• 专利附录
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    • 专利摘要:
    PURPOSE: Provided is a method for producing a trimethylhydroquinone diacetate (TMHQ-DA) with high yield and high purity, by using a catalyst system and separation system having price competitiveness. CONSTITUTION: The method for producing a TMHQ-DA by esterification and displacement of 4-oxoisophorone and an acylating agent by using sulfuric acid, is characterized in that the 4-oxoisophorone and an acylating agent are reacted at normal temperature for 3 hours, the reaction mixture is washed with water so as to entirely solidify the product, and then TMHQ-DA is extracted from the solidified product with extractant. Amount of the used sulfuric acid catalyst is 0.1-50 mol% with respect to 1 mol of 4-oxoisophorone.
    公开号:KR20030028892A
    申请号:KR1020010061179
    申请日:2001-10-04
    公开日:2003-04-11
    发明作者:김정수；이시준；이상훈；유익상
    申请人:에스케이 주식회사；
    IPC主号:
    专利说明:

    Method for preparing trimethylhydroquinone (TMHQ) diester with high yield and high purity}
    [1] The present invention relates to a method for preparing trimethylhydroquinone diacetate (TMHQ-DA) with high yield and high purity. A high yield of TMHQ-DA was prepared from the reactant 4-oxoisophorone as shown in Scheme 1, and the commercially available TMHQ-DA was obtained by a separation and purification process through solidification and extraction with a suitable solvent. And improved production methods that can be produced with high purity.
    [2]
    [3] TMHQ or TMHQ-DA is an important substance that produces α-tocopherol through condensation with isophytol under appropriate catalytic conditions. At this time, the production method of TMHQ or TMHQ-DA is divided into two methods using a trimethylmethylphenol (TMP) and α-IP (α-isophorone) depending on the reaction starting material.
    [4] In the method using TMP, TMHQ is prepared by a two-step reaction as in Scheme 2 below, TMP itself is relatively expensive compared to α-IP, and the yield of the oxidation step, which is the first step in Scheme 2, is not high, In addition, since a large amount of by-products are generated during oxidation, the reaction is not easy in two steps, but it does not seem to have a great advantage in the commercialization process.
    [5]
    [6] On the other hand, the reaction using α-ISP as the reaction starting material requires three steps of isomerization, oxidation and esterification, as shown in Scheme 3 below, but the starting material α-IP is much cheaper than TMP, Increasing the yield of the reaction is relatively competitive in terms of cost.
    [7]
    [8] In addition, when TMP is used, the α-tocopherol prepared therefrom is unstable, and thus, an additional acylation reaction for condensation reaction into an α-tocopheryl acetate is required. However, when TMHQ-DA is used, isopyitol is used. Since the α-tocopheryl acetate is directly prepared by condensation with, one step of preparation may be omitted. This is equivalent to the number of TMP production steps and reaction steps in terms of the reaction step, but not only does the size difference of the reactor occur due to the difference in the molecular weight of the compound before and after the condensation reaction (the molecular weight before the condensation reaction is small), The use of TMHQ-DA is known to be superior in yield and purity to TMHQ.
    [9] On the other hand, the method for producing TMHQ-DA from 4-oxoisophorone has been studied in recent years. Daicel Co., Ltd. uses an acidic ion exchange resin (Amberyst 15, Nafion NR50) as a catalyst in EP 0850910A1, and reacts 4-oxoisophorone at 60-100 ° C. for 6 hours in the presence of acetic anhydride. TMHQ-DA was prepared, wherein reaction yield was 84-88%, separation yield was 55-60%. In the above method, TMHQ-DA was prepared using a protic Y-type zeolite and sulfated zirconia as a catalyst, resulting in a reaction yield of 74 to 75% and a separation yield of 52%. However, in the case of the above method, first, the reaction yield is rather low, and in particular, the separation yield is very low. The low separation yield is due to the small difference in solubility of by-products and TMHQ-DA in the mixed solvent (ethyl acetate and n-hexane) system used to obtain TMHQ-DA by recrystallization. The TMHQ-DA is also melted, and the amount of loss is large.
    [10] In the case of Degussa, TMHQ-DA was produced in US Pat. No. 5,969,176 with a yield of 88.35% to 92.8% using trifluoromethanesulfonic acid as a catalyst, and 87.5 to 90.2 using boric acid and sulfuric acid as catalysts. TMHQ-DA was prepared in% yield.
    [11] Degussa also prepared TMHQ-DA in 93-94% reaction yield using chlorosulfonic acid and / or pyrogenic sulfuric acid (30-65%) as catalyst in US Pat. No. 6,063,968. However, the trifluoromethanesulfonic acid used in the case of the US Patent No. 5,969,176 is very hygroscopic, and in the case of the US Patent No. 6,063,968 exothermic sulfuric acid is a toxic unstable material, it is difficult to apply to commercialization process.
    [12] In the case of Degussa, TMHQ-DA was prepared in US Pat. No. 6,103,924 using protic zeolite (HY zeolite or H-β zeolite) in 94-97% of initial yield (yield not considering purity). . However, when using a solid catalyst such as zeolite, the cost and amount of the catalyst (about 50% by weight of 4-oxoisophorone) are large, the separation process between the solid catalyst and the product is complicated, and TMHQ-DA is adsorbed in the zeolite. Due to this, there may be disadvantages such as a reduction in separation yield. In addition, the amount of acetic anhydride used is about 750 mol%, so that the conversion rate may be maintained only by using an excessive amount of about 550 mol%.
    [13] Accordingly, in the present invention, using the above trace amount of sulfuric acid as a catalyst, TMHQ-DA is prepared in a high reaction yield (94-96%), and the prepared TMHQ-DA is 100% pure without a large separation loss by using a proper extraction solvent. A method for producing TMHQ-DA crystals in high yield was developed.
    [14] Accordingly, it is an object of the present invention to provide a method capable of producing high yield and high purity TMHQ-DA using a catalyst system and a separation and purification system having a competitive price.
    [15] Still another object of the present invention is to develop a process for easy and commercialized design and commercialization of the separation and purification process as smoothly as possible.
    [16] The method of the present invention for achieving the above object is a reaction mixture mainly containing TMHQ-DA of 94-96% purity through esterification and dislocation reaction of 4-oxoisophorone and acetic anhydride as reactants using sulfuric acid as a catalyst After distilling under reduced pressure, washing with water to solidify, and then extract impurities several times with a suitable solvent system (single or mixed solvent) containing nonpolar hydrocarbons, unsaturated hydrocarbons or alcohols to obtain TMHQ-DA having a purity of 100%. It consists of manufacturing in high yield. In addition, TMHQ-DA dissolved in the extractant had little separation loss by distilling the solvent and adding it to the separation process again.
    [17] Looking at the present invention in more detail as follows.
    [18] The present invention relates to an esterification reaction and the last step in the reaction of obtaining TMHQ-DA from α-isophorone as in Scheme 3, and TMHQ-DA, a reaction product according to the present invention, is used to prepare α-tocopherol. As such, reaction yield and purity are the most important manufacturing steps.
    [19] According to the present invention, when TMHQ-DA was prepared through esterification and rearrangement of 4-oxoisophorone and an acylating agent, by-products having a molecular weight and structure similar to that of TMHQ-DA were produced together. The prepared TMHQ-DA produces α-tocopherol by condensation reaction with isopytol, and condensation reaction with isopyitol also occurs in the by-products, thereby producing by-products similar to α-tocopherol. Since α-tocopherol is a C25 heavy hydrocarbon, it is very difficult to separate it from analogous by-products through distillation and the like, and thus the purity of TMHQ-DA is commercially important in this condensation reaction step.
    [20] Accordingly, the present inventors use a trace amount of sulfuric acid as a catalyst to increase the reaction yield as much as possible in the esterification and dislocation reaction steps (reaction of side reactions), and by using a suitable extraction solvent containing a non-polar hydrocarbon, unsaturated hydrocarbon or alcohols. A method for producing TMHQ-DA with high yield and high purity by extraction and removal was developed.
    [21] Sulfuric acid, the catalyst used in the present invention, showed excellent results when the amount used was about 0.1 to 50 mol% (0.001 to 0.5 mol) based on 1 mol of 4-oxoisophorone. In particular, a small amount of about 0.5 mol% (0.3 wt%) was used. The reaction was terminated within 3 hours at room temperature alone, and the reaction yield was 95% or more.
    [22] Acylating agents used in the present invention include acetic anhydride, acetyl chloride, carboxylic anhydrides having 2 to 4 carbon atoms, or carboxylic acid halides having 2 to 4 carbon atoms. In this case, the conversion rate reached 100% even when only 25-50 mol% of the acyl anhydride, an acylating agent, was used in an amount of about 250-300 mol% relative to the reactant. The acylating agent showed an equivalent result in reaction time and yield even when acetyl chloride was used in addition to acetic anhydride.
    [23] In addition, the reaction was terminated within 3 hours regardless of the amount of the catalyst used, even if the reaction proceeds at room temperature in terms of the reaction temperature, in particular, the temperature increase portion due to the exothermic reaction is cooled in the initial reaction of adding 4-oxoisophorone. There was no need to reduce the cost of operation, which was commercially effective.
    [24] In the separation process, the reaction mixture can be washed with water to solidify the entire reaction product, which is filtered and extracted several times with a single or mixed solvent containing non-polar hydrocarbons and unsaturated hydrocarbons or alcohols. -DA (70% is obtained by one time separation purification and 100% by several times recovering the product from the extraction solvent), so the separation and purification process is competitive in terms of cost and ease of operation. Suitable single or mixed solvents for this process include non-polar hydrocarbons having 5 to 10 carbon atoms such as n-pentane, cyclopentane, n-hexane, cyclohexane, n-heptane, n-octane, n-nonane, n-decane and the like. Polar solvents such as ethyl acetate and diethyl ether or unsaturated and aromatic solvents having 6 to 10 carbon atoms such as cyclohexene, benzene, toluene and xylene or alkyl alcohols having 1 to 10 carbon atoms such as methanol, ethanol and butanol are suitable.
    [25] In particular, when used alone, nonpolar hydrocarbons and alkyl alcohols are suitable. When using as a mixed solvent, it is preferable to use a polar solvent such as a nonpolar hydrocarbon and ethyl acetate together, but a relatively small amount of a polar solvent. .
    [26] When n-hexane is used as the extraction solvent, three times extraction with 6 ml of solvent per 1 g of the reaction mixture yields TMHQ-DA having a purity of about 100% with a yield of 72%. TMHQ-DA dissolved in the extraction solvent is also obtained. When the solvent was removed and extracted with n-hexane again, almost all of the solvent was recovered with about 100% purity.
    [27] When n-butanol was used as the extraction solvent, TMHQ-DA with 100% purity could be obtained by extracting twice under the same conditions as n-hexane, but the yield (about 60%) was lowered once with a yield of about 40%. Since the product must be extracted again from the disadvantages of increasing the number of iterations of the separation and purification process.
    [28] From the point of view of the amount of the extraction solvent used, it is preferable to use 1 to 100 ml of extraction solvent per 1 g of the reaction product crystal, and in particular, 5 to 20 ml is most effective.
    [29] As described above, in the present invention, 4-HQO isophorone and acylating agent were obtained in a reaction yield of 94 to 96% using a trace amount of sulfuric acid catalyst within 3 hours at room temperature. The reaction product was solidified with water, and this solid was again obtained through separation and purification using an extraction solvent to obtain high yield and high purity TMHQ-DA.
    [30] Hereinafter, the present invention will be described in more detail with reference to Examples and Comparative Examples, but the scope of the present invention is not limited to the following Examples.
    [31] Comparative Example 1
    [32] 15.2 g (100 mmol) of 4-oxoisophorone and 1.5 g of "Amberyst 15" (Rohm & Hass), a strong acidic ion exchange resin, were added to a 100 ml round bottom flask, and 30.6 g (300 mmol) of acetic anhydride was added. After reacting at 60 ° C. for 6 hours, the progress of the reaction was confirmed by gas phase chromatography. As a result, the conversion rate of 4-oxoisophorone was 97.0%, purity 90.7%, and reaction yield 88.0%. After the reaction product was filtered to remove the catalyst, acetic acid was removed on a rotary evaporator, and TMHQ-DA was crystallized with ethyl acetate and hexane in the same manner as in EP 0850910A1 to obtain 12.7 g of crystals (crystallization yield 59.9%, Purity 98.7%). Finally, the yield of separation and purification was 59.1%.
    [33] Comparative Example 2
    [34] 15.2 g (0.1 mol) of 4-oxoisophorone and 7.8 g of HY zeolite (SiO 2 / Al 2 O 3 = 120) and 76.6 g (0.75 mol) of acetic anhydride were added to a 250 ml round bottom flask, and the mixture was heated at 90 ° C. for 3 hours. After the reaction, the progress of the reaction was confirmed by gas phase chromatography. As a result, the 4-oxoisophorone conversion was 99%, the purity was 93.1%, and the reaction yield was 92.17%. After cooling the reaction mixture to room temperature, acetic acid was removed on a rotary evaporator and 200 ml of distilled water was added to obtain crystals. The obtained crystals were filtered off and dried to give 19.1 g of a reaction mixture (crystallization yield 90.1%). Although the purity was 93.1%, there was no difference, but due to the problem of adsorption of the product to the solid catalyst zeolite, a much smaller amount of crystal was obtained than the reaction yield. When the separation purification method developed in the present invention is used, almost no yield loss occurs in the separation purification process, and finally, the yield of separation purification was 83.9%.
    [35] Comparative Example 3
    [36] Under the same conditions as in Comparative Example 1, the reaction was carried out by reducing acetic anhydride to 30.6 g (300 mmol). As a result of checking the reaction degree after 3 hours, the conversion rate of 4-oxoisophorone was significantly low, about 85%. In addition, the reaction was carried out for 4 hours, and after performing the reaction for 7 hours, the reaction progress was confirmed by gas phase chromatography. The conversion was 98.6% and the purity was 93.0%. In the same crystallization method as in Comparative Example 1, 19.0 g of a reaction mixture was obtained (crystallization yield 89.6%, purity 93%). Finally, the yield was about 83%.
    [37] Example 1
    [38] Into a 100 ml round bottom flask, 15.2 g (100 mmol) of 4-oxoisophorone, 1.96 g (20 mmol) of sulfuric acid, and 30.6 g (300 mmol) of acetic anhydride were added and reacted at room temperature for 3 hours, followed by gas phase chromatography. Check the progress. As a result, 4-oxoisophorone conversion was 100%, purity 95.5%, and reaction yield 95.5%. After cooling the reaction mixture to room temperature, acetic acid was removed on a rotary evaporator and 200 ml of distilled water was added to obtain crystals. It was neutralized (pH 6-7) by adding 1 M aqueous NaOH solution, filtered and dried to obtain 21.0 g of reaction mixture crystals (crystallization yield 99.1%, purity 95.5%). After extraction three times with 126 ml of n-hexane (6 ml of extraction solvent per 1 g of reaction mixture), the solid obtained by filtration was dried to obtain 15.1 g (72%) of 100% TMHQ-DA of purity. The weight and purity of the solid obtained by removal were 4.9 g (28%) and 83.9%. Finally, the yield was 94.6%.
    [39] Example 2
    [40] The reaction was carried out under the same conditions as in Example 1 by changing the acylating agent to acetyl chloride or reducing the concentration of acetic anhydride to 250 mmol. As a result of the reaction, there was no difference in reaction yield and reaction time due to the change of acylating agent and the decrease of concentration of. The reaction results are shown in Table 1 below.
    [41] Reaction time and yield for acylating agent No.baseAcylating agentReaction timeReaction yield (%) One4-oxoisophorone: 100 mmol Sulfuric acid: 20 mmol Reaction temperature: Room temperatureAcetic anhydride / 300 mmol3 hours95.5 2Acetic anhydride / 250 mmol3 hours95.2 3Acetyl chloride / 300 mmol3 hours95.1 4Acetyl Chloride / 250 mmol3 hours94.8
    [42] Example 3
    [43] Under the same conditions as in Example 1, the reaction was performed while changing the amount of sulfuric acid used as a catalyst from 0.1 mmol (0.1 mol%) to 100 mmol (100 mol%). Specific catalyst usage and thus yield are shown in Table 2 below.
    [44] Yield according to the change of catalytic amount No.baseSulfuric acid (mmol)% Yield (conversion / selectivity)Solidification yield (%)Separation Purification Yield (1st / Final) One4-oxoisophorone: 100 mmol acetic anhydride: 300 mmol Reaction temperature: Room temperature Reaction time: 3 hours0.193.199.770 / 92.2 20.595.1≒ 10072 / 94.3 3One95.599.271.5 / 94.1 4596.0≒ 10069.8 / 95.0 51095.7≒ 10072 / 94.6 62096.099.171.2 / 94.2 75092.299.570.8 / 90.7 810081.4≒ 10065.2 / 75.8
    [45] * Isolation purification yield is based on obtaining TMHQ-DA of 99.5% purity or higher
    [46] As shown in Table 2, when the sulfuric acid (conc.) Catalyst is used at 0.1 to 50 mol%, the reaction yield was excellent at 92 to 96%, and crystallization yield using water and n-hexane as an extraction solvent. Excellent yields were obtained for the separation and purification of TMHQ-DA using.
    [47] At this time, the crystallization yield was 99-100% as the yield obtained by crystallization of TMHQ-DA and some by-products after the completion of the reaction (compared to the theoretical value when the product was converted to TMHQ-DA). It is the total production yield including the yield in the separation and purification process. The primary yield in the separation and purification yield was calculated by filtering the crystals of 100% TMHQ-DA purity remaining after extraction three times with n-hexane, weighing them, and finally obtaining the extracted n-hexane again. The crystals containing by-products were again extracted with n-hexane to obtain TMHQ-DA having a purity of 100%, and this process was repeated once, and the separation and purification yield including TMHQ-DA with 100% purity obtained by repeating this process once. That is, the yield of 100% purity TMHQ-DA crystals obtained by a total of three extractions. In conclusion, the final separation tablet yield means the yield of TMHQ-DA with 100% purity obtained through reaction, crystallization and separation purification. Finally, 100% purity TMHQ-DA was obtained by the separation and purification yield of 94-95% by this experiment.
    [48] Example 4
    [49] The reaction was carried out while varying the amount of sulfuric acid used as a catalyst under the same conditions as in Example 3 to 0.5 mmol, 1 mmol, 5 mmol, 10 mmol and 20 mmol, and the same crystallization method was used. However, separation and purification were performed by changing the extraction solvent to n-butanol, extraction was performed three times for each separation purification, and total separation and purification was performed three times. The yield is shown in Table 3 below.
    [50] Yield when using n-butanol as extraction solvent No.baseSulfuric acid (mmol)% Yield (conversion / selectivity)Solidification yield (%)Separation tablet yield (primary / final) One4-oxoisophorone: 100 mmol acetic anhydride: 300 mmol Reaction temperature: Room temperature Reaction time: 3 hours0.595.110039.8 / 88.4 2One95.599.241.1 / 90.1 3596.0≒ 10040.5 / 89.6 41095.7≒ 10040.3 / 90.5 52096.099.140 / 89.8
    [51] When n-butanol was used as the extraction solvent, the solubility in TMHQ-DA was relatively higher than that of n-hexane, so in the case of n-hexane, three times of separation and purification processes were sufficient, but when n-butanol was used, Even when the ash was performed, the yield was slightly lower than that of n-hexane at 88.4 to 90.5%.
    [52] Example 5
    [53] Under the same conditions as in Example 3, the reaction was carried out while varying the amount of sulfuric acid used as a catalyst to 0.5 mmol, 1 mmol, 5 mmol, 10 mmol and 20 mmol, and the same crystallization method was used. However, separation and purification were performed using a mixed solvent of n-hexane + ethyl acetate (20: 1 vol%) as an extraction solvent. Extraction was performed three times for each separation purification, and the total separation purification process was performed five times. The yield is shown in Table 4 below.
    [54] Yield when using a mixed solvent of n-hexane and ethyl acetate as extraction solvent No.baseSulfuric acid (mmol)% Yield (conversion / selectivity)Solidification yield (%)Separation tablet yield (primary / final) One4-oxoisophorone: 100 mmol acetic anhydride: 300 mmol Reaction temperature: Room temperature Reaction time: 3 hours0.595.110066.2 / 92.3 2One95.599.267.0 / 92.6 3596.0≒ 10068.0 / 92.5 41095.7≒ 10066.8 / 93.2 52096.099.167.4 / 93.2
    [55] In the case of using the solvent mixture of n-hexane and ethyl acetate, the solubility in TMHQ-DA was slightly increased compared to n-hexane, but decreased than that of n-butanol. Finally, there was no significant difference from using n-hexane alone, and the final separation yield showed good results of 92.2-93.2%.
    [56] As described above, in the present invention, 4-HQO isophorone and an acylating agent were obtained in a reaction yield of 94 to 96% using a trace amount of sulfuric acid catalyst within 3 hours at room temperature. The reaction product was solidified with water, and this solid was again obtained through separation and purification using an extraction solvent to obtain high yield and high purity TMHQ-DA.
    [57] Compared with the prior art, it is relatively inexpensive in terms of cost, and although the operation cost is low due to the use of a small amount of catalyst and the reaction proceeding at room temperature, the separation and purification yield through solidification are high. The excellent TMHQ-DA showing a high yield of about 93 to 94% was obtained at low cost. Therefore, in the future, it is expected that the commercially important TMHQ-DA can be produced in high yield, high purity, and commercially economically.
    权利要求:
    Claims (11)
    [1" claim-type="Currently amended] In the process for preparing TMHQ-DA through esterification and rearrangement of 4-oxoisophorone and acylating agent,
    In the presence of a sulfuric acid catalyst, 4-oxoisophorone and an acylating agent are reacted at room temperature within 3 hours, and the reaction mixture is washed with water to solidify the entire reaction product, followed by extraction with an extraction solvent. How to make TMHQ-DA.
    [2" claim-type="Currently amended] The method of claim 1, wherein the sulfuric acid catalyst is used in an amount of 0.1 mol% to 50 mol% based on 1 mol of 4-oxoisophorone.
    [3" claim-type="Currently amended] The method of claim 1, wherein the sulfuric acid catalyst is used in an amount of 0.5 mol% based on 1 mol of 4-oxoisophorone.
    [4" claim-type="Currently amended] The method of claim 1, wherein the acylating agent is acetic anhydride, acetyl chloride, carboxylic anhydride having 2 to 4 carbon atoms or carboxylic acid halide having 2 to 4 carbon atoms.
    [5" claim-type="Currently amended] The method according to claim 1 or 4, wherein the acylating agent is 250 to 300 mol% based on the amount of 4-oxoisophorone used.
    [6" claim-type="Currently amended] The method of claim 1, wherein the extraction solvent is n-pentane, cyclopentane, n-hexane, cyclohexane, n-heptane, n-octane, n-nonane, n-decane, ethyl acetate, diethyl ether, cyclohexene At least one selected from the group consisting of benzene, toluene, xylene, methanol, ethanol and butanol.
    [7" claim-type="Currently amended] 7. The method of claim 6, wherein the extractant is n-peptane, cyclopentane, n-hexane, cyclohexane or n-heptane.
    [8" claim-type="Currently amended] 7. The method according to claim 6, wherein the extractant is n-peptane, cyclopentane, n-hexane, cyclohexane or a mixed solvent of n-heptane and ethyl acetate.
    [9" claim-type="Currently amended] The method of claim 7 or 8, wherein the extraction solvent is n-hexane.
    [10" claim-type="Currently amended] The method of claim 1, wherein the extraction solvent is characterized in that 1 to 100ml per 1g of reaction product crystals.
    [11" claim-type="Currently amended] The method of claim 1, wherein the extraction solvent is characterized in that 5 to 20ml per 1g of reaction product crystals.
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    同族专利:
    公开号 | 公开日
    KR100645669B1|2006-11-13|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    法律状态:
    2001-10-04|Application filed by 에스케이 주식회사
    2001-10-04|Priority to KR1020010061179A
    2003-04-11|Publication of KR20030028892A
    2006-11-13|Application granted
    2006-11-13|Publication of KR100645669B1
    优先权:
    申请号 | 申请日 | 专利标题
    KR1020010061179A|KR100645669B1|2001-10-04|2001-10-04|Method for preparing trimethylhydroquinoneTMHQ diester with high yield and high purity|
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