PROCESS FOR OXIDIZING 2,6-DIISOPROPYLNAPHTHALENE

Abstract: In this improved process for oxidising 2,6-diisopropylnaphthalene the oxidation is by molecular oxygen in the presence of basic compounds the total consumption of which at the end of the reaction is at least 0.06 gm equivalent (preferred 0.2-1.0 gm equivalent) per starting molecule of 2,6-diisopropylnaphthalene (the end of the reaction is when at least 80 wt.% is oxidised, preferred 99 wt.%). The main oxidised products in the intermediate mixture are the dihydroperoxide, the monohydroxy monohydroperoxide, and the dihydroxide of 2,6-diisopropylnaphthalene. The intermediate mixture is reacted with an acid in the presence of hydrogen peroxide to produce 2,6-dihydroxynaphthalene. The reaction with the acid can be carried out after purification and/or dehydration of the intermediate mixture, acetone, if necessary, being added. 2,6-diacetoxynaphthalene may be obtd. by reacting the 2,6-dihydroxynaphthalene with glacial acetic acid.

Description: This invention relates to a process for oxidizing 2,6-diisopropylnaphthalene, and processes for producing 2,6-dihydroxynaphthalene and 2,6-diacetoxynaphthalene. 2,6-Dihydroxynaphthalene (to be referred to sometimes as 2,6-DHN hereinafter) can be obtained by oxidizing 2,6-diisopropylnaphthalene (to be referred to sometimes as 2,6-DIPN hereinafter) to form 2,6-diisopropylnaphthalene dihydroperoxide (to be referred to sometimes as DHP hereinafter) and acid-cleaving the product in the presence of an oxidation catalyst. 2,6-Diisopropylnaphthalene is useful as a raw material for synthetic resins, synthetic fibers, medicines, agricultural chemicals, dyes, etc. A batchwise process for oxidizing p-diisopropylbenzene, different from 2,6-diisopropylnaphthalene, has previously been known which comprises oxidizing p-diisopropylbenzene with molecular oxygen at a temperature of 80 to 120 o C until the concentration of hydroperoxide calculated as p-diisopropylbenzene monohydroperoxide in the oxidation reaction product becomes at least 115% by weight while optionally feeding an aqueous alkaline solution having a pH higher than 10 so as to maintain the pH of the oil layer in the reaction system at 9 to 11 during the reaction and while on the other hand, optionally removing the aqueous layer from the reaction system so as to maintain the amount of water in the reaction system at 5 to 60% by weight (see JP-B-44066/1980 and JP-A-72144/1973). In the aforesaid oxidation of p-diisopropylbenzene, the amount of water in the aqueous layer of the reaction system is adjusted to 5 to 60% by weight while the pH of the oil layer is maintained at 9 to 11 during the reaction. JP-A-34,138/1976 discloses a process which comprises bringing beta-isopropylnaphthalene into intimate contact with molecular oxygen in an aqueous alkaline medium with stirring at about 75 to 100 o C in the presence of 25 to 1,000 ppm, based on beta-isopropylnaphthalene, of a specific nickel (II), rhodium (I) or Ir compound (catalyst); separating the reaction mixture into an aqueous layer and an oily layer; and recovering beta-isopropylnaphthalene hydroperoxide from the oily layer. Likewise, GB-A-654,035 discloses a process for producing beta-isopropylnaphthalene hydroxide, which comprises reacting beta-isopropylnaphthalene with molecular oxygen in the liquid phase at an elevated temperature in the substantial absence of a heavy metal oxidation catalyst. The processes described in the above-cited JP-A-34,138/1976 and GB-A-654,035 are for the oxidation of monoisopropylnaphthalene and not for the oxidation of diisopropylnaphthalene. U.S.-A-4,503,262 discloses a process for converting 2,6-diisopropylnaphthalene to 2,6-diisopropylnaphthalene hydroperoxide, which comprises dissolving the 2,6-diisopropylnaphthalene in a C₅₋₁₄ aliphatic hydrocarbon and bringing the solution into contact with an oxygen-containing gas in a basic medium at an elevated temperature in the range of about 50 o C to about 100 o C under atmospheric pressure in the presence of a catalyst selected from the group consisting of oxides, hydroxides and organic acid salts of heavy metals, and mixtures thereof. US-A-4,503,262 discloses that the process described there has the advantage of increasing the rate of the reaction and improving the yield and purity of hydroperoxide. DE-B-2646032 discloses a process for the production of aromatic hydroxy-compounds and aliphatic ketones by cleavage of a secondary alkyl-aromatic hydroperoxide in the presence of an acid catalyst characterised in that the reaction is carried out in the presence of a phenol or amine anti-oxidant. Houben-Weyl, Methoden der Organische Chemie, E13 pages 144-159, published by Georg Thieme Verlag, Stuttgart, 1988, discloses the oxidation of hydroxy compounds to hydroperoxy compounds by hydrogen peroxide and Houben-Weyl, Methoden der Organische Chemie. VI/Ic, volume 1, pages 117-127, published by Georg Thieme Verlag, Stuttgart, 1976 discloses the acid cleavage of aromatic-α-hydroperoxides to produce phenols. US-A-3933921 discloses a process for the production of hydroperoxides by oxidation of an aromatic hydrocarbon having at least one tertiary carbon atom, selected from cumene, cymene, butylbenzene, diisopropyltoluene, diisopropylbenzene isopropylnaphthalenes and diisopropylnaphthalenes. An emulsion phase is formed by powerfully mixing at least a part of the aromatic hydrocarbon and an aqueous alkaline solution and the oxidation is carried out with oxygen or an oxygen-containing gas at a pH from 5-12 and a temperature from 80-150°C. The present invention provides a process for producing 2,6-dihydroxynaphthalene, which comprises (1) oxidising 2,6-diisopropylnaphthalene with molecular oxygen in the presence of an aqueous solution comprising a base to form a mixture containing 2,6-diisopropylnaphthalene dihydroperoxide, 2,6-diisopropylnaphthalene, monohydroxymonohydroperoxide and 2,6-diisopropylnaphthalene dihydroxide, said oxidation reaction being performed by using from 0.2 to 1.0 gram-equivalent, per mole of 2,6-diisopropylnaphthalene as the starting material, of a basic compound until the reaction is stopped, while maintaining a pH in the aqueous phase of 11 to 14, and (2) subjecting said mixture to acid cleavage in the presence of hydrogen peroxide. This oxidation process of the invention gives a product resulting from oxidation of at least one of the isopropyl groups of 2,6-diisopropylnaphthalene to a 2-hydroxyprop-2-yl or 2-perhydroxyprop-2-yl group as a main oxidation product. It is not the purpose of this invention to perform the above oxidation until the main oxidation product is a product resulting from oxidation of the isopropyl groups of 2,6-diisopropylnaphthalene to a higher oxidation state to form formyl or carboxyl groups. In particular, the dihydroxyperoxide, monohydroxymonohydroperoxide and dihydroxide of 2,6-diisopropylnaphthalene occupy a greater portion of the oxidation product, for example at least 50 mole% based on the oxidised 2,6-diisopropylnaphthalene. In oxidising 2,6-diisopropylnaphthalene with molecular oxygen in the presence of a base in the oxidation process of this invention, the oxidation reaction is carried out by using from 2.0 to 1.0 gram-equivalent, per mole of 2,6-diisopropylnaphthalene used as the starting material, of a basic compound (namely, by adding from 0.2 to 1.0 gram-equivalent, per mole of 2,6-diisopropylnaphthalene as the starting material, of a basic compound to the reaction system) until the reaction is stopped. This amount is understood as the amount of the basic compound used (charged) based on the amount charged of 2,6-diisopropylnaphthalene on an average per unit time. The basic compound to be present in the reaction system may be added at a time to the reaction system before the start of the reaction, or may be added in some portions to the reaction system. Preferably, one portion of the basic compound is added to the reaction system before the start of the reaction, and the remaining portions, to the reaction system during the reaction. Examples of suitable basic compounds include alkali metal compounds such as sodium hydroxide, potassium hydroxide, sodium hydrogen carbonate, potassium hydrogen carbonate, sodium carbonate and potassium carbonate, and alkaline earth metal compounds such as calcium hydroxide, magnesium hydroxide and strontium hydroxide. These basic compounds may be used singly or in combination. The alkali metal compounds are preferred, and potassium hydroxide and sodium hydroxide are especially preferred. Preferably the pH of the aqueous phase in the oxidation reaction system is from 12 to 14. Preferably the basic compound is added as an aqueous solution to the reaction system, having a concentration of 1 to 25% by weight. According to the oxidation process of this invention using the aforesaid specific proportion of the basic compound, 2,6-diisopropylnaphthalene is oxidized in a high conversion, for example, in a conversion of at least 80%, preferably at least 95%, more preferably at least 99%. In this invention, the reaction product composed mainly of the dihydroperoxide, monohydroxymonohydroperoxide and dihydroxide can be obtained as an oxidation product. Furthermore, according to the oxidation process of this invention, the rate of the reaction is high so that even when the reaction temperature is lowered, a permissible reaction rate can be achieved. The oxidation process of this invention is usually carried out by mixing an aqueous phase containing the basic compound and an organic phase containing 2,6-diisopropylnaphthalene with mechanical stirring to create an emulsified condition, and blowing molecular oxygen into this condition. The emulsified condition may be formed by mechanically mixing the aqueous phase and the organic phase with stirring. The co-presence of a known emulsifier such as sodium stearate at this time facilitates emulsification. Intense stirring is preferred. The organic phase may be composed of 2,6-diisopropylnaphthalene itself. Alternatively, when the reaction is performed in the presence of an organic solvent in the reaction system, it may be composed of 2,6-diisopropylnaphthalene and the organic solvent. The organic solvent may, preferably, include aromatic hydrocarbons substituted by secondary alkyl, benzene, halogenated aromatic hydrocarbons, halogenated aliphatic hydrocarbons, aliphatic saturated hydrocarbons, alicyclic hydrocarbons, nitro compounds, nitriles, sulfoxides (and so on). Preferably, the aromatic hydrocarbons substituted by secondary alkyl are, for example, those of the following formula (I) wherein R¹ and R² represent a lower alkyl group, R³ represents hydrogen, a lower alkyl group, a lower alkyl-substituted phenyl group or halogen, X and Y are both hydrogen atoms, or may be bonded to each other to form a sub stituted or unsubstituted tetralin or naphthalene ring together with the benzene ring to which they are bonded, and m represents an integer of 1, 2 or 3, with the proviso that m groups may be identical or different. Specific examples of these compounds are alkylbenzenes such as cumene, diisopropylbenzene, triisopropylbenzene, methylisopropylbenzene (cymene), fluoroisopropylbenzene, chloroisopropylbenzene, bromoisopropylbenzene, sec-butylbenzene, sec-amylbenzene and sec-hexylbenzene; biphenyls such as diisopropylbiphenyl; tetralins such as isopropyltetraline; and alkylnaphthalenes such as beta-isopropylnaphpthalene. Of these, isopropylbenzenes such as cumene, diisopropylbenzene, triisopropylbenzene and halogenated isopropylbenzene are preferably used. Examples of the halogenated aromatic hydrocarbons are chlorobenzene, dichlorobenzene, bromobenzene, dibromobenzene, fluorobenzene and difluorobenzene. Examples of the halogenated aliphatic hydrocarbons are chloroform, carbon tetrachloride, dichloroethane, trichloroethane and H(CF₂) n Cl (where n is 5 to 10). Examples of the aliphatic saturated hydrocarbons are hexane, heptane, octane, nonane, decane, undecane and dodecane. Examples of the alicyclic hydrocarbons are cyclohexane, cycloheptane, chlorocyclohexane and dichlorocyclohexane. Examples of the nitro compounds are nitrobenzene and nitromethane. Examples of the nitriles are benzonitrile and acetonitrile. Examples of the sulfoxides are dimethyl sulfoxide, dimethylsulfone and tetramethylenesulfone (sulfolane). The use of halogenated aromatic hydrocarbons such as chlorobenzene and dichlorobenzene is preferred because such solvents are easily available and permit easy after-treatment operation after the reaction. The amount of the organic solvent is preferably 20 to 1000 parts by weight, more preferably 50 to 300 parts by weight, per 100 parts by weight of 2,6-diisopropylnaphthalene. Usually, the basic aqueous phase in the reaction mixture preferably occupies 5 to 80% by weight, especially 20 to 70% by weight, of the reaction mixture. The 2,6-diisopropylnaphthalene used as a reaction material is preferably of high purity, and 2,6-diisopropylnaphthalene having a purity of at least 85% can be used as a starting material in the oxidation process of this invention. Molecular oxygen may be an oxygen gas alone, but a mixture of oxygen and an inert gas, for example air, usually suffices. The amount of molecular oxygen required is usually 5 to 15 Nl/hour, calculated as oxygen gas, per 100g of 2,6-diisopropylnaphthalene charged for the oxidation reaction, but is not particularly limited. The oxidation reaction temperature is usually 70 to 150 o C, preferably 80 to 110 o C. The reaction time varies depending upon the reaction temperature and other conditions, but is usually 6 to 100 hours, preferably 7 to 50 hours. By the oxidation reaction under these conditions, a 2,6-diisopropylnaphthalene conversion of at least 80% can be obtained. The reaction is usually carried out under atmospheric pressure, but as required, may be carried out under atmospheric pressure to an elevated pressure of 50 kg/cm², or under reduced pressure. The reaction mixture obtained by performing the oxidation process of this invention as above contains such oxidation products as the dihydroperoxide, monohydroxymonohydroperoxide and dihyroxide of 2,6-diisopropylnaphthalene. The composition of the oxidation reaction mixture can be determined, for example, by separating it into an organic phase and an aqueous phase, extracting the aqueous phase with ether, combining the extract with the organic phase, and subjecting the resulting mixture to liquid chromatography. Investigations of the present inventors have shown that the dihydroperoxide, monohydroxymonohydroperoxide and dihydroxide contained in the reaction mixture obtained by performing the oxidation process of this invention as above can be converted in one step to 2,6-dihydroxynaphthalene by subjecting them to acid cleavage in the presence of hydrogen peroxide. The acid cleavage may be carried out on the oxidation product obtained by oxidizing these compounds with hydrogen peroxide, but preferably, it is carried out in the presence of hydrogen proxide. In either case, hydrogen peroxide converts the monohydroxide or dihydroxide of 2,6-diisopropylnaphthalene contained in the oxidation reaction product to 2,6-diisopropylnaphthalene dihydroperoxide. In order to subject the reaction mixture of oxidation to acid cleavage, the reaction mixture is then subjected to an after-treatment comprising optionally removing the reaction solvent, adding a water-insoluble or sparingly water-soluble organic solvent to form an organic phase and an aqueous phase, separating the organic phase, and subjecting the separated organic phase to acid cleavage. The removal of the reaction solvent optionally carried out before adding the water-insoluble or sparingly water-soluble organic solvent is for the purpose of removing part or the whole of the organic solvent when the oxidation reaction mixture is obtained by performing the oxidation reaction in the presence of the organic solvent. Ketones or hydrocarbons, for example, are used as the water-insoluble or sparingly water-soluble organic solvents. The ketones are especially preferred. Water-insoluble dialkylketones having 5 to 11 carbon atoms are preferably used as the water-insoluble or sparingly water-soluble ketones. Examples of the ketones are methyl isopropyl ketone, methyl isobutyl ketone (MIBK), diisobutyl ketone, diisopropyl ketone, ethyl isobutyl ketone, propyl butyl ketone and amyl butyl ketone. Of these, methyl isobutyl ketone is especially preferred in this invention. The reason for using the water-insoluble or sparingly water-soluble organic solvent is as follows: In particular, when the conversion of 2,6-diisopropylnaphthalene does not reach at least 80%, the proportion of an oxidation product which is liquid at the high temperature used in the oxidation reaction but solidifies when cooled to room temperature, for example 2,6-diisopropylnaphthalene dihydroperoxide, increases in the oxidation reaction mixture and there is created a condition in which the solidified oxidation product takes in it the aqueous phase containing the basic compound. The water-insoluble or sparingly water-soluble organic solvent is used to separate the aqueous phase efficiently from this condition and form an organic phase containing the oxidation product. The water-insoluble or sparingly water-soluble organic solvent is excellent in that it forms an organic phase which contains a small amount of the basic compound and from which water can be easily removed by distillation. If the organic phase contains a large amount of the basic compound or water, acid cleavage of the organic phase gives the desired 2,6-dihydroxynaphthalene in a markedly decreased yield. Preferably, the water-insoluble or sparingly water-soluble organic solvent, especially a ketone, is added in an amount of 0.2 to 10 parts by weight, especially 0.3 to 5 parts by weight, per part by weight of the oxidation reaction mixture to which it is to be added. The organic solvent is brought into sufficient contact with the oxidation reaction mixture, and then the mixture is maintained at a temperature of usually 30 to 90 o C whereby an organic phase and an aqueous phase are formed. Then, the organic phase is separated from the aqueous phase and recovered. The aqueous phase containing the basic compound used at the time of the oxidation reaction is usually discarded. The organic phase is washed with water if required. According to this invention in which the water-insoluble or sparingly water-soluble organic solvent is used, an organic base having a very low basic compound content can be obtained as stated above. For example, in a preferred embodiment in which methyl isobutyl ketone is used, it is even possible to separate and recover an organic phase containing not more than 20 ppm of the basic compound. According to the present invention, the organic phase containing the water-insoluble or sparingly water-soluble organic solvent is then subjected to acid cleavage. The organic phase separated in the previous step may directly be subjected to acid cleavage. Preferably, the separated organic phase is subjected to distillation to remove water as much as possible by azeotropic distillation, and then subjected to acid cleavage. By removing a maximum of water, the yield of 2,6-dihydroxynaphthalene as the final desired product of acid cleavage can be increased. Furthermore, when water is removed from the organic phase by azeotropic distillation, acetone is added to the organic phase, and the mixture is subjected to acid cleavage, the yield of 2,6-dihydroxynaphthalene is further increased although no entirely clear reason can be assigned to it. The azeotropic distillation can be advantageously carried out usually under a reduce pressure of 50 to 200 mHg and at a temperature of 50 to 90 o C. Desirably, dehydration is carried out by azeotropic distillation to a water content of not more than 3% by weight, particularly not more than 1% by weight. Usually, acetone is added in an amount of 5 to 1200 parts by weight per 100 parts by weight of the residue from the azeotropic distillation. A source of hydrogen peroxide used in the acid cleavage may be hydrogen peroxide, an aqueous solution of hydrogen peroxide, or a substance which generates hydrogen peroxide under the reaction condition, for example sodium peroxide or calcium peroxide. The aqueous solution of hydrogen peroxide is preferred. Hydrogen peroxide is believed to perform the action of converting the hydroxyl groups of the monohydroxymonohydroperoxide and dihydroxide of 2,6-diisopropylnaphthalene into hydroperoxy groups and converting the monohydroxymonoperoxide and dihydroxide to dihydroperoxide. The dihydroperoxide undergos acid cleavage to form 2,6-dihydroxynaphthalene. The source of hydrogen peroxide may be used in an amount of preferably 0.9 to 2 moles, more preferably 1.0 to 1.5 moles, per mole of the hydroxyl groups of carbinols such as the monohydroxymonoperoxide, dihydroxide and monohydroxide of 2,6-dihydroxynaphthalene. By using hydrogen peroxide in such a proportion, the formation of by-products based on the condensation of these carbinols can be markedly inhibited. As an acid catalyst in the acid cleavage reaction, there are preferably used inorganic acids such as sulfuric acid, hydrochloric acid and phosphoric acid, strongly acidic ion exchange resins, solid acids such as silica gel and silica-alumina, organic acids such as chloroacetic acid, methanesulfonic acid, benzenesulfonic acid and toluenesulfonic acid, and heteropolyacids such as phosphotungstic acid and phosphomolybdic acid. The acid catalyst may be directly added to the reaction system. When it has solubility, it may be dissolved in a suitable inert solvent and then added to the reaction system. The amount of the acid catalyst, although varying depending upon its type and the reaction conditions, is usually 0.005 to 10% by weight, preferably 0.01 to 10%, based on the entire reaction mixture. The acid cleavage reaction is carried out preferably at 0 to 100 o C, more preferably 20 to 80 o C. After the reaction, 2,6-dihydroxynaphthalene is separated from the reaction mixture by the following methods. A first method comprises adding an aqueous solution of an alkaline compound, such as an aqueous solution of sodium carbonate or sodium hydrogen carbonate, to the reaction mixture to neutralize the acid catalyst contained in it, evaporating part of the organic solvent contained in the reaction mixture to form an aqueous phase and a first organic phase, separating the first organic phase, further evaporating the organic solvent from the first organic phase to concentrate it, adding a hot aromatic hydrocarbon to the concentrate to extract by-products, and precipitating 2,6-dihydroxynaphthalene as crude crystals. Another method (second method) is the same as the first method up to the step of evaporating the organic solvent from the first organic layer to concentrate it. Thereafter, it comprises adding water to the concentrate to form a slurry containing 2,6-dihydroxynaphthalene as solids, adding an aromatic hydrocarbon to the slurry, heating the slurry to dissolve the solids, and cooling the separated and recovered aqueous phase to precipitate crude crystals of 2,6-dihydroxynaphthalene. By concentrating the acid cleavage reaction mixture and mixing the concentrate with an aromatic hydrocarbon in the presence or absence of water, the by-products of the reaction are extracted with the aromatic hydrocarbon and removed. As a result, 2,6-dihydroxynaphthalene can be obtained as crude crystals from which most of 6-isopropyl-2-naphthol as a main by-product has been removed. As the aromatic hydrocarbon for this purpose, benzene, toluene, xylene, trimethylbenzenes, cumene, cymene, diisopropylbenzene, etc. are preferably used. The crude crystals of 2,6-dihydroxynaphthalene may be purified, for example, by dissolving the 2,6-diisopropylnaphthalene crude crystals under heat in a solvent suitable for its purification by recrystallization to form a solution, and cooling the solution to recrystallize the crude crystals to remove tiny amounts of colored substances. As a result, nearly pure 2,6-dihydroxynaphthalene can be obtained. Examples of the recrystalization solvent are water, lower alcohols such as methanol, ethanol and propanol, aliphatic ketones such as acetone, methyl ethyl ketone and MIBK, linear or cyclic ethers such as diethyl ether, dioxane and tetrahydrofuran, acetonitrile and nitromethane. They may be used singly or in combination. Of these, water or a mixture of water and acetone having an acetone content of 0 to 90% by weight, particularly a mixture of 5 to 50% of aetone and water, is preferred. The recrystallization solvent is used in a proportion of 0.2 to 50 parts by weight per part by weight of the 2,6-dihydroxynaphthalene crude crystals. The resulting crystals are separated from the liquid and dried to give a pure product. According to this invention, the 2,6-dihydroxynaphthalene formed by the acid cleavage reaction may be converted into a diacetyl compound from the reaction mixture obtained after the acid cleavage reaction and can be recovered as the diacetoxy compound. Desirably, the conversion to the diacetoxy compound is effected by a method corresponding to the first method of separating 2,6-dihydroxynaphthalene as described above in which, however, acetic anhydride is added together when adding the aromatic hydrocarbon; a method corresponding to the first and second methods in which, however, after the crude DHN is taken out, the crude DHN is added to an aromatic hydrocarbon and acetic anhydride is added in the presence of a ketone such as acetone or MIBK, acetic acid, etc.; a method in which acetic anhydride is added to the acid cleavage reaction product itself; or a method in which water is removed from the acid cleavage reaction product (which may, or may not, be neutralized), and then acetic anhydride is added. Acetic anhydride is used in a proportion of at least 1 mole, preferably 1 to 10 moles, per mole of the hydroxyl groups of 2,6-dihydroxynaphthalene to be acetylated. The acetylation reaction may be carried out in the absence of catalyst, but usually it is carried out in the presence of an acid catalyst or a basic catalyst. Sulfuric acid and boron fluoride, for example, are preferably used as the acid catalyst. Examples of the basic catalyst are pyridine and sodium acetate. Acetyl chloride may be used in the above methods as an acetylation agent besides acetic anhydride. The acetylation reaction is carried out usually at a temperature of 0 to 200 o C. After the reaction, the reaction mixture is filtered or cooled to crystallize 2,6-diacetoxynaphthalene. It is recovered as crystals by filtration. The following examples illustrate the present invention in detail. The following abbreviations are used in these examples. 2,6-DIPN: 2,6-diisopropylnaphthalene DHP: dihydroperoxide of 2,6-diisopropylnaphthalene HHP: monohydroxymonohydroperoxide of 2,6-diisopropylnaphthalene DCA: dihydroxide of 2,6-diisopropylnaphthalene MCA: monohydroxide of 2,6-diisopropylnaphthalene MHP: monohydroperoxide of 2,6-diisopropylnaphthalene 2,6-DHN: 2,6-dihydroxynaphthalene 2,6-DAN: 2,6-dihydroxynaphthalene diacetate EXAMPLE 1 A 500 ml autoclave (made from SUS318L) equipped with a rotating stirrer (curved inclined paddle-type stirring vanes, vane size 55 mm in diameter), a gas blowing tube, a thermometer sheath and a reflux condenser was charged with 50g of 2,6-diisopropylnaphthalene, 100g of a 4.5% by weight aqueous solution of sodium hydroxide and 0.1g of alpha,alpha'-azobis(cyclohexane-1-carbonitrile). While passing air at a rate of 20 liters/hr, the reaction was carried out for 9 hours under reaction conditions involving a temperature of 100 o C, a pressure of 5 kg/cm²-G and a stirrer rotating speed of 1300 rpm (peripheral speed 374 cm/sec.). After the reaction, the autoclave was opened, and the reaction mixture was taken out. Methyl isobutyl ketone (MIBK) was added to the reaction mixture to dissolve the solids, and the solution was separated into an organic phase and an aqueous phase by using a separating funnel. The aqueous phase was adjusted to pH 3 with dilute hydrochloric acid, and then extracted with diethyl ether. The organic phase and the diethyl ether extract were analyzed for composition. The results of the reaction were as follows:- Conversion of 2,6-diisopropylnaphthalene: 99.5 mole% Yield of DHP: 15.4 mole % Yield of HHP: 34.0 mole % Yield of DCA: 17.1 mole % Yield of MHP: 7.3 mole % Yield of MCA: 4.7 mole % EXAMPLES 2-3 Example 1 was repeated except that the concentration of NaOH in the aqueous sodium hydroxide solution was changed as shown in Table 1. The results are shown in Table 1. EXAMPLES 4-5 Example 1 was repeated except that an aqueous solution of each of the bases indicated in Table 2 was used instead of the 4.5% aqueous solution of sodium hydroxide. The results are shown in Table 2. EXAMPLE 6 (1) A 5-liter autoclave equipped with a rotating stirrer, a gas blowing tube, an alkali supply tube, a thermometer sheath and a reflux condenser was charged with 1100 g of 2,6-DIPN, 550g of a 4.5% by weight aqueous solution of NaOH, 650g of H₂O and 5.5g of 2,6-diisopropylnaphthalene hydroperoxide (which had been formed in advance by oxidizng 2,6-DIPN and reserved as an initiator). While passing air at a rate of 195 Nl/hr, the reaction was carried out at a reaction temperature of 100 o C, under a reaction pressure of 6 kg/cm²-G, at a stirring speed of 1000 rpm. With the start of the reaction, a 10% by weight aqueous solution of NaOH was fed, and the reaction was stopped 26 hours later. The amount of the 10% by weight aqueous NaOH solution fed during this time was 1422 cc (NaOH/2,6-DIPN=0.87 equivalent/mole). After the reaction, the autoclave was opened, and the reaction mixture was taken out. To the oxidation reaction mixture, 2200g of MIBK was added, and the mixture was separated into an oil phase (MIBK phase) and an aqueous phase. As a result of analysis by liquid chromatography, the composition of the oxidation reaction product contained in the oil phase was as follows:- (2) A 2-liter glass reactor equipped with a rotating stirrer, a reflux condenser, an acid cleavage material feed tube and an acid catalyst solution feed tube was charged with 84.9g of an acetone solution containing 1.7% by weight of H₂SO₄, and placed over a hot water bath at 65 o C. When acetone began refluxing by heating, a mixture of 708g of the MIBK solution of the oxidation product obtained in (1) above, 67g of a 60% aqueous solution of hydrogen peroxide and 219g of acetone began to be fed into the reactor through the acid cleavage material feed tube. Simultaneously with the starting of feeding the acid cleavage material, 129g of the acetone solution containing 1.7% H₂SO₄ also began to be fed from the acid catalyst solution feed tube, and the feeding was finished in 1 hour. The amounts of the cleavage material and the acetone solution of H₂SO₄ were measured by small-sized metering pumps. Thereafter, the reaction was carried out for 3 hours. The above acid cleavage reaction was carried out twice, and the resulting reaction mixtures were combined. Liquid chromatographic analysis showed that the acid cleavage product had the following composition. (3) Then, 2000 g of the acid cleavage reaction mixture was taken, and to neutralize H₂SO₄ contained in it, a 2% aqueous solution of sodium carbonate was gradually added until the pH of the solution reached about 4. Then, to remove acetone and MIBK contained in the acid cleavage reaction mixture, the following concentrating operation was carried out. Acetone was first evaporated under atmospheric pressure by means of a rotary evaporator to obtain an aqueous phase and an oil phase. The oil layer was separated from the aqueous layer and again subjected to a rotary evaporator under a reduced pressure of 20 to 30 mmHg to evaporate MIBK and obtain a concentrate. This concentrate contained 45.7% by weight of 2,6-dihydroxynaphthalene and 8.0% by weight of 6-isopropyl-2-naphthol. A 2-liter separable flask equipped with a rotating stirrer, a thermometer and a reflux condenser was charged with 400g of the above concentrate and 1200g of cumene, and placed over a hot water bath at 70 o C. The contents of the flask were stirred at the same temperature for 15 minutes. Then, the temperature of the hot water bath was gradually lowered to precipitate crystals further. Finally, it was cooled to room temperature to precipitate the crystals fully. Thereafter, the crystals were separated by filtration, and dried to give 236g of crude crystals of 2,6-dihydroxynaphthalene (the ratio of 2,6-dihydroxynaphthalene crystals recovered 96.8%). The resulting crude crystals contained 75.0% by weight of 2,6-dihydroxynaphthalene and 0.9% by weight of 6-isopropyl-2-naphthol. Twenty-five grams of the dried crude crystals were added to 100g of an acetone/water (20/80) mixed solvent and heated to 60 o C to dissolve them. The crystals were separated by filtration, and dried under reduced pressure. The purity of the 2,6-dihydroxynaphthalene crystals, determined by gas chromatographic analysis, was 99.0%, and the 2,6-dihydroxynaphthalene crystals had a melting point of 220.5 to 222.5 o C. EXAMPLE 7 (1) A 500 ml autoclave (made from SUS 316L) equipped with a rotating stirrer, a gas blowing tube, a thermometer and a reflux condenser was charged with 50g of 2,6-diisopropylnaphthalene, 100g of a 4.5% aqueous solution of sodium hydroxide and 0.1g of alpha,alpha'-bis(cyclohexane-1-carbonitrile). While air was blown at a rate of 20 liters/hour with intense stirring of the contents, the reaction was carried out at a reaction temperature of 100 o C under a pressure of 5 kg/cm²-G for 9 hours. The conversion of 2,6-diisopropylnaphthalene was 99.3%. Methyl isobutyl ketone (100g) was added to the resulting oxidation reaction product, and the oil phase (methyl isobutyl ketone phase) was separated from the aqueous phase. The above oxidation reaction was then carried out three times in the same way, and the resulting oily layers of the oxidation reaction products were combined. The conversions of 2,6-diisopropylnaphthalene in these reactions were 99.5%, 99.4%, and 99.2%, respectively. The oxidation product contained in the combined oily phase was determined to be as follows by liquid chromatographic analysis. The water content of the oily phase was 3.0% as a result of analysis by the Karl-Fischer's method. The amount of the alkali was 15 ppm. (2) Then, a 300 ml glass reactor equipped with a rotating stirrer, a reflux condenser, an acid cleavage material feed tube and an acid catalyst solution feed tube was charged with 6.6g of an acetone solution containing 1.7% by weight of sulfuric acid. The reactor was placed over a hot water bath kept always at 65 o C. When acetone began refluxing by heating, a mixture of 55g of the MIBK solution of the oxidation product (oil phase), 4.0g of a 60% aqueous solution of hydrogen peroxide and 17g of acetone began to be fed from the acid cleavage material feed tube. Simultaneously with the starting of feeding the acid cleavage material, 10g of an acetone solution containing 1.7% of sulfuric acid began to be fed from the acid catalyst solution feed tube, and the feeding was finished in 1 hour. The amounts of the cleavage material and the acetone solution of sulfuric acid fed were determined by small-size metering pumps. Thereafter, the reaction was carried out for 3 hours. After the reaction, the acid cleavage reaction product was analyzed by liquid chromatography and gas chromatography, and found to contain 9.6% by weight of 2,6-dihydroxynaphthalene. Accordingly, the result of the re-oxidation and acid cleavage using hydrogen peroxide was that the yield of 2,6-dihydroxynaphthalene is 99.5 mole% based on DHP, HHP and DCA contained in the acid cleavage material. The overall yield of 2,6-dihydroxynaphthalene based on the 2,6-diisopropylnaphthalene charged was 62 mole%. EXAMPLE 8 In Example 7, the reoxidation and acid cleavage reaction of the acid cleavage material using hydgen peroxide were carried out in the same way as in Example 8, (2) except that a portion of the MIBK solution (oily phase) of the oxidation reaction product obtained in Example 8, and 2.7g [0.8 mole per mole of (HHP+DCAx2+MCA)] of a 60% aqueous solution of hydrogen peroxide were used. After the reaction, the acid cleavage reaction mixture contained 7.8% by weight of 2,6-dihydroxynaphthalene. Analysis of the reaction mixture by liquid chromatography and gas chromatography showed that the reaction mixture contained by-products resulting from condensation of the carbinols in addition to the unreacted HHP, DCA and MCA. The result of this reaction was that the yield of 2,6-dihydroxynaphthalene was 80 mole%. The same reaction was carried out using varying amounts of hydrogen peroxide. The results are shown in Table 3. Table 3 also gives the results obtained in Example 7 above. EXAMPLE 9 A portion of the MIBK solution (oily phase) of the oxidation product obtained in Example 7 was taken, washed twice with water, and used in acid cleavage reaction. The reaction was carried out in the same way as in Example 7, (2) except that phosphotungstic acid was used instead of sulfuric acid as the acid catalyst, and the concentration of phosphotungstic acid in its acetone solution was adjusted to 0.6% by weight. The acid cleavage reaction mixture contained 9.0% by weight of 2,6-dihydroxynaphthalene. The result in the reoxidation and acid cleavage using hydrogen peroxide was that the yield of 2,6-dihydroxynaphthalene is 94 mole% based on DHP, HHP and DCA contained in the cleavage material. COMPARATIVE EXAMPLE 1 (1) The same autoclave as used in Example 7, (1) was charged with 75g of 2,6-diisopropylnaphthalene, 75g of a 1% aqueous solution of sodium hydroxide and 0.1g of alpha,alpha'-bis(cyclohexane-1-carbonitrile) While air was blown at a rate of 20 liters/hour with intense stirring of the contents, the reaction was carried out for 5 hours at a reaction temperature of 100 o C under a pressure of 5 kg/cm²-G. The conversion of 2,6-diisopropylnaphthalene was 72%. The resulting reaction product was reacted in the same way as in Example 7, (1) to give an oily phase containing the oxidation product. The oxidation product in the oily phase had the following composition. (2) Acid cleavage reaction was carried out subsequently under the same reaction conditions as in Example 7, (2) using the same apparatus as used therein. Hydrogen peroxide was used in an amount equal to the theoretically required amount (HHP+DCAx2+MCA). After the acid cleavage reaction, the yield of 2,6-dihydroxynaphthalene (based on DHP, HHP and DCA contained in the acid cleavage material) was 97.5%. The overall yield of 2,6-dihydroxynaphthalene based on the 2,6-diisopropylnaphthalene charged in the oxidation reaction was 16 mole%. EXAMPLE 10 (1) A 500 ml autoclave (SUS 316L) equipped with a rotating stirrer, a gas blowing tube, a thermometer and a reflux condenser was charged with 75 g of 2,6-diisopropylnaphthalene, 75g of a 4.5% aqueous solution of sodium hydroxide and 0.1g of alpha,alpha'-bis(cyclohexane-1-carbonitrile). While air was blown at a rate of 20 liters/hour with intense stirring of the contents, the reaction was carried out for 9 hours at a reaction temperature of 100 o C under a pressure of 5 kg/cm²-G. The conversion of 2,6-diisopropylnaphthalene as 99.5%. Methyl isobutyl ketone (150g) was added to the oxidation reaction product, and the oily layer (methyl isobutyl ketone phase) was separated from the aqueous phase. The oxidation product contained in the oily phase had the following composition as a result of analysis by liquid chromatography. (2) Then, a 300 ml glass reactor equipped with a rotating stirrer, a reflux condenser, an acid cleavage material feed tube and an acid catalyst solution feed tube was charged with 28.3g of an acetone solution containing 1.7% by weight of sulfuric acid. The reactor was placed over a hot water bath kept always at 65 o C. When acetone began refluxing by heating, a mixture of 236g of the MIBK solution (oil phase) of the oxidation product, 17.2g of a 60% aqueous solution of hydrogen peroxide and 73g of acetone began to be fed from the acid cleavage material feed tube. Simultaneously with the starting of feeding the acid cleavage material, 43g of an acetone solution containing 1.7% of sulfuric acid began to be fed from the acid catalyst solution feed tube, and the feeding was finished in 1 hour. The amounts of the cleavage material and the acetone solution of sulfuric acid fed were determined by small-size metering pumps. Thereafter, the reaction was carried out for 3 hours. The above acid cleavage reaction was carried out twice, and the resulting reaction mixtures were combined. As a result of analysis by liquid chromatography, the acid cleavage reaction product had the following composition. (3) Then, 150 g of the acid cleavage reaction mixture was taken, and in order to neutralize sulfuric acid contained in it, a 2% aqueous solution of sodium carbonate was gradually added until the pH of the solution reached about 4. Then, to remove acetone and MIBK contained in the acid cleavage reaction mixture, the following concentrating operation was carried out. First, acetone was evaporated under atmospheric pressure by means of a rotary evaporator to obtain an aqueous phase and an oil phase. The oil phase was separated from the aqueous phase, and again subjected to a rotary evaporator under a reduced pressure of 20 to 30 mmHg to evaporate MIBK and to obtain a concentrate. Evaporation of MIBK was stopped just before the crystals began to precipitate. The concentrate contained 21.6% by weight of 2,6-dihydroxynaphthalene and 4.4% by weight of 6-isopropyl-2-naphthol. A 500 ml separable flask equipped with a stirrer, a thermometer, a reflux condenser and a concentrate dropping opening was charged with 290g of cumene, and placed on a hot water bath at 70 o C. The above concentrate (69g) was gradually added dropwise to the flask to precipitate crystals. After the addition, the temperature of the hot water bath was gradually lowered to precipitate the crystals further. Finally, it was cooled to room temperature to precipitate the crystals fully. The crystals were then separated by filtration and dried to give 23g of crude crystals of 2,6-dihydroxynaphthalene (the ratio of 2,6-dihydroxynaphthalene crystals recovered 80%). The crude crystals contained 50.7% by weight of 2,6-hydroxynaphthalene and 0.7% by weight of 6-isopropyl-2-naphthol. EXAMPLE 11 One hundred grams of the acid cleavage reaction mixture obtained in Example 10, (1) was taken, and as in Example 10, (1), treated with a 2% aqueous solution of sodium carbonate to neutralize sulfuric acid. Then, acetone was evaporated to form an aqueous phase and an oily phase. The oily phase was separated from the aqueous phase. The separated oily phase was charged into a 300 ml separable flask equipped with a stirrer, a thermometer, a distillate withdrawing device and a dropping funnel, and the flask was placed over an oil bath kept at 100 to 110 o C. MIBK was removed as an azeotrope with water. Water was occasionally supplied from the dropping funnel to make up for the water drawn from the reaction mixture with the distillation of the azeotropic mixture. After MIBK was evaporated, the reaction mixture become slurry-like. Water was added to this slurry containing 2,6-dihydroxynaphthalene to adjust the total amount to 130g. The slurry was then transferred to a 300 ml glass autoclave. Fifty grams of cumene was introduced into the autoclave. After the pressure of the inside of the autoclave was elevated to 5 kg/cm²-G with nitrogen, the mixture was heated to 160 o C and stirred. After the solids were completely dissolved, heating and stirring were stopped, and the mixture was allowed to stand. The oily phase was drawn from the mixture. Stirring of the contents was resumed and the contents were allowed to cool. When the contents nearly reached room temperature, they were taken out and filtered to give 11.5g of wet crude crystals of 2,6-dihydroxynaphthalene. The crude crystals contained 1.2%, based on 2,6-dihydroxynaphthalene, of 6-isopropyl-2-naphthol. The crude crystals (11g) were dissolved in 135g of a 20% aqueous solution of acetone, and subjected to active carbon treatment and purification by recrystallization as in Example 10 to give 8.1g of purified 2,6-dihydroxynaphthalene as crystals having a purity of 99.8% and a melting point of 220.9 to 222.0 o C. EXAMPLE 12 Sixty parts by weight of acetone was added to 100 parts by weight of the oily phase containing the oxidation product obtained in Example 7, (1) to prepare an MIBK/acetone mixed oily phase which was subjected to acid cleavage by the following method to obtain 2,6-dihydroxynaphthalene. A 300 ml glass reactor equipped with a rotating stirrer, a reflux condenser, an acid cleavage material feed tube and an acid catalyst solution feed tube was charged with 6.6 g of an acetone solution containing 1.7% by weight of sulfuric acid. The reactor was placed over a hot water bath always maintained at 65 o C. When acetone began to be refluxed by heating, feeding of a mixture of 72g of the MIBK/acetone mixed oily phase of the oxidation product and 4.0g of a 60% aqueous solution of hydrogen peroxide from the acid cleavage material feed tube was started. Simultaneously with the feeding of the acid cleavage material, 10g of an acetone solution containing 1.7% sulfuric acid began to be fed from the acid catalyst solution feed tube, and the feeding was finished in 1 hour. The amounts of the acid cleavage material and the acetone solution of sulfuric acid were determined by small-sized metering pumps. Thereafter, the reaction was further carried out for 3 hours. As a result of analysis by liquid chromatography and gas chromatography after the reaction, the acid cleavage reaction product contained 9.6% by weight of 2,6-dihydroxynaphthalene. Accordingly, the result of the reaction in this case was that the yield of 2,6-dihydroxynaphthalene is 99.5 mole% based on DHP, HHP and DCA contained in the acid cleavage material. The overall yield of 2,6-dihydroxynaphthalene based on the charged 2,6-diisopropylnaphthalene was 62 mole%. EXAMPLE 13 The oily phase composed of an MIBK layer containing the oxidation reaction product obtained by the method of Example 7, (1) was distilled at 100 mmHg and 80 o C finally, and water remaining in the oily layer was removed as an azeotrope with MIBK to adjust the concentration of water in the oily layer to less than 1000 ppm as measured by the Karl-Fischer's method. Thereafter, the oily phase was subjected to acid cleavage in the same way as in Example 12. The results are shown in Table 4. EXAMPLE 14 The acid cleavage reaction product obtained in Example 6 [composition: acetone 45.2% by weight, MIBK 35.2% by weight, 2,5-dihydroxynaphthalene 10.3% by weight, 6-isopropyl-2-naphthol 1.8% by weight, others (the molecular weight is assumed to be the same as 6-isopropyl-2-naphthol) 4.0% by weight, and water 3.5% by weight] was concentrated under reduced pressure to remove acetone and MIBK and obtain a concentrate. Cumene (40g) was added to 40g of the concentrate, and 40g of acetic anhydride was added. With stirring, sulfuric acid was added dropwise to the mixture until its concentration in the mixture reached 500 ppm. The mixture was then heated to 130 o C, and after it began to be refluxed, reacted for 1 hour. The reaction mixture was allowed to cool to 20 o C, and separated into the crystals and the filtrate. From the diacetoxynaphthalene (2,6-DAN) contents of the two, the conversion and the yield of the crystals were determined. It was found that the conversion was 99 mole% (based on 2,6-DHN), the yield of the crystals obtained was 95 mole%, and the purity of the crystals was 99.5%. EXAMPLES 15-17 The concentrate obtained in Example 14 was treated in the same way as in Example 14 except that acetone, methyl isobutyl ketone (MIBK), or acetic acid was used instead of cumene. The results are shown in Table 5. EXAMPLE 18 One hundred grams of the acid cleavage product before neutralization obtained in Example 6 was fed into a 300 ml glass reactor equipped with a rotating stirrer, a reflux condenser and a dropping funnel, and the reactor was placed over a hot water bath at 65 o C. When acetone began to be refluxed by heating, dropwise addition of acetic anhydride was started. After adding 45g of acetic anhydride dropwise over 1 hour, the mixture was reacted at 60 o C for 130 minutes. As a result of analysis by liquid chromatography, the concentration of 2,6-diacetoxynaphthalene (2,6-DAN) was 10.7% by weight. The yield of 2,6-DAN based on DHN was 99.7 mole%. Acetone was evaporated from the reaction mixture, and the residue was cooled to 20 o C and separated into the crystals and the filtrate. It was found that the yield of the crystals obtained was 87 mole%, and their purity was 99.3%. Example 19 The neutralized acid cleavage product (200g) obtained in Example 6 was used, and acetone was evaporated from it, and then it was separated into an oily phase (MIBK solution) having the following composition and an aqueous phase. Some water contained in the oily phase was removed by azeotropic distillation, and the resulting MIBK solution (50g) and 22.5g of acetic anhydride were fed into a 300 ml glass reactor equipped with a rotating stirrer, a reflux condenser and a dropping funnel. With stirring, sulfuric acid was added dropwise to the mixture until its concentration in the mixture reached 500 ppm. The mixture was then heated to 130 o C, and after it began to be refluxed, reacted for one hour. As a result of analysis by liquid chromatography, the concentration of 2,6-DAN was 26.3% by weight, and the yield of 2,6-DNA was 99.7 mole%. The reaction mixture was allowed to cool to 20 o C and separated into the crystals and the filtrate, and the yield and purity of the crystals were determined. It was found that the yield of the crystals obtained was 91 mole%, and their purity was 99.2%. EXAMPLE 20 The MIBK solution obtained in Example 6, (1) was washed twice with water in an amount of 25% by weight. The resulting MIBK solution was dehydrated and concentrated continuously by an evaporator at 80 o C and 50 mmHg. Acetone was added to the concentrate in an amount corresponding to the amount of acetone which distilled out. Thus, an acid cleavage material was prepared. A 2-liter glass reactor equipped with a rotating stirrer, a reflux condenser, an acid cleavage material feed tube and an acid catalyst solution feed tube was charged with 143.1g of an acetone solution containing 0.43% by weight of H₂SO₄, and placed over a hot water bath at 65 o C. When acetone began to be refluxed by heating, feeding of a mixture of 800g of the acid cleavage material, 90.6g of a 60% aqueous solution of hydrogen peroxide and 250g of acetone from the acid cleavage material feed tube was started. Simultaneously with the starting of feeding the acid cleavage material, feeding of 214.7g of an acetone solution containing 0.43% by weight of H₂SO₄ from the acid catalyst feed tube was started, and finished in 1 hour. The amounts of the cleavage material and the acetone solution of sulfuric acid were determined by small-sized metering pumps. Thereafter, the reaction was further carried out for 2 hours. The above acid cleavage reaction was carried out three times, and the resulting reaction mixtures were combined. As a result of analysis by liquid chromatography, the acid cleavage product contained 10.0% by weight of 2,6-dihydroxynaphthalene, 1.7% by weight of 6-isopropyl-2-naphthol, and 1.7% by weight of others (the molecular weight is assumed to be the same as 6-isopropyl-2-naphthol). Four thousand grams of the acid cleavage reaction mixture was taken, and to neutralize sulfuric acid contained in it, a 2% aqueous solution of NaHCO₃ was gradually added until the pH of the solution reached about 4. Thereafter, to remove acetone and MIBK contained in the acid cleavage reaction mixture, the following concentrating operation was performed. Specifically, acetone was first evaporated under atmospheric pressure by means of a rotary evaporator to form an aqueous phase and an oily phase. The oily phase was separated from the aqueous phase. The separated oily phase was washed with 10% by weight, based on the oily phase, of water, and again subjected to a rotary evaporated under a reduced pressure of 20 to 30 mmHg to evaporate MIBK and give a concentrate. Then, a 2-liter separable flask equipped with a rotating stirrer, a thermometer and a reflux condenser was charged with 400g of the above concentrate and 120g of cumene, and placed over a hot water bath at 70 o C The mixture was stirred at the same temperature for 15 minutes, and then the temperature of the water bath was gradually lowered. At 50 o C, the crystals were separated by filtration. The resulting crude crystals contained 45.4% by weight of 2,6-dihydroxynaphthalane (the rate of recovering 2,6-dihydroxynaphthalene 100%). Then, 500g of the resulting crude crystals and 500g of cumene were introduced into a 2-liter separable flask equipped with a rotary stirrer, a thermometer and a reflux condenser. Then, 388.5g of acetic anhydride was added. The reactor was placed on an oil bath at 135 o C, and with stirring, sulfuric acid was added dropwise so that its concentration in the reaction mixture reached 500 ppm. The mixture was then heated to 130 o C, and after it began to be refluxed, reacted for 1 hour. The reaction mixture was analyzed by liquid chromatography, and found to contain 24.9% by weight of 2,6-DAN. The yield of 2,6-DAN based on DHN was 99.9 mole %. The reaction mixture was gradually cooled to 20 o C and separated into the crystals and the filtrate. The resulting crystals were rinsed with acetone. As a result, the yield of the 2,6-DAN crystals obtained was 90 mole %, and their purity was 99.2%.

Claims: A process for producing 2,6-dihydroxynaphthalene, which comprises (1) oxidizing 2,6-diisopropylnaphthalene with molecular oxygen in the presence of an aqueous phase comprising a base to form a mixture containing 2,6 diisopropylnaphthalene dihydroperoxide 2,6-diisopropylnaphthalene monohydroxymonohydroperoxide and 2,6-diisopropylnaphthalene dihydroxide, said oxidation reaction being performed by using from 0.2 to 1.0 gram-equivalent, per mole of 2,6-diisopropylnaphthalene as the starting material of a basic compound until the reaction is stopped, while maintaining a pH in the aqueous phase of 11 to 14, and (2) subjecting said mixture to acid cleavage in the presence of hydrogen peroxide. A process according to claim 1, wherein the base is added in one or more portions to the reaction system; the first portion being added before the start of the reaction and the remaining portions being added during the reaction. A process according to claim 1 or 2 wherein the base is sodium hydroxide or potassium hydroxide. A process according to claim 1, 2, or 3 wherein the oxidation is carried out until at least 99% by weight of 2,6-diisopropylnaphthalene is oxidized. A process according to any one of the preceding claims, which comprises, after the oxidation reaction with base (1) is stopped: (2) adding a water-insoluble or sparingly water-soluble ketone to the resulting oxidation reaction mixture to form an organic phase and an aqueous phase after optionally removing the organic solvent from the reaction mixture, (3) separating the organic phase, and (4) subjecting the separated organic phase to acid cleavage in the presence of hydrogen peroxide after it is optionally subjected to azeotropic distillation to remove part or the whole of water in it and thereafter acetone is optionally added to the organic phase.

Inventors: AGOO, TOKINORI, FUKUHARA, HIROSHI, HANEDA, YUTAKA, MIKI, HISAYA, SAEKI, KENJI, TAGUCHI, TORU, YOSHIMOTO, SADAO
Applicants: MITSUI PETROCHEMICAL INDUSTRIES, LTD.
Application year: 1986
Main classification: C07C409
IPC codes: C07C69, C07C37, C07C407, C07C27, C07C409, C07C39, C07C67