Process for the preparation of substituted hydroxy-hydrocinnamate esters

Abstract: The transesterification of substituted methyl or ethyl hydroxyhydrocinnamates with a higher alcohol or a polyol is greatly facilitated by the use of a trace amount of a tin catalyst. In many cases, the amount of the catalyst is so small that it is unnecessary to remove it from the final product by distillation of said product.

Description: This invention pertains to an improved process for making substituted higher aliphatic esters of hydroxyhydrocinnamates by transesterification of the corresponding methyl or ethyl ester using a very small amount of a tin catalyst. The aliphatic esters and polyesters of substituted sterically hindered hydroxyhydrocinnamic acid are well-known as effective antioxidants for a wide variety of organic materials protecting them from oxidative and thermal degradation. Many of these esters have gained wide commercial acceptance as phenolic antioxidants. Some transesterification catalysts which may be used to prepare the instant compounds include lithium amide, aluminum isopropylate and dibutyltin oxide. United States Patent No. 4,594,444 (Orban) teaches a process for the preparation of sterically hindered hydroxy-phenylcarboxylic acid esters by the transesterification of the corresponding methyl or ethyl ester with a higher aliphatic alcohol using an oxide or an organometallic compound of a metal of the fourth main group or subgroup of the periodic table as catalyst in an amount between 0.05 and 1.0 mol percent based on the methyl or ethyl ester. Higher dialkyltin oxides, particularly dibutyltin oxides, are taught as the preferred catalyst for this process. However, if the amount of tin residue in the product is too high, product properties such as stability, or toxicity are compromised and efforts must be taken to remove such residues. Additionally the residual catalyst may interfere during final application and lead to undesired discoloration or reduced heat or light stability. If the amount of tin catalyst can be reduced well below that seen in the Orban process, such residue removal efforts may be unnecessary and process economies would be evident. That is the case in the instant process where the amount of tin catalyst required is so small that its removal from the final product by distillation of said product is often unnecessary. The instant process differs from this Orban process by running the transesterification process at much lower concentrations of tin catalyst and also at lower temperature. The instant invention pertains to an improved process for the preparation of esters of substituted hydroxyhydrocinnamic acid by the transesterification of the corresponding methyl or ethyl ester with a higher aliphatic alcohol using small amounts of a tin catalyst. More particularly, the instant invention involves an improved process for the preparation of a compound of formula I wherein R 1 is alkyl of 1 to 4 carbon atoms, n is 1 to 3, when n is 1, E is a straight or branched chain alkyl of 4 to 18 carbon atoms; when n is 2, E is a straight or branched chain alkylene of 2 to 12 carbon atoms, or said alkylene interrupted by one to five O or S atoms; and when n is 3, E is a straight or branched chain alkanetriyl of 3 to 6 carbon atoms; by reaction of the corresponding methyl or ethyl ester with an alkanol or polyol of the formula E-(OH) n wherein the transesterification is carried out in the presence of 0.005 to 0.02 mol % of a tin catalyst, based on the starting methyl or ethyl ester, at a temperature of 120-200°C. The corresponding methyl or ethyl ester is a compound of formula I where n is 1 and E is methyl or ethyl; most preferably methyl. Preferably, R 1 is methyl or tert-butyl. The most preferred esters are methyl or ethyl 3,5-di-tert-butyl-4-hydroxyhydrocinnamate. When n is 1, E is preferably alkyl of 8 to 18 carbon atoms; most preferably isooctyl, lauryl or n-octadecyl; especially n-octadecyl. When n is 2, E is preferably hexamethylene, -CH 2 CH 2 SCH 2 CH 2 - or -CH 2 CH 2 OCH 2 CH 2 OCH 2 CH 2 -. When n is 3, E is preferably CH 3 C(CH 2 -) 3 or CH 3 CH 2 C(CH 2 -) 3 . Preferably the compound of formula I is isooctyl 3,5-di-tert-butyl-4-hydroxyhydrocinnamate, or n-octadecyl 3,5-di-tert-butyl-4-hydroxyhydrocinnamate. Preferably, the tin catalyst is a monoalkyltin ester, a dialkyltin ester, a dialkyltin oxide, a trialkyltin oxide, tin tetrachloride, a monoalkyltin trichloride, a dialkyltin dichloride, a trialkyltin chloride or a stannous tin ester. More preferably, the tin catalyst is butyltin tris(2-ethylhexanoate); dibutyltin bis(2-ethylhexanoate); dibutyltin diacetate; dibutyltin oxide, trioctyltin oxide, butyltin trichloride, butyltin trimethylate, dibutyltin dichloride, diphenyltin dichloride, tributyltin chloride or stannous bis(2-ethylhexanoate); especially butyltin tris-(2-ethylhexanoate), dibutyltin diacetate, butyltin trichloride, butyltin trimethylate or dibutyltin oxide. Most preferably the tin catalyst is butyltin tris-(2-ethylhexanoate); dibutyltin diacetate or dibutyltin oxide. It is noted that compounds other than those specifically listed above may also be effective catalysts for the instant transesterification reaction. The instant transesterification process is an improved process over that of Orban since it can be catalyzed by the use of a tin catalyst, especially butyltin tris-2-ethylhexanoate at levels between 0.005 - 0.02 mol % Sn catalyst based on the starting methyl or ethyl ester. The reaction goes to at least 98% completion with these tiny amounts of catalyst. The low catalyst level and high conversion rate eliminate the necessity for post-reaction separation of either catalyst or unreacted starting materials from the final ester product. Elimination of any post-reaction work-up significantly reduces production costs by reducing cycle time and elimination costs associated with waste disposal. Clear economies attend the instant process. Preferably, the amount of tin catalyst is 0.005-0.02 mol %, most prefarably 0.008-0.016 mol % based on the starting methyl or ethyl ester. Preferably, the temperature is 150-190°C, most preferably 160-190°C. The instant process is conveniently run at a pressure of between 250 and 1 mbar, preferably between 50 and 3 mbar. Although the instant process is preferably run without the presence of an inert solvent or stripping agent, the process works equally well when such an inert solvent or an inert gas stripping agent such as nitrogen is used. As mentioned above, relatively high levels of transesterification catalysts are used in the industry necessitating removal of catalyst residues from the final product. Failure to remove such catalyst residues may have deleterious effects on both the stability of the instant product itself and on its performance in end-use applications as a phenolic antioxidant. Prior art transesterification catalysts such as lithium amide, lithium methoxide and aluminum isopropylate must be used at levels ranging from 200-500 ppm of lithium or aluminun, based on the starting methyl or ethyl ester, in order to achieve acceptable conversions to final product (at least 97%). By contrast the instant invention uses dibutyltin oxide or butyltin tris-2-ethylhexanoate at a level of 0.005 - 0.02 mol % based on the starting methyl or ethyl ester. Typical values are below 50 ppm Sn. In many cases values of only 4 to 30 ppm can be achieved. Tin at these levels are shown to have no negative effects on either product stability or on final product performance in end-use applications. The instant improved process clearly eliminates any need for a post-reaction catalyst residue removal, typically acid neutralization of the basic catalysts (i.e. lithium amide or lithium methoxide) followed by repeated water washes or the use of an aqueous alkaline solution to precipitate the tin catalysts as their hydroxides. Alternatively, the separation of the hydroxyhydrocinnamate esters from the catalyst residue can be performed by an expensive operation such as distillation or crystallization of the ester. The instant process is a significant improvement over the processes of the prior art. The following experiments illustrate the instant invention. Example 1 Isooctyl 3,5-Di-tert-butyl-4-hydroxyhydrocinnamate In a three-necked, round-bottomed flask fitted with a stirrer, thermometer, reflux condenser with a trap to collect distilled off methanol and later isooctanol and a vacuum connection are added 200 g (0.684 mole) of methyl 3,5-di-tert-butyl-4-hydroxyhydrocinnamate, 178 g (1.37 moles, 100% excess) of isooctanol (Exxal®-8, Exxon) and 0.05 g (0.0000826 mole; 50 ppm of tin in final product) of butyltin tris-(2-ethylhexanoate) (Fascat® 9201, Elf-Atochem). The reaction mixture is subjected to a reduced pressure of 533 mbar (400 mm Hg) and the flask is heated to 140-150°C. Methanol begins to be evolved and is collected in the trap receiver. When the reaction mixture reaches 160°C, reflux of isooctanol is observed and becomes vigorous at 170-180°C while the evolution of methanol subsides. At this point, the excess isooctanol is then stripped into the trap receiver and the pressure in the system is ultimately reduced to 6.6 mbar (5 mm Hg). When all the excess isooctanol is removed, the residue in the flask is cooled under nitrogen and is the desired title compound in essentially quantitative yield (over 99% by weight). The product is "water-white" and contains less than 1 % by weight of starting methyl ester and less than 0.1 % by weight of isooctanol. Example 2 Isooctyl 3,5-Di-tert-butyl-4-hydroxyhydrocinnamate Following the general procedure of Example 1, using a 100% excess of isooctanol, a reaction time of 65 minutes and sufficient catalyst to leave 77 ppm of tin in the final product, a conversion of 99.8 % to the title compound is obtained with only 0.2 % of the starting methyl ester as an impurity (by GC area %). No isooctanol is seen in the final product. Example 3 Isooctyl 3,5-Di-tert-butyl-4-hydroxyhydrocinnamate Following the general procedure of Example 1, using a 60% excess of isooctanol, a reaction time of 65 minutes and sufficient catalyst to leave 61 ppm of tin in the final product, a conversion of 99.6 % to the title compound is obtained with only 0.4 % of the starting methyl ester as an impurity (by GC area%). No isooctanol is seen in the final product. Example 4 Isooctyl 3,5-Di-tert-butyl-4-hydroxyhydrocinnamate Following the general procedure of Example 1, using a 60% excess of isooctanol, a reaction time of 60 minutes and sufficient catalyst to leave 42 ppm of tin in the final product, a conversion of 98.2 % to the title compound is obtained with only 1.7% of the starting methyl ester as an impurity (by GC area %). No isooctanol is seen in the final product. Example 5 Isooctyl 3,5-Di-tert-butyl-4-hydroxyhydrocinnamate Following the general procedure of Example 1, using a 100% excess of isooctanol, a reaction time of 90 minutes and sufficient catalyst to leave 20 ppm of tin in the final product, a conversion of 97.9 % to the title compound is obtained with only 2.0 % of the starting methyl ester as an impurity (by GC area %). 0.1% of isooctanol is seen in the final product (by GC area %). Examples 1-5 show that even when the concentration of catalyst is reduced to a level leaving only 20 ppm of tin in the final product, the conversion to final product goes expeditiously to levels of at least 97% and at lower temperatures than needed in the Orban process. Examples 6-8 Using the general procedure of Example 1 with either the methyl or ethyl ester of a substituted hydroxyhydrocinnamic acid and various alkanols, the following higher esters of formula I are obtained in high yield and purity. Example R 1 E 6 tert-butyl lauryl 7 tert-butyl n-octadecyl 8 tert-butyl n-octyl Example 9 Isooctyl 3,5-Di-tert-butyl-4-hydroxyhydrocinnamate When following the general procedure of Example 1, and substituting a like mol % amount of dibutyltin oxide for the butyltin tris-(2-ethylhexanoate) as catalyst, the title compound is obtained without the need for further purification of said product by distillation. Example 10 n-Octadecyl 3,5-Di-tert-butyl-4-hydroxyhydrocinnamate In a reactor fitted with a heating/cooling bath, stirrer, thermocouple, nitrogen inlet, a reflux condenser with a trap to collect distilled off methanol, and a vacuum connection are added 438.6 g (1.5 moles, a 5% excess) of methyl 3,5-di-tert-butyl-4-hydroxyhydrocinnamate and 386.8 g (1.43 moles) of 1-octadecanol. The mixture is heated to 100°C under nitrogen with stirring. After drying at 100°C under vacuum (≤ 6.6 mbar (≤ 5 mm Hg) for 30 minutes, the mixture is heated to 120°C under nitrogen and 0.05 g (0.0002 mole) of dibutyltin oxide (Fascat® 4201, Elf-Atochem) is added. The vacuum is lowered to 133 mbar (100 mm Hg) and the reaction mixture is heated to 185°C for one hour. The vacuum is slowly lowered to 2.6 mbar (2 mm Hg) over 1.5 hours and kept at that temperature and pressure for another thirty minutes. The vacuum is broken with nitrogen and the reaction mass is cooled to 100°C. The excess methyl 3,5-di-tert-butyl-4-hydroxyhydrocinnamate is removed using a wiped-film evaporator to give the title compound as a white solid containing 30 ppm Sn. Essentially a quantitative yield (99.8) of the ester product is obtained. This 30 ppm of Sn residue is acceptable in all application tests for this ester antioxidant. To remove the tin catalyst from the hydroxyhydrocinnamate ester melt, commonly an aqueous alkaline solution is used to form an insoluble tin hydroxide. However, it is known that an alkaline medium is deleterious to such ester products resulting in yellow color formation and degradation of the ester product. For each of the reasons given above, such methods for the separation of tin catalyst residues are to be avoided whenever the level of tin catalyst residue is not detrimental to the performance of the ester antioxidant in end-use applications. The instant process affords such a method to avoid the need for later tin catalyst removal in most situations. Example 11 -15 Using the general procedure of Example 10 with either the methyl or ethyl ester of a substituted hydroxyhydrocinnamic acid and various polyols, the following higher esters of formula I are obtained in high yield and purity. Example n R 1 E 11 2 tert-butyl hexamethylene 12 2 methyl -CH 2 CH 2 SCH 2 CH 2 - 13 2 tert-butyl -CH 2 CH 2 (OCH 2 CH 2 ) 2 - 14 3 tert-butyl -CH 3 C(CH 2 -) 3 15 3 tert-butyl -CH 3 CH 2 C(CH 2 -) 3

Claims: A process for the preparation of a compound of formula I wherein R 1 is alkyl of 1 to 4 carbon atoms, n is 1 to 3, when n is 1, E is a straight or branched chain alkyl of 4 to 18 carbon atoms; when n is 2, E is a straight or branched chain alkylene of 2 to 12 carbon atoms, or said alkylene interrupted by one to five O or S atoms; and when n is 3, E is a straight or branched chain alkanetriyl of 3 to 6 carbon atoms; by reaction of the corresponding methyl or ethyl ester with an alkanol or polyol of the formula E-(OH) n wherein the transesterification is carried out in the presence of 0.005 to 0.02 mol % of a tin catalyst, based on the starting methyl or ethyl ester, at a temperature of 120-200°C. A process according to claim 1 where the methyl or ethyl ester is methyl or ethyl 3,5-di-tert-butyl-4-hydroxyhydrocinnamate. A process according to claim 1 where in the compound of formula I, R 1 is methyl or tert-butyl. A process according to claim 1 where in the compound of formula I, n is 1, and E is alkyl of 8 to 18 carbon atoms. A process according to claim 4 wherein E is isooctyl, lauryl or n-octadecyl. A process according to claim 1 where in the compound of formula I, n is 2 and E is hexamethylene, -CH 2 CH 2 SCH 2 CH 2 - or -CH 2 CH 2 OCH 2 CH 2 OCH 2 CH 2 -. A process according to claim 1 where in the compound of formula I, n is 3 and E is CH 3 C(CH 2 -) 3 or CH 3 CH 2 C(CH 2 -) 3 . A process according to claim 1 wherein the tin catalyst is a monoalkyltin ester, a dialkyltin ester, a dialkyltin oxide, a trialkyltin oxide or a stannous tin ester. A process according to claim 8 wherein the tin catalyst is butyltin tris(2-ethylhexanoate); dibutyltin bis(2-ethylhexanoate); dibutyltin diacetate; dibutyltin oxide; trioctyltin oxide or stannous bis(2-ethylhexanoate). A process according to claim 1 wherein the temperature is 150-190°C. A process according to claim 1 wherein the tin catalyst is not removed from the final product after the transesterification reaction is complete.

Inventors: DUBUIS BENOIT, KUENG PETER, ROSS JOHN RICHARD, SCHULTZ MICHAEL EUGENE, DUBUIS, BENOIT, KUENG, PETER, ROSS, JOHN RICHARD, SCHULTZ, MICHAEL EUGENE, Dubuis, Benoít, Küng, Peter
Applicants: CIBA SC HOLDING AG, CIBA SPECIALTY CHEMICALS HOLDING INC.
Application year: 1997
Main classification: C07C67
IPC codes: C07C323, C07C319, C07C69, B01J31, C07B61, C07C67