be included, typically of the aromatic amine or hindered phenol type. These and other additives that can be used in combination with the present invention are disclosed in U.S. Patent Nos. 4,136,074 and 5,402,035 U.S. Patent 4,582,618 (column 14, line 52 to column 17, line 16 inclusive).

Dispersants are well known in the lubes field and include primarily dispersants, sometimes referred to as "ashless", since they contain no ash-forming metals (prior to incorporation into a lubricant composition) and when added to one Lubricant composition usually contribute no ash-forming metals. Dispersants are characterized by a polar group attached to a relatively high molecular weight hydrocarbon chain.

One class of dispersants are Mannich bases. These are substances which are formed by condensation of a higher molecular weight alkyl-substituted phenol, an alkylene polyamine and an aldehyde such as formaldehyde and in the U.S. Patent 3,634,515 are described in more detail. Another class of dispersants are high molecular weight esters. These substances are similar to Mannich dispersants or the succinimides described below, except that they can be considered to have been prepared by reacting a hydrocarbyl acylating agent and a polyhydric aliphatic alcohol such as glycerine, pentaerythritol or sorbitol. Such substances are in the U.S. Patent 3,381,022 described in more detail. Other dispersants include polymeric dispersing additives, which are generally hydrocarbon-based polymers.

A preferred class of dispersants are the carboxylic dispersants. These include succinic acid-based dispersants which are the reaction product of a hydrocarbyl-substituted succinic acylating agent with an organic hydroxy compound or, in certain embodiments, an amine having at least one hydrogen atom attached to a nitrogen atom or a mixture of the hydroxy compound and the amine. The term "succinic acylating agent" refers to a hydrocarbyl-substituted succinic or succinic acid producing compound. Such substances typically include hydrocarbyl substituted succinic acid, succinic anhydrides, succinic esters (including half esters) and succinic acid halides. Succinimide dispersants are in the U.S. Patents 4,234,435 and 3,172,892 described in more detail.

The amines reacted with the succinic acylating agents to form the carboxylic dispersant composition can be monoamines or polyamines. The polyamines include, but are not limited to, alkylene polyamines such as ethylene polyamines (i.e., poly (ethyleneamines) e) such as ethylenediamine, triethylenetetramine, propylenediamine, decamethylenediamine, octamethylenediamine, di (heptamethylene) triamine, tripropylenetetramine, tetraethylenepentamine, trimethylenediamine, pentaethylenehexamine, di (trimethylene) triamine. Also suitable are higher homologs, as obtained by condensation of two or more of the above-mentioned Alkylenamine. Tetraethylenepentamines are particularly well suited.

Further, hydroxyalkyl-substituted alkyleneamines, d. H. Alkyleneamines having one or more hydroxyalkyl substituents on the nitrogen atoms and higher homologs obtained by condensation of the abovementioned Alkylenamine or hydroxyalkyl-substituted Alkylenamine by amino radicals or by hydroxy radicals.

The dispersants may be borated substances. Borated dispersants are well known and can be prepared by treatment with a borating agent such as boric acid. Typical conditions include heating the dispersant with boric acid at 100 to 150 ° C.

The amount of dispersant in a lubricant composition, if present, will typically be 0.5 to 10 weight percent or 1 to 8 weight percent or 3 to 7 weight percent. Its concentration in a concentrate will be increased accordingly, z. B. to 5 to 80 weight percent.

Detergents are generally salts of organic acids that are often overbased. Overbased metal salts of organic acids are well known to those skilled in the art and generally include metal salts in which the amount of metal present exceeds the stoichiometric amount. Such salts should have conversion levels greater than 100% (i.e., contain more than 100% of the theoretical amount of metal required to convert the acid to its "normal" or "neutral" salt). They are generally referred to as overbased, hyperalkalized or superalkalized salts and are usually salts of organic sulfuric acids, organic phosphoric acids, carboxylic acids, phenols or mixtures of two or more thereof. As will be apparent to those skilled in the art, mixtures of such overbased salts may also be used.

The overbased compositions can be prepared based on various well-known organic acid substances including sulfonic acids, carboxylic acids (including substituted salicylic acids), phenols, phosphonic acids, saligenins, salixarates and mixtures of two or more thereof.

The basic metal compounds used to prepare these overbased salts are typically an alkali or alkaline earth metal compound, although other basic metal compounds can be used. In general, compounds of Ca, Ba, Mg, Na and Li, such as their hydroxides and alkoxides lower alkanols used. Overbased salts containing a mixture of ions of two or more of these metals can be used.

Overbased substances are generally prepared by reacting an acidic substance (usually an inorganic acid or lower carboxylic acid such as carbon dioxide) with a mixture comprising an acidic organic compound, a reaction medium containing at least one inert organic solvent (mineral oil, naphtha, toluene , Xylene, etc.) for the acidic organic substance, comprising a stoichiometric excess of a metal base and a promoter.

The acidic substance used in the preparation of the overbased substance may be a liquid such as formic acid, acetic acid, nitric acid or sulfuric acid. Acetic acid is particularly suitable. It is also possible to use inorganic acid substances, such as HCl, SO ₂ , SO ₃ , CO ₂ or H ₂ S, eg. As CO ₂ or mixtures thereof, for. B. mixtures of CO ₂ and acetic acid.

Generally, the detergents may also be borated by treatment with a borating agent such as boric acid. Typical conditions include heating the detergent with boric acid at 100 to 150 ° C, the number of equivalents of boric acid being approximately equal to the number of equivalents of metal in the salt.

The amount of detergent component in a lubricant composition, if present, will typically be 0.5 to 10 weight percent, such as 1 to 7 weight percent or 1.2 to 4 weight percent. Its concentration in a concentrate will be increased accordingly, z. B. to 5 to 65 weight percent.

Examples of metal passivators are u. a. Tolyltriazole and its derivatives and benzotriazole and its derivatives. When metal passivators are used, they are typically present in the liquid composition in an amount of from 0.05 to 5 parts by weight, more typically from 0.05 to 2 parts by weight, based on the total weight of the liquid composition.

The following examples illustrate the invention in more detail without limiting it.

EXAMPLES

A) Preparation of a polyester according to the invention

A.1) butene dimerization

The butene dimerization was carried out continuously in an adiabatic reactor consisting of two partial reactors (length: 4 m each, diameter: 80 cm each) with intermediate cooling at 30 bar. The feedstock used was a raffinate II having the following composition: isobutane 2% by weight n-butane 10% by weight isobutene 2% by weight 1-butene 32% by weight trans-2-butene 37% by weight and cis-2-butene 17% by weight.

The catalyst used was a material according to DE-A 4339713 consisting of 50% by weight of NiO, 12.5% by weight of TiO ₂ , 33.5% by weight of SiO ₂ and 4% by weight of Al ₂ O ₃ , in the form of 5 × 5 mm tablets , The reaction was carried out at a rate of 0.375 kg raffinate II per liter of catalyst per hour at a recycle ratio of recycled unreacted C ₄ hydrocarbons to fresh raffinate II of 3, an inlet temperature at the 1st fractional reactor of 38 ° C and an inlet temperature at the 2nd fractional reactor of 60 ° C performed. The conversion, based on the butenes contained in the raffinate II, was 83.1%; the octene selectivity was 83.3%. By fractional distillation of the reactor effluent, the octene fraction was separated from unreacted raffinate II and the high boilers.

A.2) Hydroformylation and hydrogenation

750 g of the octene mixture prepared in Section A.1 of the Examples were batched in an autoclave with 0.13 wt .-% dicobaltoctacarbonyl Co ₂ (CO) ₈ as a catalyst with the addition of 75 g of water at 185 ° C and under a synthesis gas pressure of 280 bar reacted at a mixing ratio of H ₂ to CO of 60/40 5 hours. The consumption of synthesis gas, recognizable by a pressure drop in the autoclave, was supplemented by repressing. After the autoclave had been decompressed, the reaction effluent was freed from the cobalt catalyst by oxidative introduction of 10 wt.% Acetic acid, and the organic product phase was hydrogenated with Raney nickel at 125 ° C. and a hydrogen pressure of 280 bar for 10 h. By fractional distillation of the reaction, the isononanol fraction was separated from the C ₈ paraffins and the high boilers.

The composition of the isononanol fraction was analyzed by gas chromatography. A sample was previously trimethylsilylated with 1 ml of N-methyl-N-trimethylsilyl trifluoroacetamide per 100 μl sample for 60 minutes at 80 ° C. A separating column of the type Hewlett Packard Ultra 1 with a length of 50 m and an inner diameter of 0.32 mm and a film thickness of 0.2 μm was used. The injector temperature and detector temperature were 250 ° C, the oven temperature was 120 ° C. The split was 110 ml / min. The carrier gas was nitrogen. The pre-pressure was set to 200 kPa. 1 μl of the sample was injected and detected by FID. The following sample compositions (area percent of the gas chromatogram) were determined by this method: 11.0% 1-nonanol 20.8% 6-methyl-1-octanol 20.5% 4-methyl-1-octanol 5.3% 2-meth-1-octanol 11.0% 2,5-dimethyl-1-heptanol 8.7% 3-ethyl-1-heptanol 6.2% 4,5-dimethyl-1-heptanol 2.9% 2-ethyl-1-heptanol 2.8% 2,3-dimethyl-1-heptanol 3.0% 2-ethyl-4-methyl-1-hexanol 2.7% 2-propyl-1-hexanol 1.6% 3-ethyl-4-methyl-1-hexanol

The density of this Isononanolgemischs was measured at 20 ° C to 0.8326 and the refractive index n _D ²⁰ to 1.4353. The boiling range at normal pressure was 204 to 209 ° C.

A.3) Esterification

viscosity measurement

The viscosity of the esters is determined in a standard test according to DIN 51562-1 certainly.

In the third process step, 865.74 g of the isononanol fraction obtained in process step 2 (20% excess based on phthalic anhydride) with 370.30 g of phthalic anhydride and 0.42 g of isopropylbutyl titanate as catalyst in a 2 liter autoclave under N ₂ -einperlung (10 l / h) reacted at a stirring speed of 500 U / min and a reaction temperature of 230 ° C. The formed reaction water was continuously removed from the reaction mixture with the N ₂ stream. The reaction time was 180 minutes. Subsequently, the isononanol excess was distilled off at a vacuum of 50 mbar. 1000 g of the crude polyester were neutralized with 150 ml of 0.5% sodium hydroxide solution by stirring at 80 ° C. for 10 minutes. It formed a two-phase mixture with an upper organic phase and a lower aqueous phase (waste liquor with hydrolyzed catalyst). The aqueous phase was separated and the organic phase washed twice with 200 ml of H ₂ O. For further purification, the neutralized and washed Polyester stripped with steam at 180 ° C and 50 mbar vacuum for 2 h. The purified polyester was then dried for 30 minutes at 150 ° C / 50 mbar by passing an N ₂ stream (2 l / h), then stirred for 5 minutes with activated charcoal and suction filtered through a suction filter with filter aid Supra-Theorit 5 (temperature 80 ° C).

The polyester obtained has a density of 0.973 g / cm ³ , a viscosity of 73.0 mPa · s and a refractive index n _D ²⁰ of 1.4853.

A.4) Hydrogenation of the ester

A meso / macroporous alumina support in the form of 4 mm extrudates having a BET surface area of 238 m ² / g and a pore volume of 0.45 ml / g was treated with an aqueous ruthenium (III) nitrate solution , which had a concentration of 0.8 wt .-%, soaked. 0.15 ml / g (about 33% of the total volume) of the pores of the carrier had a diameter in the range of 50 nm to 10,000 nm, and 0.30 ml / g (about 67% of the total pore volume) of the pores of the carrier had a pore diameter in the range from 2 to 50 nm. The volume of solution absorbed by the carrier during the impregnation corresponded approximately to the pore volume of the carrier used. Subsequently, the support impregnated with the ruthenium (III) nitrate solution solution was dried at 120 ° C. and activated (reduced) at 200 ° C. in a water stream. The catalyst thus prepared contained 0.5% by weight of ruthenium, based on the weight of the catalyst. A continuously operated plant consisting of two series-connected tubular reactors (main reactor 160 ml, d _inside = 12 mm, l = 1400 mm, and postreactor 100 ml, d _inside = 12 mm, l = 1000 mm) was filled with the catalyst described in the preparation example ( Main reactor 71.5 g, post-reactor 45.2 g). The main reactor was in trickle mode with circulation operations (liquid load 12 m / h), the downstream reactor in the straight pass in the upflow mode. The phthalic acid ester prepared in process step 3 was pumped through the reactor cascade with pure hydrogen at an average temperature of 128 ° C. in the main reactor and 128 ° C. in the after-reactor and a pressure of 200 bar (feed rate 66 g / h). The catalyst loading in the main reactor was 0.6 kg phthalic acid ester / l _cat. × h. Gas chromatographic analysis of the reactor effluent showed that the phthalate had been> 99.9% reacted.

The polyester obtained has a density of 0.936 g / cm ³ , a viscosity of 47 mPa · s at 20 ° C, determined according to DIN 51562-1 , and a refractive index n _D ²⁰ of 1.462.

B) Cloud point measurement

The cloud point of the ester according to Example A.4 was determined according to DIN ISO 3015 determined to -80 ° C.

C) Check compatibility with sealing material

The seal compatibility test with sealing material acrylonitrile-butadiene copolymer was carried out at 100 ° C over a period of 168 hours according to standard method ISO 1817 in the presence of the ester obtained as in A.4).

The sealing material showed a volume change of + 33.3% (expansion). D) Table 1: Lubricant Formulations A and B (all values in% by weight) Formulation A with DIDA Formulation B with ester according to Example A.4 PAO 6 (Nexbase ^® 2006 polyalphaolefin available from Neste Oil NV, Belgium) 52.0% 52.0% DIDA 10.0% - Ester according to Example A.4 - 10.0% Thickeners (Lubrizol ^® 8406, polyisobutylene, available from Lubrizol) 13.0% 13.0% Thickeners (Lubrizol ^® 8407 from Lubrizol) 13.0% 13.0% Additives (AnglamolR ^® 6004, additive package, available from Lubrizol) 12.0% 12.0% Viscosity at 40 ° C DIN 51562-1 113.8 mm ² / s 123.3 mm ² / s Viscosity at 100 ° C DIN 51562-1 16.7 mm ² / s 17.0 mm ² / s Viscosity Index (VI) ASTM D 2270 160 150 Density at 15 ° C DIN 51757 0.8660 g / ml 0.8686 g / ml cloud point DIN ISO 3015 -32.0 ° C <-80.0 ° C

DIDA example as Synative ^® ES DIDA by BASF SE, Ludwigshafen,.

The seal compatibility test with sealant acrylonitrile-butadiene copolymer was carried out at 100 ° C for a period of 168 hours according to the standard method ISO 1817 carried out in the presence of Formulation A or Formulation B.

The sealant exhibited a volume change of + 12.0% (extension) in the presence of Formulation A and a volume change of 12.6% (extension) in the presence of Formulation B.

QUOTES INCLUDE IN THE DESCRIPTION

This list of the documents listed by the applicant has been generated automatically and is included solely for the better information of the reader. The list is not part of the German patent or utility model application. The DPMA assumes no liability for any errors or omissions.

Cited patent literature

• DE 4339713 A [0015, 0093]
• US 4582618 [0075]
• US 3634515 [0077]
• US 3381022 [0077]
• US 4234435 [0078]
• US 3172892 [0078]

Cited non-patent literature

• DIN 51562-1 [0008]
• DIN 51562-1 [0009]
• DIN 51757 [0010]
• DIN 51423 [0010]
• O'Connor et al. in Catalysis Today, 6, (1990) p. 329 [0014]
• J. Falbe (ed.): New Synthesis with Carbon Monoxides, Springer, Berlin, 1980 [0020]
• "Ullmann's Encyclopedia of Industrial Chemistry", 5th Edition, VCH Verlagsgesellschaft mbH, Weinheim, Volume A1, p. 214 ff. And Volume A9, pp. 572-575 [0036]
• "Macropores" and "mesopores" are used in the context of the present application as described in Pure Appl. Chem., 45, p. 79 (1976) [0043]
• "Foam Control Agents" by Henry T. Kemer (Noyes Data Corporation, 1976), pages 125-162 [0057]
• DIN 51562-1 [0062]
• DIN 51562-1 [0068]
• "Lubricant Additives" by CV Smalheer and R. Kennedy Smith (Lesius-Hiles Company Publishers, Cleveland, Ohio, 1967 [0073]
• "Foam Control Agents" by Henry T. Kerner (Noyes Data Corporation, 1976), pages 125-162 [0075]
• DIN 51562-1 [0097]
• DIN 51562-1 [0101]
• DIN ISO 3015 [0102]
• DIN 51562-1 [0104]
• DIN 51562-1 [0104]
• ASTM D 2270 [0104]
• DIN 51757 [0104]
• DIN ISO 3015 [0104]
• ISO 1817 [0106]

Claims (10)

A lubricant composition comprising A) at least one base lubricating oil, B) at least one polyester comprising reacting an entire mixture comprising phthalic acid, optionally in the form of its esters or anhydrides, and an alcohol mixture comprising 1-nonanol, monomethyloctanols, dimethylheptanols and monoethylheptanols, and subsequent hydrogenation of the entire mixture is obtainable, wherein the polyester has a determined according to DIN 51562-1 dynamic viscosity at 20 ° C in the range of 40 to 62 mPa · s, and C) lubricating oil additives, characterized in that the alcohol mixture is a proportion of 6 wt .-% to 16 wt .-% 1-nonanol, 25 wt .-% to 55 wt .-% monomethyloctanols, 10 wt .-% to 30 wt .-% dimethyl heptanols and 7 wt .-% to 15 wt. % Monoethylheptanols, based on the total weight of the alcohol mixture. Lubricant composition according to claim 1, characterized in that the base lubricating oil is hydrorefined mineral oil and / or synthetic hydrocarbon oil. A lubricant composition according to claim 2, characterized in that the hydrotreated mineral oil is selected from the group consisting of hydrotreated naphthenic mineral oil and hydrotreated paraffinic mineral oil of API Base Oil Classification Group II and Group III. A lubricant composition according to claim 2, characterized in that the synthetic hydrocarbon oil is selected from the group consisting of isoparaffinic synthetic oil, synthetic GTL oil and poly-α-olefin (PAO) of API Base Oil Classification Group IV. Lubricant composition according to one or more of claims 1 to 4, characterized in that the polyester has a determined according to DIN 51562-1 dynamic viscosity at 20 ° C in the range of 40 to 60 mPa · s. Lubricant composition according to one or more of claims 1 to 5, characterized in that the alcohol mixture contains a proportion of 25 wt .-% to 55 wt .-% Monomethyloctanolen, based on the total weight of the alcohol mixture. Lubricant composition according to one or more of claims 1 to 6, characterized in that the alcohol mixture contains a proportion of 10 wt .-% to 30 wt .-% dimethyl heptanols, based on the total weight of the alcohol mixture. Lubricating composition according to one or more of Claims 1 to 7, characterized in that the lubricating oil additives are selected from the group consisting of lubricity improvers, viscosity improvers, combustion improvers, corrosion and / or oxidation inhibitors, pour point depressants, extreme pressure agents, antiwear agents, anti-foaming agents, detergents, dispersants, Antioxidants and metal passivators are selected. Lubricant composition according to one or more of claims 1 to 8, characterized in that the alcohol mixture is present in a molar ratio in the range of 1: 1 to 2: 1 with respect to phthalic acid, optionally in the form of their esters or their anhydrides. Lubricant composition according to one or more of claims 1 to 9, characterized in that it contains 0.1% by weight to 50% by weight of component A), 50% by weight to 90% by weight of component B) and 0, 1 wt .-% to 40 wt .-% component C).