PROCESS FOR THE PREPARATION OF DERIVATIVES OF FATTY ACIDS

Abstract: The invention relates to a process for the preparation of a mixture of branched and oligomeric fatty acids, by contacting a composition comprising unsaturated straight chain fatty acids with an ionic liquid.

Description: PROCESS FOR THE PREPARATION OF DERIVATIVES OF FATTY ACIDS. The present invention relates to a process for the preparation of a mixture of branched and oligomeric fatty acids, by contacting a composition comprising unsaturated straight chain fatty acids with an ionic liquid. Fatty acids are versatile building blocks in various parts of the chemical industry, ranging from lubricants, polymers, solvents to cosmetics and much more. Fatty acids are generally obtained by hydrolysis of triglycerides of vegetable or animal origin. Naturally occurring triglycerides are esters of glycerol and generally straight chain, even numbered carboxylic acids, in size ranging from 10-24 carbon atoms. Most common are fatty acids having 12, 14, 16 or 18 carbon atoms. The fatty acids can either be saturated or contain one or more unsaturated bonds . Long, straight chain saturated fatty acids (C10:0 and higher) are solid at room temperature, which makes them difficult to process in a number of applications. The unsaturated long chain fatty acids like e.g. oleic acid are liquid at room temperature, so easy to process, but are unstable because of the existence of a double bond. Derivatives of fatty acids that are branched (i.e. branched fatty acids) mimic the properties of the straight chain in many respects, however, they do not have the disadvantages associated with them. For example branched C18.0 (commercially known as isostearic acid) is liquid at room temperature, but is not as unstable as unsaturated C18:l, since the unsaturated bonds are prone to oxidation. Therefore, branched fatty acids are for many applications more desirable than straight chain fatty acids. Apart from branched fatty acids other fatty acid derivatives, such as oligomerised fatty acids, find use in similar and other applications. Oligomeric fatty acids refer to materials prepared by coupling of the monomer units, of which typically dimeric and trimeric species are desired building blocks in plastics, the personal care industry, lubricants, etcetera. Mixtures comprising oligomerised fatty acids and branched fatty acids can be likewise useful. Currently, branched and oligomeric fatty acids are obtained by isomerisation / oligomerisation of the straight chain, unsaturated fatty acids. The reaction is conventionally carried out using a clay catalyst, and is generally performed at high temperature (e.g. 250°C) . A common process is the preparation of branched C18:0 and dimerised C18 (i.e. C36 dicarboxylic acids) from unsaturated straight chain C18:l (or also C18:2). A disadvantage in this conventional process is that substantial amounts of aromatic dimers are formed. Such compounds are undesirable for a number of reasons, of which the most notable are: they do not contribute to the properties desired, and they can present a health hazard. The latter precludes the use of conventional dimer acids for certain highly desirable applications in the personal product and cosmetics industries . In addition, the prior art processes suffer from the disadvantage that although a reasonable amount of polymerised product is obtained, the ratio of dimerised to trimerised and higher fatty acids is fixed and cannot easily be tuned to market demand. Hence, there is a need for a process for the preparation of a mixture comprising branched and oligomeric fatty acids, in which mixture the concentration of aromatic dimers is low, or preferably substantially zero. It has now been found that the above objectives can be met by a process for the preparation of a mixture comprising branched fatty acids and dimerised fatty acids, wherein a source comprising unsaturated fatty acids or derivatives thereof, is contacted with an ionic liquid. An ionic liquid is herein to be understood as a salt (or a mixture of salts) in its liquid form (i.e. molten). Preferably, to lead to the desired products, in the process according to the invention, the source comprises at least 50% by weight of fatty acids or derivatives thereof, having at least one unsaturated carbon- carbon bond in the fatty acid chain. It is also preferred that at least 50% by weight of said fatty acids or derivatives of fatty acids have a fatty acid chain length of between 8 and 24 carbon atoms. A preferred fatty acid in this respect is oleic acid or derivatives thereof. Regarding the derivatives in the source as mentioned, esters are preferred, with alkylesters being the most preferred. Of these alkylesters, the most preferred ones are the fatty acid esters of alcohols having 1-4 carbon atoms, e.g. methanol, ethanol, propanol . Hence, a preferred source for performing the reaction according to the invention comprises oleic acid, methyl oleate, and/or ethyl oleate. With respect to the type of ionic liquid, a wide variety of possibilities exists. However, it will be clear that the preferred ionic liquids are the ones that are liquid at relatively low temperatures. Although some salts have very high melting points (i.e. common NaCl has a melting point of approx. 850°C) , there are salts known which melt under less severe conditions. An example of such salts are mixtures of two or more salts. In the case in which a mixture of two salts is used, the resulting ionic liquid is called a binary ionic liquid. Hence, it is preferred that in the process as set out above the ionic liquid comprises a binary ionic liquid. Preferred binary ionic liquids comprise a metal (III) chloride and/or an organic halide salt, e.g. [A] + X " . Also, inorganic halide salts can be used. Suitable metal (III) chlorides include aluminium (III) chloride and iron (III) chloride. Regarding the organic halide, an unsymmetrical imidazolium or pyridinium halide has the advantage that isomerisation / oligomerisation may now occur under mild conditions, contrary to conventional processes. A preferred unsymmetrical imidazolium halide is 1-methyl -3 -ethyl imidazolium chloride. A distinct advantage of the presently invented process over the known processes is that there is no need to carry out a reaction for branching and/or oligomerisation of fatty acids at elevated temperatures: as long as the temperature is high enough for the salt which is used as the reaction "solvent" (or medium) to be in its liquid form (i.e. molten) . An additional advantage is that substantially no aromatic and/or cyclic dimers are formed in the process according to the invention. Therefore, it is preferred that the process according to the invention is carried out at temperatures below 250°C. More preferred are operating temperatures of below 150°C, or even below 50°C, as long as the ionic liquid is chosen such that the mixture of ionic liquid and reactants is a liquid. Some reaction systems are even active at temperatures below 0°C. At such temperatures, the amount at cracked products obtained can be low, and following this, such a temperature can be preferred for some cases. As an additional advantage, there is no need for performing the reaction under increased pressure, and therefore, it is preferred for the reaction according to the invention to be carried out at atmospheric pressure. Yet a further advantage of the present process is that long reaction times are not needed. Generally, the reaction can be shorter than 60 minutes, in many cases even shorter than 15 minutes. In the process according to the invention, the ratio of ionic liquid : fatty acid reactant is preferably larger than 1:1, preferably at least 3:1, and most preferably at least 6:1. In a practical set up, the process will be preferably be operated in a (semi- ) continuous way, and the products are separated from the reactants and ionic liquid. The expensive unsymmetrical imadazolium or pyridinium halide can be easily separated from the product by extraction with solvents such as dichloromethane and hexane etc, together with mixtures thereof. The imidazolium or pyridinium species can then be recycled following evaporation or distillation of the solvent. The invention is further illustrated by the following examples, which are not to be interpreted as limiting the invention thereto. Example 1: Branching/oligomerisation of methyl oleate. In a dry box, 1-methyl-3 -ethylimidazolium chloride (3.55g, 24.20 mmol) was added to triply sublimed aluminiu (III) chloride (6.45g, 48.40 mmol), in a 100cm 3 round bottomed flask, equipped with a dinitrogen inlet, Teflon stirrer bar and a stopper. The two solids were left to stand for 1 h without stirring, at which point the melt had partially formed. The melt was transferred to a fume cupboard and connected to a supply of dinitrogen, and cooled to a reaction temperature of 0°C. Methyl oleate (3.56g, 12.10 mmol, molar ratio of ionic liquid to methyl oleate 6:1) was added dropwise by pipette over a 10 minute period, and the whole system kept under a constant stream of dinitrogen to prevent air / moisture entering the reaction. The reaction was allowed to proceed for lhr, at which point the reaction mixture was quenched by the addition of water and crushed ice (50cm 3 ) . The resultant organic phase was then extracted with 3 x 30 cm 3 aliquots of dichloromethane . The combined organic extracts were dried using MgS0 4 , filtered, and the solvent evaporated using a rotary evaporator. The various products were separated by flash chromatography on lOOg of silica, using a gradient elution (500ml of 2%, followed by 5%, followed by 10% ethyl ethanoate in 40-60° petroleum ether.) Following separation the products were identified by a combination of 1 H & 13 C NMR, GCMS and infra-red. Selectivities for the various products obtained under these conditions are presented in Table 1. This table also outlines the results of other experiments performed in the same manner as outlined in this example but using various ionic liquid : methyl oleate ratios, reaction times and reaction temperatures. Selectivity to branched / oligomeric fatty esters can be tailored to demand by controlling either the reaction rate or the ratio of ionic liquid : fatty acid reactant. Short reaction times and low temperatures favouring the production of branched monomer and dimer moieties, long reaction times / high temperatures favouring the production of trimer and higher polymeric species . Similarly high dilution of the unsaturated fatty ester feedstocks in the ionic liquid catalyst / solvent system favour the production of branched and dimer moieties. Analysis of the dimer fractions obtained from all these experiments, by NMR, revealed the complete absence of cyclic or aromatic structures. Table 1: Effective of ionic liquid : reactant mole ratio, reaction temperature and reaction on time on product selectivity. Mol Temp Reac. %BM %LM %DIM %TRIM %Poly % rat. /°C time Crac mins 3:1 -40 10 26 1 38 19 <10 0 3:1 0 10 20 1 19 30 <20 5 1.1: -40 10 17 1 18 43 20 0 1 1.1: 25 10 25 2 14 32 20 0 1 (BM = Branched monomer, LM = Linear monomer, DIM = Dimer, TRIM = trimer, Poly = Polymer, Crac = Cracked products) * Note the oligomeric fractions in this experiment were not separated. The cracked products observed are sweet smelling volatile low molecular fatty acid esters. Example 2 : Effect of reaction temperature Example 1 has been repeated using the same conditions, except that the ionic liquid : fatty acid reactant ratio is now 6:1, and the reaction has been performed at various temperatures (see table 2) . All other conditions remained the same. Table 2: Effect of temperature at a ionic liquid fatty acid reactant ratio = 6:1 Temperatur % Monomer % Dimer % Trimer & % Cracked e / °C higher products polymers -40 13.5 .5 80.9 1.1 -10 17.4 3.2 54.6 24.7 0 18.3 6 49.3 26.4 8 21.1 5.3 50.3 23.3 25 20.5 15.7 43.8 19.9 50 16.1 9.6 34.6 39.7 60 14 11.4 33.5 41.1 120 11.9 5.8 32.3 50.0 Example 3: Effect of water addition In a dry box, l-methyl-3-ethylimidazolium chloride (3.55g, 24.20mmol) was added to a triply sublimed aluminiu (III) chloride (6.45g, 48.40 mmol) in a 100cm 3 round bottomed flask, equipped with a dinitrogen inlet, Teflon stirrer bar and a stopper. The two solids were left to stand for lh without stirring (to avoid excessive reaction rate and heat build up) until the melt had partially formed. The melt was then stirred for 4h at which point the aluminium(III) chloride had reacted. The melt was then transferred to a fume cupboard to and connected to a supply of dinitrogen. A mixture of methyl oleate (3,50g, 12.0mmol, 50mol%) and water (O.lOg, 0.1ml) was added dropwise and stirred at room temperatrue for 1.5h. Water and crushed ice (50cm 3 ) was added and the product was extracted with dichloromethane (3 x 30cm 3 ) . The combined organic extracts were dried (MgS0 4 ) , fltered and the solvent evaporated on a rotary evaporator. This gave 3. lOg of a straw coloured oil . The various products were separated by flash chromatography on lOOg of silica, using a gradient elution (500ml of 2%, followed by 5%, followed by 10% ethyl ethanoate in 40-60° petroleum ether.) Following separation the products were identfied by a combination of 1 H & 13 C NMR, GCMS and infrared. Selectivities for the various products obtained under these conditions are listed below: Cracked products : 21% Monomer + dimer: 38% Trimer + polymer: 42% * : the cracked products comprise mainly branched fatty acids having between 7 and 18 carbon atoms. NMR analysis of the dimer fractions reveals the absence of cyclic or aromatic structures. Example 4: Alternative extraction to preserve l-methyl-3- ethylimadazolium chloride In a dry box, 1 -methyl -3 -ethylimadazolium chloride (3.55g, 24.20 mmol) was added to doubly sublimed aluminium (III) chloride (6.45g, 48.40 mmol) in a 100cm 3 round bottomed flask, equipped with a dinitrogen inlet, Teflon stirrer bar and a stopper. The two solids were left to stand for 0.5 hour without stirring (to avoid excessive reaction rate and heat build up) until the melt had partially formed. The melt was then stirred for 3 hours until all the aluminium(III) chloride had reacted. The melt was transferred to a fume cupboard and connected to a supply of dinitrogen. The reaction vessel was cooled to 0°C with an ice bath and methyl oleate (3.0g, 10.0 mmol, 30w/w%) was added dropwise over a fifteen minute period. After a further 5mins, dichloromethane (25cm 3 ) was added and the product extracted with hexane (3 x 33cm 3 aliquots) . The solvent was evaporated from the combined organic extracts to give 3.3lg of the aluminium adduct of the products. A further 0.84g of adduct was obtained by washing the melt with 3 x 33 cm 3 aliquots of 50:50 dichloromethane / hexane, followed by evaporation of the solvent. The adducts were destroyed by addition of water (50ml) , extracted with dichloromethane (2 x 20ml) , dried (MgS0 4 ) , filtered and the solvent evaporated on a rotary evaporator. This gave a total of 2.37g of colourless oil (79% of starting product - Remainder is accounted for by volatile products produced as a consequence of cracking reactions) . The extracts were separated by Kugelrohr distillation at 2mmHg pressure. Cracked products * : 21% Monomer: 14% Dimer: 8% Trimer + Polymer: 57% * : the cracked products comprise mainly branched fatty acids having between 7 and 18 carbon atoms. Analysis of the dimer fraction by NMR indicates the absence of cyclic or aromatic dimer structures. Example 5: Effect of iron based ionic liquid on fatty acid oligomerisation Preparation of 58% Iron (III) Chloride In a dry-box, triply sublimed FeCl 3 (8.96g, 55.2 x 10 "3 mol) was added to 1- ethyl -3 -methyl imidazolium chloride (5.86g, 40 x 10 "3 mol). The two solids were left stirring overnight . Oligomerisation of methyl oleate in 58% FeCl 3 - [emim]Cl In a dry box, 58% FeCl 3 - [emim] Cl (14.82, 40 x 10 "3 mol) was transferred to a 3 -necked 200 ml round-bottomed flask equipped with a dinitrogen inlet, Teflon stirrer bar and stoppers. The melt was transferred to a fume cupboard and connected to a supply of dinitrogen. Methyl oleate (3.0g, 3.4cm 3 , 10 x 10 "3 mol) was added dropwise over a 10 minute period . The reaction mixture was left stirring overnight. A sample was then removed from the reaction mixture and quenched with distilled water. The product was extracted with dichloromethane, dried (MgS0 4 ) and the solvent removed on a rotary evaporator. The sample was analysed by proton NMR which indicated that the reaction was complete. The NMR also showed that some chlorination had occured. Distilled water was added to the bulk mixture to quench the combined organic extracts were dried (MgS0 4 ) , filtered and the solvent removed on a rotary evaporator. A sample of the crude product (0.7lg) was separated by fractional distillation under vacuum (2.0mmHg) on a Kugelrohr apparatus. This produced the following yields: Monomer 0.23g (32.4%) Dimer 0.06g (8.5%) Trimer + polymer 0.28g (39.4%) Cracked products 0.14g (19.7%) Crude Product X H NMR (500 MHz / CDC1 3 / TMS) (δ / ppm) 0.85 - 0.89 (d + t, 4H) , 1.28 - 1.29 (m, 28H) , 1.61 (m, 2H) , 2.28 - 2.33 (t, 2H) , 3.66 - 3.67 (ε, 3H) , 3..87 - 3.89 (m, 0.3H). 13 C NMR (75MHz / CDC1 3 / TMS) (δ / ppm) 14.548, 23.103, 25.397, 25.580, 26.920, 29.584, 29.674, 29.736, 30.057, 32.002, 32.334, 34.582, 38.959, 52.064, 64.787, 174.763 Note that GCMS showed that there was a high proportion (estimated to be 50%) of the monomer which had been chlorinated . A breakdown of the products detected by GCMS results is given below: Retention time / s M + Product 544 - 552 242 C 14 Methyl ester 580 - 591 256 C 15 Methyl ester 612 - 631 270 C 16 Methyl ester 654 - 657 284 C 17 Methyl ester 688 - 734 298 C 18 Methyl ester 766 - 881 332 Chlorinated C ιe Methyl ester

Claims: CLAIMS 1. Process for the preparation of a mixture comprising branched fatty acids and oligomerised fatty acids, wherein a source comprising unsaturated fatty acids or derivatives thereof, is contacted with an ionic liquid. 2. Process according to claim 1, characterized in that the source comprises at least 50% by weight of fatty acids or derivatives thereof, having at least one unsaturated carbon- carbon bond in the fatty acid chain. 3. Process according to claim 2, characterized in that the fatty acid feedstock or derivative thereof, comprises of at least 80% by weight of unsaturated fatty acid or derivatives thereof. 4. Process according to claim 1-3, characterized in that at least 50% by weight of fatty acids or derivatives thereof have a fatty acid chain length of between 10 and 24 carbon atoms. 5. Process according to claim 4, characterized in that the fatty acid feedstock or derivative thereof comprises at least 40% by weight of oleic acid or derivative thereof . 6. Process according to claim 5, characterized in that the fatty acid feedstock or derivative thereof comprises of at least 70% by weight of oleic acid. 7. Process according to any of claims 1-6, characterized in that the fatty acid derivative is an alkyl ester of a fatty acid. 8. Process according to claim 7, characterized in that the fatty acid derivative is an ester of fatty acid and an alcohol having 1-4 carbon atoms. 9. Process according to any of claims 1-8, characterized in that the ionic liquid comprises a binary ionic liquid. 10. Process according to any of claims 1-9, characterized in that the ionic liquid comprises a metal (III) chloride and/or an organic halide. 11. Process according to claim 10, characterized in that the metal (III) chloride is aluminium(III) or iron (III) chloride. 12. Process according to claim 10, characterised in that the organic halide is an unsymmetrical imidazolium halide or a pyridinium halide. 13. Process according to claim 12, characterized in that the unsymmetrical imidazolium halide is l-methyl-3- ethylimidazolium chloride. 14. Process according to any of claims 1-13, characterized in that it is carried out at temperatures below 150°C, or preferably at temperatures below 50°C. 15. Process according to any of claims 1-14, characterized in that the reaction is performed under atmospheric pressure. 16. Process according to any of claims 1-15, characterized in that the ionic liquid : fatty acid reactant ratio is larger than 1:1, preferably at least 3:1. 17. Process according to any of claims 1-16, characterized in that substantially no aromatic dimers are produced during the reaction. 18. Process according to claims 1-17 in which the products are separated from the reactants and ionic liquid. 19. Process according to claim 18 in which the imadazolium or pyridinium halide is separated from the product / A1C1 3 adduct by extraction with a polar solvent. 20. Process according to claim 18 in which the product is liberated from the product / A1C1 3 adduct by hydrolysis in water.

Inventors: ADAMS CHRISTOPHER JOHN, EARLE MARTYN E, HAMILL JENNIFER, LOK CORNELIS MARTINUS, ROBERTS GLYN, SEDDON KENNETH R, ADAMS, CHRISTOPHER, JOHN, EARLE, MARTYN, E., HAMILL, JENNIFER, LOK, CORNELIS, MARTINUS, ROBERTS, GLYN, SEDDON, KENNETH, R.
Applicants: ADAMS CHRISTOPHER JOHN, EARLE MARTYN E, HAMILL JENNIFER, LOK CORNELIS MARTINUS, ROBERTS GLYN, SEDDON KENNETH R, UNICHEMA CHEMIE BV, ADAMS, CHRISTOPHER, JOHN, EARLE, MARTYN, E., HAMILL, JENNIFER, LOK, CORNELIS, MARTINUS, ROBERTS, GLYN, SEDDON, KENNETH, R., UNICHEMA CHEMIE B.V.
Application year: 1997
Main classification: C07C53
IPC codes: C07B37, C07C51, C07C53, C07C67