JP2006036653A - Method for producing 1,3-cyclohexanediol - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a 1,3-cyclohexanediol high in cis-form content. <P>SOLUTION: The method for producing the 1,3-cyclohexanediol comprises hydrogenating resorcinol in the presence of a base metal catalyst, wherein the hydrogenation reaction is carried out in the presence of at least one metal compound selected from an alkali metal compound and an alkaline earth metal compound. <P>COPYRIGHT: (C)2006,JPO&NCIPI

Description

  The present invention relates to a method for producing 1,3-cyclohexanediol (hereinafter abbreviated as “1,3-CHD”). More specifically, resorcin is hydrogenated in the presence of a base metal catalyst and at least one metal compound selected from the group consisting of alkali metal compounds and alkaline earth metal compounds to obtain 1,3-CHD having a high cis-isomer content. It relates to a manufacturing method.

  1,3-CHD is a very useful compound as an intermediate for producing pharmaceuticals, agricultural chemicals, polymer compounds and the like.

  The following methods are known as methods for producing 1,3-CHD. For example, (1) a method of hydrogenating 1,3-cyclohexanedione with sodium borohydride (Patent Document 1), (2) a method of hydrogenating resorcin in the presence of a nickel catalyst (Non-Patent Documents 1 to 3), (3) A method in which resorcin is hydrogenated using a catalyst in which a ruthenium / silica-supported catalyst further supports a basic metal is known (Patent Document 2).

  In the above method (1), compounds of Group 1 (Group IA), Group 2 (Group IIA), Group 12 (Group IIB), Group 13 (Group IIIB) of the periodic table are further added to the reaction system, Although the selectivity of the cis isomer is improved, a large amount of sodium borohydride must be used, and a large amount of waste is generated. Furthermore, since 1,3-cyclohexanedione as a raw material is produced by hydrogenating resorcin using expensive palladium as a catalyst, it is difficult to say that it is an industrially advantageous production method. In method (2), 1,3-CHD is produced by hydrogenation, but the production ratio of the obtained cis isomer and trans isomer is not mentioned, and the yield is low. It was. In the method (3), a cis isomer is generated with a selectivity of 75% or more, but it is difficult to say that the method is industrially advantageous because it uses a ruthenium catalyst that is an expensive noble metal catalyst. is there. In view of such a current situation, there has been a demand for the emergence of a method capable of producing 1,3-CHD having a high cis-isomer content rate advantageously and with low productivity.

JP 2003-300919 A Korean Patent Application No. 2003-92889 Journal of Chemical Society, p. 2103 (1950) Journal of Chemical Society, p. 1586 (1949) Pharmaceutical Journal, Vol. 58, 657 (1938)

  An object of this invention is to provide the method of manufacturing 1,3-CHD with high cis-isomer content industrially advantageously.

  As a result of intensive studies to achieve the above-mentioned problems, the present inventors hydrogenate resorcin in the presence of at least one metal compound selected from the group consisting of a base metal catalyst and an alkali metal compound and an alkaline earth metal compound. As a result, it has been found that 1,3-CHD having a high cis-isomer content can be produced industrially advantageously, and the present invention has been completed based on this finding.

  That is, the present invention provides the following method for producing 1,3-CHD.

  Item 1 In producing 1,3-cyclohexanediol by hydrogenating resorcin in the presence of a base metal catalyst containing at least one selected from the group consisting of iron, cobalt, nickel, copper and zinc, the hydrogenation reaction is performed. The manufacturing method characterized by performing in presence of the at least 1 sort (s) of metal compound chosen from the group which consists of an alkali metal compound and an alkaline-earth metal compound.

  Item 2 The method according to Item 1, wherein the metal compound is used in an amount of 1 to 50 mol% based on resorcin.

  Item 3. The method according to Item 1 or 2, wherein the base metal catalyst is a base metal catalyst containing at least one selected from the group consisting of nickel and cobalt.

  Item 4 The metal compound is lithium hydroxide, sodium hydroxide, potassium hydroxide, lithium carbonate, sodium carbonate, potassium carbonate, lithium bicarbonate, sodium bicarbonate, potassium bicarbonate, magnesium hydroxide, calcium hydroxide, hydroxide Item 4. The production method according to any one of Items 1 to 3, which is at least one selected from the group consisting of strontium, barium hydroxide, magnesium carbonate, calcium carbonate, strontium carbonate, and barium carbonate.

  According to the present invention, by resorcinating resorcin, 1,3-CHD having a high cis-isomer content, which is usefully used as an intermediate for resins, agricultural chemicals, pharmaceuticals and the like, can be advantageously produced industrially.

  As the resorcin used in the present invention, those produced according to a conventionally known method can be widely used, and those commercially available as industrial raw materials can be used as they are. Furthermore, if necessary, a product that has been purified by a conventionally known method such as recrystallization or sublimation to reduce the sulfur content that inhibits the hydrogenation reaction can be used.

  In addition to the resorcin, resorcin derivatives in which the hydroxyl group is protected with a protecting group such as a silyl group or an alkyl group can also be used.

Base metal catalyst The base metal catalyst according to the present invention is a catalyst containing a base metal capable of nuclear hydrogenation of an aromatic ring, and examples of the base metal include iron, cobalt, nickel, copper, and zinc. Among these, nickel and cobalt are preferable from the viewpoint of reactivity and selectivity, and nickel is particularly recommended. The base metal is not limited to zero-valent metals, but includes inorganic compounds such as nitrates, sulfates, acetates, chlorides, bromides, oxides, hydroxides, acetylacetonate compounds, amine compounds, phosphine compounds, and carbonyl compounds. It may be a complex or the like.

  Further, in addition to the base metal, a modified catalyst to which one or more of boron, magnesium, aluminum, silicon, calcium, titanium, chromium, manganese, palladium, silver, tin, barium, molybdenum and the like are added may be used.

  The base metal catalyst can be used as it is, but is usually used as a sponge metal type catalyst or a carrier-supported type catalyst.

  As the sponge metal type catalyst, those conventionally known or commercially available can be widely used, and examples thereof include a sponge nickel catalyst, a sponge cobalt catalyst, a sponge copper catalyst, a sponge iron catalyst, and a sponge zinc catalyst. A catalyst and a sponge cobalt catalyst are preferable, and a sponge nickel catalyst is particularly preferable from the viewpoint of high selectivity.

  The sponge metal type catalyst can be used as it is in a water-containing state after development, or can be used after water has been replaced with a suitable solvent. The solvent used for replacing water is not particularly limited as long as it is compatible with water and is inert to the hydrogenation reaction.

  Conventionally supported or commercially available catalysts can be widely used as the carrier-supported catalyst, and examples thereof include a stabilized nickel catalyst, a sulfur-resistant nickel catalyst, a flake nickel catalyst, and a supported cobalt catalyst. Among these, a stabilized nickel catalyst and a sulfur-resistant nickel catalyst are preferable.

  Examples of the carrier used for the carrier-supported catalyst include diatomaceous earth, pumice, activated carbon, graphite, silica gel, alumina, magnesium oxide, zirconium oxide, titanium oxide, zeolite, calcium carbonate, barium sulfate, and the like. Alumina and the like are preferable. These carriers can be used alone or in combination of two or more.

  The supported amount of the metal component of the carrier-supported catalyst is not particularly limited, but is usually about 1 to 90% by weight, preferably 20 to 80% by weight, as a metal component, with respect to the total weight of the catalyst.

  The form of these carrier-supported catalysts is not particularly limited, and a powder form, a tablet form or the like can be appropriately selected and used according to the desired reaction form. In general, powder catalysts are preferred for batch or continuous suspension reactions, and tablet catalysts are often used for fixed bed reactions.

  The method for producing these carrier-supported catalysts is not particularly limited, and can be easily produced by a conventionally known method such as an impregnation method or a coprecipitation method. Usually, a commercially available product can be used as it is or after being subjected to a suitable activation treatment such as a reduction treatment before use.

  The form of these base metal catalysts is not particularly limited, and is suitably selected and used in the form of a powder, a molded catalyst, etc. according to the selected reaction method. The powdered catalyst is usually used for a batch or continuous suspension bed hydrogenation reaction, and the shaped catalyst is used for a fixed bed continuous hydrogenation reaction. Moreover, as a shaping | molding catalyst, although suitably selected by the magnitude | size of the reactor to be used, the column shape of diameter 2-6mm and height 2-8mm is preferable normally.

  The amount of the catalyst used in the hydrogenation reaction is usually in the range of 0.1 to 50% by weight, preferably 0.5 to 20% by weight, particularly preferably 1 to 10% by weight, based on the raw material resorcin. % Is recommended. Within this range, the hydrogenation reaction can be carried out at an economically advantageous and sufficient reaction rate.

Solvent This reaction can be carried out without solvent, but is preferably carried out using a solvent. The solvent to be used is not particularly limited as long as it is inert under the hydrogenation reaction conditions. For example, water, an aliphatic alcohol having 1 to 8 carbon atoms, preferably 1 to 4 carbon atoms, 3 to 10 carbon atoms, preferably Examples thereof include alicyclic alcohols having 6 to 9 carbon atoms and chain or cyclic ethers containing 1 to 5 (preferably 2 to 3) ether groups.

  Of these, aliphatic alcohols and chain ethers are preferred from the viewpoint of resorcin solubility and reaction selectivity.

  More specifically, water, methanol, ethanol, n-propyl alcohol, iso-propyl alcohol, n-butyl alcohol, iso-butyl alcohol, sec-butyl alcohol, tert-butyl alcohol, pentanol, hexanol, heptanol, octanol , 2-ethylhexanol, 2-methoxyethanol, 2-ethoxyethanol, propylene glycol monomethyl ether, ethylene glycol, propylene glycol, cyclohexanol, methylcyclohexanol and other alcohol solvents, diethyl ether, diisopropyl ether, dibutyl ether, methyl tert -Butyl ether, dimethoxyethane, diethylene glycol dimethyl ether, triethylene glycol dimethyl ether, tet Hydrofuran, 1,3-dioxolane, ether solvents such as dioxane and the like. Among these, iso-propyl alcohol, propylene glycol monomethyl ether, dimethoxyethane, and diethylene glycol dimethyl ether are preferable. These solvents can be used alone or in combination of two or more.

  The amount of the solvent used is not particularly limited, but is about 0.5 to 100 times by weight, preferably about 1 to 10 times by weight with respect to resorcin. If it is less than 0.5 times by weight, it tends to be difficult to dissolve the raw material, and even if it is used in excess of 100 times by weight, there is no advantage to meet it, and the solvent removal operation after the reaction is complicated. This is not economically desirable.

Metal Compound In the hydrogenation reaction of the present invention, the cis-isomer content in the produced 1,3-CHD is increased by allowing at least one metal compound selected from the group consisting of alkali metal compounds and alkaline earth metal compounds to coexist. be able to.

  Examples of the alkali metal include lithium, sodium, potassium, rubidium, and cesium. Among these, lithium, sodium, and potassium are preferable.

  Examples of the alkaline earth metal include magnesium, calcium, strontium, and barium. Among these, calcium, magnesium, and barium are preferable, and calcium and barium are particularly recommended.

  Among the above metal compounds, alkaline earth metal compounds are more preferable because of their high hydrogenation reaction selectivity.

  The form of the alkali metal and alkaline earth metal is not particularly limited. For example, hydroxide, hydride, carbonate, bicarbonate, sulfite, phosphate, hydrogen phosphate, boron of the metal. Examples thereof include acid salts, hydrogen borate salts, organic acid salts, and alkoxides. Among these, hydroxides, carbonates, hydrogen carbonates, organic acid salts having 1 to 2 carbon atoms, and alkoxides having 1 to 2 carbon atoms are preferable, and hydroxides are particularly preferable.

  Among the above metal compounds, preferred specific examples of the alkali metal compound include lithium hydroxide, sodium hydroxide, potassium hydroxide, lithium carbonate, sodium carbonate, potassium carbonate, lithium hydrogen carbonate, sodium hydrogen carbonate, potassium hydrogen carbonate, Lithium formate, sodium formate, potassium formate, lithium acetate, sodium acetate, potassium acetate, lithium oxalate, sodium oxalate, potassium oxalate, lithium methoxide, sodium methoxide, potassium methoxide, lithium ethoxide, sodium ethoxide, Examples include potassium ethoxide, and lithium hydroxide, sodium hydroxide, potassium hydroxide, lithium carbonate, sodium carbonate, potassium carbonate, lithium hydrogen carbonate, sodium hydrogen carbonate, and potassium hydrogen carbonate are particularly recommended. These alkali metal compounds may be either anhydrides or hydrates.

  Preferable specific examples of the alkaline earth metal compound include magnesium hydroxide, calcium hydroxide, strontium hydroxide, barium hydroxide, magnesium carbonate, calcium carbonate, strontium carbonate, barium carbonate, magnesium formate, calcium formate, strontium formate, formic acid. Barium, magnesium acetate, calcium acetate, strontium acetate, barium acetate, magnesium oxalate, calcium oxalate, strontium oxalate, barium oxalate, magnesium methoxide, calcium methoxide, strontium methoxide, barium methoxide, magnesium ethoxide, calcium Ethoxide, strontium ethoxide, barium ethoxide, etc., especially magnesium hydroxide, calcium hydroxide, strontium hydroxide , Barium hydroxide, magnesium carbonate, calcium carbonate, strontium carbonate, barium carbonate. These alkaline earth metal compounds may be either anhydrides or hydrates.

  The said metal compound can be used individually or in combination of 2 or more types as appropriate.

  The amount of the metal compound used is usually about 0.1 to 100 mol%, preferably 1 to 50 mol%, more preferably 2 to 30 mol%, and particularly preferably 2.5 to mol with respect to resorcin. A range of 10 mol% is recommended. Within this range, the reaction can be carried out with a sufficient production rate and selectivity.

  The hydrogenation reaction is preferably carried out by substituting the interior of the system with an inert gas such as nitrogen gas or argon gas and then substituting with hydrogen.

  The reaction temperature of hydrogenation is usually in the range of 30 to 200 ° C, preferably 50 to 150 ° C. When the temperature is lower than this temperature range, a sufficient reaction rate cannot be obtained, and when the temperature is higher, a side reaction and a decomposition reaction are accompanied, so that the yield tends to decrease, which is not economically preferable.

  The reaction pressure is a hydrogen partial pressure, usually in the range of about 0.5 to 30 MPa, preferably about 2 to 20 MPa. If it is less than 1 MPa, it is difficult to obtain a practical reaction rate. On the other hand, if it exceeds 20 MPa, no significant significance is observed, and a special pressure-resistant facility is required, which is economically disadvantageous.

  The reaction time varies depending on the amount of the catalyst and various conditions, but it is preferable to appropriately select the conditions so as to be usually about 0.5 to 50 hours, and 1 to 20 hours from an industrial viewpoint.

  The reaction method of the present invention includes a method using a liquid phase suspension bed in which a hydrogenation catalyst is dispersed in a reaction solution, a fixed bed flow reaction in which a hydrogenation catalyst is fixed in a reactor and a reaction solution is allowed to act on this. The method by is adopted.

  After completion of the reaction, the catalyst is separated and removed by a known method such as filtration or centrifugation, and then the solvent is distilled off if necessary. 1,3 by a conventional method such as extraction, distillation, sublimation, crystallization, chromatography or the like. -CHD can be obtained. At that time, in addition to the above method as a method for removing the alkali metal compound and alkali metal compound added at the time of reaction, a method of blowing carbon dioxide and depositing it as a carbonate of the corresponding metal and filtering it off, an ion exchange resin The method of processing etc. are mentioned. If a cis-isomer with higher purity is required, the purity of the cis-isomer can be further increased by conventional methods such as distillation, sublimation, recrystallization, and chromatography.

  By hydrogenating resorcin according to the above hydrogenation method, the content of cis 1,3-CHD in 1,3-CHD obtained is at least 60% or more, preferably 70% or more, particularly preferably 75 % Or more of 1,3-CHD can be obtained.

  EXAMPLES The present invention will be described in detail below with reference to examples, but the present invention is not limited to these examples. In addition, the conversion, CHD selectivity, and cis selectivity of each Example and Comparative Example were analyzed by gas chromatography (GC) and calculated using the following formula.

A small amount of the reaction solution after completion of the GC sample preparation reaction was taken, acidified by adding dilute hydrochloric acid, and then diluted with methanol for preparation.

Conversion rate Conversion rate (%) = 100−Sres
Sres: Resorcin remaining rate (GC area%)

CHD selectivity CHD selectivity (%) = (Scis + Strans) / conversion rate × 100
Scis: Production rate of cis-1,3-CHD (GC area%)
Strans: Trans-1,3-CHD production rate (GC area%)

Cis selectivity cis selectivity (%) = Scis / (Scis + Strans) × 100
Scis: Production rate of cis-1,3-CHD (GC area%)
Strans: Trans-1,3-CHD production rate (GC area%)

  The sponge metal-type catalyst in the following examples was used in a water-containing state in which the water stored after development was measured to have a predetermined weight with pure metal, and then the supernatant water was separated by gradient separation. .

Example 1
In a 500 ml autoclave equipped with an electromagnetic induction stirrer, resorcin 30 g (0.27 mol), isopropyl alcohol (hereinafter abbreviated as “IPA”) 120 g, developed sponge nickel catalyst (NDT-90, manufactured by Kawaken Fine Chemical Co., Ltd.) After 1.5 g and 0.54 g (0.014 mol) of sodium hydroxide were added and the inside of the autoclave was replaced with hydrogen, a hydrogenation reaction was performed at a gauge pressure of 5.0 MPa and 100 ° C. The reaction was performed while replenishing the consumed hydrogen, and continued until no pressure decrease was observed. After completion of the reaction, the reaction mixture was cooled and the catalyst was removed by filtration under reduced pressure. The resulting colorless and transparent liquid was analyzed by gas chromatography. The results are shown in Table 1.

Example 2
The same procedure as in Example 1 was performed except that 120 g of diethylene glycol dimethyl ether (hereinafter abbreviated as “diglyme”) was used instead of IPA. The results are shown in Table 1.

Example 3
The same operation as in Example 1 was conducted except that the amount of sodium hydroxide used was 2.18 g (0.055 mol). The results are shown in Table 1.

Example 4
The same procedure as in Example 1 was performed except that 0.57 g (0.014 mol) of lithium hydroxide monohydrate was used instead of sodium hydroxide. The results are shown in Table 1.

Example 5
The same procedure as in Example 1 was performed except that 0.90 g (0.014 mol) of potassium hydroxide was used instead of sodium hydroxide. The results are shown in Table 1.

Example 6
The same procedure as in Example 1 was performed except that 0.90 g (0.014 mol) of calcium hydroxide was used instead of sodium hydroxide. The results are shown in Table 1.

Example 7
The same procedure as in Example 1 was performed except that 4.29 g (0.014 mol) of barium hydroxide octahydrate was used instead of sodium hydroxide. The results are shown in Table 1.

Example 8
The same procedure as in Example 1 was performed except that 4.29 g (0.014 mol) of barium hydroxide octahydrate was used instead of sodium hydroxide, and 120 g of diglyme was used instead of IPA. The results are shown in Table 1.

Example 9
The same procedure as in Example 1 was performed except that 1.44 g (0.014 mol) of sodium carbonate was used instead of sodium hydroxide. The results are shown in Table 1.

Example 10
The same procedure as in Example 1 was performed except that 1.36 g (0.014 mol) of calcium carbonate was used instead of sodium hydroxide. The results are shown in Table 1.

Example 11
A 500 ml autoclave equipped with an electromagnetic induction stirrer was charged with 1.5 g of a stabilized nickel catalyst (N103, manufactured by JGC Chemical Co., Ltd.) and 120 g of IPA, and the inside of the autoclave was replaced with hydrogen. The catalyst was activated by heating and stirring for a period of time. After cooling, 30 g of resorcin and 0.54 g of sodium hydroxide were added, the inside of the autoclave was replaced with hydrogen, and then a hydrogenation reaction was performed at a gauge pressure of 5.0 MPa and 100 ° C. The reaction continued until no pressure reduction was seen while replenishing the consumed hydrogen. After completion of the reaction, the reaction mixture was cooled and the catalyst was filtered off under reduced pressure. The resulting colorless transparent liquid was analyzed by GC. The results are shown in Table 1.

Example 12
The same procedure as in Example 1 was performed except that 1.5 g of a developed sponge cobalt catalyst (ODHT-60, manufactured by Kawaken Fine Chemical Co., Ltd.) was used instead of the sponge nickel catalyst. The analysis results are shown in Table 1.

Comparative Example 1
The same operation as in Example 1 was performed except that sodium hydroxide was not used. The results are shown in Table 1.

Comparative Example 2
The same operation as in Example 11 was performed except that sodium hydroxide was not used. The results are shown in Table 1.

1,3-CHD produced by the method of the present invention can be suitably used as a raw material for synthetic intermediates such as pharmaceuticals, agricultural chemicals and polymer compounds.

Patent applicant New Nippon Rika Co., Ltd.

Claims (4)

  In producing 1,3-cyclohexanediol by hydrogenating resorcin in the presence of a base metal catalyst containing at least one selected from the group consisting of iron, cobalt, nickel, copper and zinc, the hydrogenation reaction is carried out with an alkali metal. The manufacturing method characterized by performing in presence of the at least 1 sort (s) of metal compound chosen from the group which consists of a compound and an alkaline-earth metal compound.   The manufacturing method according to claim 1, wherein the metal compound is used in an amount of 1 to 50 mol% with respect to resorcin.   The manufacturing method according to claim 1 or 2, wherein the base metal catalyst is a base metal catalyst containing at least one selected from the group consisting of nickel and cobalt. The metal compound is lithium hydroxide, sodium hydroxide, potassium hydroxide, lithium carbonate, sodium carbonate, potassium carbonate, lithium hydrogen carbonate, sodium hydrogen carbonate, potassium hydrogen carbonate, magnesium hydroxide, calcium hydroxide, strontium hydroxide, The production method according to claim 1, which is at least one selected from the group consisting of barium hydroxide, magnesium carbonate, calcium carbonate, strontium carbonate and barium carbonate.