KR20150086366A - Use of polyesters as lubricants - Google Patents

Abstract

The present invention relates to the reaction of a mixture comprising cyclohexane-1,2-dicarboxylic acid and an alcohol mixture comprising 1-nonanol, monomethyloctanol, dimethylheptanol and monoethylheptanol and the subsequent reaction of the total mixture To a novel use of a polyester obtainable by hydrogenation as a lubricant and to a lubricant composition comprising the polyester.

Description

USE OF POLYESTER AS LUBRICANTS [0002] USE OF POLYESTERS AS LUBRICANTS [0003]

The present invention relates to the reaction of a mixture comprising cyclohexane-1,2-dicarboxylic acid and an alcohol mixture comprising 1-nonanol, monomethyloctanol, dimethylheptanol and monoethylheptanol and the subsequent reaction of the total mixture To a novel use of a polyester obtainable by hydrogenation as a lubricant and to a lubricant composition comprising the polyester.

Commercial lubricant compositions are made from a number of different natural or synthetic ingredients. The lubricant composition comprises a base oil and further additives. 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.

Currently Group II and Group III hydro-refined (hydrorefined) paraffinic mineral oils, GTL synthetic oils and poly-alpha-olefins are preferably used as base oils in lubricant compositions. However, the base oil adversely affects the sealing material forming part of the engine and the mechanical transmission unit. In particular, the use of the base oil results in the shrinkage of sealing materials such as acrylonitrile butadiene rubber.

Polyesters, however, are known to accelerate the expansion of the sealing material. Thus, certain polyesters are used in the lubricant compositions to counteract the shrinking effect of modern base oils.

Currently, DIDA (diisodecyl adipate), DITA (diisotridecyl adipate) and TMTC (trimethylol propanol caprylate) are used to achieve this purpose. The melting point of the ester is -30 캜, -20 캜 and -10 캜, respectively.

When used as a component of a lubricant composition, in view of the properties of existing polyesters, an improved low temperature, expressed as a low haze, while maintaining the overall advantageous properties of a lubricant formulation such as the expansion of sealing materials such as acrylonitrile butadiene rubber There is a need to provide a novel polyester which exhibits the properties of a polyester.

It is therefore an object of the present invention to provide a polyester which exhibits improved low temperature properties represented by low haze and which, when used as a component of the lubricant composition, yields a high degree of swelling of the sealing material, such as acrylonitrile butadiene rubber to be.

The problem is solved by the reaction with a total mixture comprising phthalic acid (optionally in the form of its ester or an anhydride thereof) and an alcohol mixture comprising 1-nonanol, monomethyloctanol, dimethylheptanol and monoethylheptanol, Wherein the polyester has a dynamic viscosity at 20 DEG C in the range of from 40 to 64 mPa.s, measured according to DIN 51562-1, as a lubricant obtainable by subsequent hydrogenation of the total mixture, .

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

The polyester of the present invention preferably has a density at 20 占 폚 according to DIN 51757 of 0.85 to 1.00 g / cm3, more preferably 0.90 to 0.98 g / cm3, most preferably 0.94 to 0.96 g / cm3. The refractive index n _D ²⁰ according to DIN 51423 is preferably from 1.455 to 1.469, more preferably from 1.456 to 1.468, and most preferably from 1.460 to 1.466.

The alcohol mixture used according to the invention is particularly advantageously obtainable in a process starting from a hydrocarbon mixture comprising two or more stages and containing butene. In the first step, butene is dimerized to yield a mixture of isomeric octenes. Octene mixture after dihydro formate is milhwa calculate the C ₉ aldehyde, and then is hydrogenated to yield the alcohol mixture. In this reaction sequence, specific, prescribed parameters must be adhered during at least butene dimerization, preferably during butene dimerization and hydroformylation.

Thus, it is preferred that the isomeric octene mixture is obtained by contacting a hydrocarbon mixture comprising butene with a heterogeneous catalyst comprising nickel oxide. The isobutene content of the hydrocarbon mixture is in each case preferably not more than 5% by weight, in particular not more than 3% by weight, particularly preferably not more than 2% by weight, most preferably not more than 1.5% by weight, based on the total butene content. Suitable hydrocarbon streams are those known as C ₄ cuts which are a mixture of butene and butane available in large amounts from the FCC plant or from the steam cracker. A particularly preferred starting material used is known as raffinate II, which is an isobutene-dwarf C ₄ cut.

Preferred starting materials include 50 to 100% by weight, preferably 80 to 95% by weight of butene and 0 to 50% by weight, preferably 5 to 20% by weight of butane. The following makeup of Buten can be presented as a general guide to quantification:

  1-butene 1 to 98% by weight,

  cis-2-butene 1 to 50% by weight,

  trans-2-butene 1 to 98% by weight, and

  Isobutene 5% by weight or less.

Possible catalysts are, for example, O'Connor et al., Catalysis Today, 6, (1990) p. ≪ RTI ID = 0.0 > 329 < / RTI > Supported nickel oxide catalysts may be used, and possible support materials are silica, alumina, aluminosilicates, aluminosilicates having a layered structure, and zeolites. Particularly suitable catalysts are the precipitates obtainable by nickel salts and silicates, for example aqueous solutions of sodium silicate and sodium nitrate, and, if appropriate, further components such as aluminum salts, for example, aluminum nitrate, Catalyst.

Especially preferred are NiO, SiO _2, TiO ₂ and / or ZrO _2, and also, if appropriate, a catalyst essentially consisting of the Al ₂ O _3. The most preferred catalysts comprise 10 to 70% by weight of nickel oxide, 5 to 30% by weight of titanium dioxide and / or zirconium dioxide and 0 to 20% by weight of aluminum oxide as the significant active components and the balance being silicon dioxide . This type of catalyst precipitates the catalyst composition at a pH of between 5 and 9 by adding an aqueous solution comprising nickel nitrate to an aqueous alkali metal water glass solution comprising titanium dioxide and / or zirconium dioxide, filtering, To < RTI ID = 0.0 > 650 C. < / RTI > For details of the preparation of the catalyst, reference can be made to DE-A 4339713. The entire contents of which are incorporated herein by reference.

The butene-containing hydrocarbon mixture is contacted with the catalyst at a temperature of preferably 30 to 280 ° C, particularly 30 to 140 ° C, particularly preferably 40 to 130 ° C. This takes place preferably at a pressure of from 10 to 300 bar, especially from 15 to 100 bar, particularly preferably from 20 to 80 bar. Where the pressure is typically set such that the olefin-rich hydrocarbon mixture is in a liquid or supercritical state at a selected temperature.

Examples of suitable reactors for contacting the hydrocarbon mixture with the heterogeneous catalyst are tube-bundle reactors and shaft furnaces. Furnaces are desirable, because capital expenditure is low. The dimerization can be carried out in a single reactor in which the oligomerization catalyst can be arranged in one or more fixed beds. Another approach is to use a reactor cascade consisting of two or more, preferably two, reactors arranged in series, wherein the butene dimerization in the reaction mixture is carried out in the presence of the reactor (s) prior to the last reactor in the cascade Is driven at only a partial conversion rate at the time of passage and the desired final conversion rate is not achieved until the reaction mixture passes through the last reactor of the cascade. The butene dimerization preferably takes place in an adiabatic reactor or in an adiabatic reactor cascade.

After leaving the reactor or, respectively, the last reactor of the cascade, the octene formed and, if appropriate, the higher oligomer are separated and removed from the unconverted butene and butane in the reactor effluent. The oligomer formed can be purified in a subsequent vacuum fractionation step to yield a pure octene fraction. During butene dimerization, a small amount of dodecene is generally also obtained. They are preferably separated and removed from the octene before the subsequent reaction.

In a preferred embodiment, some or all of the reactor effluent, consisting of butene and butane, which are essentially free of the oligomers and are not converted, is returned. It is preferred to choose to return the concentration of oligomer in the reaction mixture to the ratio of the formula not exceeding 35% by weight, preferably not exceeding 20% by weight, based on the hydrocarbon mixture of the reaction. This measurement increases the selectivity of butene dimerization with respect to these octenes, which yields particularly preferred alcohol mixtures after hydroformylation, hydrogenation and esterification.

The obtained octenes are converted to the aldehydes having one additional carbon atom in a second process step, by hydroformylation using a synthesis gas in a manner known per se. The hydroformylation of olefins for the production of aldehydes is known singly and is described, for example, in J. Falbe, (ed.): New Synthesis with Carbon monoxide, Springer, Berlin, Hydroformylation occurs in the presence of a catalyst which is homogeneously dissolved in the reaction medium. The catalysts commonly used in the present invention can be prepared by reacting compounds or complexes of transition metal group VIII, in particular Co, Rh, Ir, Pd, Pt or Ru compounds, or complexes of such metals (for example amine-containing or phosphine- Lt; RTI ID = 0.0 > and / or < / RTI >

For the purposes of the present invention, the hydroformylation preferably takes place in the presence of a cobalt catalyst, in particular dicobaltoctacarbonyl [Co ₂ (CO) ₈ ]. This takes place preferably at a synthesis gas pressure of 120 to 240 DEG C, especially 160 to 200 DEG C, and 150 to 400 bar, especially 250 to 350 bar. The hydroformylation preferably takes place in the presence of water. The ratio of hydrogen to carbon monoxide in the synthesis gas mixture 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 multistage process comprising the following four stages: preparation of the catalyst (pre-carbonylation), catalyst extraction, olefin hydroformylation and removal of the catalyst from the reaction product (De-cobaltation). In the first step of the process, pre-carbonylation, a cobalt salt aqueous solution, such as cobalt formate or cobalt acetate, is reacted with carbon monoxide and hydrogen as starting material to produce the catalyst complex required for the hydroformylation. In the second stage of the process, catalyst extraction, the cobalt catalyst prepared in the first stage of the process is extracted from the aqueous phase, preferably using olefins, using the organic phase to be hydroformylated. Besides olefins, the use of reaction products and by-products of hydroformylation for catalyst extraction is sometimes advantageous if they are insoluble in water and liquids under the selected reaction conditions. After phase separation, the cobalt catalyst loaded organic phase is fed to the hydroformylation, which is the third stage of the process. In the fourth stage of the process, de-cobaltation, the organic phase of the reactor effluent has no cobalt carbonyl complex in the presence of the workpiece, which may contain formic acid or acetic acid by treatment with oxygen or air. Meanwhile, the cobalt catalyst is destroyed by oxidation, and the resulting cobalt salt is again extracted into the aqueous phase. The cobalt salt aqueous solution obtained from the de-cobaltation is returned to the pre-carbonylation, the first stage of the process. The obtained crude hydroformylation product can be fed directly to the hydrogenation. Another method is to isolate the C ₉ fraction from it in a conventional manner, for example by distillation, and feed it to the hydrogenation.

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

Examples of cobalt compounds which may be used include cobalt (II) chloride, cobalt (II) nitrate, amine or hydrate complexes thereof, cobalt carboxylates such as cobalt formate, cobalt acetate, cobalt ethylhexanoate and cobalt Naphthenate (Co salt of naphthenic acid), and also cobalt caprolactamate complex. Under the conditions of hydroformylation, the catalytically active cobalt compound forms itself as cobalt carbonyl. It is also possible to use carbonyl complexes of cobalt, such as dicobaltoctacarbonyl, tetra-cobalt dodecacarbonyl and hexacobalthexadecarbonyl.

The aldehyde mixture obtained during the hydroformylation is reduced to yield the primary alcohol. Partial reduction generally occurs immediately under the conditions of hydroformylation, and it is also possible to control the hydroformylation in such a manner as to yield essentially a complete reduction. However, the resulting hydroformylation product is generally hydrogenated in a further step using a hydrogen gas or a hydrogen-containing gas mixture. The hydrogenation generally takes place in the presence of a heterogeneous hydrogenation catalyst. The hydrogenation catalyst used may comprise any desired catalyst suitable for the hydrogenation of an aldehyde to yield a primary alcohol. Examples of suitable commercial catalysts are copper chromite, cobalt, cobalt, nickel, nickel compounds, which include small amounts of chromium or other promoters if appropriate, and mixtures of copper, nickel and / or chromium. The nickel compound is generally in the form supported on a support material, such as alumina or diatomaceous earth. It is also possible to use a catalyst comprising a noble metal such as platinum or palladium.

A suitable method of effecting the hydrogenation is a trickle-flow process in which the mixture to be hydrogenated and the hydrogen gas or, respectively, the hydrogen-containing gas mixture pass simultaneously, for example, over a fixed bed of the hydrogenation catalyst .

The hydrogenation preferably takes place at a hydrogen pressure of from 50 to 250 DEG C, especially from 100 to 150 DEG C, and from 50 to 350 bar, especially from 150 to 300 bar. The desired isononanol fraction in the reaction effluent obtained during hydrogenation can be separated and separated by fractional distillation from C ₈ hydrocarbons and high-boiling products.

Gas-chromatographic analysis of the resulting alcohol mixture can provide a relative amount of individual compounds (percentages are presented as percentages by gas chromatogram area):

The proportion of 1-nonanol in the alcohol mixture of the present invention is preferably 6 to 16% by weight, more preferably 8 to 14% by weight, based on the total weight of the alcohol mixture.

The proportion of monomethyloctanol is preferably 25 to 55% by weight, more preferably 35 to 55% by weight, and 6-methyl-1-octanol and 4-methyl- It is particularly preferred to constitute at least 25% by weight, very particularly preferably at least 35% by weight, based on the weight.

The ratio of dimethylheptanol and monoethylheptanol is preferably 15 to 60 wt%, more preferably 20 to 55 wt%, and the ratio of 2,5-dimethyl-1-heptanol, 3-ethyl- And 4,5-dimethyl-1-heptanol together constitute at least 15% by weight, in particular 20% by weight, based on the total weight of the alcohol mixture. The proportion of hexanol is preferably 4 to 10% by weight, more preferably 5 to 10% by weight, based on the total weight of the alcohol mixture.

The alcohol mixture of the present invention is preferably 70 to 100%, more preferably 70 to 98%, most preferably 80 to 98%, still more preferably 85 to 95%, relative to the total weight of the alcohol mixture 1-nonanol, monomethyloctanol, dimethylheptanol and monoethylheptanol.

Preferably, the alcohol mixture comprises from 6% to 16% by weight of 1-nonanol, from 25% by weight to 55% by weight of monomethyloctanol, from 10% by weight to 30% by weight of dimethylheptanol, and from 7% By weight to 15% by weight monoethylheptanol.

Preferably, the alcohol mixture is reacted with phthalic acid (optionally in the form of its ester or an anhydride thereof) in a molar ratio ranging from 1: 1 to 2: 1, more preferably from 1: 1 to 1.3: 1 exist.

Preferably, the alcohol mixture comprises 6.0 to 16.0% by weight, preferably 7.0 to 15.0% by weight, particularly preferably 8.0 to 14.0% by weight of n-nonanol; 12.8 to 28.8% by weight, preferably 14.8 to 26.8% by weight, particularly preferably 15.8 to 25.8% by weight of 6-methyloctanol; 12.5 to 28.8% by weight, preferably 14.5 to 26.5% by weight, particularly preferably 15.5 to 25.5% by weight of 4-methyloctanol; 3.3 to 7.3% by weight, preferably 3.8 to 6.8% by weight, particularly preferably 4.3 to 6.3% by weight 2-methyloctanol; 5.7 to 11.7% by weight, preferably 6.3 to 11.3% by weight, particularly preferably 6.7 to 10.7% by weight 3-ethylheptanol; 1.9 to 3.9% by weight, preferably 2.1 to 3.7% by weight, particularly preferably 2.4 to 3.4% by weight 2-ethylheptanol; 1.7 to 3.7% by weight, preferably 1.9 to 3.5% by weight, particularly preferably 2.2 to 3.2% by weight of 2-propylhexanol; From 3.2 to 9.2% by weight, preferably from 3.7 to 8.7% by weight, particularly preferably from 4.2 to 8.2% by weight, of 3,5-dimethylheptanol; 6.0 to 16.0% by weight, preferably 7.0 to 15.0% by weight, particularly preferably 8.0 to 14.0% by weight, of 2,5-dimethylheptanol; 1.8 to 3.8% by weight, preferably 2.0 to 3.6% by weight, particularly preferably 2.3 to 3.3% by weight 2,3-dimethylheptanol; From 0.6 to 2.6% by weight, preferably from 0.8 to 2.4% by weight, particularly preferably from 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, particularly preferably 2.5 to 3.5% by weight 2-ethyl-4-methylhexanol; By weight of other alcohols (the total sum of said components being 100% by weight) of from 0.5 to 6.5% by weight, preferably from 1.5 to 6% by weight, particularly preferably from 1.5 to 5.5% by weight.

The density of the alcohol mixture of the present invention at 20 占 폚 is preferably 0.75 to 0.9 g / cm3, more preferably 0.8 to 0.88 g / cm3, and most preferably 0.82 to 0.84 g / cm3. 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 atmospheric pressure is preferably 190 to 220 占 폚, more preferably 195 to 215 占 폚, and most preferably 200 to 210 占 폚.

The preparation of the polyesters of the invention is carried out in a manner known per se (see, for example, Ullmann's Encyclopedia of Industrial Chemistry, 5th edition, VCH Verlagsgesell-schaft mbH, Weinheim, Vol. et seq. and Vol. A9, pp. 572-575). The chain lengths of the polyesters and, respectively, the average molecular weights can be controlled through the point in time at which the alcohol mixture is added and the amount of the mixture, which can readily be routinely measured by a person skilled in the art. The catalyst used is a conventional esterification catalyst, preferably dialkyl titanate ((RO) ₂ TiO ₂ , where examples of R are iso-propyl, n-butyl and isobutyl), methanesulfonic acid and sulfuric acid And more preferably the catalyst is isopropyl-n-butyl titanate.

In one preferred embodiment, the initial charge in the reaction vessel comprises a mixture of phthalic acid and a total amount of an alcohol. The reaction mixture is first heated to 100-140 < 0 > C and homogenized by stirring. The heating is then continued at atmospheric pressure at 160-190 ° C. The esterification starts with removal of water, preferably at about 150 < 0 > C. The water of the formed reaction is removed by distillation through the column. If the alcohol mixture is distilled throughout the procedure, it is returned to the reaction vessel. The reaction vessel is then heated to 200-250 DEG C and the additional water of the reaction is stripped at a pressure of 150-300 mbar by passing nitrogen through the reaction mixture. The residue and the excess alcohol mixture are stripped here using an increased flow rate of nitrogen and stirring. The reaction mixture is then filtered at 100-140 < 0 > C.

Preferably, the hydrogenation of the total mixture is carried out in the presence of at least one metal of the subgroup VIII of the Periodic Table of the Elements, either alone or in combination with one of the subgroups I or VII of the Periodic Table of the Elements, as applied to the support (the support has a macropore) ≪ / RTI > in the presence of a catalyst comprising hydrogen and at least one of the above metals.

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

In a further embodiment, the catalyst is present in an amount such that 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 has a pore diameter in the range of from 50 nm to 10 000 nm 50 to 90% of the pore volume of the support is formed by mesopores having a pore diameter in the range of 2 to 50 nm, and the sum of the pore volume ratios is 100%.

In a further embodiment, the catalyst has from 0.01 to 30% by weight, based on the total weight of the catalyst, of the active metal applied to the support, the support having an average pore diameter of at least 0.1 [mu] m and a BET surface area of less than 15 m2 / g . The support which can be used is in principle also comprising mesopores and / or micropores in addition to all supports with macropores, i.e. supports and macropores exclusively having macropores only.

In principle, all metals in subgroup VIII of the Periodic Table of the Elements may be used as active metals. Platinum, rhodium, palladium, cobalt, nickel or ruthenium or a mixture of two or more thereof is preferably used as the active metal, and in particular ruthenium is used as the active metal. Copper and / or rhenium is preferably used among the metals of subgroup I or VII or subgroup I and VII of the Periodic Table of the Elements, all of which may in principle be used as well.

In the context of this application, the terms " macropore "and" mesopore " Chem., 45, page 79 (1976), that is to say as a pore whose diameter is greater than 50 nm (macropore) or whose diameter is 2 nm to 50 nm (mesopore).

The content of the active metal is generally 0.01 to 30% by weight, preferably 0.01 to 5% by weight, particularly preferably 0.1 to 5% by weight, based on the total weight of the catalysts used in each case.

The polyesters of the present invention can be used as lubricants in industrial oils. Industrial oils include but are not limited to: light engine oil, industrial engine oil, marine engine oil, crankshaft oil, compressor oil, refrigerator oil, hydrocarbon compressor oil, ultra low pressure lubricants and fats, high temperature lubricants and fats, wire rope, Lubricants, weaving machine oils, refrigerator oils, air and space lubricants, air turbine oils, transmission oils, gas turbine oils, spindle oils, spin oils, traction fluids, transmission oils, plastic transmission oils, passenger car transmission oils, truck transmission oils Transmission oil, heat transfer oil, heat transfer oil, transformer oil, fat, chain oil, drilling detergent for soil investigation, hydraulic oil, chain saw oil and gun oil for transmission oil, transmission oil, transmission oil, industrial gear oil, insulation oil, instrument oil, brake fluid, , A pistol, and a rifle lubricant.

Industrial oils preferably contain further additives such as polymer thickeners, viscosity index improvers, antioxidants, corrosion inhibitors, detergents, dispersants, emulsifiers, defoamers, dyes, wear protection additives, EP (extreme pressure) antiwear: antiwear) additives and friction modifiers.

In addition, the industrial oils may be selected from other base oils and / or co-solvents such as mineral oils (Gr I, II or III oils), polyalphaolefins, alkylnaphthalenes, mineral oil soluble polyalkylene glycols, silicone oils, phosphate esters and / And may include a carboxylic acid ester.

Typical additives found in hydraulic oils include dispersants, detergents, corrosion inhibitors, antiwear agents, anti-foaming agents, friction modifiers, seal swelling agents, emulsifiers, VI improvers, and pour point depressants.

Examples of dispersants include polyisobutylene succinimide, polyisobutylene succinate esters, and Mannich Base ashless dispersants.

Examples of detergents include metallic alkyl phenates, sulfated metallic alkyl phenates, metallic alkyl sulfonates and metallic alkyl salicylates.

Examples of antiwear additives include organoborates, organophosphites, organic sulfur-containing compounds, zinc dialkyldithiophosphates, zinc diaryldithiophosphates, and phosphosulfurized hydrocarbons.

Examples of friction modifiers include fatty acid esters and amides, organomolybdenum compounds, molybdenum dialkyl thiocarbamates and molybdenum dialkyl dithiophosphates.

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

The polyesters of the present invention can be used as lubricants in metal pore fluids.

Depending on the application, for example, straight oil (knit oils) or soluble oils, the metalworking fluid is known in the art to improve the properties of the composition in an amount ranging from 0.10 to 40% ≪ / RTI > The additive may be a metal deactivator; Corrosion inhibitors; Antimicrobial agents; Anticorrosives; Emulsifiers; A coupler; Extreme pressure; Antifriction; Rust inhibitors; Polymeric component; Anti-inflammatory agents; disinfectant; antiseptic; Antioxidants; Chelating agents; pH adjusting agents; An abrasion inhibitor comprising an active sulfur abrasion additive package; And a metal pore fluid additive package containing at least one of the above-mentioned additives.

Depending on the end-use application, minor amounts of additives such as anti-fogging agents may optionally be added in amounts ranging from 0.05 to 5.0% by volume in one embodiment, and less than 1% by weight in other embodiments. Non-limiting examples include rhamsan gum, hydrophobic and hydrophilic monomers, styrene or hydrocarbyl-substituted styrene hydrophobic monomers and hydrophilic monomers, molecular weights in the range of from about 0.3 to 4x10 ⁶ (viscosity average molecular weight) Oil soluble organic polymers such as isobutylene, styrene, alkyl methacrylate, ethylene, propylene, n-butylane vinyl acetate, and the like. In one embodiment, polymethyl methacrylate or poly (ethylene, propylene, butylene or isobutylene) in the molecular weight range of 1 to 3 x 10 ⁶ is used.

For certain applications, small amounts of prior art foam inhibitors may also be added to the composition in amounts ranging from 0.02 to 15.0 wt%. Non-limiting examples include polydimethylsiloxane (often terminated with trimethylsilyl), alkyl polymethacrylates, polymethylsiloxanes, N-acylamino acids with long chain acyl groups and / or salts thereof, alkyl alkylene oxides and / or acyl Alkylamino acids having a long chain alkyl group and / or a salt thereof, acetylenediols and ethoxylated acetylenediols, silicones, hydrophobic materials (for example, silicas), 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, oxo-alcohols, fluorosurfactants, waxes such as ethylene Bisstereamide wax, polyethylene wax, polypropylene wax, ethylene bis stearamide wax, and paraffin wax. It should. Foam control agents may be used with suitable dispersants and emulsifiers. Additional active foam control agents are described in "Foam Control Agents ", by Henry T. Kemer (Noyes Data Corporation, 1976), pages 125-162.

The metalworking fluid further comprises an antistatic agent comprising an overbased sulfonate, a sulphurised olefin, a chlorinated paraffin and an olefin, a sulphurised olefin, an amine terminated polyglycol, and a sodium dioctylphosphate salt. In another embodiment, the composition further comprises a corrosion inhibitor comprising a carboxylic acid / boric acid diamine salt, a carboxylic acid amine salt, an alkanolamine and an alkanolamine borate.

The metalworking fluid further comprises an oil soluble metal deactivator in an amount of 0.01 to 0.5% by volume (based on the final oil volume). Non-limiting examples triazole or thiadiazole, in particular aryl-triazole, such as benzotriazole and tolyl triazole, these triazole-alkyl derivatives, and benzo-thiadiazole, e.g., R (C ₆ H ₃₎ N ₂ S, wherein R is H or C ₁ to C ₁₀ alkyl.

A small amount of at least an antioxidant in the range of 0.01 to 1.0% by weight can be added. Non-limiting examples are antioxidants of the aminic or phenolic type or mixtures thereof, for example butylated hydroxytoluene (BHT), bis-2,6-di-t-butylphenol derivatives, sulfur- , And sulfur-containing essential oil bisphenols.

The metal pore fluid further comprises at least 0.1 to 20% by weight of at least an extreme pressure agent. Non-limiting examples of extreme pressure agents include zinc dithiophosphate, molybdenum oxysulfide dithiophosphate, molybdenum amine compounds, sulfurized oils and fats, sulfurized fatty acids, sulfurized esters, olefin sulfides, dihydrocarbyl polysulfides, thiocarbamates , Thioterpene, and dialkyl thiodipropionate.

In another embodiment, the invention relates to a lubricant composition comprising the following components:

A) One or more lubricating base oils,

B) Reaction with a total mixture comprising a phthalic acid (optionally in the form of its ester or an anhydride thereof) and an alcohol mixture comprising 1-nonanol, monomethyloctanol, dimethylheptanol and monoethylheptanol, At least one polyester obtainable by subsequent hydrogenation whereby the polyester has a dynamic viscosity at 20 DEG C in the range of from 40 to 64 mPa.s measured according to DIN 51562-1 and

C) Lubricant additives.

For the sake of brevity, any preferred embodiment that refers to the use of the polyesters of the present 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 30% to 90% by weight of component A), 0.1% to 50% by weight of component B) and 0.1% to 40% by weight of component C) .

More preferably, the lubricant composition comprises 50 wt% to 90 wt% of component A), 3.5 wt% to 45 wt% of component B), and 1 wt% to 30 wt% of component C).

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

The viscosity of the lubricant composition at 40 캜 is preferably from 60 to 140 mm 2 / s, more preferably from 70 to 130 mm 2 / s, most preferably from 80 to 120 mm 2 / s, measured in accordance with DIN 51562-1 .

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

Preferably the lubricating oil additive is selected from the group consisting of lubricity improving agents, viscosity improvers, combustion improvers, corrosion and / or oxidation inhibitors, pour point depressants, extreme pressure agents, antiwear agents, anti-foam agents, detergents, dispersants, antioxidants and metal passivators .

Typical lubricity improvers are ester-based lubricity improvers having a common acid-based lubricity improving agent having a fatty acid as a main component thereof and a glycerin mono fatty acid ester as a main component thereof. These compounds may be used alone or in combination of two or more kinds. The fatty acids used in the lubricity improving agent are preferably those having a mixture of unsaturated fatty acids of about 12 to 22 carbons, but preferably about 18 carbons, which are oleic acid, linoleic acid and linolenic acid as the main constituents thereof.

Viscosity improvers include, but are not limited to, polyisobutene, polymethylacrylate esters, polyacrylate esters, diene polymers, polyalkyl styrenes, alkenyl aryl conjugated diene copolymers, polyolefins, and multifunctional viscosity improvers .

Pour point depressants are typically a particularly useful type of additive that is often included in the lubricating oils described herein, including components such as polymethacrylates, styrene-based polymers, crosslinked alkylphenols, or alkylnaphthalenes. See, for example, page 8 of "Lubricant Additives" by C. V. Smalheer and R. Kennedy Smith (Lesius-Hiles Company Publishers, Cleveland, Ohio, 1967).

For example, corrosion inhibitors, extreme pressure agents, and antiwear agents include dithiophosphorus esters; Chlorinated aliphatic hydrocarbons; But are not limited to, boron-containing compounds including borate esters and molybdenum compounds.

Antifoam agents used to reduce or prevent the formation of stable foams include silicon or organic polymers. Examples of these and additional defoamer compositions are described in "Foam Control Agents" by Henry T. Kerner (Noyes Data Corporation, 1976), pages 125-162. Additional antioxidants may also typically include aromatic amine or incompatible phenolic types. These and other additives that can be used in combination with the present invention are described in more detail in U.S. Patent No. 4,582,618 (including column 14, line 52 to column 17, line 16).

Dispersants are those that are well known in the lubricant art and often referred to as "ashless" dispersants (prior to mixing the lubricating compositions), which do not contain ash-forming metals and when they are added to the lubricant composition, And does not contribute to any ash forming metal. Detergents are characterized by polar groups attached to relatively high molecular weight hydrocarbon chains.

One family of dispersants is Mannich bases. These are formed by condensation of higher molecular weight, alkyl substituted phenols, alkylene polyamines, and aldehydes such as formaldehyde and are described in more detail in U.S. Patent No. 3,634,515. Another class of dispersants are higher molecular weight esters. The material is prepared by reacting the Mannich dispersant or succinimide described below with an aqueous solution of a succinimide or a mixture thereof, except that they may be seen to be prepared by the reaction of a hydrocarbyl acylating agent and a polyhydric aliphatic alcohol such as glycerol, pentaerythritol, or sorbitol. similar. Such materials are described in greater detail in U.S. Patent No. 3,381,022. Other dispersants include polymeric dispersant additives, which are generally hydrocarbon-based polymers.

A preferred class of dispersants is carboxyl dispersants. The carboxylic dispersant comprises a succinic-based dispersant, which is the reaction product of a hydrocarbyl substituted succinic acylating agent and an organic hydroxy compound, or in certain embodiments, an amine containing at least one hydrogen attached to a nitrogen atom, or A mixture of the above-mentioned hydroxy compound and an amine. The term "succinic acylating agent" refers to a hydrocarbon-substituted succinic acid or succinic acid-producing compound. Such materials typically include hydrocarbyl-substituted succinic acids, anhydrides, esters (including half-esters), and halides. Succinimide dispersants are more fully described in U.S. Patent Nos. 4,234,435 and 3,172,892.

The amine that reacts with the succinic acylating agent to form the carboxyl dispersant composition may be a monoamine or a polyamine. The polyamines are principally derived from alkylene polyamines such as ethylene polyamines (i.e., poly (ethylene amines)) such as ethylenediamine, triethylenetetramine, propylenediamine, decamethylenediamine, octamethylenediamine, di (heptamethylene) Propylene tetramine, tetraethylene pentamine, trimethylene diamine, pentaethylene oxamine, di (trimethylene) triamine. Higher order homologues such as those obtained by condensing two or more of the above-described alkylene amines are also useful. Tetraethylenepentamine is particularly useful.

Hydroxyalkyl-substituted alkylene amines, i. E., Alkylene amines having at least one hydroxy-alkyl substituent on the nitrogen atom are likewise useful, either through an amino radical or via a hydroxy radical, Such are also the higher order homologues obtained by the condensation of hydroxyalkyl-substituted alkylene amines.

The dispersant may be a borate material. The borate dispersant is a well known material and can be prepared by treatment with a borating agent such as boric acid. Typical conditions include heating the dispersant with boric acid at 100-150 < 0 > C.

The amount of dispersant in the lubricant composition, if present, will typically be from 0.5 to 10 wt%, alternatively from 1 to 8 wt%, alternatively from 3 to 7 wt%. Its concentration in the concentrate will be correspondingly increased, for example, by 5 to 80% by weight.

Detergents are generally salts of organic acids, which are often overbased. Metal perchlorinated salts of organic acids are well known in the art and generally include metal salts in which the amount of metal present is greater than stoichiometric. These salts are said to have a conversion level of greater than 100% (i.e., they contain more than 100% of the theoretical amount of metal required to convert the acid to its "normal" or "neutral" salt). They are usually referred to as overbased, hyperbased or superbased salts and are generally referred to as salts of organic sulfuric acids, organic phosphoric acids, carboxylic acids, phenols, or two of the above Or more. As will be appreciated by those skilled in the art, mixtures of such overbased salts may also be used.

The overbased vaporization composition can be prepared by a variety of well known techniques including sulfonic acids, carboxylic acids (including substituted salicylic acids), phenols, phosphonic acids, saligenin, salixarate, and mixtures of any two or more thereof Lt; RTI ID = 0.0 > acidic < / RTI >

The basicly reacting metal compound used to prepare the overbased salt is often an alkali or alkaline earth metal compound, but other basicly reactive metal compounds may also be used. Compounds of Ca, Ba, Mg, Na and Li, such as the hydroxides and alkoxides of these lower alkenols, are usually used. An overbased salt containing a mixture of two or more ions of the metal may be used.

The overbasing material generally comprises an acidic material (typically an inorganic acid or a lower carboxylic acid such as carbon dioxide) with an acidic organic compound, at least one inert, organic solvent (mineral oil, naphtha, toluene, xylene, etc.) With a mixture comprising a reaction medium comprising a base, a stoichiometric excess of a metal base, and a promoter.

The acidic material used in the preparation of the overbased vaporizable material may be a liquid, such as formic acid, acetic acid, nitric acid, or sulfuric acid. Acetic acid is particularly useful. Inorganic acidic materials such as HCl, SO ₂ , SO ₃ , CO ₂ , or H ₂ S, such as CO ₂ or mixtures thereof, such as a mixture of CO ₂ and acetic acid, may also be used.

Detergents can also generally be borated by treatment with a borating agent such as boric acid. Typical conditions include heating the detergent at 100-150 ° C with boric acid, the number of equivalents of boric acid roughly coinciding with the number of equivalents of metal in the salt.

The amount of detergent component in the lubricant composition, if present, will typically be from 0.5 to 10 wt%, such as from 1 to 7 wt%, or from 1.2 to 4 wt%. Its concentration in the concentrate will correspondingly increase, for example, from 5 to 65% by weight.

Examples of metal passivators include, without limitation, tolyltriazole and derivatives thereof, and benzotriazole and derivatives thereof. If used, the metal passivator is typically present in the fluid composition in an amount of 0.05 to 5 parts by weight, more typically 0.05 to 2 parts by weight, based on the total weight of the fluid composition.

The following examples illustrate the invention in more detail without limitation.

Example

A) Preparation of polyester of the present invention

A.1) Butene dimerization

The butene dimerization was carried out continuously in an adiabatic reactor consisting of two sub-reactors (length: 4 m in each case, diameter: 80 cm in each case) with intermediate cooling at 30 bar. The starting product used was raffinate II with the following makeup:

  Isobutane 2 wt%

  n-butane 10 wt%

  Isobutene 2 wt%

  1-butene 32 wt%

  trans-2-butene 37% by weight and

  cis-2-butene 17% by weight.

The catalyst used was in the form of a 5 x 5 mm tablet according to DE-A 4339713, consisting of 50 wt.% NiO, 12.5 wt.% TiO ₂ , 33.5 wt.% SiO ₂ and 4 wt.% Al ₂ O ₃ It was the manufactured material. The reaction was carried out at a feed rate of 0.375 kg of raffinate II per 1 l of catalyst and hourly, a recovery ratio of unreacted C ₄ hydrocarbons returned to fresh raffinate II of 3, an inlet temperature in the first sub- Lt; RTI ID = 0.0 > sub-reactor. ≪ / RTI > The conversion reported in butene present in raffinate II was 83.1% and the octane selectivity was 83.3%. Using fractional distillation of the reactor effluent, the octene fraction was separated and separated from unreacted raffinate II and from the high-boiling water.

A.2) Hydroformylation and hydrogenation

750 g of the octene mixture prepared according to Example A.1 of the Example was continuously discontinued for 5 hours in an autoclave with 0.13% by weight of dicobaltoctacarbonyl Co ₂ (CO) ₈ as catalyst, 75 g of water With the addition, at 185 DEG C, the reaction was carried out at a synthesis gas pressure of 280 bar and a H ₂ to CO ratio in the mixture of 60/40. Additional material was injected into the make-up to consume the synthesis gas, which is presented as a pressure drop in the autoclave. After release of the pressure in the autoclave, the reaction effluent, together with 10% strength acetic acid by weight, is oxidatively released from the cobalt catalyst by introducing air and the organic product phase is hydrogenated at 125 ° C at a hydrogen pressure of 280 bar for 10 h Hydrogenated using Raney nickel. The isononanol fraction was separated and removed from C ₈ paraffin and high boiling water by fractional distillation of the reaction effluent.

The composition of the isonanoanol fraction was analyzed by gas chromatography. Samples were pre-trimethylsilylated at 80 ° C for 60 minutes using 1 ml of N-methyl-N-trimethylsilyltrifluoroacetamide per 100 μl of sample. A Hewlett Packard Ultra 1 separation column with a length of 50 m and an inner diameter of 0.32 mm with a film thickness of 0.2 μm was used. The injector temperature and the detector temperature were 250 ° C and the oven temperature was 120 ° C. The split was 110 ml / min. The carrier gas used was nitrogen. The entry pressure was set at 200 kPa. 1 μl of sample was injected and detected by FID. The composition determined for the sample by this method (% by gas chromatogram area) was as follows:

  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 the iso-nonanol mixture was measured as 0.8326 at 20 占 폚 and 1.4353 as a refractive index n _D ²⁰ . The boiling range at atmospheric pressure was 204 to 209 占 폚.

A.3) Esterification

Viscosity measurement

The viscosity of the ester is measured in a standard test according to DIN 51562-1.

In a third process step, the fraction iso-nonanol of 865.74 g obtained in process step 2 and isopropyl butyl titanate of the (20% excess relative to the phthalic anhydride) 370.30 g of phthalic anhydride and 0.42 g of, as a catalyst, N ₂ sparged (10 l / h) in a 2 l autoclave at a stirring rate of 500 rpm and a reaction temperature of 230 < 0 > C. The water of the formed reaction was continuously removed from the reaction mixture along with the N ₂ stream. The reaction time was 180 minutes. The isonanol excess was then distilled off under reduced pressure of 50 mbar. 1000 g of crude polyester were neutralized with 150 ml of a 0.5% strength aqueous sodium hydroxide solution while stirring at 80 占 폚 for 10 minutes. This yielded a two-phase mixture having an upper organic phase and a lower aqueous phase (a waste liquid containing hydrolyzed catalyst). Remove the aqueous phase and the organic phase was washed twice with H ₂ O in 200 ml. For further purification, the neutralized and washed polyester was stripped with steam at a reduced pressure of 180 < 0 > C and 50 mbar for 2 hours. The purified polyester was then dried by passing through a N ₂ stream (2 l / h) for 30 minutes at 150 ° C / 50 mbar, then stirred for 5 minutes with activated carbon, and the supra- The filter was filtered off (at a temperature of 80 ° C).

The polyester produced 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 esters

A meso / macroporous aluminum oxide support in the form of a 4 mm extrudate, having a BET surface area of 238 m 2 / g and a pore volume of 0.45 ml / g, was immersed in a ruthenium (III) nitrate aqueous solution having a concentration of 0.8 wt% . 0.15 ml / g of the pores of the support (approximately 33% of the total volume) has a diameter in the range of 50 nm to 10,000 nm, and 0.30 ml / g of the pores of the support (approximately 67% of the total pore volume) nm < / RTI > The volume of solution taken up by the support during the course of the immersion corresponds roughly to the void volume of the support used. The support immersed in the ruthenium (III) nitrate solution is then dried at 120 ° C and activated (reduced) in a stream of water at 200 ° C. The catalyst so obtained contained 0.5 wt% ruthenium, based on the weight of the catalyst. The - (reactor 100 ml, d _internal = 12 mm, l = 1000 mm main reactor 160 ml, d _internal = 12 mm, l = 1400 mm , and after) continue to operate equipment which is composed of two tube reactors connected in series (71.5 g of the main reactor, 45.2 g of the post-reactor) as described in the Production Example. The main reactor was operated with circulation to the dripping system (liquid hourly space velocity 12 m / h), and the post-reactor was operated with straight-through passage in liquid phase mode. The phthalester prepared in process step 3 was pumped through the reactor cascade (feed 66 g / h) with pure hydrogen at 128 ° C in the main reactor and at an average temperature of 128 ° C in the post- Respectively. The catalyst time-space velocity in the main reactor was 0.6 kg phthaloester / 1 _cat xh. Analysis of the reaction efflux by gas chromatography showed> 99.9% conversion of the phthal ester.

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

B) Measurement of cloud point

The haze of the ester according to Example A.4 was measured to be -80 占 폚 in accordance with DIN ISO 3015.

C) Compatibility test with sealing materials

The seal compatibility test with the sealing material acrylonitrile-butadiene copolymer was carried out at 100 DEG C for 168 hours in accordance with standard method ISO 1817 in the presence of an ester as obtained in A.4).

The sealing material showed a volume change of + 33.3% (expansion).

D)

Table 1: Lubricant Formulations A and B (all values are in wt-%)

DIDA is available, for example, as Synative ES DIDA from BASF SE, Ludwigshafen.

The seal compatibility test with the sealing material acrylonitrile-butadiene copolymer was carried out at 100 DEG C for 168 hours in the presence of Formulation A and Formulation B, respectively, according to the standard method ISO 1817. [

The sealing material showed a volume change of + 12.0% (swelling) in the presence of Formulation A, and a volume change of 12.6% (swelling) in the presence of Formulation B.

Claims (15)

Reaction with a total mixture comprising a phthalic acid (optionally in the form of its ester or an anhydride thereof) and an alcohol mixture comprising 1-nonanol, monomethyloctanol, dimethylheptanol and monoethylheptanol, A polyester obtainable by subsequent hydrogenation, whereby the polyester has a dynamic viscosity at 20 DEG C in the range of from 40 to 64 mPa.s measured according to DIN 51562-1 as a lubricant for the polyester. 2. Use according to claim 1, characterized in that the polyester has a dynamic viscosity at 20 DEG C in the range of from 42 to 62 mPa.s measured according to DIN 51562. 3. Use according to claim 1 or 2, characterized in that the alcohol mixture contains a proportion of from 25% to 55% by weight monomethyloctanol, based on the total weight of the alcohol mixture. 4. Use according to any one of claims 1 to 3, characterized in that the alcohol mixture contains a proportion of from 10% by weight to 30% by weight of dimethylheptanol, based on the total weight of the alcohol mixture. The process according to any one of claims 1 to 4, wherein the alcohol mixture comprises from 6% by weight to 16% by weight of 1-nonanol, from 25% by weight to 55% by weight monomethyloctanol, % ≪ / RTI > to 30% by weight of dimethyl heptanol and 7% to 15% by weight of monoethyl heptanol. 6. Process according to any one of claims 1 to 5, characterized in that the alcohol mixture is present in a molar ratio in the range of 1: 1 to 2: 1 with respect to the phthalic acid (optionally in the form of its ester or its anhydride) Usage. A lubricant composition comprising:
A) one or more lubricating base oils,
B) reaction with a total mixture comprising phthalic acid (optionally in the form of its ester or an anhydride thereof), and an alcohol mixture comprising 1-nonanol, monomethyloctanol, dimethylheptanol and monoethylheptanol, At least one polyester obtainable by subsequent hydrogenation of the mixture whereby the polyester has a dynamic viscosity at 20 DEG C in the range of 40 to 64 mPa.s measured according to DIN 51562-1 and
C) Lubricant additives. 8. A lubricant composition according to claim 7, wherein the lubricating base oil is a hydrorefined mineral oil and / or synthetic hydrocarbon oil. The lubricant composition of claim 8, wherein the hydro-refined mineral oil is selected from the group consisting of hydro-refined naphthenic mineral oil, API base oil classification group II, and Group III hydro-refined paraffinic mineral oil. The lubricant composition according to claim 8, wherein the synthetic hydrocarbon oil is selected from the group consisting of poly-alpha-olefins (PAO) belonging to isoparaffinic synthetic oil, GTL synthetic oil and API base oil classifying group IV. 11. Lubricant composition according to any one of claims 7 to 10, characterized in that the polyester has a dynamic viscosity at 20 DEG C in the range of 42 to 61 mPa.s measured according to DIN 51562-1. 12. A lubricant composition according to any one of claims 7 to 11, characterized in that the alcohol mixture contains a proportion of from 25% to 55% by weight monomethyloctanol, based on the total weight of the alcohol mixture. 13. The lubricant composition according to any one of claims 7 to 12, characterized in that the alcohol mixture contains a proportion of 10 to 30% by weight of dimethylheptanol relative to the total weight of the alcohol mixture. 14. The process according to any one of claims 7 to 13, wherein the alcohol mixture comprises from 6% to 16% by weight of 1-nonanol, from 25% by weight to 55% by weight monomethyloctanol, % ≪ / RTI > to 30% by weight of dimethyl heptanol and 7 to 15% by weight of monoethylheptanol. The lubricant composition of claim 7, wherein the lubricating oil additive is 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, antifoaming agents, ≪ RTI ID = 0.0 > and / or < / RTI >