Biobased industrial antioxidants

Abstract

The present disclosure relates to a method of increasing the oxidative stability of a composition comprising adding to the composition one or more compounds of the Formula 1: wherein n is an integer from 2-6; R is C1-C22 alkyl; R2 is C3-C12 alkyl; R3 is hydrogen or C1-C10 alkyl; to the composition.

Description

BIOBASED INDUSTRIAL ANTIOXIDANTSCROSS-REFERENCE TO RELATED APPLICATIONS

[0001] This application claims the benefit of U.S. Provisional Application No. 63 / 634,865, filed April 16. 2024, and U.S. Provisional Application No. 63 / 707.570, filed October 15, 2024, each of which is incorporated by reference herein in its entirety.TECHNICAL FIELD

[0002] The present disclosure relates to biobased industrial antioxidants that can be used in a variety of applications. Such as lubricants, oils, greases, dielectric and cooling fluids. Use of biobased ingredients is increasingly preferred to lower the carbon footprint of industrial products.BACKGROUND

[0003] Most if not all industrial materials such as lubricants and fluids breakdown during use leading to additional costs such as production inefficiencies, downtime for equipment, and the expense of replacing old materials with new. In some applications, for example in an off-shore wind turbine, these costs can be very significant. For this reason, the lifetime of fluids is critically important.

[0004] One of the leading ways in which these materials degrade is through oxidation. Accordingly, manufacturers of these materials routinely include antioxidants in their formulations to extend the lifetime of materials in use and during storage.

[0005] The present disclosure relates to biobased materials that can be utilized as an antioxidant in these applications. While many antioxidants exist on the market, biobased solutions for this sector are relatively unknown. Biobased means that the materials described herein are derived from sustainable plant sources as opposed to non-regenerable or sustainable sources such as petroleum. Biodegradability means that the lubricants and process fluids (hereinafter "fluids") have the ability in a natural environment to degrade over a period of time, which may be measured by tests such as those promulgated by the Organization of Economic Co-Operation and Development (OECD). Renewable biobased products contain, by definition, high levels of renewable carbons, and standards are being set to encourage increasingly greater levels of renewability. For example, the European Ecolabel now stresses that hydraulic fluids should be biodegradable and preferably contain at least 50 percent by weight renewable carbons.SUMMARY

[0006] Efficiency of mechanical systems is of utmost importance to the manufacturers of those systems and the users thereof. Making a system more efficient can have numerous benefits such as better and longer performance, reduced wear and down time, lower energy costs, and longer life for batten’ operated mechanism. Currently this is of extreme importance in the electric vehicle (EV) arena. The internal combustion engines of traditional cars and trucks pose a significant inconvenience to consumers by the fact that they require frequent and expensive oil changes over the course of their lifetime. EVs provide the opportunity for less frequent lubricant changes and even the possibility of “life-time filf’ where changes are unnecessary. However, these fluids must resist oxidation for their lifetime and biobased biodegradable antioxidant component would be highly desirable.

[0007] The compositions described herein exhibit the surprising ability improve the oxidative stability of oil based compositions when included in minor amounts. These compositions have an additional advantage in that in addition to their antioxidant benefits they also function as lubricants themselves whereas traditional antioxidants do not have this property.

[0008] In addition, it was surprisingly discovered that addition of a small percentage of the compounds of Formula 1 or Formula 3 to a base oil can dramatically increase the oxidative stability of a material to which it is added such as a base oil, lubricating composition, or other material such as a natural or synthetic ester, an industrial chemical such as an amide..

[0009] Disclosed is a method of increasing the oxidative stability of a composition comprising adding to the composition one or more compounds of the Formula 1 :wherein n is an integer from 2-6; R is C1-C22 alkyl; R2 is C3-C12 alkyl; R3 is hydrogen or C1-C10 alkyl; to the composition.BRIEF DESCRIPTION OF THE FIGURES

[0010] Figure 1 shows the GPC data for an Example of the present disclosure (Example 1 IB) where the polymeric distribution of the material is represented.

[0011] Figure 2 shows the color change or erucamide samples over time in the presence and absence of antioxidants.DETAILED DESCRIPTION

[0012] Reference will now be made in detail to certain aspects of the disclosed subject matter. While the disclosed subject matter will be described in conjunction with the enumerated claims, it will be understood that the exemplified subject matter is not intended to limit the claims to the disclosed subject matter. One aspect described in conjunction with a particular embodiment is not necessarily limited to that embodiment and can be practiced with any other embodiment(s).

[0013] Throughout this document, values expressed in a range format should be interpreted in a flexible manner to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a range of ‘‘0. 1% to 5%” or “0. 1% to 5%” should be interpreted to include not just 0.1% to 5%, but also the individual values (e.g., 1%, 2%, 3%, and 4%) and the sub-ranges (e.g., 0.1% to 0.5%, 1.1% to 2.2%, 3.3% to 4.4%) within the indicated range.

[0014] As used herein, the singular forms "a," "an," and "the" and similar referents in the context of describing the elements (especially in the context of the following claims) include plural referents unless the context clearly dictates otherwise. For example, reference to "a substituent" encompasses a single substituent as well as two or more substituents, and the like. It is understood that any term in the singular may include its plural counterpart and vice versa, unless otherwise indicated herein or clearly contradicted by context.

[0015] As used herein, the following terms have the following meanings unless expressly stated to the contrary.

[0016] The term “of’ is used to refer to a nonexclusive “or” unless otherwise indicated. The statement “at least one of A and B” has the same meaning as “A. B, or A and B.”

[0017] In addition, it is to be understood that the phraseology or terminology employed herein, and not otherwise defined, is for the purpose of description only and not of limitation. Any use of section headings is intended to aid reading of the document and is not to be interpreted as limiting; information that is relevant to a section heading may occur within or outside of that particular section. Any publications, patents, and patent documents referred to in this document are incorporated by reference herein in their entirety, as though individually incorporated by reference. In the event of inconsistent usages between this document and those documents soincorporated by reference, the usage in the incorporated reference should be considered supplementary to that of this document; for irreconcilable inconsistencies, the usage in this document controls.

[0018] As used herein, the terms "for example," "for instance," "such as." or "including" are meant to introduce examples that further clarify more general subject matter. Unless otherwise specified, these examples are provided only as an aid for understanding the applications illustrated in the present disclosure and are not meant to be limiting in any fashion.

[0019] In the methods described herein, the acts can be carried out in any order without departing from the principles of the disclosure, except when a temporal or operational sequence is explicitly recited. Furthermore, specified acts can be carried out concurrently unless explicit claim language recites that they be carried out separately. For example, a claimed act of doing X and a claimed act of doing Y can be conducted simultaneously within a single operation, and the resulting process will fall within the literal scope of the claimed process.

[0020] The term “substantially” as used herein refers to a majority of, or mostly, as in at least about 50%, 60%, 70%, 80%, 90%, 95%, 96%, 97%, 98%, 99%, 99.5%, 99.9%, 99.99%, or at least about 99.999% or more, or 100%. In some aspects, substantially means greater than 90%. In some aspects, substantially means greater than 75%.

[0021] The term “alkyl” as used herein means a saturated or unsaturated, branched, or straight-chain monovalent, or divalent, hydrocarbon radical derived by the removal of one, or two, hydrogen atoms from the carbon atoms of a parent alkane, alkene, or alkyne. In some aspects, one or more of the alky l groups are substantially saturated. In some aspects, one or more of the alkyl groups are fully or partially saturated.

[0022] The terms C1-C22 alkyl; C2-C12, C3-C12; and C1-C10 alkyl means alkyl groups containing 1-22, 2-12, 3-12 and 1-10 carbons. Any similar numerical ranges should be considered likewise. In some aspects, alkyl groups may be branched. In other aspects, alkyl groups may be unbranched or straight. In other aspects the alkyl groups may be a mixture of branched or unbranched. One or more of the alkyl groups may be saturated, unsaturated, or a mixture there of. In other aspects, the alkyd groups may substituted, unsubstituted, or a mixture thereof.

[0023] The term “Substituted” as used herein means that one of the hydrogen atoms of the alkyl chain is replaced by another substituent. In some aspects, the alkyl groups are substituted in one more places by hydroxyl, amino, dialkyl amino, alkyl acetylated hydroxyl, an alkyl ester, or an alkyl ether substituent. In some embodiments, the alkyl group is substituted with a hydroxyl or alkyl acetylated hydroxyl group.

[0024] The term “Base Oil” as used herein means the primary lubricating components of a lubricant formulation not including additional performance additives. The base oil may be a single lubricating components or a mixture of multiple lubricating components depending on the particular needs of the intended application.

[0025] Unless specifically indicated otherwise, all percentage reported herein are intended to be percentages by weight of the final composition referenced (i.e., wt%).Compounds of Formula 1wherein n is an integer from 2-6; R is C1-C22 alkyl; R2 is C3-C12 alkyl; R3 is hydrogen or C1-C10 alkyl.

[0026] In some aspects, the compounds of Formula 1 are those wherein R is a C3-C12 alkyl. In other aspects, R is a branched Ce-Cio alkyl. In other aspects, R is 2-ethylhexyl.

[0027] In some aspects, the compounds of Formula 1 are those where R2 is a C5-C11 alkyl. In other aspects, R2is a straight chain saturated or unsaturated C7-C11 alkyd. In other aspects, R2is a straight chain C11 alkyl.

[0028] In some aspects, the compounds of Formula 1 are those where R3 is a branched C4- C12 alkyd. In other aspects, R3 is a straight chain C4-C8 alkyd. In other aspects, R3 is a straight chain Ce alkyl.

[0029] In some aspects, the compounds of Formula 1 are those where R is 2-ethylhexyl, R2 is a straight chain C9 alkyl, and R? is a straight chain Cs alkyl.

[0030] In one aspect, a subset of the compounds of Formula 1 can be represented as compounds of Formula 3.Preparation of compounds of Formulas 1 and 3

[0031] Compounds of Formulas land 3 can be prepared through the oligomerization of a hydroxy substituted fatty acid (or mixture of hydroxy substituted fatty acids) and subsequent esterification of the remaining acid groups with an alcohol. Hydroxy substituted fatty acids are known in the art, commercially available, and may be prepared by one of skill in the art. As shown in the Examples 12-hydroxystearic acid and 10-hydroxystearic acid maybe used to prepare compounds of Formula 1. Either enantiomer, or a mixture thereof, of the hydroxystearic acid is functional in the present disclosure. Other hydroxy substituted fatty acids are known in the art and may be prepared by example through epoxidation of an unsaturated fatty acid followed by reductive ring opening can yield a variety of monohydroxy Patty acid residues. 10-hydroxystearic acid (CAS: 638-26-6) is known in the art and can be purchased or prepared by enzymatic treatment of oleic acid. 12-Hydroxy stearic acid (CAS: 106-14-9) can be directly derived from castor oil and is commercially available from a variety of companies such as Gokul Overseas, Jayant AgroOrganics Ltd, De Monchy UK Ltd; Acme Hardesty, or Hampshire Commodities Ltd. Because commercially available 12-hydroxystearic acid is derived from castor oil, it typically contains a quantity of stearic acid as an impurity. A representative example of commercially available 12- hydroxystearic acid is shown in the examples.

[0032] A hydroxy substituted fatty acid, or mixture of acids, can be oligomerized at elevated temperature using a tin, titanium, or nitrogen containing catalyst where the formed water is removed. The reaction is typically performed in the absence of a solvent, but some a smallamount of solvent could optionally be used. The water removal may be accomplished by means of an entrainer, reduced pressure, and / or nitrogen sparging. The result of this step is an oligomerized acid which includes a distribution of compounds of Formula 2 as follows:wherein n is an integer from 2-6; R2 is C3-C12 alkyl; R3 is hydrogen or C1-C10 alkyl.

[0033] The progress of the oligomerization may be tracked by the reduction in acid value of the reactants. The degree of oligomerization may be limited by the presence of other fatty acids in the starting materials that effectively endcap the reactive hydroxyl group. For example, typically, a distribution is achieved with the majority of the oligomers containing between 2 and 6 units and greater than 50% containing 3 or more units. Figure 1 shows the GPC distribution of an Example 11B of the present disclosure. In addition, pre-oligomerized hydroxy fatty acids are also commercially available such a Hypermer LP1 from Croda.

[0034] The Compounds of Formula 2 can then be esterified by reaction with a straight or branched alcohol having from 1 to 22 carbon atoms. In certain aspects, the alcohol may be selected from methanol, ethanol, isopropanol, butanol, 2-ethylhexanoL 2-(2-butoxypropoxy)propan-l-ol (DPnB), 1-decanol, 1-octanol, 2-octanol, and Isofol 18 (2-Octyl decyl). Additional tin, titanium, nitrogen, or acid containing catalyst may be employed at this point, and formed water is removed, yielding an esterified product of Formula 1 with an AV of less than 1.0 KOH / g or less than 0.2mg KOH / g.

[0035] Alternatively, compounds of Formula 1 can be prepared in a single pot by reacting a hydroxy fatty acid with an alcohol directly. In this case, the hydroxy fatty acid is heated in the presence of an excess of alcohol under nitrogen. Catalyst such as TNBT is typically added part way though the reaction to reach an AV of less than 0.2mg KOH / g.

[0036] The compounds of Formula 1 and 3 may be used as antioxidants in the preparation of composition useful a variety of applications including, but not limited to, lubricating the interface of two mechanical surfaces. The interface may be any two surfaces that require lubrication. For example, but not limited to, surfaces such as gears, motors, drilling, milling, hydraulics, and like. In some aspects, the lubricant is a gear oil. The gear oils may be eitherautomotive or industrial gear oils. Automotive (EV and ICE) gear oils include those suitable for use in manual transmissions, transfer cases and differentials which all typically use ahypoid gear. By transfer case we mean a part of a four-wheel drive system found in four-wheel drive and allwheel drive systems. It is connected to the transmission and also to the front and rear axles by means of driveshafts. It is also referred to in the literature as a transfer gearcase, transfer gearbox, transfer box or jockey box. Industrial gear oils include those suitable for use with spur, helical, bevel, hypoid and worm gears. Specifically included are those suitable for use in windmill gear boxes which typically have helical gears.

[0037] Automotive gear oils will normally have a viscosity in the range of SAE 50 to SAE 250, and more usually will range from SAE 70W to SAE 140. Suitable automotive base oils also include cross-grades such as 75W-140, SOW-90, 85W-140, 85W-90, and the like. Automotive gear oils are classified by the American Petroleum Institute (API) using GL ratings. API classification subdivides all transmission oils into 6 classes as follows.

[0038] API GL-1 are oils for light conditions. They consist of base oils without additives. Sometimes they contain small amounts of antioxidizing additives, corrosion inhibitors, depressants, and antifoam additives. API GL-1 oils are designed for spiral-bevel, worm gears and manual transmissions without synchronizers in trucks and farming machines.

[0039] API GL-2 are oils for moderate conditions. They contain antiwear additives and are designed for worm gears. Recommended for proper lubrication of tractor and farming machine transmissions.

[0040] API GL-3 are oils for moderate conditions and contain up to 2.7% antiwear additives. Designed for lubricating bevel and other gears of truck transmissions. They are not recommended for hypoid gears.

[0041] API GL-4 are oils for various conditions - light to heavy. They contain up to 4.0% effective anti-scuffing additives. Designed for bevel and hypoid gears which have small displacement of axes, the gearboxes of trucks, and axle units. Recommended fornon-synchronized gearboxes of US trucks, tractors and buses and for main and other gears of all vehicles. These oils are basic for synchronized gearboxes, especially in Europe.

[0042] API GL-5 are oils for severe conditions. They contain up to 6.5% effective antiscuffing additives. The general application of oils in this class are for hypoid gears having significant displacement of axes. They are recommended as universal oils to all other units of mechanical transmission (except gearboxes). Oils in this class, which have special approval of vehicle manufacturers, can be used in synchronized manual gearboxes only. API GL- 5 oils canbe used in limited slip differentials if they correspond to the requirements of specification MILL-21050 or ZF TE-ML-05. In this case, the designation of class will be another, for example, API GL-5+ or API GL-5 LS.

[0043] API GL-6 are oils for very heavy conditions (high speeds of sliding and significant shock loadings). They contain up to 10% high performance anti-scuffing additives. They are designed for hypoid gears with significant displacement of axes. Class API GL-6 are not often applied any more as it is considered that class API GL-5 well enough meets the most severe requirements.

[0044] Most modem gearboxes require a GL-4 oil. and separate differentials (where fitted) require a GL-5 oil.

[0045] Industrial gear oil specifications are governed primarily by American Gear Manufacturers Association (AGMA) in North America or by individual manufacturers themselves. A typical specification for American industrial gear oils is shown below in Table 1.Table 1.

[0046] In Europe, as well as most of the Rest of the World, industrial gear oil specifications are typically written by Deutches Institut fur Normung (e.g., DIN51517-3).Lubricant formulations

[0047] The compounds of Formulas 1 and 3 or mixtures thereof, may be formulated into any composition in need of increased oxidative stability including lubricating compositions. Preparation of lubricating compositions is known in the art and any effective method may be utilized. Typically, ingredients in the formulation are mixed at ambient or elevated temperatures. Mixing can be performed batchwise or continuously as desired. In certain embodiments, the lubricating composition further comprises one or more additives known to those in the art such as friction modifiers, viscosity modifiers, antioxidants, anti-wear additives, extreme pressure additives, defoamers, demulsifers, and corrosion inhibitors. Additives are typically included in the final formulations at a level between 1 and 20% depending on the particular application and needs of the user. Additives may be included separately or as part of what is known in the art as an add pack. An add pack is a commercially available mixture of additives formulated by a supplier for inclusion in particular base oils and for particular applications. In some aspects, the lubricating composition comprises 1 %- 10% additives by weight. In some aspects, the lubricating composition comprises 2%-6% additives by weight.

[0048] Base oils in which the compositions of this disclosure are employed can be based on natural or synthetic oils, or blends thereof can be formulated into final gear oil formulations, provided the lubricant has a suitable viscosity for use in desired applications. The base oils for such use can be mineral oil base stocks such as for example conventional and solvent-refined paraffinic neutrals and bright stocks, hydrotreated paraffinic neutrals and bright stocks, naphthenic oils, cylinder oils, etc., including straight run and blended oils.

[0049] In some aspects, base oil is selected from the group consisting of polyalphaolefins (PAOs), synthetic esters such as polyol esters, polyalkylene glycols (PAGs), oil soluble polyalkylene glycols (OSPs), mineral oils (Groups I, II, and III), fatty acid esters, long chain alkyl esters such as those described and disclosed in WO2022 / 258664, natural oils, greases, petrolatum, waxes, wax esters, and mixtures thereof.

[0050] Synthetic base stocks can also be used in the practice of this invention, such as for example PAO, alkylated aromatics, polybutenes, diesters, polyol esters, polyglycols, polyphenyl ethers, etc., and blends thereof. Polyalphaolefins are typically manufactured from C8 to C14 olefins, and the result is generally combinations of dimers, trimers, tetramers, pentamers, and soforth. It is also known for PAOs and esters to be blended with mineral oils to form semi synthetics. Synthetic base oils are preferred, especially base oils having PAO or mixtures of PAOs as a major component. PAOs are well known and readily available such as Chevron - Synfluid, Exxon - Spectrasyn, INEOS - Durasyn, and the like. Synthetic esters are also well known such as Oleon - Radialube, NYCO - NYCOBASE, Lanxess - Hatcol, and Exxon - Esterex. The skilled artisan is well aware of the technical properties of these materials and how to blend them to a desired outcome.

[0051] The compounds of Formula 1 may be used in base oils in the preparation of a final composition. In some aspects, the composition comprises 0.5% to 95% of one or more of the compounds of Formula 1. In some aspects, the base oil comprises 0.5% to 75% of one or more of the compounds of Formula 1. In some aspects, compounds of Formula 1 comprise between 2 and 10%; between 2% and 8%, between 4% and 8%, or betw een 4% and 10% of the lubricating composition.

[0052] The compounds of Formula 3 may be used in base oils in the preparation of a final lubricating formulation. In some aspects, the composition comprises 0.5% to 95% of one or more of the compounds of Formula 3. In some aspects, the base oil comprises 0.5% to 75% of one or more of the compounds of Formula 3. In some aspects, compounds of Formula 3 comprise between 2 and 10%; between 2% and 8%, between 4% and 8%, or between 4% and 10% of the lubricating composition.

[0053] In some aspects, the composition further comprises one more compounds of Formula 4. In some aspects, the base oil comprises 0.5% to 20% of one or more of the compounds of Formula 3 and further comprises one more compounds of Formula 4.EXAMPLESTable 2.

[0054] The commercially availablel2-hydroxystearic acid utilized had the following fatty acid composition shown in Table 3.Table 3.Examples 1A-F

[0055] A 2000 ml 5-necked round-bottomed flask equipped with a magnetic sealed stirrer guide with a PTFE centrifugal stirrer, temperature feedback probe and isomantle, a nitrogen inlet and outlet via a distillation head, Liebig condenser, receiver flask and exit bubbler, was charged with 12-hydroxystearic acid (450g, 1.44 mol; 1.98 equiv.) and the contents heated to 190°C with N2 purge (15ml min '). with stirring (420 rpm) once molten. When the reaction temperature was achieved, vacuum was applied to 200 mbar (maintaining a nitrogen purge). After 1.5 h the pressure was lowered to 50 mbar and after 2.5h the reaction was cooled and the AV measured as 78.0mg KOH / g. The reaction was restarted and continued for a further 30 min to give an AV of 70.7mg KOH / g. The reaction was cooled to below expected esterification reaction temperature, the distillation head was replaced with a Dean and Stark trap with vertical double surface Liebig condenser. 2-Ethylhexan-l-ol (2-EH; 95.0g, 0.72 mol; 1 equiv.) was charged to the reaction vessel and the Dean and Stark trap filled with an additional 33 ml of 2-EH. The reaction was heated to 190°C and vacuum applied with caution to achieve a steady reflux of 2-EH into the trap. Refluxwas maintained during the reaction by lowering the pressure as necessary. After 8h under reaction conditions (1 Ih total reaction time) the AV was measured to be 7.0mg KOH / g. Catalyst (TNBT, 0.2 ml) was added and the reaction allowed to progress for a further 5.5 h (16.5h total reaction time), after which the AV of the reaction had reached <0.2mg KOH / g. The reaction temperature was adjusted to 125°C and full vacuum applied to remove the excess 2-EH through the trap. When distillation of 2-EH ceased the trap was replaced with a simple distillation arm, 5g decolorizing charcoal was added to the reaction vessel and the nitrogen headspace purge was replaced with a sparge placed as low as possible in the vessel without contacting the stirrer paddle. Full vacuum was applied to strip out the remaining free 2-EH and maintained for 3h. The vessel was repressurized through the sparge and the product oligo-ester vacuum filtered through a bed of Celite filter aid to yield 1A [2-ethylhexyl poly (12-hydroxy stearate)] as a pale yellow viscous liquid.

[0056] Example IB was a repeat experiment with the same stoichiometry as 1 A, however, the hydroxystearic acid oligomerization was run for 4 hours to an AV of 65.3mg KOH / g prior to the introduction of the 2-EH.

[0057] Example 1C was a repeat experiment with the same stoichiometry as 1 A, however, the hydroxystearic acid oligomerization was run for 3.5 hours to an AV of 70 mg KOH / g prior to the introduction of the 2-EH.

[0058] Example ID is a repeat of 1C.

[0059] Example IE is repeat of Example 1A with a 10% stoichiometric increase in 2-EH.Example 2

[0060] The material from Example 1 was returned to a reaction vessel. A second 250ml 3-necked flask was charged with 50ml distilled water and a sizable quantity of anti-bumping granules, and fitted with a sintered gas distribution tube via a length of PTFE tubing. The gas distribution tube was introduced into the sample reaction vessel so that the sintered end was as low7as possible without fouling the stirred blade. The steam vessel was placed in a water bath on a hot-plate stirrer with a set point of 30°C. The reaction vessel contents were heated to 115°C under a separate nitrogen purge. At the set temperature the nitrogen purge was shut off and vacuum applied, causing low7temperature steam to be drawor through the gas distribution tube and sparge through the reaction bulk. After approximately 3 hours the heat was removed and the vacuum tap closed. Once at room temperature the vacuum was released though the steam sparge by repressurising the steam generator flask.Example 3

[0061] A 1000ml 5-necked round-bottomed flask equipped magnetic sealed stirrer guide with PTFE centrifugal stirrer, temperature feedback probe and isomantle, a nitrogen inlet and outlet via a Dean and Stark trap. Liebig condenser and exit bubbler was charged with Hypermer LP1 (520.0g. 0.297 mol CO2H; 1 equiv.) and 2-ethylhexan-l-ol (57.9g, 0.445 mol; 1.5 equiv.) and the mixture heated to 220°C with a nitrogen purge of 80ml min1and stirring at 500 rpm. After 2.5h the temperature was reduced to 180°C, 0.2 ml TNBT was added and the reaction allowed to progress for a further 16h, after which time the AV had fallen to 1.36mg KOH / g. An additional 0.2ml TNBT was added and the reaction continued for a further 24h after which time the AV had fallen to 0.1 mg KOH / g. The temperature was reduced to 120°C and vacuum applied with a nitrogen sparge for 3h and the product filtered through SW-10 cellulose filter aid overnight to yield the material of Example 3.Example 4

[0062] 12-hydroxy stearic acid (491.6g, 1.67 mol) and 2-octanol (108.4g, 0.83 mol, -50% excess) were charged to a 5-necked round bottomed flask equipped with a nitrogen headspace purge (~30ml / min), overhead stirrer with centrifugal stirrer bar (~500rpm), temperature feedback loop, Dean-Stark receiver with organic circulation and collection flask. The Dean-Stark receiver was fitted with a vertical condenser and a dreschel bottle to ensure a nitrogen atmosphere. Note: For 12-hydroxystearic acid mol calculation, the average Mwt was calculated from the acid value. The reaction was initially heated to 180°C before gradually increasing the temperature to 200°C, rate of heating controlled by rate of water evolution, ~ 2 hours. TnBT catalyst (~0.2g) and 2- octanol (~10mls) were added to the reaction vessel. Acid Value < 20mgKOH / g. The reaction was maintained at 200°C until the reaction was complete (AV < 0.2mgKOH / g). An additional dose of TnBT catalyst (0.2g) and 2-octanol (~10mls) were added after 16 hours. The product was cooled to 110°C, then activated carbon (~1 wt%) was added to the reaction vessel and vacuum was applied (< 5 mbar). Reaction conditions were maintained for 5 hours before the product was discharged and filtered. The material was vacuum filtered using Fibra-cel SW-10 as the filter aid. The product, 2-octyl poly(12-hydroxystearate), a clear, pale yellow, viscous liquid.Example 5

[0063] 12-hydroxystearic acid (955.4g, 3.25 mol) and 1-decanol (244.7g, 1.55 mol, -50% excess) were charged to a 5-necked round bottomed flask equipped with a nitrogen headspacepurge (~30ml / min), overhead stirrer with centrifugal stirrer bar (~450rpm), temperature feedback loop, Dean-Stark receiver with organic circulation and collection flask. The Dean-Stark receiver was fitted with a vertical condenser and a dreschel bottle to ensure a nitrogen atmosphere. Note: For 12-hydroxy stearic acid mol calculation, the average Mwt was calculated from the acid value. The reaction was initially heated to 160°C before gradually increasing the temperature to 200°C, rate of heating controlled by rate of water evolution, ~ 3 hours. Tyzor TnBT catalyst (~0.4g) and 1 -decanol (~25mls) were added to the reaction vessel, Acid Value < 30mgKOH / g. The reaction was maintained at 200°C until the reaction w as complete (AV < 0.2mgKOH / g), approximately 24 hours. The product was cooled to 145°C. then activated carbon (~1 wt%) was added to the reaction vessel and vacuum was applied (< 5 mbar). Reaction conditions were maintained for 5 hours before the product w as discharged and filtered. The material was vacuum filtered using Fibra-cel SW-10 as the filter aid. The product, 1 -decyl poly (12-hydroxy stearate) was an off white, paste like solid.Example 6

[0064] 12-hydroxy stearic acid (327.2g, 5.29 mol total) and 2-ethyl hexanol (344.1, 2.64 mol, -50% excess) were charged to a 5-necked round bottomed flask equipped with a nitrogen headspace purge (~30ml / min). overhead stirrer with centrifugal stirrer bar (~500rpm). temperature feedback loop, and a Dean-Stark receiver with organic circulation and collection flask. The Dean- Stark receiver was fitted with a vertical condenser and a dreschel bottle to ensure a nitrogen atmosphere. Note: For 12-hydroxy stearic acid mol calculation, the average Mwt was calculated from the acid value. The reaction was initially heated to 165°C before gradually increasing the temperature to 190°C, rate of heating controlled by rate of water evolution, - 1 hours until and AV of less than 15 was achieved actual AV = 13.2 mgKOH / g. The reaction was maintained at 190°C as TnBT catalyst was added (~1.7g). The reaction was maintained at 190°C until the reaction was complete (AV < 0.2mgKOH / g), approximately 38 hours. The reaction w as cooled to 120°C. The reaction was then reconfigured, removing the Dean-stark receiver and replacing with a simple distillation arm, the nitrogen headspace purge was reconfigured to a sub-surface nitrogen sparge and then vacuum w as applied (< 5 mbar, to strip off any free 2-ethylhexanol. Reaction conditions were maintained for 5 hours before the reaction w as repressurized and sampled for acid value (AV = 0.12 mgKOH / g) and GC analysis to determine the free 2-ethyl hexanol content of ~l,500ppm.

[0065] The reaction was reconfigured for steam stripping: a subsurface nitrogen sparge was connected to a 1 liter, 3 necked round bottomed flask filled with water, ~500g, and antibumping granules. The nitrogen / steam exhaust tube from the 3 necked flask was connected to a sub-surface sparge in the reactor vessel. The reaction was heated to 110°C and vacuum applied (<20 mbar), the nitrogen flow to the vessel was reduced to a minimal amount. The water in the flask was heated gently with a heat gun to allow the water to remain at room temperature and a vigorous bubbling of gas (nitrogen + steam) in the reaction vessel observed: for a constant vacuum, the temperature of the water will dictate the vigor of the steam strip process. These conditions were maintained for 3 hours before re-pressurizing and replacing the steam sparge with the nitrogen purge. The product was sampled for acid value (AV= 0. 12mg KOH / g) and GC analysis to determine the free 2-ethyl hexanol content (<60ppm, Target <100 ppm). The product was discharged, filtered (filter aid: Celite® 512) and subject to full analytical work up. The product, 2-ethylhexyl poly 12-hydroxy stearate, a clear, amber, viscous liquid.

[0066] Material from Example 6 was analyzed by GPC to determine the distribution of repeating units.Table 4.Example 7

[0067] Material prepared according to Example 6 (550.0g), activated carbon (~1 wt%) and Tonsil Optium 210-ff (~1 wt%) were charged to a 5-necked round bottomed flask equipped with a sub-surface nitrogen sparge (~30ml / min), overhead stirrer with centrifugal stirrer bar (~400rpm), temperature feedback loop, condenser set for distillation removal and collection flask. The collection flask was fitted with both a dreschel bottle, to ensure a nitrogen atmosphere, andvacuum capabilities. The reaction was heated to 110°C and then vacuum was applied (< 5 mbar). Reaction conditions were maintained for 3 hours before the reaction was re-pressurized and the product discharged and filtered, using Celite® 512 as a filter aid. The product was a clear, amber, viscous liquid.Example 8

[0068] Material prepared according to Example 6 (550.0g) and acetic anhydride (110 mis, large excess) were charged to a 5-necked round bottomed flask equipped with a sub-surface nitrogen sparge (~30ml / min), overhead stirrer with centrifugal stirrer bar (~400rpm), temperature feedback loop, condenser set for distillation removal and collection flask. The collection flask was fitted with both a dreschel bottle, to ensure a nitrogen atmosphere, and vacuum capabilities. The reaction was heated to and maintained at 100°C for approximately 5 hours before the reaction was reconfigured for steam stripping: a subsurface nitrogen sparge was connected to a 1 liter, 3 necked round bottomed flask filled with water, ~500g, and anti-bumping granules. The nitrogen / steam exhaust tube from the 3 necked flask was connected to a sub-surface sparge in the reactor vessel. The reaction was heated to 110°C and vacuum applied (<20 mbar), the nitrogen flow to the vessel was reduced to a minimal amount. The water in the flask was heated gently with a heat gun to allow the water to remain at room temperature and a vigorous bubbling of gas (nitrogen + steam) in the reaction vessel observed: for a constant vacuum, the temperature of the water will dictate the vigor of the steam strip process. These conditions were maintained for 3 hours before repressurizing and replacing the steam sparge with the nitrogen purge. Activated carbon (~1 wt%) was added to the vessel and vacuum was applied (< 5 mbar). Reaction conditions were maintained for 3 hours before the reaction was repressurized and the product discharged and filtered, using Celite® 512 as a filter aid. The product, 2-ethylhexyl poly-12-hydroxystearyl acetylate, a clear, pale yellow, viscous liquid.Example 9

[0069] A 2000 ml 5-necked round-bottomed flask equipped magnetic sealed stirrer guide with PTFE centrifugal stirrer, temperature feedback probe and isomantle, a nitrogen inlet and outlet via a Dean and Stark trap, Liebig condenser and exit bubbler was charged with 12- hydroxystearic acid (1000 g. 3.19 mol; 1 equiv.) and 2-ethylhexan-l-ol (519.2 g, 3.99 mol; 1.25 equiv.) and the mixture heated with a set point 200°C with N2 purge (15 ml min ') and stirring (520 rpm) once molten. The Dean and Stark trap initially filled with 2-EH but once this wasdisplaced by the water of reaction the level of water in the trap was held at greater than ca. 80% maintained the excess of alcohol in the reaction vessel. After 3 h the temperature of the reaction had reached 200°C and the set point was increased to 220°C. After a further 1.5 h a total of 54 ml water had been removed from the reaction vessel. Catalyst (TNBT, 0.2 ml) was added and the reaction allowed to progress for a further 16 h after which the AV of the reaction had reached <0.2mg KOH / g. An additional 0.2 ml TNBT was added and the reaction continued for a further 3 h. The mixture was cooled to 110°C, de-colorizing charcoal (5g) added and vacuum applied cautiously to prevent foaming to remove excess 2-EH for 2h. The charcoal was removed by filtration and full vacuum applied at 125°C with a nitrogen sparge until no free 2-EH was detected in the product by GC or odor.Example 10

[0070] A 1000 ml 5-necked round-bottomed flask equipped magnetic sealed stirrer guide with PTFE centrifugal stirrer, temperature feedback probe and isomantle, a nitrogen inlet and outlet via a Liebig condenser was charged with a sample of 2-ethylhexyl 12-hydroxystearate (from Example 9, 550g; nom. 1.333 mol) and the reactant heated to 90°C. Slow addition of acetic anhydride (125ml; 136.0g, 1.333 mol) was started Only a minimal exotherm was observed and when the reaction temperature began to fall heating was applied to raise the temperature to 110°C. After 50ml of acetic anhydride was added the addition was stopped and a sample taken to ensure reaction was occurring. Addition was completed more rapidly and 0.1ml methanesulphonic acid was added as catalyst. After completion of the reaction the excess acetic anhydride and formed acetic acid was distilled out under vacuum. De-colorizing charcoal (5g) was added and heating at 125°C under vacuum was continued for a further 3 h before filtration of the final product with SW-10 cellulose filter aid.

[0071] Table 5 shows the oxidative stability (induction time) of the Examples described above.Table 5.Benchmark 1 is a commercially available endcapped estolide sold by Biosynthetics under the product code BT22. Benchmark 2 is a commercially available high performing pentaerythritol tetraisostearate esters sold by Cargill Incorporated under the brand name Priolube 3987.

[0072] Tables 5, 6, and 7 show the comparison of the stability of a compounds of Formula 1 with an endcapped acylated version as well with two commercial benchmarks. It is very surprising that the Examples of formula 1 containing free hydroxyl groups (as demonstrated by the hydroxyl value) are approximately 7 times more stable than the corresponding acylated version. This is a dramatic and unexpected increase in oxidative stability that would be highly advantageous to an end user.Table 6.Table 7.Example 11: 2-ethylhexyl poly(12-hydroxystearate) scale up

[0073] The vessel was inspected to ensure it was clean and in working order before the oil jacket was set to 90°C constant oil temperature. The vessel was sealed, ensuring the mam dram valves were shut before a full vacuum was applied to assess if the vessel was vacuum tight. The vacuum was released with nitrogen before the 12-hydroxy stearic acid was charged via the sight glass port. For batch quantities Table 8 below. Once charged the sight glass port was closed and the constant oil temperature was increased to 160°C with 100 ml / min nitrogen headspace.

[0074] Once the 12-HSA was fully molten the stirrer was turned on (150 rpm), the temperature was increased to 190°C constant reactor temperature and the nitrogen headspace w asincreased to 200 ml / min. An initial pressure of 800 mbar was applied as the contents temperature reached 190°C; pressure was then reduced to 200 mbar over 10 minutes and then held for 1.5 hrs. After which the pressure was reduced to <50 mbar and held for a further 1 hr. The vacuum was broken with nitrogen and the vessel pressurized to 1100 mbar. The contents were sampled via the sparge valves and an acid value was measured. After sampling, nitrogen was blown down the sparge for 10 minutes. If the acid value was between 70-80 mg KOH g'1and the reaction was deemed complete and progressed to the next stage; if it was not in specification the pressure was reduced to <50 mbar and the reaction continued. Until the desired AV was reached.

[0075] The vessel was cooled to <140°C constant reactor temperature before a small access port on the lid of the vessel was unscrewed. The required 2-ethyl hexanol was charged to the vessel before the port was reclosed. Additionally, the binary' separator was filled with l / 3rdwater and 2 / 3rd2-ethyl hexanol. The vessel was then set to 190°C constant reactor temperature and once reached the pressure was reduced to 800 mbar. The pressure was then reduced periodically to maintain a suitable level of reflux.

[0076] After approximately 6-7 hours, the vacuum was broken with nitrogen and the vessel pressurized to 1100 mbar. The contents were sampled via the sparge valves and an acid value was measured. If the acid value was <10 mg KOH g'1, the pressure was released, and tetra n-butanol titanate (TnBT)was added via the small access port on the lid. The reaction was then continued by decreasing the pressure until reflux was achieved. If the acid value was > 10 mg KOH g’1, the reaction was just continued and sampled again an hour later. After sampling, nitrogen was blown down the sparge for 10 minutes.

[0077] After the TnBT was added, the reaction was continued, and the pressure reduced to ensure a suitable reflux was maintained. Periodically the vessel was sampled, using the same procedure detailed above, until the acid value was <0.2 mg KOH g"1and the reaction w as deemed complete.

[0078] Once complete the vessel was set to 125°C constant reactor temperature and the stirrer speed was increased to 200 rpm. The binary separator w as drained; with any water being discarded and any 2-ethyl hexanol kept for further batches. Once at temperature the pressure in the vessel was reduced to <50 mbar and free 2-ethyl hexanol distilled out of the vessel into the binary' separator. Once the 2-ethyl hexanol had stopped distilling, the vessel was set to 110°C and the vacuum was broken with nitrogen.

[0079] A vacuum rated nylon tube was attached to the reactor and the other end was attached to a valve fitted to a 500 ml three-neck flask. A thermometer and a second valve werefitted to the other necks of the flask. The three-neck flask was then placed into a DrySyn block on a hotplate with a feedback probe in the block. Water and anti-bumping granules were placed into the flask and the block was heated to 110°C.

[0080] The pressure of the 50 L vessel was reduced to <50 mbar and, with the second valve on the 500 ml flask closed and the first valve open, reactor valves were opened. This reduced the pressure in the 500 ml flask and generated steam that was rawn into the 50 L vessel via the sparge. The generated steam was collected in the binary separator along with any 2-ethyl hexanol. After the 2-ethyl hexanol had stopped being removed from the vessel, valves were closed and the vacuum of the vessel was broken with nitrogen.

[0081] The vessel was pressurized to 1100 mbar before the contents were sampled via the sparge valves and an acid value was measured. After sampling, nitrogen was blown down the sparge for 10 minutes. A 2-ethyl hexanol content w as determine and if >100 ppm the steam stripping was continued. If the 2-ethyl content was <100 ppm the stripping was deemed complete.

[0082] With batches 11B, 11C, and HD, the vessel was set to a constant reactor temperature of 90°C and the pressure was reduced to <50 mbar to dry. These conditions were maintained for 1 - 2 hours. The vacuum was broken with nitrogen and the vessel was pressurized to 1100 mbar. The bottom valves were opened and the material w as discharged into pre-weighed containers.

[0083] With batch HA, the vessel was set to a constant reactor temperature of 90°C and pressurized to 1100 mbar. The bottom valves were opened and the material was discharged into pre-weighed containers. The material was then charged to the 30 L glass vessel with Norit SA. The oil jacket was set to 90°C and a vacuum of <50 mbar was applied. These conditions were maintained for 1-2 hours before the vacuum was broken with nitrogen. The material was then discharged into pre-weighed containers.

[0084] All four batches were filtered via Buncher funnel using C elite 545 filter aid and a Whatman 54 filter paper. Once filtered the material was discharged into pre-weighed containers. l ' lTable 8. 50 L Reaction Quantities and DetailsTable 9.Example 12: Fractionation Effects

[0085] The material from Example 1 IB was sent through a 4” Pope wiped film evaporator (WFE) under vacuum at various condition to separate out the lower molecular weight components. Four different WFE conditions were evaluated leading to 4 sets of residues and distillates set out in Table 10 below.Table 10.

[0086] Tablel 0, shows that polymer content and properties may be modified by separation of components via treatment with a WFE. Materials with higher polymer content may be produced. Depending on desired characteristics, separation of components may be desirable in some applications.Example 13: Effects of change in hydroxyl positionExample 13A: 2-Ethylhexyl polv-10-hydroxy stearic acid

[0087] 10-Hydroxy stearic acid (900g, 95% purity, prepared via enzymatic process as described in Example 17 with subsequent recrystallisation) was heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. 1 h. Once at temperature the pressure was gradually decreased to 175 mbar in 3 hrs and then further reduced to <50 mbar. After reaching the acid value (75 mg KOH / g) the reaction was stopped and cooled to yield poly 10HSA.

[0088] Poly-10HSA from above and 190 g 2-ethylhexanol were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. 1 h. During heating up a vacuum of 300 mbar was applied. The vacuum was slowly decreased in 6 h to 100 mbar. At an AV of 19 mg KOH / g 0.6g TBT was added. After another 7h in which the pressure was further decreased to 90 mbar the reaction was stopped at an AV of 0.2mg KOH / g. The excess 2-ethylhexanol was distilled off. The final product was bleached (10g Norit SA4) and steam stripped at 110°C for 4 hours. The product was dried and 4g Supercel filter aid was added. After a time consuming filtration (24 h) the product 13A was isolated and analyzed (see below).Example 13B: Ethylhexyl polv 10-hvdroxystearate / stearate (86 / 14)

[0089] To mimic the stearic acid content of the commercially available 12-hydroxystearic acid, a comparison was done by dosing stearic acid into the starting 10-hydroxy stearic acid.

[0090] 10-Hydroxy stearic acid (810g) (95% purity, prepared via enzymatic process with subsequent recrystallisation) and 90g Stearic acid (98% pure) were heated in a 2L round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. Ih. Once at temperature the pressure was gradually decreased to 200 mbar in 2 hrs and then further reduced to <50 mbar. After reaching the acid value (73mg KOH / g) the reaction was stopped and cooled to yield poly lOHAS / stearic acid.

[0091] Poly 1 OHSA / stearic and 190g 2-ethylhexanol were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. Ih. After reaching the reaction temperature the pressure was decreased in 2 hours to 300 mbar. At an AV of 25mg KOH / g 0.6g TBT was added. The pressure was reduced to 100 mbar. After another 7.5h the reaction was stopped at an AV of 0.2mg KOH / g. The excess 2- ethylhexanol was distilled off. The final product was bleached (10g Norit SA4) and steam stripped at 110°C for 3.5 hours. The product was dried and 4g Supercel filter aid was added. After a time consuming filtration (~ 5 h) the product 13B was isolated and analyzed (see below).Example 14: Effects of unsaturation in backboneExample 14A: 2-Ethylhexyl polv 12-hydroxystearate / ricinoleate (97k^ / 21 / ^)

[0092] 12 Hydroxy stearic acid (877.5g) and 22.5g Ricinoleic acid were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. Ih. Once at temperature the pressure was gradually decreased to 200 mbar in 2.5 hrs and then further reduced to <50 mbar. After reaching the acid value (73mg KOH / g) the reaction was stopped and cooled.

[0093] Poly 12HSA / ricinoleic from above and 190g 2-ethylhexanol were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. Ih. After reaching the reaction temperature the pressure was decreased in 3.5 hours to 300 mbar. At an AV of 20 mg KOH / g 0.6g TBT was added. The pressure was reduced to 100 mbar in 2.5 h. After another 7.5 h the reaction was stopped at an AV of 0.2mg KOH / g. The excess 2-ethylhexanol was distilled off. The final product was bleached (10g Norit SA4) and steam stripped at 110°C for 4 hours. The product was dried and 4.4g Supercel filter aid was added. After filtration the product 14A was isolated and analysed (see Table 11).Example 14B: 2-Ethylhexyl poly-12-hydroxystearate / ricinoleate (95 / 5)

[0094] 12 Hydroxy stearic acid (978g) and 51.5g ricinoleic acid were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. Ih. Once at temperature the pressure was gradually decreased to 200 mbar in 3.5 hrs and then further reduced to <50 mbar. After reaching the acid value (72 mg KOH / g) the reaction was stopped and cooled to yield poly 12HSA / ricinoleic.

[0095] Poly 12HSA / ricinoleic from above and 217g 2-ethylhexanol were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. Ih. After reaching the reaction temperature the pressure was decreased in 4 hours to 300 mbar. At an AV of 16.6mg KOH / g 0.68g TBT was added. The pressure was reduced to 100 mbar in 1.5h. After another 6 h the reaction was stopped at an AV of 0. 12 mg KOH / g. The excess 2-ethylhexanol was distilled off. The final product was bleached (11g Norit SA4) and steam stripped at 110°C for 4 hours. The product was dried and 4.8g Supercel filter aid was added. After filtration the product was isolated and analyzed. The acid value was higher than expected (0.86mg KOH / g). Therefore 975 g product was mixed with 50g 2-ethylhexanol and esterified at 190°C and 150 mbar until the AV was 0.12mg KOH / g. The excess 2-ethylhexanol was distilled off. The final product was bleached (11g Norit SA4) and steam stripped at 110°C for 4 hours. The product was dried and 4.8g Supercel filter aid was added. After filtration the final product 14B was isolated and analyzed (see Table 11)Example 14C: Ethylhexyl polv-12-hydroxystearate / ricinoleate (92k^ / 71 / ^)

[0096] 12-Hydroxy stearic acid (865g) and 65 g ricinoleic acid were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. 1 h. Once at temperature the pressure was gradually decreased to 200 mbar in 2 hrs and then further reduced to <50 mbar. After reaching the acid value (73mg KOH / g) the reaction was stopped and cooled.

[0097] Poly 12HSA / ricinoleic prepared above and 196g 2-ethylhexanol were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. 1 h. After reaching the reaction temperature the pressure was decreased in 1.5 hours to 250 mbar. At an AV of 16mg KOH / g 0.6g TBT was added. The pressure was reduced to 100 mbar in 3 h. After another 5 h the reaction was stopped at an AV of 0.13mg KOH / g. The excess 2-ethylhexanol w as distilled off. The final product was bleached(lOgNorit SA4) and steam stripped at 110°C for 4 hours. The product was dned and 4.4g Supercel filter aid was added. After filtration the product 14C was isolated and analysed (see Table 11).Table 11.Example 15: Effect of Acetylation and reduction of hvdroxyl valueExample 15A: Acety lation to Hydroxyl Value of 29 mg KOH g'1

[0100] Poly-12-HSA from Example 11B, (1264.2g, 1.01 mol) was placed into a round bottom 5-neck flask. The flask was fitted with a stirrer, temperature probe, pressure equalizing dropping funnel, nitrogen headspace (30ml min'1) and a takeoff arm leading to a horizontal condenser. The condenser was attached to a collection flask that was fitted with a nitrogen outlet leading to a Dreschel bottle filled with weak potassium hydroxide solution in water and phenolphthalein indicator.

[0101] The temperature of the vessel was increased to 130°C and acetic anhydride (48.8g, 0.48 mol) was placed into the dropping funnel. Once at temperature, acetic anhydride was slowly added to the vessel over 2 hours. The nitrogen flow was increased to 50ml min'1and held for 1.75 hours before the material was steam stripped.

[0102] Steam stripping was carried out by changing the nitrogen headspace to a nitrogen sparge (50ml min'1). The sparge was connected to an auxiliary vessel filled with reverse osmosis water and with a nitrogen inlet. The auxiliary vessel was placed in a water bath held at 60°C. The Dreschel bottle was replaced with a vacuum pump and the pressure in the main vessel was reduced to ~60 mbar, thus reducing the pressure of the auxiliary vessel and causing steam to be generated. The generated steam was carried into the main vessel through the sparge by the nitrogen. After 15 minutes the temperature of the vessel was reduced to 110°C and held for 30 minutes. The pressure of the vessel was then reduced to 40 mbar and held for a further 20 minutes before the vacuum was broken with nitrogen.

[0103] The sparge was replaced with a nitrogen headspace and the vessel pressure reduced to 20 mbar to dry. After ~2 hours the vacuum was broken with nitrogen and the material was sampled (SI). An acid value of 0.28mg KOH g'1and a hydroxyl value of 29mg KOH g'1was measured. The nitrogen headspace was replaced with a nitrogen sparge, and the steam stripping was continued with a vessel pressure of 20 mbar. After 5.5 hours the vacuum was broken with nitrogen and the nitrogen sparge replaced with nitrogen headspace. The temperature of the vessel was reduced to 90°C and the material was dried again at a vessel pressure <30 mbar. After a further 3.25 hours, the vacuum was broken with nitrogen and a sample (S2) was taken. An acidvalue of 0.19mg KOH g’1and a hydroxyl value of 29mg KOH g’1was measured. As the acid value was <0.2mg KOH g’1a further, larger, sample was taken. In total ~220g of material was sampled as Example 15 A.Example 15B: Acetylation to Hvdroxyl Value of 1 Img KOH g’1

[0104] The remaining material was acetylated further by placing acetic anhydride (30.4g, 0.30 mol) into the dropping funnel and heating the vessel to 130°C. Once at temperature, acetic anhydride over 2.25 hours and then allowed to react for a further 1.5 hours before the vessel was cooled to 110°C and steam stripped. Steam stripping was carried out by changing the nitrogen headspace to a nitrogen sparge (50ml min’1). The sparge was connected to an auxiliary vessel filled with reverse osmosis water and with a nitrogen inlet. The auxiliary vessel was placed in a water bath held at 60°C. The Dreschel bottle was replaced with a vacuum pump and the pressure in the main vessel was reduced to <30 mbar, thus reducing the pressure of the auxiliary vessel and causing steam to be generated. The generated steam was carried into the main vessel through the sparge by the nitrogen.

[0105] After 5 hours the steam stripping was stopped by breaking the vacuum with nitrogen and the sparge was replaced with nitrogen headspace. The vessel was cooled to 90°C before the pressure was reduced to <80 mbar for 2 hours. A sample (S3) was taken with an acid value of 0.16mg KOH g’1and a hydroxyl value of 1 Img KOH g’1was measured. As the acid value was <0.2mg KOH g’1a further, larger, sample was taken. In total ~235g of material was sampled as Example 15B.Example 15C: Acetylation to Hvdroxyl Value of 3 mg KOH g’1

[0106] The remaining material was acetylated further by placing acetic anhydride (20.0g, 0.20 mol) into the dropping funnel and heating the vessel to 130°C. Once at temperature, acetic anhydride over 1 hour and then allowed to react for a further 4 hours before the vessel was cooled to 110°C and steam stripped. Steam stripping was carried out by changing the nitrogen headspace to a nitrogen sparge (50ml min’1). The sparge was connected to an auxiliary vessel filled with reverse osmosis water and with a nitrogen inlet. The auxiliary vessel was placed in a water bath held at 60°C. The Dreschel bottle was replaced with a vacuum pump and the pressure in the main vessel was reduced to <20 mbar, thus reducing the pressure of the auxiliary vessel and causing steam to be generated. The generated steam was carried into the main vessel through the sparge by the nitrogen.

[0107] After 5.4 hours the steam stripping was stopped by breaking the vacuum with nitrogen and the sparge was replaced with nitrogen headspace. The vessel was cooled to 90°C before the pressure was reduced to <20 mbar for 2.5 hours. A sample (S4) was taken with an acid value of 0.05mg KOH g’1and a hydroxyl value of 3mg KOH g’1was measured. As the acid value was <0.2mg KOH g'1the reaction was deemed complete and the material isolated as Example 15C.

[0108] Table 12 clearly demonstrates the dramatically surprising effect that increasing the proportion of free hydroxyl groups (as measured by hydroxyl value) has on oxidative stability. A modest increase in hydroxyl value from 3 to 11 over triples the oxidative stability. There is greater than a 10 fold difference between the starting material of Example 11 and the most acylated Example of 15C.Table 12.Example 16: Effects of Differing Esterifying AlcoholsPoly 12-hvdroxy stearic acid

[0109] 12 Hydroxy stearic acid (1 100g) was heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. Ih. Once at temperature the pressure was gradually decreased to 200 mbar in 1.5-2 hrs and then further reduced to <50 mbar. After reaching the acid value (70-75mg KOH / g) the reaction was stopped and cooled.Example 1 A: Hexyl poly 12-hydroxy stearate

[0110] Poly-12HSA (860g) as prepared above and Hexanol (160g) were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a Dean Stark separator to 190°C in approx. Ih. After 1 ,5h a vacuum of 750 mbar was applied. Subsequently the vacuum was slowly decreased in 5h to 375 mbar. At an AV of 10.3mg KOH / g 0.43g TBT was added. After another 6.5h in which the pressure was further decreased to 200 mbar the reaction was stopped at an AV of 0.2mg KOH / g.

[0111] The excess of hexanol was distilled off at 120°C. 947g final product was bleached (10g Norit SA4) and steam stripped at 110°C for 3 hours. The product was dried and 5g Supercel filter aid was added. After filtration the product was analyzed (see below).Example 16B: 2-Octyl decyl poly-12-hydroxystearate

[0112] Poly-12HSA (900g) as prepared above and 495g of Isofol 18 were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. 1 h. During heating up a vacuum of 600 mbar was applied. Subsequently the vacuum was slowly decreased in 4h to 125 mbar. At an AV of 11.9mg KOH / g 0.46g TBT was added. After another 7 h in which the pressure was further decreased to 25 mbar the reaction was stopped at an AV of 0.2mg KOH / g.

[0113] The product was distilled using a 2-stage molecular distillation set-up. The excess of Isofol 18 was distilled off (1ststage 155-160°C / 10'3mbar; 2ndstage 185°C / 10'3mbar). 1064g final product was bleached (10g Norit SA4) and steam stripped at 110°C for 4 hours. The product was dried and 5 g Supercel filter aid was added. After filtration the product was analyzed (see below).Example 16C: Isostearyl poly 12-hydroxystearate

[0114] Poly 12HSA (900g) as prepared above and 493 g Isostearyl alcohol (3515) were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. 1 h. During heating up a vacuum of 300 mbar was applied. The vacuum was slowly decreased in 5 h to 100 mbar. At an AV of 9. 1 mg KOH / g 2.4g 20% TBT solution was added. After another 6.25 h in which the pressure was further decreased to 25 mbar the reaction was stopped at an AV of 0. 14 mg KOH / g.

[0115] The product was distilled using a 2-stage molecular distillation set-up. The excess of isostearyl alcohol was distilled off (1ststage 150-160°C / 10’3mbar ; 2ndstage 185°C / 10'3mbar). 935 g final product was bleached (10g Norit SA4) and steam stripped at 110°C for 4 hours. The product was dried and 5 g Supercel filter aid was added. After filtration the product was analyzed (see below).Example 16D Stearyl poly- 12-hydroxystearate

[0116] Poly 12HSA (900g) as prepared above and 495g Stearyl alcohol were heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C in approx. Ih. During heating up a vacuum of 300 mbar was applied. Subsequently the vacuum was slowly decreased in 5 h to 100 mbar. At an AV of 9. Img KOH / g 2.4g 20% TBT solution was added. After another 6.25h in which the pressure was further decreased to 25 mbar the reaction was stopped at an AV of 0. 14mg KOH / g.

[0117] The product was distilled using a 2-stage molecular distillation set-up. The excess of isostearyl alcohol was distilled off (1ststage 150-160°C / 10’3mbar ; 2ndstage 185°C / 10'3mbar). 935g final product was bleached (10g Norit SA4) and steam stripped at 110°C during 4 hours. The product was dried and 5g Supercel filter aid was added. After filtration the product was analyzed (see below).Example 16E: Methyl poly 12-hvdroxystearate

[0118] 12HSA (900g) as prepared above was heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C. Methanol was dosed to reactor (approx. 350 ml / h). At an AV of 25mg KOH / g 0.5 g TBT was added. After 5 h the reaction temperature was increased to 205°C. After a total reaction time of lOh the reaction was stopped at an AV of 0.17mg KOH / g (preliminary product).

[0119] This reaction was repeated with 400 g 12HSA. The product was molecular distilled at 280°C and 3.5xl0'3mbar to create a top and bottom fraction.

[0120] The final product (methyl poly-12-hydroxystearate) was a mixture of 837g of the preliminary product and 148g of the top fraction of the molecular distilled repeat.

[0121] The final product (985g) was bleached (10g Norit SA4) and steam stripped at 1 10°C during 3 hours. The product was dried and 5g Supercel filter aid was added. After filtration the product was analyzed (see below).Example 16F: Isopropyl polv 12-hydroxy stearate

[0122] The first batch was prepared by esterifying poly 12HSA with isopropanol. For the second batch the isopropyl ester was prepared by esterifying 12HSA with isopropanol to a low acid value. Both batches were molecular distilled to separate the low molecular components from the mix. The isopropyl ester was prepared by mixing molecular distilled top and bottom fractions in the ratio described below.

[0123] 12HSA (1000g) as prepared above was heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C. The product was esterified to an AV of 75mg KOH / g. IPA was dosed to the mix. After 7h an AV of 34mg KOH / g was reached and 0.3g TBT was added. After a total reaction time of 21h another 0.3g TBT was added and the temperature was increased to 210°C. In 4h the AV was 0.25mg KOH / g and the reaction was stopped. In total 5 liter of IPA was dosed to the reactor. The recovered product was molecular distilled at 280°C and 3.5xl0’3mbar (approx. 1 OOml / hr) to yield product a top fraction product (16F1).

[0124] 12HSA (1250g) as prepared above was heated in a 2 liter round bottom flask equipped with nitrogen inlet and a take-off adaptor connected to a horizonal water condenser to 190°C. IPA was dosed to reactor (approx. 350 ml / h). After 4h at an AV of 35mg KOH / g 0.5g TBT was added. After 10.5h at an AV of 3.7 another 0.3g of TBT was added. During the following 3h the AV increased to 9.4mg KOH / g. It was decided to switch to a new bottle of IPA. After a total reaction time of 26h the reaction was stopped at an AV of 0.3mg KOH / g. The product was molecular distilled at 280°C and 3.5xl0'3mbar (approx. 1 OOml / hr) to create a top fraction(16F2) and a bottom fraction (16F3).

[0125] The final product was a mixture of 360g top fraction of molecular distilled 16F1, 120g top fraction of molecular distilled 16F2 and 700g bottom fraction of molecular distilled 16F3.

[0126] The combined fractions were bleached (12g Norit SA4) and steam stripped at 1 10°C during 3 hours. The product was dried and 5g Supercel filter aid was added. After filtration the product (16F) was analyzed (see below).Table 13.Example 17: Preparation of 10-hvdroxystearic acid

[0127] A tank was filled with 280 liters of demineralized water. Citric acid (473 g) and Na2HPO4 (1.65 kg) were added to the tank. The pH of the entire mixture was 7.0 ± 0.5. MgSO4.7H2O (689 g) was added to the tank and the mixture was stirred for 15 minutes. The temperature of the resulting mixture was adjusted to 20-25 °C. Oleic acid (7 kg) was added to the solution, followed by the addition the of the hydratase enzyme PDN Cl 00 V2 from Biocatalysts Ltd (140 g) and the resulting mixture was stirred for 24 hours 20-25 °C. The mixture was then heated to 50°C and kept at this temperature for 1 hour. The mixture was then cooled to 30°C and filtered over a 1 pm nylon filter. The solid precipitate was dried and taken from the filter affording 10-hydroxy stearic acid.Example 18: Ester Examples

[0128] The following esters were prepared by standard esterification techniques through the dehydration of an acid and an alcohol or were acquired commercially from Cargill Incorporated.Table 14.Example 19: Antioxidant EffectBlend preparation

[0129] To prepare the blends, the appropriate ester from Table 14 and material from Examples 1 IB or Example 3 were measured first into the beaker in the desired quantities to reach 100g. The mixture was stirred using a mixer set at 400 rpm, at 60°C for 20 minutes. This procedure was carried out for all required blends.

[0130] Oxidative performance of the blends was measure and reported in Table 15 below.Table 15.Rapid Oxy run at 140C as described below.

[0131] From Table 15 a surprising antioxidant affect can be seen. Inclusion of 4% of a either material from Example 3 or 11b or can double or triple the oxidative stability of an ester based lubricant.Example 20: Antioxidant effects on alkylamides.

[0132] The stability of erucamide was compared without antioxidants, in combination with material from Example 11b, and in combination with a commercially available antioxidant (Irganox 1010). Distilled erucamide (obtained from Cargill Incorporated without any added antioxidants) analysis is set out in Table 16 below.Table 16.

[0133] Erucamide(ER) was melted in an oven at 110°C under nitrogen and portions were placed into 100 ml Durans bottle. Each portion was placed onto a hotplate stirrer set to 150°C / 300 rpm before the required amount of Irganox 1010 or material from Example 11B was added and stirred for 15 minutes to prepare the test samples according to Table 17 below.Table 17.

[0134] Amide sample under investigation were melted under nitrogen in an oven set to 1 10°C. Once molten amide is poured into a clean and fresh LICO spectrometry tube (11mm circular cuvette for use in a LICO 690 spectrophotometer. The tube is filled to approximately 2 cm from the top of the tube. The amide is then allowed to cool to room temperature and stoppered once cooled. Cotton wool is used as a stopper for tests carried out in air, ensuring a gap between the top of the amide and the cotton wool.

[0135] The LICO tubes were placed in a preheated oven set to the storage temperature 90°C. Periodically the LICO tube is removed from the oven and the color measured as per manufacturer’s instructions. Additionally, gentle heating may be required during the color measurement to ensure the sample remains molten. Each amide sample was tested in duplicate.

[0136] The results in Table 18 and Figure 2 show the protective effect of the material of Example 11B. Over the course the test period of 215 hours the development in the Hazen color value was reduced by approximately 20%. While the standard chemical antioxidant showedincreased performance, it was surprising that the naturally derived material of Example 11B performed half a well. Use of this material would all reduction in the amount of chemical antioxidant required.Table 18.

[0137] Figure 2 shows the color change or erucamide samples over time in the presence and absence of antioxidants and material from Example 1 IB.Example 21: Antioxidant effects on triglyceride transformer oils

[0138] The stability of a triglyceride based natural transformer fluid was compared without the presence of material from Example 11b. FR3 try glyceride based transformer oil (obtained from Cargill Incorporated without any added antioxidants) was tested for oxidative stability in the presence and absence of antioxidants. Results are set out in Table 19 below.

[0139] Sample for evaluation were prepared according to the procedure in Example 19.Table 19.Analytical MethodsViscosity

[0140] Viscosity of the samples was measured on an Anton Parr Stabinger Viscometer SVM3001 Viscometer in accordance with method ASTM D445. Material was added to the viscometer and the kinematic viscosity measured at 40°C (KV40) and at 100°C (KV100); with the machine also measuring the viscosity index (VI) and density.RapidOxy

[0141] Materials of the present disclosure have exceptional oxidative stability. This stability can make it time consuming to assess stability at lower temperature. The samples were evaluated at three different temperatures to understand more fully their stability. Samples were all evaluated on an Anton Parr RapidOxy 100 instrument in accordance with ASTM D8206. Method conditions are listed in Table 16. A sample size of 4grams was used in a standard glass dish. The temperature utilized was either 140°C, 160°C. or 180°C as indicated. The apparatus was pressurized to 700kPa with pure oxygen and test completion is determined by the time it takes for the peak pressure to drop by 10% or 50%. Accordingly, 10% or 50% reduction was used as an indication of rapid onset of oxidation or Oxidation Induction Time (OIT). OIT should be determined on compounds of Formulas 1 and 3, and on base oils, and lubricant formulations, without addition of any additives or antioxidants. In some aspects, the OIT of the lubricating compositions, base oils, compounds of Formula 1, and Compounds of Formula 3 is greater than 500hr as determined according to ASTM D8206 at 160°C. In some aspects, the OIT of the lubricating compositions, base oils, compounds of Formula, 1 and Compounds of Formula 3 is greater than 750hr as determined according to ASTM D8206 at 160°C. In some aspects, the OIT of the lubricating compositions, base oils, compounds of Formula, 1 and Compounds of Formula 3 is greater than lOOOhr as determined according to ASTM D8206 at 160°C.Table 21.

[0142] Samples from Example 11B we also evaluated for thermal degradation via Thermogravimetric analysis (TGA) under a nitrogen atmosphere to ensure the oxidative stability data was not skewed at a higher temperature do to degradation. Samples were evaluated from 90°C to 900°C under nitrogen on standard equipment. No significant degradation was seen to occur at temperatures under 240°C.

[0143] The term “Acid Value"’ (AV) as used herein is defined as the weight of KOH in mg needed to neutralize the organic acids present in 1g of test sample and it is a measure of the free fatty acids present in the composition. AV can be determined by the AOCS Official Method Cd 3d-63.

[0144] The term “Hydroxyl Value’’ as used herein is defined as the hydroxyl value, expressed in milligrams of potassium hydroxide and corresponds to the number of hydroxyl groups present in 1 g of a sample, is one of the traditional characteristics of oils and fats. Hydroxyl Value may be determined by AOCS Standard Method Cd 13-60.

[0145] The GPC analysis was carried out using Instrument: Agilent 1260 infinity GPC / SEC multi detector suite. Solvent: Tetrahydrofuran, Detector Refractive Index, sample concentration 1% (w / v), Injection Volume 50pl, Temperature: 40°C, Flow rate: Iml / minute, 2 x (PLGel 3pm 100A, 300x7.5mm) and 1 x (PLGel, 3pm, 50x7.5mm) Guard Colum. Results are shown in Figure 1.Aspects of the disclosure

[0146] In some aspects, the compounds of Formula 1 may have an acid value (AV) of less than 0.25, or less than 0.20.

[0147] In some aspects, the compounds of Formula 3 may an acid value (AV) of less than 0.25, or less than 0.20. or between 0.05 and 0.2.

[0148] In some aspects, the compounds of Formula 1 may have a hydroxyl value of more than 10, or more than 20 or more than 35. In some aspects, the compounds of Formula 1 mayhave a hydroxyl value of between 10 and 70 or between 35 and 70. In some aspects, the compounds of Formula 1 may have a hydroxyl value of between 35 and 60.

[0149] In some aspects, the compounds of Formula 3 may have a hydroxyl value of more than 10, or more than 20 or more than 35. In some aspects, the compounds of Formula 3 may have a hydroxyl value of between 10 and 70 or between 35 and 70. In some aspects, the compounds of Formula 3 may have a hydroxyl value of between 35 and 60.

[0150] In some aspects, the compounds of Formula 1 and compounds of Formula 4 may have a hydroxyl value of more than 10, or more than 20 or more than 35. In some aspects, the compounds of Formula 1 and compounds of Formula 4 may have a hydroxyl value of between 10 and 70 or between 35 and 70. In some aspects, the compounds of Formula 1 and compounds of Formula 4 may have a hydroxyl value of between 35 and 60.

[0151] In some aspects, the compounds of Formula 3 and compounds of Formula 4 may have a hydroxyl value of more than 10. or more than 20 or more than 35. In some aspects, the compounds of Formula 3 and compounds of Formula 4 may have a hydroxyl value of between 10 and 70 or betw een 35 and 70. In some aspects, the compounds of Formula 3 and compounds of Formula 4 may have a hydroxyl value of between 35 and 60.

[0152] One aspect is the use of a compound of Formula 1 or Formula 3 as an antioxidant.

[0153] In some aspects, the composition comprises 0.5 - 10% of one or more compounds of the Formula 3 wherein R is 2-ethylhexyl.

[0154] In some aspects, the composition comprises 0.5 - 10% of one or more compounds of the Formula 1 wherein R is C1-C22 alkyl, R2 is a saturated or unsaturated C7 or C9 alkyl; and R3 is a Ce or Cs alkyl.

[0155] In some aspects, the composition comprises 2% to 10% of one or more compounds of the Formula 3 w herein R is 2-ethylhexyl.

[0156] In some aspects, the composition comprises 2% to 10% of one or more compounds of the Formula 3 wherein R is 2-ethylhexyl and the composition further comprises a member selected from the group consisting of polyalphaolefins (PAOs), synthetic esters such as polyol esters, polyalkylene glycols (PAGs), oil soluble polyalkylene glycols (OSPs), mineral oils (Groups I, II, and III), fatty acid esters, natural oils, wax esters, and mixtures thereof.

[0157] In some aspects, the composition comprises 2% to 10% of one or more compounds of the Formula 3 wherein R is 2-ethylhexyl and further comprises a polyalphaolefin (PAO).

[0158] In some aspects, the composition comprises 2% to 10% of one or more compounds of the Formula 3 w herein R is 2-ethylhexyl and further comprises a polyalphaolefin (PAO).

Claims

CLAIMS1. A method of increasing the oxidative stability of a composition comprising adding to the composition one or more compounds of the Formula 1:wherein n is an integer from 2-6; R is C1-C22 alkyl; R2 is C3-C12 alkyl; R3 is hydrogen or C1-C10 alkyl; to the composition.

2. The method of claim 1, wherein the composition comprises 2-10% of the compounds of Formula 1.

3. The method of claim 2, wherein the compounds of Formula 1 have an acid value of less than 0.25 or an acid value between 0.05 and 0.2.

4. The method of claim 1, wherein the compounds of Formula 1 have a hydroxyl value of greater than 35 or a hydroxyl value between 35 and 70.

5. The method of any of claims 1-4, wherein the composition comprises a member selected from the group consisting of polyalphaolefins (PAOs), synthetic esters such as polyol esters, polyalkylene glycols (PAGs). oil soluble polyalkylene glycols (OSPs), mineral oils (Groups I, II, and III), fatty acid esters, long chain esters, natural oils, greases, petrolatum, waxes, wax esters, and mixtures thereof.

6. The method of claim 5, wherein the composition comprises a polyalphaolefin.

7. A method of claim 1, comprising adding to the composition one or more compounds of the Formula 3:wherein n is an integer from 2-6 and R is C1-C22 alkyl.

8. The method of claim 7, wherein R is 2-ethylhexyl.

9. The method of claims 7 and 8, wherein the compounds of Formula 3 have an acid value of less than 0.25 or an acid value between 0.05 and 0.2; and wherein the compounds of Formula 3 have a hydroxyl value of greater than 35 or a hydroxyl value between 35.

10. The method of any of claims 7-9, wherein the composition comprises a member selected from the group consisting of polyalphaolefins (PAOs), synthetic esters such as polyol esters, polyalkylene glycols (PAGs). oil soluble polyalkylene glycols (OSPs), mineral oils (Groups I, IT, and III), fatty acid esters, long chain ester natural oils, greases, petrolatum, waxes, and mixtures thereof.

11. The composition of claim 10, wherein the composition comprises a polyalphaolefin or fatty acid ester or long chain ester.

12. The method of claim 1, wherein the composition is a lubricant.

13. The method of claim 12. wherein the lubricant is a grease, hydraulic fluid, transmission fluid, engine oil, or gear fluid.

14. The use of a compound of Formula 1 or Formula 3 as an antioxidant.

Images