PROCESS FOR THE PRODUCTION OF 2-HYDROXYNAPHTHALENE-6-CARBOXYLIC ACID

Abstract: In a process for producing 2-hydroxynaphthalene-6-­ carboxylic acid by reacting substantially anhydrous potas­ sium beta-naphtholate with carbon dioxide, the improve­ ment wherein the reaction is carried out at a temperature of at least 180°C and a carbon dioxide pressure of at least 1 kg/cm².G using as a starting material potassium beta­ naphtholate or a mixture which contain potassium betanaph­ tholate and is liquid under the reaction conditions.

Description: Title: PROCESS FOR THE PRODUCTION OF 2-HYDROXY N PHTHALENE-6-CARBOXYLIC ACID This invention relates to a process for producing 2-hydroxynaphthalene-6-carboxylic acid by the reaction of potassium beta-naphtholate with carbon dioxide. 2-Hydroxynaphthalene-6-carboxylic acid is an aromatic hydroxycarboxylic acid which has recently attracted attention as a material for polymers in combination with p-hydroxybenzoic acid because a polyester derived from this carboxylic acid and p-hydroxybenzoic acid gives fibers having high tensile strength and heat stability. Little, however, has been described in the literature about the method of synthesizing 2-hydroxynaphthalene-6-carboxylic acid, and to the best of the knowledges of the present inventors, U. S. Patent No. 1,593,816 to Andre et al. is the only pertinent reference. This U. S. Patent specification discloses a process for synthesizing 2-hydroxynaphthalene-6-carboxylic acid by the reaction of solid potassium beta-naphtholate with carbon dioxide. The U. S. Patent states that the reaction is carried out at 170 to 2300C for 8 hours, but is silent on the other reaction conditions, particularly the pressure of carbon dioxide and the proportion of by-product 2-hydroxynaphthalene-3-carboxylic acid. Furthermore, according to the process of the U. S. Patent, the final product is not sufficiently separated from the by-product acid or free beta-naphthol. Upon repeating the process of this U. S. Patent, the present inventors found that the yield of 2-hydroxynaphthalene-6carboxilic acid is as low as less than 1096, and the total yield of it and the by-product 2-hydroxynaphthalene-3 carboxylic acid is less than 30% (see Referential Example given hereinbelow). Hence, this process is unsuitable for commercial production of 2-hydroxynaphthal en e-6-carboxylic acid having such a purity as a material for polymers requires. It is an object of this invention therefore to provide a commercial process for producing 2-hydroxynaphthalene-6-carboxylic acid in quantities. The present inventors investigated a process for reacting substantially anhydrous potassium beta-naphtholate with carbon dioxide using a starting material mixture which is liquid under the reaction conditions employed. This work has led to the discovery that good results can be obtained in regard to the yield, work-up, etc. of 2 hydroxynaphthalene-6-carboxylic acid by reacting anhydrous potassium beta-naphtholate with carbon dioxide at a temperature above the melting point of the potassium betanaphtholate which is about 2350C; performing the reaction of potassium beta-naphtholate with carbon dioxide by using a starting mixture which contains potassium beta-naphtholate and of which melting point has been lowered by incorporating a small amount of free beta-naphthol; and also by performing the reaction in a liquid system containing a reaction medium having a melting point of not more than 1800C because this reaction medium renders a mixture of it with potassium beta-naphtholate liquid under the reaction conditions, dilutes free beta-naphthol present in the reaction system and increases the proportion of 2-hydroxynaphthalene-6carboxylic acid formed. Thus, the present invention provides, in a process for producing 2-hydroxynaphthalene-6-carboxylic acid by reacting substantially anhydrous potassium beta-naphtholate with carbon dioxide, the improvement wherein the reaction is carried out at a temperature of at least 1800C and a carbon dioxide pressure of at least 1 kg/cm2.G using as a starting material potassium beta-naphtholate or a mixture which contains potassium beta-naphtholate and is liquid under the reaction conditions. According to the process of this invention, 2 hydroxynaphthalene-6-carboxylic acid of high purity can be obtained in high yields by a simple and economical means. The yield of the product is about 40% or higher which is more than twice as high as that obtained by the prior process cited above. The liquid reaction mixture obtained after the reaction is easy to work up, and the desired product and by-product 2-hydroxynaphthalene-3-carboxylic acid which is also useful can be obtained in high purity, and the free beta-naphthol can be recovered almost completely. These favorable results are unexpected, and the present invention has, for the first time, established a commercial process for producing 2-hydroxynaphthalene-6 carboxylic acid of high purity which has an increasing demand in industry. Examples of the reaction medium having a melting point of not more than 1800C used in a preferred embodiment of the process of this invention include aliphatic, alicyclic and aromatic hydrocarbons such as gasoline, kerosene, light oil (gas oil), lubricant oils, white oil, alkylbenzenes, alkylnaphthalenes, diphenyl and diphenylalkanes, and aromatic ethers such as diphenyl ether, anisole and ditolyl 0 ether. Those having a boiling point of 150 to 400 C are especially suitable. Petroleum-type hydrocarbons, especially light oil (gas oil) and kerosene, are preferred as the hydrocarbons. Potassium beta-naphtholate used in the reaction can be prepared in a customary manner from beta-naphthol and potassium hydroxide. It should be sufficiently dehydrated for use in the invention. According to the invention, the reaction between potassium beta-naphtholate and carbon dioxide is carried out at a temperature of at least 1800C, preferably 240 to 3500C, especially preferably 240 to 3000C, and a carbon dioxide pressure of at least 1 kg/cm2.G preferably 1 to 15 kg/cm2,G, more preferably at least 5.5 kg/cm2.G, especially preferably 5.5 to 15 kg/cm2.G. The starting mixture containing potassium beta-naphtholate should form a liquid system under the reaction conditions. This can be achieved by the selection of the reaction temperature and the addition of not more than 0.1 mole, per mole of potassium beta-naphtholate, of free beta-naphthol or the aforesaid reaction medium. The reaction medium is used in an amount preferably 0.5 to 10 times, especially preferably 0.5 to 5 times, the weight of potassium betanaphtholate. Larger amounts of the reaction medium may be used, but do not give better results in regard to the yield of the desired product, etc. From the standpoint of economy and work-up procedures, the upper limit of the amount of the reaction medium is preferably 10 times the weight of potassium beta-naphtoolate. The reaction medium acts effectively to dilute free beta-naphthol formed in the liquid reaction system and to increase the proportion of 2-hydroxynaphthalene-6-carboxylic acid formed. If required, the reaction of potassium betanaphtholate with carbon dioxide may be carried out in the presence of not more than 0.1 mole, preferably 0.01 to 0.05 mole, per mole of potassium beta-naphtholate, of free beta-naphthol. For example, potassium beta-naphtholate containing free beta-naphthol, which is obtained by reacting potassium hydroxide in an amount short of theoretical with beta-naphthol, can be reacted with carbon dioxide in accordance with the invention. This procedure makes it possible to prevent the reaction products from depositing dirts or forming a coating on the liquid surface. The addition of free beta-naphthol is especially advantageous when the reaction products are formed in high yields. Since, however, free beta-naphthol tends to decompose 2 hydroxynaphthalene-6-carboxylic acid, better results can usually be obtained by not adding it before reaction with carbon dioxide. In a preferred embodiment of the invention, workup is carried out as follows: Water is added to the reaction mixture after the reaction. The mixture is adjusted to pH 6.5-8 with an acid such as sulfuric acid or hydrochloric acid to free the unreacted potassium beta-naphtholate as beta-naphthol. When a reaction medium layer exists, it is separated before or after formation of free beta-naphthol. If required, a tarry layer containing beta-naphthol and resinous matter is separated in liquid form preferably by sedimentatiQn at 80 to 1000C. The separated tarry layer is preferably washed with water, and the washing is reused as a portion of water to be added. Then, betanaphthol is extracted from the water layer by using a hydrophobic extracting solvent which is preferably liquid 0 at 110 C or lower. Examples of suitable extracting solvents include hydrocarbons such as benzene, toluene, xylene, hexane and cyclohexane; halogenated hydrocarbons such as chlorobenzene, dichloromethane, dichloroethane and chloroform; nitrated hydrocarbons such as nitrobenzene and nitromethane; ethers such as dibutyl ether and diphenyl ether; ketones such as cyclohexanone, diisobutyl ketone and acetophenone; and alcohols having at least 4 carbon atoms such as n-butyl alcohol n-octyl alcohol and 2-ethylhexyl alcohol. Preferably, the extraction is carried out by using the extracting solvent in an amount 0.3 to 2 times, especially 0.5 to 1.5 times, the volume of the water layer at a temperature of 30 to 11OOC, especially 50 to 1000C. beta Naphthol in the reaction medium layer can be recycled directly for reuse. Alternatively, beta-naphthol in the reaction medium layer and the extract may be recovered as an aqueous solution of potassium beta-naphtholate by reacting it with an aqueous solution of potassium hydroxide. The beta-naphthol in the tarry layer is recovered, for example, by vacuum distillation. The aqueous solution ofv potassium beta-naphtholate and the beta-naphthol which are thus recovered are recycled to a step of preparing the starting material and can be re-used. By this extracting procedure, a trace of the reaction medium in the water layer can be removed, and the resinous matter does not substantially get mixed with the extract. To recover the desired products, the pH of the water layer after the extraction is adjusted to 3.5 - 6, preferably 3.5 - 5.5, with an acid. Thus, 2-hydroxynaphthalene-6-carboxylic acid precipitates selectively. Adjustment of the pH of the mother liquor to 1 - 3, preferably 1.5 2.5, results in the precipitation of a mixture of 2 hydroxynaphthalene-3-carboxylic acid and 2-hydroxynaphthalene6-carboxylic acid. Separation of the mixture into the constituent acids can be effected, for example, by recrystallization from an organic solvent or a mixture of it with water. The process of this invention can be performed batchwise or continously. The continuous process is described specifically with reference to the accompanying drawing which is a diagram showing the steps of the process of this invention. A mixture of potassium beta-naphtholate and a reaction medium stored in a storate tank 1 is sent to a reaction tank 2 where the starting mixture is reacted with carbon dioxide at the aforesaid temperature and carbon dioxide pressure. The residence time is preferably 2 to 6 hours. The reaction mixture from the reaction tank 2 is preferably cooled by a heat exchanger 3. Then, it is mixed with water in a water-mixing tank 4 with stirring. The mixture is then separated into a reaction medium layer and a water layer in a separating tank 5. Beta-naphthol can be recovered from the reaction medium layer (upper layer) by using a recovery device (not shown). Then, the water layer (lower layer) from the separating tank 5 is adjusted to pH 6.5 - 8 with an acid in a pH-adjusting tank 6 and sent to a separating tank 7 where the tarry layer is sedimented in liquid form. beta-Naphthol can be recovered. from the tarry layer by using a vacuum distillation device (not shown), etc. The upper layer of the separating tank-7 is sent to an extracting device 8 (preferably a centrifugal extracting device) where it is extracted with a hydrophobic extracting solvent. From the solvent layer, beta-naphthol is recovered by using a recovery device (not shown). The water layer whose pH has been adjusted as above in the pHadjusting tank 6 may be directly sent to the extracting device 8 without going through the separating tank 7. The water layer which has left the extracting device 8 is introduced into an acid precipitation tank 9 where acid precipitation is effected at a pH of 3.5 to 6 by adding an acid. The precipitate is then separated by a centrifugal separator 10. The crystals obtained from the centrifugal separator 10 are substantially pure 2-hydroxynaphthalene6-carboxylic acid. By subjecting the mother liquor to acid precipitation in a separate acid precipitation tank (not show) at a pH of 1 to 3, a mixture of 2-hydroxynaphthalene 3-carboxylic acid and 2-hydroxynaphthalene-6-carboxylic acid is obtained, which can be fractionated by using an alcohol, etc. The work-up step of the reaction mixture is advantageously carried out at a nearly constant temperature 0 preferably in the range of 80 to 100 C, and for this purpose, an ordinary warming or heating device may be used. The aqueous solution of potassium beta-naphtholate and beta-naphthol recovered from the reaction medium layer, the extracting solvent layer and the tarry layer are recycled to the step of preparing the starting material. If required, a part of beta-naphthol is recycled to the storage tank 1. - The reaction medium and the extracting solvent which have been separated are recycled to the storage tank 1 and the extracting device 8 for reuse. According to the process of this invention, the yield of 2-hydroxynaphthalene-6-carboxylic acid based on potassium beta-naphtholate can usually be 40% or more by performing the reaction for 2 to 5 hours. The total yield of the products including 2-hydroxynaphthalene-3carboxylic acid amounts to about 60%. The ratio-between- the two acids can be properly adjusted. By using a relatively high reaction temperature or relatively low carbon dioxide pressure, the proportion of 2-hydroxynaphthalene-6-carboxylic acid can be increased. The total yield of the two acids based on the consumed beta-naphthol exceeds 85%, and the ratio of recovery of beta-naphthol exceeds 85%. The reaction media which can be used in this invention are relatively inexpensive and have good properties. Moreover, free beta-naphthol formed during the reaction needs not to be removed, and can be recovered as above for re-use. The reaction medium and extracting solvent can be recycled for re-use without the need for subjecting them to a heating or cooling step, and this is quite advantageous for thermal economy. There are scarcely any losses of the reaction medium and the extracting solvent by degradation, etc., and the ratio of recovery of these materials is more than 99.5%. The process of this invention is also advantageous from the viewpoint of thermal economy because the separation of the reaction medium layer, the separation of the tarry layer and the extraction of the water layer after the reaction can be carried out at substantially the same temperature. In addition, according to this invention, all process steps for producing 2-hydroxynaphthalene-6-carboxylic acid from beta-naphthol can be practiced continuously. Hence, the present invention provides a process which is very advantageous commercially. The following non-limitative examples illustrate the present invention more specifically. Referential Example According to what should be the best conditions of the process (solid phase process) described in U. S. Patent No. 1,593,816, 182 g of solid potassium beta-naphtholate was reacted with carbon dioxide in a stirred autoclave at a temperature of 2300C and a carbon dioxide pressure of 4 kg/ cm .G for a period of 8 hours. There were only obtained 18.4 g (yield 9.8% based on potassium beta-naphtholate) of 2-hydroxynaphthalene-6-carboxylic acid and 34.2 g (yield 18.2% based on potassium beta-naphtholate) of 2-hydroxynaphthalene-3-carboxylic acid. (The two acids were analyzed by gas-chromatography after esterifying them with diazomethane.) Example 1 A pressure reaction kettle was charged with 364 g of light oil (gas oil having a boiling range of 200 to 3100C) and 182 g of potassium beta-naphtholate. With stirring, potassium beta-naphtholate was reacted with carbon dioxide 0 at a temperature of 260 C and a carbon dioxide pressure of 6 kg/cm2.G for a period of 4 hours. The reaction mixture was added to 830 ml of water, and the mixture was heated at 1000C for 30 minutes to decompose the by-product 2-hydroxynaphthalene-l--carboxylic acid salt. The mixture was separated at 85 0C into a light oil layer and a water layer. The water layer was adjusted to pH 7.0 with.dilute sulfuric acid, and the tarry layer sedimented was separated at the same temperature. The water layer was extracted with 500 ml of toluene at 800C. Then, the water layer was adjusted to pH 4.5 with dilute sulfuric acid and cooled to room temperature, whereupon 71.4 g of 2-hydroxynaphthalene-6-carboxylic acid was obtained as crystals. The mother liquor after separation of the crystals was adjusted to pH 2.0 with dilute sulfuric acid to give 18.8 g of crystals containing 3.8 g of 2hydroxynaphthalene-6-carboxylic acid and 15.0 g of 2 hydroxynaphthalene-3-carboxylic acid (the contents -of the two acids were measured by esterifying them with diazomethane and analyzing the esters by gas-chromatography). The mixture was fractionally recrystallized from dilute methanol to give the respective acids in pure form. The yield of 2-hydroxynaphthalene-6-carboxylic acid based on potassium beta-naphtholate was 40.0% and the total yield of the two acids on the same basis was 48.0%. beta-Naphthol was recovered in a total amount of 65.5 g from the light oil layer, the tarry layer and the toluene layer. The total yield of the two acids based on the consumed beta-naphthol was 88., and the ratio of recovery of beta-naphthol was 87.5%. Example 2 The procedure of Example 1 was followed except that 273 g of l-phenyl-l-(2,3-dimethylphenyl)ethane having a boiling range of 292 to 3060C was used instead of the light oil in Example 1. There were obtained 65.0 g of 2-hydroxy naphthalene-6-carboxylic acid and 16.2 g of 2-hydroxynaphthalene-3-carboxylic acid, and 69.5 g of beta-naphthol was recovered. The yield of 2-hydroxynaphthalene-6-carboxylic acid based on potassium beta-naphtholate was 34.6 %, and the total yield of the two acids on the same basis was 43.2%. The total yield of the two acids based on the consumed beta-naphthol was 83.6%, and the ratio of recovery of beta-naphthol was 85.0%. Example 3 The procedure of Example 1 was followed except that 546 g of kerosene having a boiling range of 180 to 2800C was used instead of the light oil in Example 1. There were obtained 73.2 g of 2-hydroxynaphthalene-6-carboxylic acid and 14.3 g of 2-hydroxynaphthalene-3-carboxylic acid, and 67.0 g of beta-naphthol was recovered. The yield of 2hydroxynaphthalene-6-carboxylic acid based on potassium beta-naphtholate was 38.9%, and the total yield of the two acids was 46.5%. The total yield of the two acids based on the consumed beta-naphthol was 86.9%, and the ratio of recovery of beta-naphthol was 86.9%. Example 4 The procedure of Example 1 was followed except that 546 g of Dowtherm (a mixture of 75% of diphenyl ether and 25% of diphenyl) was used instead of the light oil in Example 1. There were obtained 64.7 g of 2-hydroxynaphthalene-6-carboxylic acid and 16.3 g of 2-hydroxynaphthalene3-carboxylic acid, and 69.6 g of beta-naphthol was recovered. The yield of 2-hydroxynaphthalene-6-carboxylic acid based on potassium beta-naphtholate was 34.4%, and the total yield of the two acids on the same basis was 43.1%. The total yield of the two acids based on the consumed betanaphthol was 83.3%, and the ratio of recovery of betanaphthol a:as 84.9%. Example 5 By using the device shown in the accompanying drawing, the reaction and work-up in accordance with this invention were continuously carried out. A liquid dispersed mixture composed of anhydrous potassium beta-naphtholate and light oil (gas oil) in a weight ratio of 91:182 was put in the storage tank 1. The mixture was sent in an amount of 273 kg per hour to reaction tank 2 kept at a carbon dioxide pressure of 6 kg/ cm2.G, and reacted with carbon dioxide at 2600C. The residence time was 4 hours. The reaction mixture which left the reaction tank 2 was cooled by heat exchanger 3, and mixed in water-mixing tank 4 with 400 liters/hr of water with stirring. The temperature of the mixture was adjusted to 850C, and the mixture was then introduced into 0 separating tank 5 where it was separated at 85 C into a light oil layer and a water layer. From the upper light oil layer, beta-naphthol was recovered by using a recovery device (not shown). The lower water layer was adjusted to pH 7.0 with dilute sulfuric acid in pH-adjusting tank 6, and then separated at 850C in separating tank 7. The lower tarry layer separated in the separating tank 7 was subjected to a vacuum distillation device (not shown) to recover beta-naphthol. The upper layer in the separating tank 7 was sent to a centrifugal extracting device 8 wherein it was extracted at 850C with 250 liters/hr of xylene. The xylene layer was sent to a recovery device (not shown) to recover naphthol. The water layer which left the extracting device 8 was sent to acid precipitation tank 9 where it was subjected to acid precipitation at a pH of 4.5, and the precipitate was separated by centrifugal separator 10. There was obtained 35.8 kg/hr of 2-hydroxynaphthalene-6 carboxylic acid as crystals. The mother liquor left after the centrifugal separation was adjusted to pH 2.0 with dilute sulfuric acid in a separate acid precipitation device (not shown) to give hourly 9.5 kg of crystals containing 1.9 kg of 2-hydroxynaphthalene-6-carboxylic acid and 7.6 kg of 2-hydroxynaphthalene-3-carboxylic acid. The mixture was fractionally recrystallized from dilute methanol by a recrystallization device (not shown) to give the respective acids nn preform. The yield of 2-hydroxynaphthalene-6-carboxylic acid based on.potassium beta-naphtholate was 40.1%, and the total yield of the two acids was 48.2%. 32.6 kg of betanaphthol was recovered hourly. The total yield of the two acids based on the consumed beta-naphtholate was 88.1%, and the ratio of recovery of beta-naphthol was 87.5%. Example 6 By using the device shown in the accompanying drawing, the reaction and work-up were carried out in accordance with this invention were carried out continuously. A -liquid dispersed mixture composed of anhydrous potassium beta-naphtholate and light oil (gas oil) in a weight ratio of 91:182 was stored in storage tank 1. The mixture was sent in an amount of 273 kg per hour to reaction tank 2 kept at a carbon dioxide pressure of 9 kg/cm2.G, and reacted with carbon dioxide at 2800C. The residence time was 3 hours. The reaction mixture which left the reaction tank 2 was cooled by heat exchanger 3, and mixed with 400 liters/hr of water with stirring in water-mixing tank 4. The temperature of the mixture was adjusted to 0 85 C, and the mixture was then introduced into separating tank 5 where it was separated at 850C into a light oil layer and a water layer. From the upper light oil layer, beta-naphthol was recovered by using a recovery device (not shown). The lower water layer was adjusted to pH 7.0 with dilute sulfuric acid in pH-adjusting tank 6, and then without going through separating tank 7, was directly sent to centrifugal extracting device 8 where it was extracted 0 at 85 C with 300 ml/hr of xylene. The xylene layer was sent to a recovery device (not shown) to recover beta- naphthol. The water layer which left the extraction device 8 was sent to acid precipitation tank 9 where it was subjected to acid precipitation with dilute sulfuric acid at a pH of 4.2. The precipitate was separated by centrifugal separator 10. There was obtained hourly 35.3 kg of 2hydroxynaphthalene-6-carboxylic acid as crystals. The mother liquor left after the centrifugal separation was adjusted to pH 2.0 with dilute sulfuric acid in a separate acid precipitation device (not shown) to give 4.7 kg of crystals consisting of 1.5 kg of 2-hydroxynaphthalene-6carboxylic acid and 3.2 kg of 2-hydroxynaphthalene-3 carboxylic acid. The mixture was fractionally recrystallized from dilute methanol in a recrystallization device (not shown) to give the respective acids in pure form. The yield of 2-hydroxynaphthalene-6-carboxylic acid based on potassium beta-naphtholate was 39.1 %, and the total yield of the two acids on the same basis was 42.6%. 36.8 kg of beta-naphthol was recovered. The total yield of the two acids based on the consumed beta-naphthol was 87.1%, and the ratio of recovery of beta-naphthol was 87.3%. Example 7 Light oil (455 g), 182 g of potassium betanaphtholate and 6.5 g of beta-naphthol were charged into a pressure reaction kettle, and the same operation as in Example 1 was carried out. There were obtained 71.2 g of 2-hydroxynaphthalene-6-carboxylic acid and 15.7 g of 2 hydroxynaphthalene-3-carboxylic acid, and 74.8 g of betanaphthol was recovered. The yield of 2-hydroxynaphthalene6-carboxylic acid based on potassium beta-naphtholate was 37.9%, and the total yield of the two acids on the same basis was 46.2%. The total yield of the two acids based on the consumed beta-naphthol was 87. 8, and the ratio of recovery of beta-naphthol was 89.0%. Example 8 182 g of potassium beta-naphtholate was put in a pressure reaction kettle, and reacted with carbon dioxideat a temperature of 2600C and a carbon dioxide pressure of 9 kg/cm2.G for a period of 6 hours. The reaction mixture was worked up in the same way as in Example 1 except that the reaction medium was separated. There were obtained 38.0 g of 2-hydroxynaphthalene-6-carboxylic acid and 18.8 g of 2-hydroxynaphthalene-3-carboxylic acid, and 83.5 g of beta-naphthol was recovered. The yield of 2-hydroxynaphtha lene-6-carboxylic acid based on potassium beta-naphtholate was 20.2%, and the total yield of the two acids on the same basis was 30.2%. The total yield of the two acids based on the consumed beta-naphthol was 70.2%, and the ratio of recovery of beta-naphthol was 81.7%.

Claims: PRAT iE CLAIM IS: 1. In a process for producing 2-hydro.ynaphthalene- 6-carboxylic acid by reacting substantially anhydrous potassium beta-naphtholate with carbon dioxide, the improvement wherein the reaction is carried out at a 0 temperature of at least 180 C and a carbon dioxide pressure 2 of at least 1 kg/cm .G using as a starting material potassium beta-naphtholate or a mixture which contains potassium betanaphtholate and is liquid under the reaction conditions. 2. The process of claim 1 wherein said starting mixture contains not more than 0.1 mole of free betanaphthol per mole of potassium beta-naphtholate. 3. The process of claim 1 or 2 wherein the carbon 2 dioxide pressure is at least 5.5 kg/cm2.G. 4. The process of any one of claims 1 to 3 wherein said starting mixture contains a reaction medium having a melting point of not more than 1800C. 5. The process of claim 4 wherein said reaction medium is at least one member selected from the group consisting of aliphatic hydrocarbons, alicyclic hydrocarbons, aromatic hydrocarbons and aromatic ethers. 6. The process of claim 4 or 5 wherein said reaction medium has a boiling point of 150 to 4000C. 7. The process of claim 5 or 6 wherein the aliphatic, alicyclic or aromatic hydrocarbons are hydrocarbons of the petroleum series. 8. The process of any one of claims 4 to 7 wherein the amount of said reaction medium is 0.5 to 10 times the weight of potassium beta-naphtholate. 9. The process of any one or claims 1 to 8 wherein in order to obtain 2-hydroxynaphthalene-6-carboxylic acid selectively from the reaction mixture after the reaction, the pH of the solution or suspension containing a mixture of 2-hydroxynaphthalene-6-carboxylic acid and 2-hydroxynaphthalene-3-carboxylic acid and/or the salts thereof is adjusted to 3.5 to 6. 10. The process of any one of claims 1 to 9 wherein water is added to the reaction mixture after the reaction; the reaction medium, if present, is separated; if required, the tarry layer is precipitated in liquid form from the water layer and separated; beta-naphthol is extracted from the water layer by using a hydrophobic extracting solvent which is liquid at a temperature of not more than 1100C; and the water layer left after the extraction is subjected to acid precipitation.

Inventors: KUWAE, YOSHIHIKO, MURAMOTO, YASUKAZU, TSUCHIYA, HIROAKI, UENO, RYUZO
Applicants: KABUSHIKI KAISHA UENO SEIYAKU OYO KENKYUJO
Application year: 1981
Main classification: C07C65
IPC codes: C07C67, C07C51, C07C65