Method for alkylation of phenols, and catalyst therefor

Abstract: A method of alkylating a phenol is disclosed which comprises contacting a phenol having a hydrogen atom in at least one of the ortho-positions relative to the hydroxyl group with an alcohol in the gaseous phase at an elevated temperature in the presence of a catalyst comprising iron oxide, silica, chromium oxide, germanium oxide and an alkali metal compound. The catalyst, which itself forms an aspect of the invention, exhibits a long duration of catalytic activity and requires less frequent regeneration and replacement than conventional catalysts.

Description: This invention relates to a method of alkylation of phenols and to a catalyst therefor. More specifically, it relates to a method of selective alkylation of phenols in the ortho-position and to a catalyst therefor. Phenols alkylated in the ortho-position are useful as an industrial material for a variety of products. For example, 2,6-xylenol is used as a material for a polyphenylene oxide resin, and 2,3,6-trimethylphenol as a material for vitamin E. A method for producing ortho-alkylated phenols has been known, in which a phenol compound and an alcohol are allowed to catalytically react with each other in a gaseous phase to alkylate the phenol compound in the ortho-position. U.K. Patent 717,588 discloses a method using, as a catalyst, a metal oxide, preferably aluminum oxide. Japanese Patent Publication No. 6894/1967 discloses a method using, as a catalyst, magnesium oxide. Japanese Patent Publication No. 11101/1966 discloses a method using, as a catalyst, manganese oxide. Further, Japanese Patent Publication No. 51367/1982 discloses a method using, as a catalyst, chromium oxide. However, the aluminum oxide catalyst is not satisfactory in view of activity and alkylation selectivity to the ortho-position. The magnesium oxide catalyst does not exhibit sufficient activity although it has comparatively high selectivity to the ortho-position. That is, the magnesium oxide catalyst requires a very high reaction temperature of 475 to 600° C, and hence, is disadvantageous in regard to energy. The period over which it remains active also needs to be improved. Further, the manganese oxide catalyst and chromium oxide catalyst manifest a sharp decline in activity with the progress of the reaction, although they have comparatively high activity and selectivity. The present inventor has made a diligent study to develop a catalyst system which exhibits high activity at a low temperature which is advantageous in energy terms, and which remains active for a long time and has excellent selectivity to the ortho position. As a result, the following catalysts have already been found. US-A-3,953,529 (see corresponding Japanese Patent Publications Nos. 12689/1977 and 12690/1977) discloses a method of alkylating phenols in the ortho-position by reacting the phenols with an alcohol in the presence, as a catalyst, of: a. a mixture of iron oxide and silica, or b. a mixture of iron oxide, silica and chromium oxide. US-A-4,024,195 (see corresponding Japanese Patent Publication No. 12692/1977) discloses a method of alkylating phenols by reacting the phenols with an alcohol in the presence, as a catalyst, of a mixture of iron oxide, silica, chromium oxide and an alkali metal compound. Of these catalysts the mixture of iron oxide, silica, chromium oxide and an alkali metal compound remains active much longer than the conventional catalysts, while maintaining high selectivity to the ortho-position. However, the catalyst activity decreases with time as a carbonaceous substance deposits on the catalyst and the catalyst is gradually sintered. Hence, when the above catalyst is used industrially, periodic catalyst regeneration operation to remove the deposited carbonaceous substance and replacement of catalyst used for a certain period are required. This invention seeks therefore to provide a novel alkylating catalyst and a method of alkylating phenols in the presence of the catalyst. Accordingly the invention provides a catalyst suitable for use in alkylating a phenol which comprises iron oxide, silica, chromium oxide, germanium oxide and an alkali metal compound wherein the Fe:Si:Cr:Ge:alkali metal atomic ratio is 100:0.1-20:0.1-5:0.1-10:0.01-5. The catalyst of the invention can achieve alkylation of phenols with high selectivity to the ortho-position and at high yields as compared with conventional catalysts. Moreover, the catalyst of this invention ("present catalyst" hereinafter) makes it possible to carry out the alkylation reaction at a lower temperature as compared with conventional catalysts, whereby it is possible to prevent deposition of a carbonaceous substance on the catalyst and sintering of the catalyst which are causes for deterioration of catalyst activity. Therefore, the catalyst remains active for longer than conventional catalysts, and the frequency of catalyst regeneration and replacement can be reduced. These advantages are industrially significant. The invention also provides a method of alkylating phenols which comprises contacting a phenol having a hydrogen atom in at least one of the ortho-positions with regard to the hydroxyl group with an alcohol in the gaseous phase at an elevated temperature in the presence of the catalyst of the invention. Phenols used as a material in the method of this invention have a hydrogen atom in at least one of the ortho-positions. Preferred examples of such phenols are compounds represented by the following formula (I). wherein R¹, R², R³ and R⁴, which are the same or different, each represents hydrogen, an alkyl group, a cycloalkyl group, an aryl group or an alkylaryl group. In formula (I), as an alkyl group, alkyl groups having 1 to 6 carbon atoms are preferred, and the alkyl groups may be linear or branched. Examples of such alkyl groups are methyl, ethyl, n-propyl, iso-propyl, n-butyl, n-pentyl, and n-hexyl groups. As a cycloalkyl group, preferred examples are cyclopentyl and cyclohexyl groups. As an aryl group, preferred examples are phenyl and naphthyl groups. As an alkylaryl group, preferred examples are phenyl and naphthyl groups which are substituted with an alkyl group having 1 to 6 carbon atoms. Examples of the phenols of formula (I) are phenol, o-cresol, m-cresol, p-cresol, 2,3-xylenol, 2,4-xylenol, 2,5-xylenol, 3,5-xylenol, 3,4-xylenol, 2,3,4-trimethylphenol, 2,3,5-trimethylphenol, 2,4,5-trimethylphenol, 2,3,4,5-tetramethylphenol, o-ethylphenol, m-ethylphenol, p-ethylphenol, 2,3-diethylphenol, 2,4-diethylphenol, 2,5-diethylphenol, 3,5-diethylphenol, 3,4-diethylphenol, 2,3,4-triethylphenol, 2,3,5-triethylphenol, 2,4,5-triethylphenol, o-propylphenol, o-phenylphenol, p-phenylphenol, o-cyclohexylphenol and p-cyclohexylphenol. As an alcohol used as the other material in the method of this invention, saturated aliphatic alcohols having 1 to 4 carbon atoms are preferred. These alcohols may be linear or branched. Examples of such alcohols are methanol, ethanol, n-propanol, isopropanol, n-butanol and iso-butanol. Of these, methanol and ethanol are preferred, and methanol is particularly preferred. The present catalyst contains iron oxide, silica, chromium oxide, germanium oxide and an alkali metal compound in a Fe:Si:Cr:Ge:alkali metal atomic ratio of 100:0.1-20:0.1-5:0.1-10:0.01-5, preferably of 100:0.1-5:0.1-3:0.1-5:0.01-1. The present catalyst can be produced according to various known methods. For example, at first, a mixture of an iron compound, a silicon compound, a chromium compound and a germanium compound is prepared by a) a co-precipitation method, b) a kneading method or c) a combination of a co-precipitation method and a kneading method. When the mixture is calcined, the metal compounds in the mixture become corresponding metal oxides. Then, an alkali metal compound is deposited on the mixture and the resultant solid is calcined. The deposition is carried out by a') an impregnation method, b') a kneading method or c') an evaporation and dry-solidification method. The impregnation method is generally used. The method for preparation of the present catalyst will be further specifically explained below. While an aqueous solution of a mixture of predetermined amounts of iron, silicon and chromium compounds is stirred at a temperature between 10° C and 100° C, an alkali agent is added to the solution to adjust the solution to pH of 6 to 9, whereby a precipitate is obtained. Then, the predetermined amount of a germanium compound is added to the precipitate, and the resultant mixture is further continuously stirred. Then, the resultant precipitate is fully washed with water and filtered to obtain a mixture of the iron compound, the silicon compound, the chromium compound and the germanium compound. This mixture is then dried at 100 to 350 C, and immersed in an aqueous solution of an alkali metal compound, and the mixture is filtered. Thereafter, the resultant solid is dried at 100 to 200 C, and then calcined in a stream of air at 400 to 600° C for 3 to 15 hours. Examples of the iron compound used for the preparation of the present catalyst are ferric nitrate, ferric sulfate, ferric chloride, ferrous nitrate, ferrous sulfate and ferrous chloride. Of these, ferric nitrate is particularly preferred. Examples of the silicon compound are sodium silicate, silica sol (colloidal silica) and organosilicon compounds. Examples of the chromium compound are trivalent chromium salts such as chromium nitrate, chromium sulfate and chromium chloride; chromates; and perchromates. Examples of the germanium compound are germanium tetrachloride, germanium oxide and organogermanium compounds. Examples of the alkali metal compound are nitrates, sulfates, carbonates or hydroxides of lithium, sodium, potassium, rubidium or cesium. Of these, a nitrate, sulfate or carbonate of potassium or lithium is particularly preferred. Presence of halogen such as chloride is undesirable. An alkaline substance is used as a pH regulator in the preparation of the mixture of an iron compound, a silicon compound, a chromium compound and a germanium compound. Examples of such an alkaline substance are ammonia, urea and hydroxides of alkali metals, such as sodium hydroxide. Of these, ammonia is particularly preferred. In this invention, both a phenol and an alcohol are fed to a reaction system as gaseous substances, preferably in a phenol/alcohol molar ratio of 1:1-10. These gases to be fed may contain steam and inert gases such as nitrogen, as a diluent, and steam is particularly preferred, since steam has effects of preventing decomposition of the alcohol, which improves the recovery ratio of the alcohol, and of preventing deposition of a carbonaceous substance on the catalyst. The steam is contained in an amount of 0.5 to 5 mols per mol of the phenol. The reaction temperature is preferably between 300° C and 450° C, more preferably between 300° C and 400° C. The reaction pressure may be ordinary pressure, elevated pressure or reduced pressure. When an elevated pressure is employed, a gage pressure of 0.5-40 kg/cm² is chosen. After the reaction, the reaction product is condensed, or subjected to absorption with an organic solvent and separated by distillation, etc., whereby an intended product is obtained. According to this invention, the above alkylation method of this invention can give a product mainly containing corresponding ortho-alkylated phenols. According to this invention, therefore, there is also provided a method of producing an orthoalkylated phenol. This invention will be explained further in detail by reference to Examples, in which reaction results were defined by the following equations. Phenol reaction ratio = [amount of phenol fed (mol) - amount of phenol unreacted (mol)] / amount of phenol fed (mol) x 100 Yield of component of product = amount of component produced (mol) / amount of phenol fed (mol) x 100 Selectivity to o-position (mol%) = [amount of 2,6-xylenol produced (mol) + amount of o-cresol produced (mol)] / [amount of phenol fed (mol) - amount of phenol unreacted (mol)] x 100 Methanol recovery ratio (%) = [amount of methanol recovered (mol)] / [amount of methanol fed (mol) - (amount of 2,6-xylenol produced x 2 + amount of o-cresol produced)] (mol) x 100 EXAMPLE 1 and COMPARATIVE EXAMPLE 1 12 Kilograms of nonahydrated ferric nitrate and 118.9 g of nonahydrated chromium nitrate were dissolved in 120 liters of purified water, and while the mixture was stirred at room temperature, a dilute solution of 61.3 g of water glass No. 3 (SiO₂ content 30 %) in 3 liters of water was added. Then, while the mixture was stirred continuously, a 10 % aqueous ammonia was slowly added dropwise to the mixture. And, when the mixture solution showed pH of 8.0 and when a precipitate was fully formed, the addition of the aqueous ammonia was stopped. And, a suspension of 7.8 g of germanium dioxide in 0.5 liter of purified water was added, and the resultant mixture solution was further stirred continuously for 1 hour to give a precipitate. The precipitate was washed with water, filtered and dried at 120° C for 20 hours, and then, the precipitate was further dried at 350° C for 5 hours. The resultant product was immersed in 2,024 g of an aqueous solution containing 3.74 g of potassium carbonate for 16 hours, and filtered, dried at 120° C for 3 hours, and calcined in a stream of air at 470° C for 7 hours to obtain a catalyst. The catalyst had a Fe₂O₃:SiO₂:Cr₂O₃:GeO₂:K₂CO₃ composition of 100:2:1:0.5:0.1 (molar ratio). The catalyst was pulverized and formed into 7 to 8-mesh spherical particles, and 60 ml of the particles were packed in a stainless reaction tube. And, a mixture gas containing methanol, phenol and steam (H₂O) in a molar ratio of 5:1:1 was fed, together with 10 mℓ/minute of a nitrogen gas, into the catalyst layer maintained at 330° at a rate of LHSV = 0.6kg/ℓ·hr. Table 1 shows the results. Further, the above reaction was repeated under the same conditions by using a catalyst containing no germanium dioxide. The results are shown as Comparative Example also in Table 1. EXAMPLES 2-6 and COMPARATIVE EXAMPLE 2 The same procedure as that of Example 1 was carried out to prepare various catalysts having 7 to 8-mesh spherical particle form but having a different content of germanium dioxide as shown in Table 2. The same reaction as that described in Example 1 was carried out under the same conditions as those in Example 1 by using the resultant catalysts. Table 2 shows the results obtained after 500 hours' reaction. Further, a catalyst containing no germanium dioxide was prepared in the same way as above, and Table 2 also shows the results of the reaction carried out in the same conditions in the presence of the catalyst containing no germanium dioxide. EXAMPLE 7 and COMPARATIVE EXAMPLE 3 The same procedure as that of Example 1 was carried out to prepare a catalyst having 7 to 8-mesh spherical particle form and having an Fe₂O₃:SiO₂:Cr₂O₃:GeO₂:K₂CO₃ composition of 100:2:1:2:0.1 (molar ratio). A stainless reaction tube was charged with 60 ml of the catalyst, and a mixture gas containing methanol, phenol and H₂O in a molar ratio of 5:1:1 was fed, together with 10 mℓ/minute of a nitrogen gas, to the reaction tube at a rate of LHSV = 0.6 kg/ℓ·hr. While the reaction temperature was adjusted and maintained such that the yield of 2,6-xylenol became about 80 mol%, the reaction was continued. The catalyst was regenerated at intervals of about 2,000 hours during the reaction. The results are shown in Table 3. Further, a catalyst containing no germanium dioxide was prepared in the same way as above. Table 4 shows the results when the same reaction as above was carried out in the presence of the catalyst containing no germanium dioxide (Comparative Example 3). EXAMPLE 8 and COMPARATIVE EXAMPLE 4 The same procedure as that of Example 1 was carried out to prepare a catalyst having 7 to 8-mesh spherical particle form and having an Fe₂O₃:SiO₂:Cr₂O₃:GeO₂:K₂CO₃ composition of 100:2:1:1:0.1 (molar ratio). A stainless reaction tube was charged with 60 ml of the catalyst, and a mixture gas containing methanol, m-cresol and H₂O in a molar ratio of 5:1:1 was fed, together with 10 mℓ/minute of a nitrogen gas, into the catalyst layer maintained at 322°C at a rate of LHSV = 0.6 kg/ℓ.hr. Table 5 shows the results. Further, a catalyst containing no germanium dioxide was prepared in the same way as above, and the same reaction as above was carried out in the presence of the catalyst (Comparative Example 4). Table 6 shows its results.

Claims: A catalyst suitable for use in alkylating a phenol which comprises iron oxide, silica, chromium oxide, germanium oxide and an alkali metal compound wherein the Fe:Si:Cr:Ge:alkali metal atomic ratio is 100:0.1-20:0.1-5:0.1-10:0.01-5. A catalyst according to claim 1 wherein the Fe:Si:Cr:Ge:alkali metal atomic ratio is 100:0.1-5:0.1-3:0.1-5:0.01-1. A catalyst according to claim 1 or 2 wherein the alkali metal compound is a nitrate, sulphate, carbonate or hydroxide of lithium, sodium, potassium, rubidium or caesium. A catalyst according to claim 1, 2 or 3 which includes substantially no halogen. A method of alkylating a phenol which comprises contacting a phenol having a hydrogen atom in at least one of the ortho-positions relative to the hydroxyl group with an alcohol in the gaseous phase at an elevated temperature in the presence of a catalyst as claimed in any one of the preceding claims. A method according to claim 5, wherein the phenol has the following formula (I) wherein R¹, R², R³ and R⁴, which are the same or different, each represents hydrogen, an alkyl group, a cycloalkyl group, an aryl group or an alkylaryl group. A method according to claim 5 or 6, wherein the alcohol is a linear or branched C₁-C₄ saturated aliphatic alcohol. A method according to claim 5, 6 or 7, wherein the elevated temperature is from 300°C to 450°C.

Inventors: ITO MUNEO, ITO, MUNEO
Applicants: MITSUBISHI GAS CHEMICAL CO, MITSUBISHI GAS CHEMICAL COMPANY, INC.
Application year: 1990
Main classification: C07C37
IPC codes: C07C37, C07C39, B01J23, C07B61