Process for alkylation on the aromatic ring of phenols or of ethers of phenols

Abstract: A process for producing aromatic ring alkylated phenols, wherein said process comprises reacting a phenol represented by the general formula (1): wherein each of R 1 , R 2 , R 3 , R 4 and R 5 independently represents a hydrogen atom, or a linear or branched alkyl group having 1 to 10 carbon atoms; with a monohydric or dihydric alcohol in the presence of a hydroxide of a metal, an alkoxide of a metal, or a hydroxide of a metal and an alkoxide of a metal in a supercritical state of the alcohol.

Description: The present invention relates to a process for producing aromatic ring alkylated phenols. Aromatic ring alkylated phenols are industrially used as raw materials and intermediates of e.g. pharmaceuticals, agrochemicals, resins, various additives, polymerization inhibitors, antioxidants, disinfectants, preservatives and industrial chemicals. Among them, thymol having a structure in which an isopropyl group is bonded to the 2-position and a methyl group is bonded to the 5-position of phenol is in much demand as a vermicide. Further, 2,3,6-trimethylphenol is in much demand as a synthesis intermediate of trimethylhydroquinone which is a raw material of vitamin E. In an example for producing vitamin E from 2,3,6-trimethylphenol, in the first step, 2,3,6-trimethylphenol is oxidized to give 2,3,6-trimethylbenzoquinone which is reduced to synthesize trimethylhydroquinone. In the second step, trimethylhydroquinone and phytol are reacted in the presence of an acid catalyst to synthesize vitamin E according to US-A-5,523,420. Conventionally, for obtaining ortho-alkyled phenols, a gas phase reaction in which phenols and alcohol are vaporized and passed through a catalyst phase to cause a reaction thereof, and a liquid phase reaction utilizing Friedel Craft's reaction are known. For example, JP-A-6-25041 discloses a method in which a phenol and alcohol are reacted in the gas phase using manganese oxide as a: catalyst to produce an aromatic ring alkylated derivative of the phenol. However, this method has a problem that the reaction apparatus becomes complicated and bulky. US 4,418,224 discloses the preparation of ortho-alkylated phenols in the presence of an ortho-alkylation catalyst consisting of magnesium carbonate,magnesium hydroxide or a mixture of both. JP-A-2000-38363 discloses a method in which a phenol and alcohol are heated at 400°C in a supercritical region for alkylation using zirconium oxide as a catalyst. However, in this method, a large amount of catalyst is necessary, causing problems in cost and size of the apparatus. JP-A-10034805 discloses the production of substituted phenols under supercritical reaction conditions. The above-mentioned known methods have a problem that a large and complicated reaction apparatus is necessary and a problem that a large amount of catalyst is required. An object of the present invention is to provide a process for producing aromatic ring alkylated phenols by using a phenol and alcohol in a relatively smaller reaction vessel with a small amount of catalyst, at high reactivity. This object could be achieved on the basis of the finding that aromatic ring alkylated phenols can be easily obtained by reacting at least one phenol with at least one alcohol in a supercritical state in the presence of a hydroxide or alkoxide of a metal as a catalyst. Namely, the present invention relates to a process for producing aromatic ring alkylated phenols, wherein said process comprises reacting a phenol represented by the general formula (1): wherein each of R 1 , R 2 , R 3 , R 4 and R 5 independently represents a hydrogen atom or a linear or branched alkyl group having 1 to 10 carbon atoms; with a monohydric or dihydric alcohol in the presence of a hydroxide of a metal, an alkoxide of a metal, or a hydroxide of a metal and an alkoxide of a metal in a supercritical state of the alcohol [hereinafter, referred to as production method (I) of the present invention]. Further, the present invention relates to a process for producing aromatic ring alkylated phenols, wherein said process comprises reacting a phenol represented by the general formula (1) with a monohydric or dihydric alcohol in the presence of carbon dioxide and a hydroxide of a metal, an alkoxide of a metal or a hydroxide of a metal and an alkoxide of a metal in a supercritical state of the mixture of alcohol and carbon dioxide [hereinafter, referred to as production method (II) of the present invention]. The present invention will be illustrated in detail below. As the linear or branched alkyl group having 1 to 10 carbon atoms represented by R 1 , R 2 , R 3 , R 4 or R 5 in the phenol represented by the general formula (1), used as a raw material in the present invention, a methyl group, ethyl group, n-propyl group, isopropyl group, n-butyl group, isobutyl group and t-butyl group are exemplified, and specific examples of the phenols of the general formula (1) include phenol, o-cresol, m-cresol, p-cresol, 2,3-xylenol, 2,4-xylenol, 2,5-xylenol, 3,4-xylenol, 3,5-xylenol, anisole and t-butylphenol. The alcohol which is the other starting material in the present invention is not particularly restricted provided it is a monohydric or dihydric alcohol, and preferably a monohydric alcohol represented by the general formula (2): R 6 -OH wherein R 6 represent a linear or branched alkyl group having 1 to 10 carbon atoms. Here, as R 6 , there are exemplified a methyl group, ethyl group, n-propyl group, isopropyl group, n-butyl group, isobutyl group and t-butyl group. As the monohydric alcohol represented by the general formula (2), methanol, ethanol, n-propanol, isopropanol, n-butanol, isobutanol, t-butanol, pentanol, hexanol, heptanol, n-octanol, n-nonanol and n-decanol are exemplified and methanol, ethanol, n-propanol and n-butanol are preferable, methanol and ethanol are more preferable, and methanol is further preferable. As the dihydric alcohol, ethylene glycol and propylene glycol are exemplified. In the present invention, the molar ratio of monohydric or dihydric alcohol to phenol of the general formula (1) is appropriately determined depending on the compound used, and is usually from 1 to 1000, and preferably from 1 to 200. In the production method (I) of the present invention, the reaction is conducted under conditions wherein the monohydric or dihydric alcohol manifests a supercritical state. In the production method (II) of the present invention, the reaction is conductedunder conditions wherein the mixture of monohydric or dihydric alcohol and carbon dioxide manifests a supercritical state. Here, the supercritical condition means the following condition. A substance manifests inherent three conditions of gas, liquid and solid, but when it is above the critical temperature and the critical pressure, a fluid phase is formed which is not condensed even if pressure is applied. This condition is referred to as supercritical condition. A fluid in supercritical condition shows different nature from usual natures of liquid and gas. A fluid in supercritical condition is a "solvent which is not liquid" , in which the density thereof is near that of liquid, and the viscosity thereof is near that of gas, and heat conductivity and diffusion coefficient show intermediate natures between gas and liquid, and mass transfer becomes advantageous due to lower viscosity and higher diffusion property, and higher heat transferring property can be obtained because of higher conductivity. When a supercritical fluid is used as a reaction site, higher reactivity is obtained than in usual gas phase and liquid phase since the reaction site is under conditions of higher density and higher diffusion property as described above. Further, because the supercritical condition has a density near a liquid phase, the size of the reaction apparatus can be reduced as compared with a gas phase. In the present invention, the upper limit of reaction temperature is not restrictive, and preferably 450°C or less so that phenols represented by the general formula (1) are not decomposed. The upper limit of reaction pressure is also no restrictive, and preferably 25 MPa or less since increase of pressure resistance of the reaction apparatus is expensive. In the production method (I) of the present invention, it is necessary that the reaction is conducted under conditions wherein the monohydric or dihydric alcohol manifests a supercritical state. When methanol is used as the alcohol, the reaction is conducted under conditions of 240°C or more and 8 MPa or more since methanol has a critical temperature of 240°C and a critical pressure of 8 MPa. When ethanol is used, the reaction is conducted under conditions of 243°C or more and 6.3 MPa or more since ethanol has a critical temperature of 243°C and a critical pressure of 6.3 MPa. When n-propanol is used, the reaction is conducted under conditions of 264°C or more and 5 MPa or more since n-propanol has a critical temperature of 264°C and a critical pressure of 5 MPa. When isopropanol is used, the reaction is conducted under conditions of 235°C or more and 4.8 MPa or more since isopropanol has a critical temperature of 235°C and a critical pressure of 4.8 MPa. When n-butanol is used, the reaction is conducted under conditions of 287°C or more and 4.8 MPa or more since n-butanol has a critical temperature of 287°C and a critical pressure of 4.8 MPa. Next, the production method (II) of the present invention will be illustrated. In the production method (II) of the present invention, it is necessary that the reaction is conducted under conditions wherein the mixture of monohydric or dihydric alcohol and carbon dioxide manifests a supercritical state, in the presence of a catalyst and carbon dioxide. The mixing ratio of the above-mentioned alcohol and carbon dioxide is not particularly restricted, and is determined in view of solubility of phenols used in the reaction in the alcohol. The mixing ratio of the above-mentioned alcohol and carbon dioxide is preferably 10:90 to 99:1. Cases in which methanol is used as the alcohol and phenol is used as the phenol will be illustrated specifically. For example, when the molar ratio of methanol to carbon dioxide is 75:25, this mixture has a critical temperature of 204°C and a critical pressure of 12.75 MPa according to Journal of Chemical Thermodynamics, vol. 23, p. 970 (1991). When the aromatic ring of a phenol is methylated under temperature and pressure conditions wherein a mixture of methanol and carbon dioxide manifests a supercritical condition, temperature and pressure conditions are necessary wherein the mixture manifests a supercritical condition. For example, in the case of the above-mentioned mixture in which the molar ratio of methanol to carbon dioxide is 75:25, a temperature of 204°C or more and a pressure of 12.75 MPa or more are necessary, and a temperature of 240°C or more and a pressure of 12.75 MPa or more are more preferable. The reaction time in the production method (I) of the present invention or the production method (II) of the present invention is appropriately determined, respectively, depending on the kind of the phenol and the alcohol, andusually in a range from 1 minute to 24 hours. In the respective production method, the reaction has to be conducted in the presence of a catalyst, namely, a hydroxide of a metal, an alkoxide of a metal, a hydroxide of a metal and an alkoxide of a metal, and reactivity of alkylation of aromatic ring can be enhanced only by addition of a relatively small amount of the catalyst. Typical examples of the hydroxide of a metal include, but are not limited to, lithium hydroxide, sodium hydroxide, potassium hydroxide, magnesium hydroxide, calcium hydroxide, barium hydroxide, strontium hydroxide and germanium hydroxide. The hydroxide may be combined with an alkoxide of a metal. Examples of the alkoxide of a metal include, but are not limited to, lithium methylate, sodium methylate, potassium methylate, dimethoxymagnesium, dimethoxycalcium, dimethoxybarium, dimethoxystrontium and tetramethoxygermanium. The alkoxide may be combined with a hydroxide of a metal. The present invention can be effected in various reaction embodiments. For example, it may be conducted by a batch system, or by a flow system, and the batch system is preferable. The aromatic ring alkylated phenol represented by the general formula (1) is separated from the reaction mixture after completion of the respective reaction of the production method (I) or the production method (II) at a purity necessary for various uses. The reaction mixture may sometimes contain unreacted raw materials or other impurities in addition to the aromatic ring alkylated phenol. The separation method is not particularly restricted, and general methods such as distillation and extraction can be applied according to the nature of the substituted compound. Namely, according to the present invention, a method can be provided in which a phenol represented by the general formula (1) and a and monohydric or dihydric alcohol are used, and the aromatic ring of the phenol is alkylated in a relatively smaller reaction vessel at higher reactivity, particularly by a batch system, with a small amount of a catalyst. In the present invention, the addition amount of a catalyst is preferably from 0.01 to 20% by weight, more preferably from 0.05 to 2% by weight based on the phenol of the general formula (1) used in the reaction. According to the present invention, aromatic ring alkylated phenols can be easily obtained by reacting phenols with alcohols in a relatively smaller reaction vessel with a small amount of catalyst at high reactivity. EXAMPLES The following examples further illustrate the present invention in detail, but do not limit the scope of the present invention. Reaction materials and reaction products in the examples were identified by using a gas chromatography mass analysis apparatus HP-6890 (GC: manufacture by Yokogawa Electric Corp.)-HP5973 (MS: manufacture by Yokogawa Electric Corp.), and analyzed quantitatively by using a gas chromatography apparatus GC-353B (manufactured by GL Science) equipped with FID (flame ionization detector). The conversion and selectivity in the examples were calculated according to the following methods. Conversion was calculated by the following formula: (conversion)={1-(area of chromatograph of unreacted reaction substrates remaining in reaction solution)/(sum of areas of remaining reaction substrates and whole reaction product)}×100%. The selectivity was calculated by the following formula: (selectivity)={(area of gas chromatograph of reaction product to be calculated)/(sum of areas of gas chromatograph of whole reaction product)}×100%, while hypothesizing that areas of gas chromatograph per mol of reaction products are equivalent. Example 1 0.035 g of m-cresol (manufactured by Wako Pure Chemical Industries Ltd.), 1.358 g of methanol (manufactured by Wako Pure Chemical Industries Ltd.) and 0.33 mg of lithium hydroxide monohydrate (manufactured by Wako Pure Chemical Industries Ltd.) (0.94% by weight based on m-cresol) were charged in an autoclave (made of SUS316, inner volume: 4.5 ml) and heated up to 370°C by a sand bath, to initiate a reaction. After 15 minutes, the autoclave was quenched, and the reaction solution was removed after the temperature of the autoclave reached room temperature. Quantification was conducted according to the above-mentioned method, as a result, the conversion of m-cresol was 64 mol%, the selectivity of 2,5-xylenol was 51 mol% and the selectivity of 2,3,6-trimethylphenol was 11 mol%. Regarding other components than these reaction products, the selectivity of 2,3-xylenol was 17 mol%, the selectivity of 3,4-xylenol was 5 mol%, the selectivity of m-methylanisole was 1 mol%, the sum of the selectivity of trimethylphenols other than 2,3,6-trimethylphenol was 4 mol%, and the selectivity of 2,3,4,6-tetramethylphenol was 1 mol%. The components were separated from the reaction solution by using liquid chromatography, and 2,5-xylenol and 2,3,6-trimethylphenyl were separated therefrom. The separated solutions were analyzed by using a gas chromatography mass analysis apparatus, to confirm that 2,5-xylenol and 2,3,6-trimethylphenol were separated from the product. Since the autoclave does not have a pressure gauge, the following experiment was conducted to estimate pressure during the reaction. Namely, a pressure gauge was installed to the same autoclave, the same amounts of m-cresol and methanol were charged and heated up to 370°C by a sand bath, and the pressure was measured. The estimated value of the pressure during the reaction was 10 MPa. Example 2 0.051 g of phenol (manufactured by Wako Pure Chemical Industries Ltd.), 1.358 g of methanol and 0.75 mg of lithium hydroxide monohydrate (0.15% by weight based on phenol) were charged in an autoclave (made of SUS316, inner volume: 4.5 ml, no pressure gauge) and heated up to 400°C by a sand bath, to initiate a reaction. After 30 minutes, the autoclave was quenched, and the reaction solution was removed after the temperature of the autoclave reached room temperature. Quantification was conducted according to the above-mentioned method, as a result, the conversion of phenol was 36 mol%, the selectivity of o-cresol was 51 mol%, the selectivity of p-cresol was 10 mol%, the selectivity of 2,6-xylenol was 3 mol%, and the selectivity of 2,4-xylenol was 2 mol%. The components were separated from the reaction solution by using liquid chromatography, and o-cresol, p-cresol, 2, 6-xylenol and 2,4-xylenol were separated therefrom. The separated solutions were analyzed by using a gas chromatography mass analysis apparatus, to confirm that o-cresol, p-cresol, 2,6-xylenol and 2,4-xylenol were separated from the product. Since the autoclave does not have a pressure gauge, the following experiment was conducted to estimate pressure during the reaction. Namely, a pressure gauge was installed to the same autoclave, the same amounts of phenol and methanol were charged and heated up to 400°C by a sand bath, and the pressure was measured. The estimated value of the pressure during the reaction was 14.7 MPa. Comparative Example 1 0.051 g of phenol, 1.352 g of methanol and 1.0 mg of zirconium oxide (manufactured by Kojundo Kagaku K.K.) (2.0% by weight based on phenol) were charged in an autoclave (made of SUS316, inner volume: 4.5 ml, no pressure gauge) and heated up to 400°C by a sand bath, to initiate a reaction. After 30 minutes, the autoclave was quenched, and the reaction solution was removed after the temperature of the autoclave reached room temperature. Quantification was conducted according to the above-mentioned method, as a result, the conversion of phenol was 20 mol%, the selectivity of o-cresol was 50 mol%, the selectivity of p-cresol was 3 mol%, the selectivity of 2,6-xylenol was 2 mol%, and the selectivity of 2,4-xylenol was 1 mol%. Since the autoclave does not have a pressure gauge, the following experiment was conducted to estimate pressure during the reaction. Namely, a pressure gauge was installed to the same autoclave, the same amounts of phenol and methanol were charged and heated up to 400°C by a sand bath, and the pressure was measured. The estimated value of the pressure during the reaction was 14.7 MPa. Comparative Example 2 0.052 g of phenol, 1.358 g of methanol and 1.1 mg of zinc oxide (manufactured by Wako Pure Chemical Industries Ltd.) (2.1% by weight based on phenol) were charged in an autoclave (made of SUS316, inner volume: 4.5 ml, no pressure gauge) and heated up to 400°C by a sand bath, to initiate a reaction. After 30 minutes, the autoclave was quenched, and the reaction solution was removed after the temperature of the autoclave reached room temperature. Quantification was conducted according to the above-mentioned method, as a result, the conversion of phenol was 11 mol%, the selectivity of o-cresol was 78 mol%, the selectivity of p-cresol was 2 mol%, the selectivity of 2,6-xylenol was 3 mol%, and 2,4-xylenol was not produced. Since the autoclave does not have a pressure gauge, the following experiment was conducted to estimate pressure during the reaction. Namely, a pressure gauge was installed to the same autoclave, the same amounts of phenol and methanol were charged and heated up to 400°C by a sand bath, and the pressure was measured. The estimated value of the pressure during the reaction was 14.7 MPa. Example 3 0.045 g of p-cresol (manufactured by Wako Pure Chemical Industries Ltd.), 1.485 g of methanol and 0.25 mg of lithium hydroxide monohydrate (0.56% by weight based on p-cresol) were charged in an autoclave (made of SUS316, inner volume: 4.5 ml, no pressure gauge) and heated up to 400°C by a sand bath, to initiate a reaction. After 30 minutes, the autoclave was quenched, and the reaction solution was removed after the temperature of the autoclave reached room temperature. Quantification was conducted according to the above-mentioned method, as a result, the conversion of p-cresol was 97 mol%, and the selectivity of 2,4-xylenol was 23 mol%, and the selectivity of 2,4,6-trimethylphenol was 61 mol%. The components were separated from the reaction solution by using liquid chromatography, and 2,4-xylenol and 2,4,6-trimethylphenol were separated therefrom. The separated solutions were analyzed by using a gas chromatography mass analysis apparatus, to confirm that 2,4-xylenol and 2,4,6-trimethylphenol were separated from the product. Since the autoclave does not have a pressure gauge, the following experiment was conducted to estimate pressure during the reaction. Namely, a pressure gauge was installed to the same autoclave, the same amounts of p-cresol and methanol were charged and heated up to 400°C by a sand bath, and the pressure was measured. The estimated value of the pressure during the reaction was 15.4 MPa. Comparative Example 3 0.051 g of p-cresol, 1.350 g of methanol and 1.2 mg of zirconium oxide (2.4% by weight based on p-cresol) were charged in an autoclave (made of SUS316, inner volume: 4.5 ml, no pressure gauge) and heated up to 400°C by a sand bath, to initiate a reaction. After 30 minutes, the autoclave was quenched, and the reaction solution was removed after the temperature of the autoclave reached room temperature. Quantification was conducted according to the above-mentioned method, as a result, the conversion of p-cresol was 8 mol%, the selectivity of 2,4-xylenol was 30 mol%, and 2,4, 6-trimethylphenol was not produced. Since the autoclave does not have a pressure gauge, the following experiment was conducted to estimate pressure during the reaction. Namely, a pressure gauge was installed to the same autoclave, the same amounts of p-cresol and methanol were charged and heated up to 400°C by a sand bath, and the pressure was measured. The estimated value of the pressure during the reaction was 14.7 MPa. Comparative Example 4 0.052 g of p-cresol, 1.355 g of methanol and 1.3 mg of zinc oxide (2.3% by weight based on p-cresol) were charged in an autoclave (made of SUS316, inner volume: 4.5 ml, no pressure gauge) and heated up to 400°C by a sand bath, to initiate a reaction. After 30 minutes, the autoclave was quenched, and the reaction solution was removed after the temperature of the autoclave reached room temperature. Quantification was conducted according to the above-mentioned method, as a result, the conversion of p-cresol was 12 mol%, the selectivity of 2,4-xylenol was 81 mol% and the selectivity of 2,4,6-trimethylphenol was 4 mol%. Since the autoclave does not have a pressure gauge, the following experiment was conducted to estimate pressure during the reaction. Namely, a pressure gauge was installed to the same autoclave, the same amounts of p-cresol and methanol were charged and heated up to 400°C by a sand bath, and the pressure was measured. The estimated value of the pressure during the reaction was 14.7 MPa. Example 4 0.412 g of m-cresol, 1.500 g of isopropanol and 1.9 mg of lithium hydroxide (0.46% by weight based on m-cresol) were charged in an autoclave (made of SUS316, inner volume: 4.5 ml, no pressure gauge) and heated up to 400°C by a sand bath, to initiate a reaction. After 30 minutes, the autoclave was quenched, and the reaction solution was removed after the temperature of the autoclave reached room temperature. Quantification was conducted according to the above-mentioned method, as a result, the conversion of m-cresol was 22 mol%, and the selectivity of thymol was 62 mol%. Since the autoclave does not have a pressure gauge, the following experiment was conducted to estimate pressure during the reaction. Namely, a pressure gauge was installed to the same autoclave, the same amounts of m-cresol and isopropanol were charged and heated up to 400°C by a sand bath, and the pressure was measured. The estimated value of the pressure during the reaction was 10 MPa.

Claims: A process for producing aromatic ring alkylated phenols, wherein said process comprises reacting a phenol represented by the general formula (1): wherein each of R 1 , R 2 , R 3 , R 4 and R 5 independently represents a hydrogen atom, or a linear or branched alkyl group having 1 to 10 carbon atoms; with a monohydric or dihydric alcohol in the presence of a hydroxide of a metal, an alkoxide of a metal, or a hydroxide of a metal and an alkoxide of a metal in a supercritical state of the alcohol. The process according to Claim 1, wherein said process comprises reacting a phenol represented by the general formula (1) with a monohydric or dihydric alcohol in the presence of carbon dioxide and a hydroxide of a metal, an alkoxide of a metal or a hydroxide of a metal and an alkoxide of a metal in a supercritical state of the mixture of alcohol and carbon dioxide. The process according to Claim 1 or 2, wherein the monohydric alcohol is an alcohol represented by the general formula (2): R 6 -OH wherein R 6 represent a linear or branched alkyl group having 1 to 10 carbon atoms. The process according to Claim 3, wherein R 6 in the general formula (2) is a methyl group. The process according to any one of Claims 1 to 4, wherein the hydroxide of a metal is lithium hydroxide, sodium hydroxide, potassium hydroxide or calcium hydroxide. The process according to any one of Claims 1 to 5, wherein the alkoxide of a metal is lithium methylate, sodium methylate or potassium methylate.

Inventors: GOTO FUMISATO, SUSUKI TOMOYUKI, TANAKA KOZO, GOTO, FUMISATO, SUSUKI, TOMOYUKI, TANAKA, KOZO
Applicants: SUMITOMO CHEMICAL CO, SUMITOMO CHEMICAL COMPANY, LIMITED
Application year: 2000
Main classification: C07C37
IPC codes: C07C41, C07C37