WO2022246861A1 - 乙酰磺胺酸钾的制备方法 - Google Patents

乙酰磺胺酸钾的制备方法 Download PDF

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WO2022246861A1
WO2022246861A1 PCT/CN2021/097009 CN2021097009W WO2022246861A1 WO 2022246861 A1 WO2022246861 A1 WO 2022246861A1 CN 2021097009 W CN2021097009 W CN 2021097009W WO 2022246861 A1 WO2022246861 A1 WO 2022246861A1
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solution
reaction
cyclization
hydrolysis
agent
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PCT/CN2021/097009
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English (en)
French (fr)
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周睿
丁震
陈永旭
杨峰宝
刘刚
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安徽金禾实业股份有限公司
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Application filed by 安徽金禾实业股份有限公司 filed Critical 安徽金禾实业股份有限公司
Priority to PCT/CN2021/097009 priority Critical patent/WO2022246861A1/zh
Priority to CN202180001419.7A priority patent/CN113454074B/zh
Priority to EP21942432.2A priority patent/EP4335841A4/en
Publication of WO2022246861A1 publication Critical patent/WO2022246861A1/zh
Priority to US18/518,796 priority patent/US20240083862A1/en

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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D291/00—Heterocyclic compounds containing rings having nitrogen, oxygen and sulfur atoms as the only ring hetero atoms
    • C07D291/02—Heterocyclic compounds containing rings having nitrogen, oxygen and sulfur atoms as the only ring hetero atoms not condensed with other rings
    • C07D291/06—Six-membered rings
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper
    • B01J23/74—Iron group metals
    • B01J23/745—Iron
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/02—Sulfur, selenium or tellurium; Compounds thereof
    • B01J27/053—Sulfates

Definitions

  • the invention belongs to the technical field of fine chemical manufacturing, and in particular relates to a preparation method of acesulfame potassium.
  • Acesulfame potassium also known as AK sugar
  • AK sugar is a widely used sugar substitute food additive. Its appearance is white crystalline powder.
  • As an organic synthetic salt its taste is similar to sugarcane, and it is easily soluble in water. , Slightly soluble in alcohol, its chemical properties are stable, and it is not easy to break down and fail; it does not participate in the body's metabolism and does not provide energy; it has high sweetness and low price; it has no cariogenicity; it has good stability to heat and acid.
  • the diketene-sulfur trioxide method is widely used.
  • the specific reaction steps include: reacting sulfamic acid with amine to form amine sulfamic acid salt, and then reacting amine sulfamic acid with diketene , forming acetylacetamide salt; in the presence of sulfur trioxide, acetylacetamide salt undergoes a cyclization reaction to form a cyclic sulfur trioxide adduct; the cyclic compound is hydrolyzed to obtain the hydrolyzate (ASH); subsequent oxidation with hydrogen Potassium treatment of the hydrolyzate yields acesulfame potassium (ASK).
  • acetic acid needs to be added as a catalyst in the reaction process, which makes acetic acid impurities remain in the final product acesulfame potassium, resulting in poor color of acesulfame potassium and affecting people's experience in use.
  • the hydrolysis step of cyclic compounds is generally carried out under acidic conditions, which has the disadvantages of low yield of cyclized products, instability and easy decomposition. Although some technologies have been researched on this, there are still problems of low yield and poor quality of final products.
  • Chinese patent document CN107868064A discloses a method for synthesizing acesulfame potassium precursor cyclic compound (ASH) in a microchannel reactor.
  • the reactor carries out cyclization and hydrolysis reactions, and the total product yield is only 45-60%.
  • the disadvantage of this process is that sulfur trioxide is unstable under the reaction conditions, the cyclization reaction speed is not controlled, and side reactions are prone to occur.
  • Chinese patent document CN108191790A discloses a sulfonation microchannel reaction method and device in the production of acesulfame potassium, so that the intermediate raw material and the cyclizing agent raw material are respectively carried out in the first and second cyclization microreactors, and then Exchange heat through a heat exchanger. Because the reaction time is long, the cyclization product is easy to decompose, the yield of the hydrolysis reaction is low, and the finished product yield of acesulfame potassium is low, and the quality of the finished product is relatively poor.
  • the application is proposed so as to provide a kind of preparation method of acesulfame potassium that overcomes the above-mentioned problems or at least partially solves the above-mentioned problems.
  • a kind of preparation method of acesulfame potassium comprising:
  • Sulfonation and cyclization step dissolving sulfur trioxide in a solvent to form a cyclization agent solution; adding the cyclization agent solution to the intermediate solution to carry out sulfonation and cyclization reaction to obtain a cyclization product solution;
  • Hydrolysis step adding a hydrolyzing agent to the cyclization product solution to carry out a hydrolysis reaction to obtain a hydrolyzate solution;
  • Salt-forming step adding potassium hydroxide to the organic phase of the hydrolyzate solution to obtain acesulfame potassium.
  • the solid superacid catalyst is a SO 4 2 ⁇ /M x O y type catalyst, wherein M represents a metal atom.
  • the solid superacid catalyst is a SO 4 2 ⁇ /Fe 2 O 3 type catalyst.
  • the hydrolysis agent is deionized water or ethanol aqueous solution.
  • the hydrolysis agent is an aqueous ethanol solution, wherein the mass concentration of ethanol in the aqueous ethanol solution is 30-65%.
  • the reaction temperature of the hydrolysis reaction is 0-20°C, preferably 10-20°C; the reaction time of the hydrolysis reaction is 30-400s.
  • the ratio of the amount of sulfamic acid to the amount of sulfur trioxide is 4-8:1, preferably 6:1; the solvent is dichloromethane.
  • the ratio of the amount of sulfur trioxide to the amount of water in the hydrolyzing agent is 1:1-4, preferably 1:1-1.5.
  • the specific steps of the intermediate preparation step are:
  • Dissolving sulfamic acid in the first solvent is configured as the first reaction solution
  • Diketene is dissolved in a third solvent to configure a third reaction solution
  • the above method is carried out in a continuous reactor, and the continuous reactor is a fixed bed reactor, a continuous stirred tank reactor or a microchannel reactor.
  • the beneficial effect of the present application is that the present application replaces the traditional organic acid catalyst with a solid superacid catalyst, and the solid superacid catalyst can not only promote the smooth acylation reaction between the ammonium sulfamate solution and diketene, but also provide the efficiency of the acylation reaction; And in the hydrolysis step, instead of using an acidic solution, relying on the acidity provided by the solid super acid, the hydrolysis reaction can be completed quickly in a short time, reducing the impurities remaining in the acesulfame potassium, and making the final product acesulfame potassium better.
  • the idea of the present application is that, due to the presence of acetic acid in the production process of acesulfame potassium, the color of the final product is not good, and because sulfur trioxide and the cyclization product ASH are unstable, the precursor ASH of acesulfame potassium ASK is easy to decompose, The problem of low yield of the final product acesulfame potassium and poor quality of the finished product provides a method for preparing acesulfame potassium with simple process and suitable for continuous large-scale production.
  • the preparation method of acesulfame potassium provided by the application at least includes step S110 to step A140:
  • Intermediate preparation step S110 adding triethylamine to the sulfamic acid solution for amination reaction to generate a sulfamic acid ammonium salt solution; , carry out the acylation reaction to obtain the intermediate solution.
  • the preparation of the intermediate is more carefully divided into two small steps. First, it is the preparation of ammonium sulfamate, and then the intermediate is prepared by reacting ammonium sulfamate with diketene, that is, acetoacetamide-N-sulfonic acid triethyl amine salt.
  • the ammonium salt of sulfamic acid is obtained by adding triethylamine to the sulfamic acid solution for amination reaction.
  • sulfamic acid is dissolved in the first solvent to configure the first reaction solution
  • triethylamine is dissolved in the second solvent to configure the second reaction solution
  • the second The reaction solution is added to the first reaction solution to carry out amination reaction to form a sulfamic acid ammonium salt solution.
  • the first solvent and the second solvent are inert organic solvents that can provide a reaction environment for the amination reaction, such as dichloromethane.
  • Sulfamic acid and triethylamine react exothermicly. During the reaction, the heat generated will vaporize part of the dichloromethane, and the vaporized dichloromethane will leave the reaction system to take away the heat produced. Further, the vaporized dichloromethane Methane can also be recycled.
  • a kind of specific implementation of generating sulfamic acid ammonium salt solution is given below, and this embodiment is only used as an illustration, and the specific production process of sulfamic acid ammonium salt solution can adopt any one in the prior art.
  • the second reaction liquid is added dropwise into the first reaction liquid.
  • the pH value is 7-9, and the reaction is left to stand for 1 hour.
  • the above-mentioned reacted material is ammonium sulfamate solution.
  • solid superacid instead of traditional acetic acid.
  • the solid superacid can provide enough acidic sites for the acylation reaction. On the one hand, it can effectively catalyze the smooth progress of the acylation reaction of ammonium sulfamate and diketene. On the other hand, the solid superacid will not be mixed into the reaction product. No special treatment process is required in the follow-up, which saves post-treatment economy and time costs; and avoids the adverse effects on the product phase of the final product caused by the acetic acid impurities that are not removed in the prior art.
  • diketene is dissolved in a third solvent to prepare a third reaction solution.
  • the third solvent is an inert organic solvent that can provide a reaction environment for the amination reaction, such as dichloromethane.
  • Fill the reactor with a solid superacid catalyst add the ammonium sulfamate solution and the third reaction solution to the reactor in turn, and react under preset conditions to form acetoacetamide-N-sulfonic acid triethylamine salt solution as an intermediate body solution.
  • a continuous reactor can be selected to realize the present application, such as a fixed bed reactor, a continuous stirred tank reactor or a microchannel reactor, etc.
  • the fixed bed reactor is taken as an example to briefly explain the reaction process.
  • the reaction can be ended after the preset reaction time is reached, and the product acetoacetamide-N-sulfonic acid triethylamine salt solution is obtained. Due to the characteristics of the fixed bed reactor, the reaction can be carried out continuously and is suitable for large-scale industrial production.
  • Sulfonation and cyclization step S120 dissolving sulfur trioxide in a solvent to form a cyclization agent solution; adding the cyclization agent solution to the intermediate solution for sulfonation and cyclization reaction to obtain a cyclization product solution.
  • the present application dissolves sulfur trioxide in a solvent to form a cyclizing agent solution.
  • the solvent can be but not limited to an inert organic solvent, such as methylene chloride.
  • the solvent has a stabilizing effect on sulfur trioxide, so that the sulfur trioxide is not easy to sublimate, so that the cyclization reaction proceeds forward.
  • the cyclization agent solution is added to the intermediate solution to carry out sulfonation ring closure reaction to obtain a cyclization product solution.
  • This step reaction is an exothermic reaction, preferably carried out at a lower temperature.
  • the cyclizing agent solution can be gradually dripped into the intermediate solution, and accompanied by Stir to obtain a cyclization product solution, wherein the cyclization product is the precursor ASH of acesulfame potassium.
  • Hydrolysis step S130 adding a hydrolysis agent to the cyclization product solution to carry out a hydrolysis reaction to obtain a hydrolyzate solution.
  • this application uses a hydrolysis agent, which relies on the acidity of a solid superacid to hydrolyze the cyclization product, which can significantly increase the rate of the hydrolysis reaction and shorten the hydrolysis time.
  • the hydrolyzing agent is water or ethanol aqueous solution, and hydrolyzing with a hydrolyzing agent can significantly reduce the content of impurities in the cyclization product ASH, reduce the difficulty of subsequent acesulfame K purification, and reduce the difficulty of acesulfame K purification. the cost of.
  • Salt-forming step S140 adding potassium hydroxide solution to the organic phase of the hydrolyzate solution to obtain acesulfame potassium.
  • This step is a conventional salt-forming step. Specifically, potassium hydroxide solution can be added to the organic phase of the hydrolyzate solution to obtain acesulfame potassium.
  • this application uses a solid superacid catalyst instead of a traditional organic acid catalyst combined with a technical solution to make the final product acesulfame K better, which significantly improves the user experience;
  • the trioxide Sulfur is dissolved in a solvent to form a cyclization agent, and the hydrolysis step is separated from the acidic conditions of the prior art, and the hydrolysis agent is used for hydrolysis, which significantly improves the stability of the precursor cyclization product (ASH) of acesulfame potassium (ASK), making The reaction moves forward, which improves the conversion rate of raw materials, greatly improves the yield of cyclization product (ASH), further improves the yield of final product acesulfame potassium, and reduces the production rate of acesulfame potassium cost.
  • ASH precursor cyclization product
  • ASK acesulfame potassium
  • Solid super acid refers to the acid whose acidity exceeds 100% sulfuric acid. If the Hammett acidity function H is used to represent the acid strength, the H0 value of 100% sulfuric acid is 11.93, and the acid with H0 ⁇ -11.93 is a super acid. Solid superacids are divided into two types, one type contains halogen, fluorine sulfonic acid resin becomes fluoride immobilized compound; the other type does not contain halogen, it is composed of sulfate radicals adsorbed on the surface of metal oxides or hydroxides, burned at high temperature preparation.
  • the type of solid superacid is preferably the latter, that is, SO 4 2- /M x O y type superacid, wherein, M represents a metal atom, specifically Zn, Zr, Ti, Sn, etc.
  • M represents a metal atom, specifically Zn, Zr, Ti, Sn, etc.
  • SO 4 2- /Fe 2 O 3 type superacid catalyst is SO 4 2- /Fe 2 O 3 type superacid catalyst.
  • the hydrolysis agent is deionized water or an aqueous ethanol solution, preferably an aqueous ethanol solution, wherein the mass concentration of ethanol in the aqueous ethanol solution is preferably 30-65%.
  • the inventor used a hydrolysis agent, especially an aqueous solution of ethanol, and controlled the water content in the hydrolysis agent, which can significantly reduce the content of impurities in the acesulfame precursor ASH, and reduce the difficulty of subsequent acesulfame potassium purification. The cost of acesulfame purification is reduced.
  • the application is not limited, the consumption of hydrolyzing agent can be determined according to the consumption of sulfur trioxide, specifically, in some embodiments of the application, the consumption of sulfur trioxide and the content of water in the hydrolyzing agent
  • the ratio of the amount of substances is 1:1-4, in some other embodiments, it is 1:1-1.5. That is to say, the amount of water in the hydrolyzing agent is preferably higher than that of sulfur trioxide.
  • the application is not limited, the consumption of sulfur trioxide can be determined according to the consumption of sulfamic acid, specifically, considering economic factor, in some embodiments of the application, the consumption of sulfamic acid and The ratio of the amount of sulfur trioxide to the amount of substance is 4-8:1, and in some embodiments of the present application, the ratio of the amount of sulfamic acid to the amount of sulfur trioxide is 6:1.
  • the reaction temperature is set at 0-20°C, The middle temperature is 10-20°C; the reaction time is set to 30-400s. That is to say, the hydrolysis reaction step of the present application is preferably carried out at a lower temperature, because dichloromethane can take away a large amount of heat production, therefore, in the present application, temperature control is easier to achieve, using the prior art Any one can be used, such as air condensation technology, circulating water condensation technology and heat exchange plate, etc.
  • the reaction time of the hydrolysis reaction step can be significantly shortened, and the reaction can be completely completed within 30-400s. If the reaction temperature is lower than 0°C and the reaction time is shorter than 30s, the hydrolysis may be incomplete, which will result in incomplete hydrolysis, and some cyclization products cannot be converted, resulting in a low conversion rate of raw materials; if the reaction temperature is higher than 20°C, If the reaction time is longer than 400s, the reaction temperature will be too high, the reaction time will be too long, and the time cost will be increased, and the cyclization product will be easily decomposed, which is not conducive to the development of the reaction towards the hydrolysis reaction.
  • each drug or reagent can be made by a laboratory or factory, or a commercially available product, which is not limited in this application.
  • Preparation of intermediate solution amination reaction steps: dissolve 98kg of sulfamic acid and the first dichloromethane at a molar ratio of 1:6, and control the dissolution temperature at about 20-25°C to obtain dichlorosulfamic acid Methane solution, the first reaction solution.
  • Dissolution can be in a continuous mixing device or in a reactor.
  • Acylation reaction step dissolving diketene and third dichloromethane at a molar ratio of 1:1.5, controlling the dissolution temperature at 10-20° C. to obtain a third reaction solution.
  • the fixed bed reactor After the solid superacid catalyst is installed in the fixed bed reactor, the fixed bed reactor is started, and the circulating water is adjusted to make the circulating water work normally.
  • the amounts of the ammonium sulfonate salt solution and the third reaction solution are such that the molar ratio of sulfamic acid to diketene is 1:1.1. After the reaction starts, lower the temperature of the cooling water as much as possible, and control the temperature of the reaction system at 20-35°C; as the performance of the catalyst declines, the temperature can be slightly increased within the control range.
  • the reduction of hydrolysis reaction time can improve the purity of the product.
  • the final product of acesulfame potassium is generally used for food or medicine, and the impurities are generally measured in ppm. Therefore, the seemingly insignificant increase in purity will improve product quality. All have great benefits.
  • the hydrolysis reaction time of 30-400 seconds was observed to be beneficial to the improvement of purity.
  • the following examples provide the reaction effects under different reaction conditions, especially different hydrolysis times.
  • Example 1 (Example 1A, Example 1B, Example 1C, Example 1D, Example 1E, Example 1F, Example 1G, Example 1H)
  • Preparation of the intermediate solution when preparing the intermediate solution, use the superacid SO 4 2 ⁇ /Fe 2 O 3 as a catalyst, and refer to the preparation of the intermediate solution A for other steps.
  • Sulfonation and cyclization step dissolving sulfur trioxide in dichloromethane to form a cyclization agent solution; adding the cyclization agent solution to the intermediate solution to carry out sulfonation and cyclization reaction to obtain a cyclization product solution.
  • Hydrolysis step adding ethanol aqueous solution as a hydrolysis agent to the cyclization product solution to carry out hydrolysis reaction to obtain a hydrolyzate solution.
  • Salt-forming step adding an ethanol solution of potassium hydroxide to the organic phase of the hydrolyzate solution to obtain acesulfame potassium. Please refer to Table 1 for specific reaction conditions and reaction results.
  • Preparation of the intermediate solution when preparing the intermediate solution, use the superacid SO 4 2 ⁇ /Fe 2 O 3 as a catalyst, and refer to the preparation of the intermediate solution A for other steps.
  • Sulfonation and cyclization step dissolving sulfur trioxide in dichloromethane to form a cyclization agent solution; adding the cyclization agent solution to the intermediate solution to carry out sulfonation and cyclization reaction to obtain a cyclization product solution.
  • Hydrolysis step adding ethanol aqueous solution as a hydrolysis agent to the cyclization product solution to carry out hydrolysis reaction to obtain a hydrolyzate solution.
  • the comparative example 1 was hydrolyzed at a lower temperature than that of Example 1.
  • Salt-forming step adding an ethanol solution of potassium hydroxide to the organic phase of the hydrolyzate solution to obtain acesulfame potassium. Please refer to Table 1 for specific reaction conditions and reaction results.
  • Sulfonation and cyclization step dissolving sulfur trioxide in dichloromethane to form a cyclization agent solution; adding the cyclization agent solution to the intermediate solution to carry out sulfonation and cyclization reaction to obtain a cyclization product solution.
  • Hydrolysis step adding ethanol aqueous solution as a hydrolysis agent to the cyclization product solution to carry out hydrolysis reaction to obtain a hydrolyzate solution.
  • Salt-forming step adding an ethanol solution of potassium hydroxide to the organic phase of the hydrolyzate solution to obtain acesulfame potassium. Please refer to Table 1 for specific reaction conditions and reaction results.
  • Preparation of the intermediate solution when preparing the intermediate solution, use the superacid SO 4 2 ⁇ /Fe 2 O 3 as a catalyst, and refer to the preparation of the intermediate solution A for other steps.
  • Sulfonation and cyclization step dissolving sulfur trioxide in dichloromethane to form a cyclization agent solution; adding the cyclization agent solution to the intermediate solution to carry out sulfonation and cyclization reaction to obtain a cyclization product solution.
  • Hydrolysis step adding ethanol aqueous solution as a hydrolysis agent to the cyclization product solution to carry out hydrolysis reaction to obtain a hydrolyzate solution.
  • the comparative example 1 was hydrolyzed at a lower temperature than that of Example 1.
  • Salt-forming step adding an ethanol solution of potassium hydroxide to the organic phase of the hydrolyzate solution to obtain acesulfame potassium. Please refer to Table 1 for specific reaction conditions and reaction results.
  • Comparative Example 1 Comparative Example 1 (Comparative Example 1A, Comparative Example 1B, Comparative Example 1C, Comparative Example 1D, Comparative Example 1E)
  • Sulfonation and cyclization step dissolving sulfur trioxide in dichloromethane to form a cyclization agent solution; adding the cyclization agent solution to the intermediate solution to carry out sulfonation and cyclization reaction to obtain a cyclization product solution.
  • Hydrolysis step adding water as a hydrolysis agent to the cyclization product solution to carry out a hydrolysis reaction to obtain a hydrolyzate solution.
  • Salt-forming step adding an ethanol solution of potassium hydroxide to the organic phase of the hydrolyzate solution to obtain acesulfame potassium. Please refer to Table 1 for specific reaction conditions and reaction results.
  • the calculation method of acesulfame potassium yield is based on diketene, the ratio of the actual yield of acesulfame potassium to the theoretical yield of acesulfame potassium of diketene.
  • the hydrolysis reaction temperature of implementation of comparative example 1 is lower than that of comparative example 1, and the yield of acesulfame potassium is also significantly lower than that of embodiment, therefore, the hydrolysis reaction temperature is 0 °C - 20°C is an ideal reaction temperature.
  • Comparative Example 1 and Implementation Comparative Example 2 do not use a catalyst when preparing the intermediate solution.
  • the hydrolysis reaction takes a long time (3000s) to complete .
  • comparative example 2 The difference of implementing comparative example 2 with respect to comparative example 1 is that water is used as hydrolyzing agent in comparative example 1, and ethanol water is used as hydrolyzing agent in implementing comparative example 2, from implementing comparative example 2A and comparative example 1A, implementing comparative example Ratio 2B and comparative example 1B and implementation comparative example 2D and comparative example 1E can find out, under other conditions being all the same, adopt ethanol water as hydrolyzing agent, acesulfame potassium yield is all higher than adopting water as the implementation of hydrolyzing agent example.
  • embodiment 1 has adopted solid superacid SO 4 2- /Fe 2 O 3 as catalyst, from reaction time, has adopted solid superacid as catalyst, can significantly promote the carrying out of follow-up hydrolysis reaction, improve Reaction efficiency, shorten the hydrolysis reaction time.
  • Example 1 when the solid superacid SO 4 2- /Fe 2 O 3 is used as the catalyst and the ethanol aqueous solution is used as the hydrolysis agent, the reaction can be completed in a very short time.
  • the highest yield of honey can reach 95.4%.
  • the difference between implementation comparative example 3 and embodiment 1 is that the ratio of water in sulfur trioxide and hydrolyzing agent is different, and the ratio of water in sulfur trioxide and hydrolyzing agent is In the case of 3:1 ⁇ 4:1, the yield of acesulfame potassium has decreased.
  • hydrolyzing agent water or ethanol aqueous solution
  • water or ethanol aqueous solution can make the crude product of acesulfame potassium of higher purity, and its purity can reach more than 90%; further, use the aqueous solution of ethanol and control its water content, It can significantly reduce the amount of impurities in the acesulfame precursor ASH, that is, reduce the content of impurities in the final product acesulfame potassium, and reduce the difficulty and cost of subsequent acesulfame potassium purification.
  • using the aqueous solution of ethanol as a hydrolyzing agent can reduce the impurity content of acesulfame potassium and obtain a high-quality crude product of acesulfame potassium.
  • the inventor found that when using a solid superacid as a catalyst, the hydrolysis reaction time can be effectively reduced; with the reduction of the hydrolysis time, the reduction of the impurity content that may be produced by hydrolysis, Therefore, the use of solid superacid catalysts can maintain the high quality and high efficiency of the reaction at higher temperatures (0-20°C).
  • the color does not appear as conventional In the case of medicinal or high-grade food, it significantly improves the user experience and improves the value of the product; on the other hand, dissolving sulfur trioxide in the solvent forms a cyclization agent, in the hydrolysis step from the acidic conditions of the prior art, the hydrolysis agent is used to hydrolyze, which significantly improves the stability of the precursor cyclization product (ASH) of acesulfame potassium (ASK), makes the reaction move forward, and improves the The conversion rate of the raw material greatly improves the yield of the cyclization product (ASH), further improves the yield of the final product acesulfame potassium, and reduces the production cost of acesulfame potassium.
  • ASH precursor cyclization product
  • ASK acesulfame potassium

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Abstract

一种乙酰磺胺酸钾的制备方法，包括：在氨基磺酸溶液中加入三乙胺，进行胺化反应，生成氨基磺酸铵盐溶液；向得到的氨基磺酸铵盐溶液加入双乙烯酮，在固态超强酸催化剂的作用下，进行酰化反应，得到中间体溶液；将三氧化硫溶解在溶剂中，形成环化剂溶液；将环化剂溶液加入中间体溶液，进行磺化环合反应，得到环合产物溶液；在环合产物溶液中加入水解剂，进行水解反应，得到水解产物溶液；在水解产物溶液的有机相中加入氢氧化钾溶液，得到乙酰磺胺酸钾。上述方法能够降低安赛蜜中杂质含量，使得安赛蜜品相更好，且提高了原料的转化率，极大程度上提高了环化产物的产率，进一步的，提高了终产物安赛蜜的收率，降低了安赛蜜的生产成本。

Description

乙酰磺胺酸钾的制备方法 技术领域
本发明属于精细化工制造技术领域，具体涉及一种乙酰磺胺酸钾的制备方法。
发明背景
乙酰磺胺酸钾(安赛蜜)又称AK糖，是一种广泛使用的代糖食品添加剂，外观为白色结晶性粉末，它作为一种有机合成盐，其口味与甘蔗相似，易溶于水，微溶于酒精，其化学性质稳定，不易出现分解失效现象；不参与机体代谢，不提供能量；甜度较高，价格便宜；无致龋齿性；对热和酸稳定性好。
目前在安赛蜜的合成中，普遍采用双乙烯酮-三氧化硫法，其具体的反应步骤包括：使氨基磺酸与胺反应以形成氨基磺酸胺盐，然后将氨基磺酸胺盐与双乙烯酮反应，形成乙酰基乙酰胺盐；在三氧化硫存在下，乙酰基乙酰胺盐发生环化反应，形成环状三氧化硫加合物；将环状化合物水解获得水解产物(ASH)；随后用氢氧化钾处理水解产物从而获得乙酰磺胺酸钾(ASK)。
一方面，在反应过程中需要加入乙酸作为催化剂，这使得乙酸杂质会留存在最终产品安赛蜜中，导致安赛蜜成色不好，影响人们的使用感受。
另一方面，环状化合物水解步骤目前一般在酸性条件下进行水解，存在着环化产物产率低，且不稳定、易分解的缺陷。虽然也有一些技术对此进行了研究，但是仍然存在着产率低、最终产品质量差的问题。
如中国专利文献CN107868064A公开了一种微通道反应器中合成安赛蜜前体环状化合物(ASH)的方法，该申请主要是将一定浓度的反应中间体酰化剂和环化剂通过微通道反应器进行环化和水解反应，其产品总收率仅为45-60％，此工艺的缺点是在反应条件下三氧化硫不稳定，环合反应速度未进行控制，易发生副反应。
又如，中国专利文献CN108191790A公开了一种安赛蜜生产中磺化微通道反应方法及装置，使中间体原料和环化剂原料分别在第一和第二环合微反应器中进行，再经换热器换热。由于反应时间长，环化产物易分解，水解反应的收率较低，制得的乙酰磺胺酸钾成品收率较低，成品质量较差。
发明内容
鉴于上述问题，提出了本申请以便提供一种克服上述问题或者至少部分地解决 上述问题的一种乙酰磺胺酸钾的制备方法。
根据本申请的一方面，提供了一种乙酰磺胺酸钾的制备方法，包括：
中间体制备步骤：在氨基磺酸溶液中加入三乙胺，进行胺化反应，生成氨基磺酸铵盐溶液；向得到的氨基磺酸铵盐溶液加入双乙烯酮，在固态超强酸催化剂的作用下，进行酰化反应，得到中间体溶液；
磺化环合步骤：将三氧化硫溶解在溶剂中，形成环化剂溶液；将环化剂溶液加入中间体溶液，进行磺化环合反应，得到环合产物溶液；
水解步骤：在环合产物溶液中加入水解剂，进行水解反应，得到水解产物溶液；和
成盐步骤：在水解产物溶液的有机相中加入氢氧化钾，得到乙酰磺胺酸钾。
可选的，在上述方法中，固态超强酸催化剂为SO 4 2-/M xO y型催化剂，其中，M表示金属原子。
可选的，在上述方法中，固态超强酸催化剂为SO 4 2-/Fe 2O 3型催化剂。
可选的，在上述方法中，水解剂为去离子水或乙醇水溶液。
可选的，在上述方法中，水解剂为乙醇水溶液，其中，乙醇水溶液中乙醇的质量浓度为30～65％。
可选的，在上述方法中，水解反应的反应温度为0-20℃，优选10-20℃；水解反应的反应时间为30-400s。
可选的，在上述方法中，氨基磺酸的用量与三氧化硫的用量的物质的量的比为4～8:1，优选6:1；溶剂为二氯甲烷。
可选的，在上述方法中，三氧化硫的用量与水解剂中水的含量的物质的量的比为1:1-4，优选1:1-1.5。
可选的，在上述方法中，中间体制备步骤的具体步骤为：
在氨基磺酸溶解在第一溶剂中，配置成第一反应液；
将三乙胺溶于第二溶剂，配置成第二反应液，将第二反应液加入第一反应液中进行胺化反应，形成氨基磺酸铵盐溶液；
将双乙烯酮溶于第三溶剂，配置成第三反应液；和
在反应器中装填固态超强酸催化剂，依次向反应器加入氨基磺酸铵盐溶液和第三反应液，在预设条件下反应，形成乙酰乙酰胺-N-磺酸三乙胺盐溶液作为中间体溶液。
可选的，上述方法是在连续反应器中进行的，连续反应器为固定床反应器、连续搅拌釜反应器或微通道反应器。
本申请的有益效果在于，本申请通过将采用固态超强酸催化剂代替传统的有机酸催化剂，固态超强酸催化剂不仅能够促进氨基磺酸铵盐溶液与双乙烯酮顺利进行酰化反应，提供酰化反应效率；且在水解步骤中，可不使用酸性溶液，依赖固态超强酸提供的酸性，能够使得水解反应在短时间内快速完成，减少残留在安赛蜜中的杂质，使得最终产品安赛蜜品相更好，显著提升了用户的使用感受；另一方面，将三氧化硫溶解于溶剂中形成环化剂，提高了三氧化硫和安赛蜜(ASK)的前驱体环化产物(ASH)的稳定性，使得反应向正向移动，提高了原料的转化率，极大程度上提高了环化产物(ASH)的产率，进一步的，提高了终产物安赛蜜的收率，降低了安赛蜜的生产成本。
上述说明仅是本申请技术方案的概述，为了能够更清楚了解本申请的技术手段，而可依照说明书的内容予以实施，并且为了让本申请的上述和其它目的、特征和优点能够更明显易懂，以下特举本申请的具体实施方式。
实施本发明的方式
下面将更详细地描述本申请的示例性实施例。应当理解，可以以各种形式实现本申请而不应被这里阐述的实施例所限制。相反，提供这些实施例是为了能够更透彻地理解本申请，并且能够将本申请的范围完整的传达给本领域的技术人员。
本申请的构思在于，针对安赛蜜生产过程中由于乙酸的存在，使得最终产品成色不佳，另由于三氧化硫和环化产物ASH不稳定，造成安赛蜜ASK的前驱体ASH容易分解，使得最终产物安赛蜜的收率低、成品质量差的问题，提供了一种工艺简单、适合连续大规模生产的乙酰磺胺酸钾的制备方法。
本申请提供的乙酰磺胺酸钾的制备方法至少包括了步骤S110～步骤A140：
中间体制备步骤S110：在氨基磺酸溶液中加入三乙胺，进行胺化反应，生成氨基磺酸铵盐溶液；向得到的氨基磺酸铵盐溶液加入双乙烯酮，在固态超强酸催化剂的作用下，进行酰化反应，得到中间体溶液。
中间体的制备更细致地分为两个小步骤，首先，是氨基磺酸铵盐的制备，然后利用氨基磺酸铵盐与双乙烯酮反应制备中间体，即乙酰乙酰胺-N-磺酸三乙胺盐。
氨基磺酸铵盐采用的是在氨基磺酸溶液中加入三乙胺，进行胺化反应获得。具 体的，在本申请的一些实施例中，在氨基磺酸溶解在第一溶剂中，配置成第一反应液；将三乙胺溶于第二溶剂，配置成第二反应液，将第二反应液加入第一反应液中进行胺化反应，形成氨基磺酸铵盐溶液。第一溶剂和第二溶剂是能够为胺化反应提供反应环境的惰性有机溶剂，如二氯甲烷。氨基磺酸和三乙胺放热反应，在反应过程中，产生的热量会将部分二氯甲烷汽化，汽化后的二氯甲烷会离开反应体系将产热带走，进一步地，汽化后的二氯甲烷也可循环利用。
在第一反应液与第二反应液混合的时候，最好将第二反应液逐渐滴入第一反应液，这样能够使得反应更加充分，不会造成局部反应物浓度过大，反应程度过于剧烈。
以下给出一种生成氨基磺酸铵盐溶液的具体实施方式，该实施方式仅作为示例性说明，氨基磺酸铵盐溶液的具体生产工艺可采用现有技术中的任意一种。按照预设的氨基磺酸、第一二氯甲烷、三乙胺和第二二氯甲烷的用量比准确称料，打开反应度的计量槽阀门向干燥的反应釜中加入第一二氯甲烷，启动搅拌及循环泵；从投料孔投入氨基磺酸。关闭循环阀门，打开送料阀门，将溶料釜中混合物料送至干燥的合成釜中，利用循环水降温，待反应釜温度降至室温(约20-25℃)，得到第一反应液。
同上述过程，得到三乙胺溶于二氯甲烷的第二反应液。
将第二反应液滴加入第一反应液中，滴加结束时，pH值为7-9，静置反应1小时，上述反应完毕的物料为氨基磺酸铵盐溶液。
在得到氨基磺酸溶液后，将氨基磺酸溶液与双乙烯酮反应，得到乙酰乙酰胺-N-磺酸三乙胺盐，作为制备安赛蜜的中间体。
现有技术中，氨基磺酸溶液与双乙烯酮反应是在乙酸的环境中进行的，在后续步骤中，乙酸导致的副产物很难从最终产物安赛蜜中被完全除去，残留在安赛蜜中的乙酸导致的副产物不仅会使安赛蜜成色不佳，而且还会带来异味。
在本申请中，采用固体超强酸代替传统的乙酸有效的克服了这个问题。固体超强酸能够为酰化反应提供足够的酸性位点，一方面能够有效地催化剂氨基磺酸铵盐和双乙烯酮酰化反应的顺利进行，另一方面，固体超强酸不会混合到反应产物中，后续不用特殊的处理工艺，节约了后处理经济和时间成本；且避免了现有技术中没有除掉的乙酸杂质留存在最终产物中对最终产物的品相造成的不利影响。
为了提高双乙烯酮的闪点，将双乙烯酮溶于第三溶剂中，配置成第三反应液， 第三溶剂是能够为胺化反应提供反应环境的惰性有机溶剂，如二氯甲烷等。在反应器中装填固态超强酸催化剂，依次向反应器加入氨基磺酸铵盐溶液和第三反应液，在预设条件下反应，形成乙酰乙酰胺-N-磺酸三乙胺盐溶液作为中间体溶液。
为了实现反应的连续性，在本申请的一些实施例中，可以选择连续反应器来实现本申请，如固定床反应器、连续搅拌釜反应器或微通道反应器等。这里以固定床反应器为例，简要说明反应过程。
在固定床反应器中装填固体超强酸作为催化剂，将固定床反应器设置为预设的工作状态，先向固定床反应器通入氨基磺酸铵盐溶液，待氨基磺酸铵盐溶液正常流动后，然后再同向通入第三反应液，通过控制二者的流速，使得二者接触时间在预设条件内，同时，通过控制固定床反应器的换热装置，使得反应温度也在预设条件内，待达到预设反应时长，即可结束反应，得到产物乙酰乙酰胺-N-磺酸三乙胺盐溶液。由于固定床反应器的特点，使得本反应能够连续不断进行，适合大规模的工业生产。
磺化环合步骤S120：将三氧化硫溶解在溶剂中，形成环化剂溶液；将环化剂溶液加入中间体溶液，进行磺化环合反应，得到环合产物溶液。
区别于现有技术中直接使用三氧化硫，本申请将三氧化硫溶解在溶剂中，形成环化剂溶液，溶剂可为但不限于惰性有机溶剂，如二氯甲烷等。溶剂对三氧化硫具有稳定作用，使得三氧化硫不易升华，从而环化反应正向进行。
将环化剂溶液加入中间体溶液，进行磺化环合反应，得到环合产物溶液。该步反应为放热反应，最好在较低的温度下进行，为了增强反应可控性，不至于使得局部反应过于激烈，可以将环化剂溶液逐渐滴入到中间体溶液中，并伴随搅拌，获得环合产物溶液，其中环合产物为安赛蜜的前驱体ASH。
水解步骤S130：在环合产物溶液中加入水解剂，进行水解反应，得到水解产物溶液。
不同于传统工艺上采用酸性溶液进行水解反应，本申请采用水解剂，依赖固态超强酸的酸性进行环合产物的水解，能够显著提升水解反应的速率，缩短水解时间，伴随着水解时间降低的是水解可能产生的杂质含量的减少。在本申请的一些实施例中，水解剂为水或者乙醇水溶液，使用水解剂进行水解能够显著减少环化产物ASH中杂质的含量，降低了后续安赛蜜提纯的难度，减少了安赛蜜提纯的成本。
成盐步骤S140：在水解产物溶液的有机相中加入氢氧化钾溶液，得到乙酰磺 胺酸钾。
该步骤为常规的成盐步骤，具体的，可以在水解产物溶液的有机相中加入氢氧化钾溶液，即可得到乙酰磺胺酸钾。
综上所述，本申请通过将采用固态超强酸催化剂代替传统的有机酸催化剂结合技术方案，使得最终产品安赛蜜品相更好，显著提升了用户的使用感受；另一方面，将三氧化硫溶解于溶剂中形成环化剂，在水解步骤脱离现有技术的酸性条件，采用水解剂进行水解，显著提高了安赛蜜(ASK)的前驱体环化产物(ASH)的稳定性，使得反应向正向移动，提高了原料的转化率，极大程度上提高了环化产物(ASH)的产率，进一步的，提高了终产物安赛蜜的收率，降低了安赛蜜的生产成本。
固态超强酸催化剂的种类
固体超强酸是指酸性超过100％硫酸的酸，如用Hammett酸度函数H表示酸强度，100％硫酸的H0值为11.93，H0<-11.93的酸就是超强酸。固体超强酸分为两类，一类含卤素、氟磺酸树脂成氟化物固载化物；另一类不含卤素，它由吸附在金属氧化物或氢氧化物表面的硫酸根，经高温燃烧制备。在本申请中，固体超强酸的种类最好为后者，即SO 4 2-/M xO y型超强酸，其中，M表示金属原子，具体可以为Zn、Zr、Ti、Sn等，最好为SO 4 2-/Fe 2O 3型超强酸催化剂。
在本申请中，对固体超强酸催化剂的用量不作限制，可依据反应器的规格确定。
水解剂的种类和用量
在本申请的一些实施例中，在上述方法中，水解剂为去离子水或乙醇水溶液，最好为乙醇的水溶液，其中，在乙醇水溶液中，乙醇的质量浓度最好为30～65％。发明人经过大量的实验，使用水解剂，尤其是乙醇的水溶液并控制水解剂中水的含量，可以明显地减少安赛蜜前驱体ASH中杂质的含量，降低了后续安赛蜜提纯的难度，减少了安赛蜜提纯的成本。
对于水解剂的用量，本申请不作限制，水解剂的用量可以根据三氧化硫的用量来确定，具体的，在本申请的一些实施例中，三氧化硫的用量与水解剂中水的含量的物质的量的比为1:1-4，在另一些实施例中，为1:1-1.5。也就是说水解剂中水的物质的量最好高于三氧化硫的物质的量。
三氧化硫的用量
对于三氧化硫的用量，本申请不作限制，三氧化硫的用量可以根据氨基磺酸的用量进行确定，具体的，考虑到经济因素，在本申请的一些实施例中，氨基磺酸的 用量与三氧化硫的用量的物质的量的比为4～8:1，在本申请的一些实施例中，氨基磺酸的用量与三氧化硫的用量的物质的量的比为6:1。
水解反应条件
在本申请中，对于水解反应条件不作限制，凡是能满足水解反应需求均可；在本申请的一些实施例中，在水解反应步骤中，反应温度设为0-20℃，在又一些实施例中为10-20℃；反应时间设为30-400s。也就是说，本申请的水解反应步骤优选在较低的温度进行，由于二氯甲烷能够带走大量的产热，因此，本申请中，温控是较容易实现的，采用现有技术中的任意一种即可，如空气冷凝技术、循环水冷凝技术以及热量交换板等。由于本申请的采用了固态超强酸催化剂，能够显著缩短水解反应步骤的反应时间，在30-400s即可较为彻底地完成反应。若反应温度低于0℃，反应时间短于30s，则水解可能不完全，则会造成水解程度不彻底，一些环合产物不能得到转化，造成原料转化率低；若反应温度高于20℃，反应时间长于400s，则反应温度过高，反应时间过长，增加时间成本，且环合产物容易分解，不利于反应向水解反应方向发展。
对于上述其他未提及的反应物料的用量以及反应条件，均可参考现有技术，如在中国专利文献CN112142687A中，氨基磺酸和双乙烯酮的摩尔比例n(氨基磺酸)：n(双乙烯酮)：n(三乙胺)＝1：1.0-3.0：1.0-4.0；酰化反应温度为-40-15℃；其滴加时间10min-300min；其反应时间1-15h等。
药品或试剂来源
在本申请中，各药品或试剂均可采用实验室或者工厂自制，也可采用市售产品，本申请不作限制。
中间体溶液的制备：胺化反应步骤：将98kg氨基磺酸和第一二氯甲烷以摩尔比为1：6的比例溶解，控制溶解温度约为20-25℃，获得氨基磺酸的二氯甲烷溶液，即第一反应液。溶解可以在连续混合装置中，也可以在反应釜中。
将三乙胺和第二二氯甲烷以摩尔比为1：1的比例溶解，控制溶解的温度为10-30℃，得到第二反应液，其中，氨基磺酸和三乙胺的质量比为1:1.2。将第二反应液逐渐滴加在第一反应液所在的反应釜中进行混合搅拌，控制体系温度为20-30℃，并控制体系呈弱碱性，混合均匀后，即得到氨基磺酸铵盐溶液。
酰化反应步骤：将双乙烯酮和第三二氯甲烷以摩尔比为1：1.5的比例溶解，控制溶解的温度为10-20℃，得到第三反应液。
将固体超强酸催化剂安装至固定床反应器后，启动固定床反应器，调节循环水使循环水工作正常。
将氨基磺酸铵盐溶液通入固定床反应器内，在氨基磺酸铵盐溶液正常流动后，将第三反应液与氨基磺酸铵盐溶液同向通入固定床反应器内，控制氨基磺酸铵盐溶液和第三反应液的量，使得氨基磺酸和双乙烯酮摩尔比为1：1.1。在反应开始后，尽量调低冷却水温度，反应体系的温度控制在20-35℃；随着催化剂性能的衰退，温度在控制范围内可以略微升高。
在本申请中各实施例和对比例的中间体溶液如无特别说明，均采用上述方法制得，如有特殊说明，遵循特殊说明。
水解反应时间的减少，能够提高了产物的纯净度，最终产物乙酰磺胺酸钾一般是食用或者药用，杂质一般是以ppm计，因此，看起来微不足道的纯净度的提高，对于产品质量的提升都是有极大的好处的。30-400秒的水解反应时间观察到是有利于纯净度的提高。下述实施例给出了不同反应条件下，尤其是不同水解时间下的反应效果。
实施例1(实施例1A、实施例1B、实施例1C、实施例1D、实施例1E、实施例1F、实施例1G、实施例1H)
中间溶液的制备：在制备中间溶液时，使用超强酸SO 4 2-/Fe 2O 3作为催化剂，其他步骤参照中间体溶液A的制备。
磺化环合步骤：将三氧化硫溶解在二氯甲烷中，形成环化剂溶液；将环化剂溶液加入中间体溶液，进行磺化环合反应，得到环合产物溶液。
水解步骤：在环合产物溶液中加入乙醇水溶液作为水解剂，进行水解反应，得到水解产物溶液。
成盐步骤：在水解产物溶液的有机相中加入氢氧化钾的乙醇溶液，得到乙酰磺胺酸钾。具体反应条件和反应结果请参照表1。
实施对比例1(包括实施对比例1A、实施对比例1B、实施对比例1C)
中间溶液的制备：在制备中间溶液时，使用超强酸SO 4 2-/Fe 2O 3作为催化剂， 其他步骤参照中间体溶液A的制备。
磺化环合步骤：将三氧化硫溶解在二氯甲烷中，形成环化剂溶液；将环化剂溶液加入中间体溶液，进行磺化环合反应，得到环合产物溶液。
水解步骤：在环合产物溶液中加入乙醇水溶液作为水解剂，进行水解反应，得到水解产物溶液。实施对比例1相对于实施例1在更低的温度下进行水解。
成盐步骤：在水解产物溶液的有机相中加入氢氧化钾的乙醇溶液，得到乙酰磺胺酸钾。具体反应条件和反应结果请参照表1。
实施对比例2(实施对比例2A、实施对比例2B、实施对比例2C、实施对比例2D、实施对比例2E、实施对比例2F、实施对比例2G、实施对比例2H)
中间溶液的制备：在制备中间溶液时，不使用催化剂，其他步骤参照中间体溶液A的制备。
磺化环合步骤：将三氧化硫溶解在二氯甲烷中，形成环化剂溶液；将环化剂溶液加入中间体溶液，进行磺化环合反应，得到环合产物溶液。
水解步骤：在环合产物溶液中加入乙醇水溶液作为水解剂，进行水解反应，得到水解产物溶液。
成盐步骤：在水解产物溶液的有机相中加入氢氧化钾的乙醇溶液，得到乙酰磺胺酸钾。具体反应条件和反应结果请参照表1。
实施对比例3(实施对比例3A、实施对比例3B)
中间溶液的制备：在制备中间溶液时，使用超强酸SO 4 2-/Fe 2O 3作为催化剂，其他步骤参照中间体溶液A的制备。
磺化环合步骤：将三氧化硫溶解在二氯甲烷中，形成环化剂溶液；将环化剂溶液加入中间体溶液，进行磺化环合反应，得到环合产物溶液。
水解步骤：在环合产物溶液中加入乙醇水溶液作为水解剂，进行水解反应，得到水解产物溶液。实施对比例1相对于实施例1在更低的温度下进行水解。
成盐步骤：在水解产物溶液的有机相中加入氢氧化钾的乙醇溶液，得到乙酰磺胺酸钾。具体反应条件和反应结果请参照表1。
对比例1(对比例1A、对比例1B、对比例1C、对比例1D、对比例1E)
中间溶液的制备：在制备中间溶液时，不使用催化剂，其他步骤参照中间体溶液A的制备。
磺化环合步骤：将三氧化硫溶解在二氯甲烷中，形成环化剂溶液；将环化剂溶液加入中间体溶液，进行磺化环合反应，得到环合产物溶液。
水解步骤：在环合产物溶液中加入水作为水解剂，进行水解反应，得到水解产物溶液。
成盐步骤：在水解产物溶液的有机相中加入氢氧化钾的乙醇溶液，得到乙酰磺胺酸钾。具体反应条件和反应结果请参照表1。
表1：
Figure PCTCN2021097009-appb-000001
注：安赛蜜收率的计算方法是以双乙烯酮为基础，乙酰磺胺酸钾实际产量与双乙烯酮的乙酰 磺胺酸钾的理论产量的比值。
从对比例1和实施对比例1可以看出，实施对比例1相对于对比例1的水解反应温度低，安赛蜜的收率也明显低于实施例，因此，水解反应温度为0℃-20℃是比较理想的反应温度。
从对比例1和实施对比例2可以看出，对比例1和实施对比例2在制备中间体溶液时不使用催化剂，从表1中可以看出，水解反应需要较长时间(3000s)才能完成。
实施对比例2相对于对比例1的区别在于，在对比例1中采用水作为水解剂，而在实施对比例2使用了乙醇水作为水解剂，从实施对比例2A和对比例1A、实施对比例2B和对比例1B和实施对比例2D和对比例1E可以看出，在其他条件均相同的情况下，采用乙醇水作为水解剂，安赛蜜收率均高于采用水作为水解剂的实施例。
相对于实施对比例2，实施例1采用了固体超强酸SO 4 2-/Fe 2O 3作为催化剂，从反应时间看，采用了固体超强酸作为催化剂，能够显著促进后续水解反应的进行，提高反应效率，缩短水解反应时间。
从实施例1可以看出，在同时采用固体超强酸SO 4 2-/Fe 2O 3作为催化剂，和乙醇水溶液作为水解剂的情况下，在极短的时间内，反应即可完成，安赛蜜的收率最高可以达到95.4％。
从实施例1和实施对比例3可以看出，实施对比例3与实施例1的不同之处在于三氧化硫与水解剂中水的比例不同，在三氧化硫与水解剂中水的比例为3:1～4:1的情况下，安赛蜜的收率是有所下降的。
上述各实施例中，每组反应结束后，采用相同的成盐工艺，加入氢氧化钾溶液，具体为氢氧化钾的乙醇溶液，成盐并分离得到安赛蜜粗产品，采用高效液相色谱法对安赛蜜的纯度进行测试。经过测试，第一组反应物中的安赛蜜纯度平均为93.3％，第二组反应物中安赛蜜纯度平均为98.2％，第三组反应物种安赛蜜的平均纯度为98.8％。从结果可以看出，使用水解剂(水或者乙醇水溶液)能使得到较高纯度的安赛蜜粗产品，其纯度可达到90％以上；更进一步的，使用乙醇的水溶液并控制其含水量，可以明显的减少安赛蜜前驱体ASH中杂质的量，即降低了最终产品安赛蜜中杂质的含量，降低了后续安赛蜜提纯的难度和成本。由此可见，使用乙醇的水溶液作为水解剂，可以降低安赛蜜的杂质含量，得到高品质的安赛蜜粗产品。
综上所述，通过发明人的反复实验，发明人发现在使用固体超强酸作为催化剂的情况下，水解反应时间可以有效减少；伴随着水解时间降低的是，水解可能产生的杂质含量的减少，因此，使用固体超强酸催化剂可以使得在较高温度(0-20℃)条件下维持反应的高质量、高效进行。
在连续化生产中，反应速度慢对于同等的产量需要更大型的反应设备和更多的反应物投入，这对于生产不经济、并且大量的反应物意味着更高的风险，时间维持更久在综合考虑收率、杂质等情况下并不是有利的。因此，本申请通过将采用固态超强酸催化剂代替传统的有机酸催化剂结合技术方案，降低了水解反应时间，使得最终产品安赛蜜品相更好，在一次精制的条件下，颜色不是呈现为常规的棕黄色，而是显示为浅黄色，对于药用或者高等级食品等情况下，显著提升了用户的使用感受，提高产品的价值；另一方面，将三氧化硫溶解于溶剂中形成环化剂，在水解步骤脱离现有技术的酸性条件，采用水解剂进行水解，显著提高了安赛蜜(ASK)的前驱体环化产物(ASH)的稳定性，使得反应向正向移动，提高了原料的转化率，极大程度上提高了环化产物(ASH)的产率，进一步的，提高了终产物安赛蜜的收率，降低了安赛蜜的生产成本。
以上所述，仅为本申请的具体实施方式，在本申请的上述教导下，本领域技术人员可以在上述实施例的基础上进行其他的改进或变形。本领域技术人员应该明白，上述的具体描述只是更好的解释本申请的目的，本申请的保护范围应以权利要求的保护范围为准。
此外，本领域的技术人员能够理解，尽管在此所述的一些实施例包括其它实施例中所包括的某些特征而不是其它特征，但是不同实施例的特征的组合意味着处于本申请的范围之内并且形成不同的实施例。例如，在下面的权利要求书中，所要求保护的实施例的任意之一都可以以任意的组合方式来使用。

Claims (10)

  1. 一种乙酰磺胺酸钾的制备方法，其特征在于，包括：
    中间体制备步骤：在氨基磺酸溶液中加入三乙胺，进行胺化反应，生成氨基磺酸铵盐溶液；向得到的氨基磺酸铵盐溶液加入双乙烯酮，在固态超强酸催化剂的作用下，进行酰化反应，得到中间体溶液；
    磺化环合步骤：将三氧化硫溶解在溶剂中，形成环化剂溶液；将所述环化剂溶液加入所述中间体溶液，进行磺化环合反应，得到环合产物溶液；
    水解步骤：在所述环合产物溶液中加入水解剂，进行水解反应，得到水解产物溶液；和
    成盐步骤：在所述水解产物溶液的有机相中加入氢氧化钾，得到乙酰磺胺酸钾。
  2. 根据权利要求1所述的方法，其特征在于，所述固态超强酸催化剂为SO 4 2-/M xO y型催化剂，其中，M表示金属原子。
  3. 根据权利要求2所述的方法，其特征在于，所述固态超强酸催化剂为SO 4 2-/Fe 2O 3型催化剂。
  4. 根据权利要求1所述的方法，其特征在于，所述水解剂为去离子水或乙醇水溶液。
  5. 根据权利要求4所述的方法，其特征在于，所述水解剂为乙醇水溶液，其中，所述乙醇水溶液中乙醇的质量浓度为30～65％。
  6. 根据权利要求1所述的方法，其特征在于，所述水解反应的反应温度为0-20℃，更优选10-20℃；所述水解反应的反应时间为30-400s。
  7. 根据权利要求1所述的方法，其特征在于，所述氨基磺酸的用量与所述三氧化硫的用量的物质的量的比为4～8:1，优选6:1；
    所述溶剂为二氯甲烷。
  8. 根据权利要求1所述的方法，其特征在于，所述三氧化硫的用量与所述水解剂中水的含量的物质的量的比为1:1-4，优选1:1-1.5。
  9. 根据权利要求1所述的方法，其特征在于，所述中间体制备步骤的具体步骤为：
    在氨基磺酸溶解在第一溶剂中，配置成第一反应液；
    将三乙胺溶于第二溶剂，配置成第二反应液，将第二反应液加入第一反应液中 进行胺化反应，形成氨基磺酸铵盐溶液；
    将双乙烯酮溶于第三溶剂，配置成第三反应液；和
    在反应器中装填固态超强酸催化剂，依次向所述反应器加入所述氨基磺酸铵盐溶液和所述第三反应液，在预设条件下反应，形成乙酰乙酰胺-N-磺酸三乙胺盐溶液作为中间体溶液。
  10. 根据权利要求1～9中任一项所述的方法，其特征在于，所述方法是在连续反应器中进行的，所述连续反应器为固定床反应器、连续搅拌釜反应器或微通道反应器。
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