Process for producing and purifying 3,4-dihydrocoumarin

Abstract: A 3-(2-cyclohexanoyl)propionic acid ester is in the presence of a solid metallic catalyst, cyclized and dehydrogenised at 100° to 350°C, optionally with solvent and promotor to given 3,4-dihydrocoumarin [D] in 30-70 mol% yield and coumarin [C] 5-35 mol% and by-product dihydrocinnamic acid [A], 0.1-20 wt%; hydrogenation can convert [C] to [D]. The reaction mixture is purified by (i) to remove acidic compounds washing with an aqueous solution of an alkali (e.g., NaOH or NAHCO₃); if a strong alkali metal or alkaline earth hydroxide is used its amount is not more than 1.5 equivalent per equivalent of [D]; the amount of solution is 0.1 to 10 times by weight that of the reaction mixture. The washing reduces the content of [A] to 1% by weight of the weight of [D], and/or (ii) to remove high boiling o -ethylphenyl cyclohexylpropionate/dihydrocinnamate to 2% by weight of that of [D] distillation at a reflux ratio of not more than 5 or in a tower having 10 stages or less, at 13-13330 Pa (0.1 to 10 Torr); (i) and (ii) can be used together in either order, followed by rectification in a 5-100 stage tower at a reflux ratio of 1 to 50, to recover [D]. The product contains not more than 0.05% of [A] and is suitable for use in perfume.

Description: The present invention relates to a process for producing 3,4-dihydrocoumarin from 3-(2-cyclohexanoyl)propionic acid esters. 3,4-Dihydrocoumarin is an important compound in the perfume industry and is also useful as an intermediate for dyes, agricultural chemicals or pharmaceuticals. 3,4-Dihydrocoumarin is obtained by cyclization and dehydrogenation of a 3-(2-cyclohexanoyl)propionic acid ester in the presence of a solid metallic catalyst. Coumarin which is by-produced in the reaction is separated from the reaction mixture, for example by distillation or crystallization, for use as a product. The by-product coumarin may also be converted to 3,4-dihydrocoumarin by partial hydrogenation. Other by-products resulting from the above reaction mainly include compounds having a lower boiling point than 3,4-dihydrocoumarin, e.g., ethylbenzene, o -ethylphenol and a dihydrocinnamic acid ester; compounds having a higher boiling point than 3,4-dihydrocoumarin, such as esters (e.g., o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate), octahydrocoumarin and dihydrocinnamic acid; and tar-like substances. In order to remove these by-products, the reaction mixture per se has conventionally been subjected to rectification to recover 3,4-dihydrocoumarin. However, when a conventional purification process is carried out, o -ethylphenol and dihydrocinnamic acid become incorporated into the 3,4-dihydrocoumarin fraction during rectification, which reduces the purity of the resulting 3,4-dihydrocoumarin. O -ethylphenol has a low boiling point and gives off a phenol-like smell; similarly, dihydrocinnamic acid has a cinnamon-like smell. Each of these compounds thus impair the odor of 3,4-dihydrocoumarin for use as a perfume. It is therefore desirable to reduce the content of both o -ethylphenol and dihydrocinnamic acid in 3,4-dihydrocoumarin to about 0.05% by weight or less. In order to recover high purity 3,4-dihydrocoumarin free from impurities, complicated steps such as repetition of rectification have been required, and these also lead to a loss of 3,4-dihydrocoumarin. An object of the present invention is thus to provide a process for producing 3,4-dihydrocoumarin having sufficient purity and quality for use as a perfume. We have found that o -ethylphenol esters, e.g., o -ethylphenyl 3-cyclohexylpropionate or o -ethylphenyl dihydrocinnamate, thermally decompose into o -ethylphenol and carboxylic acids, e.g., 3-cyclohexylpropionic acid and dihydrocinnamic acid, during rectification of the reaction mixture, and that the thus released o -ethylphenol is distilled off together with 3,4-dihydrocoumarin; and that 3,4-dihydrocoumarin of high purity and high quality sufficient for use as a perfume can easily be recovered from the reaction mixture by previously distilling the reaction mixture to once separate high-boiling substances and/or washing the reaction mixture or the distillate with an alkali to remove acidic compounds such as dihydrocinnamic acid, followed by rectification. The present invention thus relates to a process of producing 3,4-dihydrocoumarin comprising cyclization and dehydrogenation of a 3-(2-cyclohexanoyl)propionic acid ester, in which the reaction mixture from the cyclization and dehydrogenation is (i) washed with an alkali to reduce the dihydrocinnamic acid content of the reaction mixture to 1% by weight or less and optionally (ii) is distilled, either before or after the washing step, to remove high-boiling substances; and then subjected to rectification to recover 3,4-dihydrocoumarin. Specific but non-limiting examples of the starting compound, i.e., 3-(2-cyclohexanoyl)propionic acid ester, include methyl 3-(2-cyclohexanoyl)propionate, ethyl 3-(2-cyclohexanoyl)propionate, propyl 3-(2-cyclohexanoyl)propionate, butyl 3-(2-cyclohexanoyl)propionate and isopropyl 3-(2-cyclohexanoyl)propionate. The cyclization and dehydrogenation reaction of the 3-(2-cyclohexanoyl)propionic acid ester is carried out by heating in the presence of a catalyst. Catalysts to be used are solid metallic catalysts comprising a metal, e.g., palladium, platinum, rhodium or ruthenium, supported on at least one carrier which is an element of Group IIA, IIIA or IVA or a compound thereof, e.g., carbon, alumina, silica gel or barium sulfate. A palladium-on-carrier catalyst is preferred. The catalyst is generally used in an amount of from 0.1 to 5% by weight, and preferably of from 0.3 to 2% by weight, based on the 3-(2-cyclohexanoyl)propionic acid ester, although the amount depends on the metal content of the catalyst. Too small an amount of the catalyst exerts considerably reduced reaction activity, and too large an amount has an excessive reaction activity which causes much by-products and also increases the catalyst cost. If desired, the solid metallic catalyst may be used in combination with a promotor, such as metallic chromium, metallic tungsten, barium sulfate, magnesium trisilicate or zirconia. The promotor is generally used in an amount of from 0.01 to 3% by weight based on the 3-(2-cyclohexanoyl) propionic acid ester. The cyclization and dehydrogenation reaction is generally effected at from 100 to 350°C, and preferably from 230 to 300°C. At temperatures lower than about 100°C, the reaction rate tends to be low. At temperatures exceeding 350°C, the starting material and/or the product tend to decompose. A reaction solvent may be used if desired. Examples of suitable solvents include phenyl ether, benzyl ether, methyl-α-naphthyl ether, ethylnaphthalene, dimethylbiphenyl, dodecane, tetradecane, tetralin, acetophenone, phenyl propyl ketone, methyl benzoate and dimethyl glutamate. The reaction is generally carried out by heating the 3-(2-cyclohexanoyl)propionic acid ester and the catalyst together with, if desired, a promotor and a solvent for several to several tens of hours. The reaction generally produces 3,4-dihydrocoumarin in a yield of about from 30 to 70 mol% and coumarin in a yield of about from 5 to 35 mol%. The reaction by-produces dihydrocinnamic acid in amount of about from 0.1 to 20% by weight based on 3,4-dihydrocoumarin and o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate in a total amount of about from 2 to 20% by weight based on 3,4-dihydrocoumarin. Besides these by-products, ethyl benzene, o -ethylphenol, a dihydrocinnamic ester, octahydro-coumarin, and tar-like substances are also by-produced. The resulting reaction mixture from the cyclization and dehydrogenation may be subjected to hydrogenation to convert coumarin present therein to 3,4-dihydrocoumarin. In the present invention, the reaction mixture obtained by the cyclization and dehydrogenation reaction is then subjected to alkali washing for removal of acidic compounds and optionally distillation for removal of high-boiling substances. Alkali washing is performed either before or after distillation. Alkalis which can be used for removal of acidic compounds include hydroxides, oxides, carbonates, hydrogencarbonates, hydrogenphosphates, and dihydrogenphosphates of alkali metals or alkaline earth metals, and compounds showing basicity when dissolved in water. Specific examples of the alkali include lithium hydroxide, sodium hydroxide, potassium hydroxide, magnesium hydroxide, calcium hydroxide, magnesium oxide, calcium oxide, sodium carbonate, potassium carbonate, magnesium carbonate, calcium carbonate, barium carbonate, sodium hydrogencarbonate, potassium hydrogencarbonate, disodium hydrogenphosphate, dipotassium hydrogenphosphate, sodium dihydrogenphosphate and potassium dihydrogenphosphate. Alkali washing is carried out by bringing the reaction mixture (or a distillate in the case when distillation precedes alkali washing, into contact with an alkali. For example, the contact may be effected by mixing with stirring, counter-flow or direct-flow contact, passing the reaction mixture through a pack of an alkali, or passing an alkali through a pack of the reaction mixture. While the alkali may be used as a solid, it is preferably used as an aqueous solution, for ease of handling. In the latter case, the aqueous solution preferably has a concentration of from 0.1 to 50% by weight, and more preferably from 1 to 10% by weight and less than the saturation point. If the concentration is less than 0.1% by weight, sufficient washing effects cannot be obtained. If it exceeds 50% by weight, the hydrolysis of 3,4-dihydrocoumarin tends to be accelerated. Concentrations above the saturation point are employable but make the operation complicated. The amount of the alkali to be used, though varying depending on the manner of contact or the concentration of dihydrocinnamic acid, generally ranges from 0.1 to 100 equivalents per equivalent of dihydrocinnamic acid. If it is less than 0.1 equivalent, sufficient washing effects cannot be obtained. If it exceeds 100 equivalents, hydrolysis of 3,4-dihydrocoumarin tends to be accelerated. Where an alkali metal or alkaline earth metal hydroxide is used as an alkali or where an aqueous solution of an alkali metal or alkaline earth metal oxide, which change to hydroxide in an aqueous solution, is used, it is preferably used in an amount of not more than 1.5 equivalents per equivalent of dihydrocinnamic acid. If such a strong alkali is used in an amount of more than 1.5 equivalents, hydrolysis of 3,4-dihydrocoumarin tends to be unfavourably accelerated. Where an alkali aqueous solution is employed, it is preferably used in an amount of from 0.1 to 10 times the weight of the reaction mixture. If it is smaller than 0.1 times, sufficient washing effects cannot be obtained. If it is larger than 10 times, it tends to result in not only an increased loss of 3,4-dihydrocoumarin into the alkaline aqueous solution but accelerated hydrolysis of 3,4-dihydrocoumarin. The alkali washing is conducted so as to reduce the dihydrocinnamic acid content to 1% by weight or less based on 3,4-dihydrocoumarin. Provided that the mixture containing 3,4-dihydrocoumarin has a dihydrocinnamic acid content of 1% by weight or less based on 3,4-dihydrocoumarin, the subsequent rectification will provide high purity 3,4-dihydrocoumarin of sufficient quality to be suitable for use as a perfume as it is. If the dihydrocinnamic acid content is more than 1% by weight based on 3,4-dihydrocoumarin, the subsequent rectification tends to result in recovery of poor quality 3,4-dihydrocoumarin having a high dihydrocinnamic acid content which is unsuitable for use as a perfume as it is. After the alkali washing, the mixture may further be washed with water to remove the remaining alkali. Simple distillation suffices for removal of high-boiling substances. Distillation may be effected while refluxing at a reflux ratio of not more than 5. Distillation may also be effected in a packed tower or a plate tower having a number of stages of 10 or less. Distillation at a reflux ratio of 5 or more or 10 or more-staged distillation is substantially equal to rectification, which is complicated. Distillation is generally carried out under a pressure of from 13 to 13330 Pa (0.1 to 100 Torr). Distillation under a pressure lower than about 13 Pa not only requires large-scaled equipment for pressure reduction but has a decreased rate of distillation, leading to reduction in productivity. If the pressure is higher than about 13330 Pa, the temperature of the still pot must be increased, and the increased temperature of the distillation pot tends to cause decomposition of 3,4-dihydrocoumarin. Distillation for removal of high-boiling substances is preferably conducted so as to reduce the total content of o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate to 2% by weight of less, and particularly 1% by weight or less, based on the amount of 3,4-dihydrocoumarin. Although compounds forming o -ethylphenol during rectification are not limited to o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate, production of o -ethylphenol during rectification can sufficiently be minimized to recover 3,4-dihydrocoumarin having high purity and sufficient quality for use as a perfume as far as the total content of these ester compounds should be controlled to 2% by weight or less based on 3,4-dihydrocoumarin. Rectification for obtaining high purity 3,4-dihydrocoumarin can be conducted by use of a packed tower or a plate tower. A suitable number of stages of the tower is from 5 to 100. If the number of stages is less than 5, separation efficiency tends to be reduced, failing to obtain 3,4-dihydrocoumarin of sufficiently high purity. If the number of stages is more than about 100, large-scaled equipment is required. The reflux ratio, while dependent on the number of stages, preferably ranges from 1 to 50, and more preferably from 5 to 20. If the reflux ratio is less than about 1, separation efficiency tends to be deteriorated, failing to obtain 3,4-dihydrocoumarin having sufficient purity. If it is more than about 50, the energy for refluxing so much increases. The rectification is generally carried out under a pressure of from 13 to 13330 Pa. Rectification under a pressure of less than 13 Pa not only requires a large-scaled apparatus for pressure reduction but also has a reduced rate of distillation, resulting in deterioration of efficiency. If the pressure is higher than about 13330 Pa, the temperature of the still pot must be elevated accordingly, and the elvated distillation temperature tends to cause decomposition of 3,4-dihydrocoumarin, o-ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate. By the process of the present invention, 3,4-dihydrocoumarin having high purity and high quality sufficient for use as a perfume as such can easily be obtained from 3-(2-cyclohexanoyl)propionic acid esters. The present invention is now illustrated in greater detail by reference to the following Examples, wherein the percentages are by weight unless otherwise indicated. EXAMPLE 1 In a 1 ℓ-volume four-necked flask were charged 308 g of methyl 3-(2-cyclohexanoyl)propionate and 3.0 g of a 5% palladium-on-carbon catalyst (5% of palladium was supported on an activated carbon carrier). The mixture was heated at 240°C for 10 hours while stirring at 300 rpm in a nitrogen atmosphere to conduct cyclization and dehydrogenation. Thereafter, the mixture was further heated while stirring at 300 rpm at 255°C for 1 hour and then at 270°C for 16 hours. After completion of the cyclization and dehydrogenation reaction, the catalyst and the like were removed by filtration to obtain 207 g of a reaction mixture. Cyclization and dehydrogenation reaction of methyl 3-(2-cyclohexanoyl)propionate was conducted two more times in the same manner as described above. The three reaction mixtures combined,weighing 624,g were found to comprise 48.1% of 3,4-dihydrocoumarin, 33.7% of coumarin, 5.3% of the sum of o-ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate, and 0.6% of dihydrocinnamic acid. Accordingly, the total content of o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate was 11.0%, and the content of dihydrocinnamic acid was 1.2%, both based on the amount of 3,4-dihydrocoumarin. In a 1 ℓ separatory funnel were charged 585 g of the above-obtained combined reaction mixture and 586 g of a 5% sodium hydrogencarbonate aqueous solution, the amount of sodium hydrogencarbonate corresponding to 14.9 equivalents per equivalent of dihydrocinnamic acid. The mixture was stirred at 400 rpm at room temperature for 20 minutes, followed by allowing to stand at room temperature for 1 hour to separate into an upper aqueous phase and a lower oily phase. The resulting oily phase and 583 g of water were charged in a 1 ℓ separatory funnel, and the mixture was stirred at room temperature and at 400 rpm for 20 minutes, followed by allowing to stand at room temperature for 1 hour whereby the mixture was separated into an upper aqueous phase and a lower oily phase. The separated oily phase weighed 572 g. As a result of gas chromatography of the washed oily phase, the dihydrocinnamic acid concentration was below the limit of detection and was thus found to be not more than 1% based on 3,4-dihydrocoumarin. The yield of 3,4-dihydrocoumarin in the above-described alkali washing was 99.0%. A 565 g aliquot of the resulting washed oily phase was subjected to simple distillation at 10 Torr to remove high-boiling substances to recover 460 g of crude 3,4-dihydrocoumarin. The resulting crude product was found to contain 54.8% of 3,4-dihydrocoumarin, 32.7% of coumarin, and 0.16% of the sum of o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate, with the concentration of dihydrocinnamic acid being below the limit of detection. Accordingly, the total content of o-ethylphenyl 3-cyclohexylpropionate and o-ethylphenyl dihydrocinnamate was 0.29%, and the content of dihydrocinnamic acid was not more than 1%, both based on the amount of 3,4-dihydrocoumarin. The above crude product was subjected to rectification by using a 33-staged packed tower at a reflux ratio of 10 under a pressure of 2666 Pa (20 Torr). As a result, 172 g of purified 3,4-dihydrocoumarin was obtained in a yield of 61% based on the 3,4-dihydrocoumarin present in the cyclization and dehydrogenation reaction mixture. The thus purified product had a 3,4-dihydrocoumarin purity of 99.7% and an o-ethylphenol content of 0.05%, with the dihydrocinnamic acid content being below the limit of detection of gas chromatography. COMPARATIVE EXAMPLE 1 In a 1 ℓ four-necked flask were charged 411 g of methyl 3-(2-cyclohexanoyl)propionate and 8.0 g of a 5% palladium-on-carbon catalyst. The mixture was heated at 240°C for 8.5 hours while stirring at 300 rpm in a nitrogen atmosphere to conduct cyclization and dehydrogenation. Thereafter, the reaction mixture was further heated at 250°C for 5.5 hours and then at 260°C for 16 hours with stirring at 300 rpm. After completion of the cyclization and dehydrogenation reaction, the catalyst and the like were removed by filtration to obtain 232 g of a reaction mixture. The same reaction was repeated to obtain 557 g of a reaction mixture in total. The resulting combined reaction mixture had a 3,4-dihydrocoumarin content of 42.3%, a coumarin content of 39.9%, a total content of o-ethylphenyl 3-cyclohexylpropionate and o-ethylphenyl dihydrocinnamate of 6.6%, and a dihydrocinnamic acid content of 1.1%. Accordingly, the total content of o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate was 15.6%, and the content of dihydrocinnamic acid was 2.6%, both based on the amount of 3,4-dihydrocoumarin. A 342 g aliquot of the resulting reaction mixture was rectified in a 33-staged packed tower at a reflux ratio of 10 under a pressure of 2666 Pa (20 Torr) to recover 93.5 g of purified 3,4-dihydrocoumarin in a yield of 65% based on the 3,4-dihydrocoumarin present in the reaction mixture. The purity of 3,4-dihydrocoumarin in the purified product was 98.2%; the o-ethylphenol content was 1.0%; and the dihydrocinnamic acid content was 0.06%. The product as obtained was unsuitable for use as a perfume. EXAMPLE 2 In a 1 ℓ-volume four-necked flask were charged 606 g of methyl 3-(2-cyclohexanoyl)propionate and 6.1 g of a 5% palladium-on-carbon catalyst. The mixture was heated at 250°C for 15.5 hours while stirring at 300 rpm in a nitrogen atmosphere to conduct cyclization and dehydrogenation. Thereafter, the mixture was further heated at 260°C with stirring at 300 rpm for 3 hours. The resulting reaction mixture as containing the catalyst was transferred to a 1 ℓ glass-made autoclave in air and heated at 120°C for 70 minutes at a hydrogen pressure of 1.96 Pa x 10⁵ (2 kg/cm²) while stirring at 1,000 rpm to conduct hydrogenation. After completion of the hydrogenation reaction, the catalyst and the like were removed from the reaction mixture by filtration to obtain 389 g of a hydrogenation reaction mixture. The resulting reaction mixture had a 3,4-dihydrocoumarin content of 67.4%, a total content of o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate of 11.4%, and a dihydrocinnamic acid content of 1.15%. Accordingly, the total content of o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate was 16.9%, and the dihydrocinnamic acid content was 1.71%, both based on the amount of 3,4-dihydrocoumarin. The resulting reaction mixture was subjected to simple distillation at 1333 Pa (10 Torr) to remove high-boiling substances to thereby recover 344 g of crude 3,4-dihydrocoumarin as a distillate. A 339 g aliquot of the distillate was washed successively with 339 g of a 5% sodium hydrogencarbonate aqueous solution and 165 g of water to obtain 322 g of crude 3,4-dihydrocoumarin, in which the 3,4-dihydrocoumarin content was 80.5%; the total content of o -ethylphenyl 3-cyclohexylpropionate and o-ethylphenyl dihydrocinnamate was 0.79%, and the dihydrocinnamic acid content was 0.38%. Accordingly, the total content of o -ethylphenyl 3-cyclohexylpropionate and o -ethylphenyl dihydrocinnamate was 0.98%, and the dihydrocinnamic acid content was 0.47%, both based on 3,4-dihydrocoumarin. A 202 g aliquot of the resulting crude 3,4-dihydrocoumarin was subjected to rectification in a 33-staged packed tower at a reflux ratio of 10 at a pressure of 666 Pa (5 Torr) to recover 126 g of purified 3,4-dihydrocoumarin in a yield of 77% based on the 3,4-dihydrocoumarin charged in the packed tower. The purity of 3,4-dihydrocoumarin was 99.7%; the o -ethylphenol content was 0.032%; and the dihydrocinnamic acid content was below the limit of detection of gas chromatography. EXAMPLE 3 In a 500 ml separatory funnel were charged 150 g of 3,4-dihydrocoumarin containing 4.0% of dihydrocinnamic acid and 150 g of a 5% sodium hydrogencarbonate aqueous solution. The amount of sodium hydrogencarbonate corresponded to 2.2 equivalents per equivalent of dihydrocinnamic acid. The mixture was stirred at room temperature at 400 rpm for 20 minutes, followed by allowing to stand at room temperature for 1 hour to separate into an upper aqueous phase and a lower oily phase. In a 500 ml separatory funnel were charged the thus separated oily phase and 150 g of water and stirred at 400 rpm at room temperature for 20 minutes, followed by allowing to stand at room temperature for 1 hour to separate into an upper aqueous phase and a lower oily phase to obtain 144 g of a washed oily phase. As a result of gas chromatography, the washed oily phase was found to have a dihydrocinnamic acid content of 0.16%, which corresponded to not more than 1% based on 3,4-dihydrocoumarin. The yield of 3,4-dihydrocoumarin in the above alkali washing was 99.1%. EXAMPLE 4 3,4-Dihydrocoumarin having a varied content of dihydrocinnamic acid was washed with an alkali in the same manner as in Example 3, except for changing the kind and amount of the alkali used as shown in Table 1 below. The results obtained are shown in Table 1. COMPARATIVE EXAMPLE 2 Alkali washing of dihydrocinnamic acid-containing 3,4-dihydrocoumarin was carried out in the same manner as in Example 3, except for using 2% sodium hydroxide aqueous solution, the amount of sodium hydroxide corresponding to 1.9 equivalents per equivalent of dihydrocinnamic acid. As a result, the dihydrocinnamic acid content in the washed oily phase was below the limit of detection, i.e., not more than 1% based on 3,4-dihydrocoumarin, but the yield of 3,4-dihydrocoumarin was 92.1%. EXAMPLE 5 In a 500 ml separatory funnel were charged 165 g of 3,4-dihydrocoumarin containing 7.0% of dihydrocinnamic acid and 165 g of a 10% aqueous solution of disodium hydrogen-phosphate dodecahydrate. To the mixture was added 15.1 g of a 20% sodium hydroxide aqueous solution while stirring at room temperature. The amount of sodium hydroxide added corresponded to 0.98 equivalent per equivalent of dihydrocinnamic acid, and the total amount of disodium hydrogenphosphate and sodium hydroxide corresponded to 2.2 equivalents per equivalent of dihydrocinnamic acid. The mixture was further stirred at 400 rpm at room temperature for 20 minutes, followed by allowing to stand at room temperature for 1 hour to separate into an upper aqueous phase and a lower oily phase to obtain 151 g of a washed oily phase. As a result of gas chromatography, the washed oily phase was found to have a dihydrocinnamic acid content of 0.05%, which corresponded to not more than 1% based on 3,4-dihydrocoumarin. The yield of 3,4-dihydrocoumarin in the above alkali washing was 97.4%. EXAMPLE 6 In a 500 ml separatory funnel were charged 165 g of 3,4-dihydrocoumarin containing 7.0% of dihydrocinnamic acid and 165 g of a 1.8% sodium hydrogencarbonate aqueous solution. The mixture was stirred at room temperature at 400 rpm for 20 minutes, followed by allowing to stand at room temperature for 1 hour to separate into an upper aqueous phase and a lower oily phase. As a result of gas chromatography, the washed oily phase was found to have a dihydrocinnamic acid content of 3.0%. Then, the resulting oily phase was charged in a 500 ml separatory funnel together with 165 g of a 1.8% sodium hydrogencarbonate aqueous solution. The amount of sodium hydrogencarbonate used in each of the first and second washing was 0.46 equivalent, respectively, i.e., 0.92 equivalent in total, per equivalent of dihydrocinnamic acid. The mixture was stirred at 400 rpm at room temperature for 20 minutes, followed by allowing to stand at room temperature for 1 hour to obtain 151 g of a washed oily phase. As a result of gas chromatography, the dihydrocinnamic acid content in the washed oily phase was found to be 0.60%, which corresponded to not more than 1% based on 3,4-dihydrocoumarin. The yield of 3,4-dihydrocoumarin in the above alkali washing was 96.8%.

Claims: A process of producing 3,4-dihydrocoumarin comprising cyclization and dehydrogenation of a 3-(2-cyclohexanoyl)-propionic acid ester, characterised in that a reaction mixture obtained by said cyclization and dehydrogenation is washed with an alkali to reduce the dihydrocinnamic acid content of said reaction mixture of 1% by weight or less, and then subjected to rectification to recover 3,4-dihydrocoumarin. A process as claimed in Claim 1, further comprising a distillation step to remove high-boiling substances, said distillation step being carried out either before or after said reaction mixture is washed with said alkali, but said distillation step being carried out before said reaction mixture is subjected to rectification. A process as claimed in Claim 2, wherein the distillation is carried out so as to reduce the total content of o -ethylphenyl 3-cyclohexlpropionic acid and o -ethylphenyl dihydrocinnamate of said high-boiling substances to 2% by weight or less based on the amount of 3,4-dihydrocoumarin. A process as claimed in Claim 2, wherein the distillation is carried out in a packed tower or plate tower of up to 100 stages and at a reflux ratio of not more than 5 and a pressure of 13 to 13330 Pa. A process as claimed in either Claim 1 or 2, wherein said washing with an alkali is carried out by using an alkali other than an alkali metal or alkaline earth metal hydroxide. A process as claimed In either Claim 1 or 2, wherein said washing with an alkali is carried out by using not more than 1.5 equivalents of an alkali metal or alkaline earth metal hydroxide per equivalent of dihydrocinnamic acid. A process as claimed in any of Claims 1, 2, 5 or 6, wherein the alkali washing is carried out by bringing the reaction mixture or distillate thereof into contact with a 0.1 to 50 weight percent aqueous solution of alkali using 0.1 to 100 equivalents of alkali per equivalent of dihydrocinnamic acid.

Inventors: NISHIDA YOSHITAKA, OKUSAKO KENSEN, SAKAI KIYOMI, SHIRAFUJI TAMIO, NISHIDA, YOSHITAKA, OKUSAKO, KENSEN, SAKAI, KIYOMI, SHIRAFUJI, TAMIO
Applicants: SUMITOMO CHEMICAL CO, SUMITOMO CHEMICAL COMPANY LIMITED
Application year: 1991
Main classification: C07D311
IPC codes: C07D311