WO2023193430A1 - 一种异山梨醇的制备方法 - Google Patents

一种异山梨醇的制备方法 Download PDF

Info

Publication number
WO2023193430A1
WO2023193430A1 PCT/CN2022/129714 CN2022129714W WO2023193430A1 WO 2023193430 A1 WO2023193430 A1 WO 2023193430A1 CN 2022129714 W CN2022129714 W CN 2022129714W WO 2023193430 A1 WO2023193430 A1 WO 2023193430A1
Authority
WO
WIPO (PCT)
Prior art keywords
molecular sieve
isosorbide
deionized water
hours
solution
Prior art date
Application number
PCT/CN2022/129714
Other languages
English (en)
French (fr)
Inventor
李素英
赵晓培
唐春晖
付吉明
柴光臻
燕兰亭
李中峰
云维采
郝寅秀
Original Assignee
山东天力药业有限公司
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 山东天力药业有限公司 filed Critical 山东天力药业有限公司
Publication of WO2023193430A1 publication Critical patent/WO2023193430A1/zh

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D493/00—Heterocyclic compounds containing oxygen atoms as the only ring hetero atoms in the condensed system
    • C07D493/02—Heterocyclic compounds containing oxygen atoms as the only ring hetero atoms in the condensed system in which the condensed system contains two hetero rings
    • C07D493/04—Ortho-condensed systems
    • 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
    • B01J29/00—Catalysts comprising molecular sieves
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/50—Catalysts, in general, characterised by their form or physical properties characterised by their shape or configuration
    • B01J35/51—Spheres
    • 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
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/60—Catalysts, in general, characterised by their form or physical properties characterised by their surface properties or porosity
    • B01J35/64—Pore diameter
    • B01J35/647—2-50 nm
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/06—Washing
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/08—Heat treatment
    • B01J37/082—Decomposition and pyrolysis
    • B01J37/088—Decomposition of a metal salt
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/12—Oxidising
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B01J2229/186—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself not in framework positions
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/20—After treatment, characterised by the effect to be obtained to introduce other elements in the catalyst composition comprising the molecular sieve, but not specially in or on the molecular sieve itself
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/34—Reaction with organic or organometallic compounds
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/37—Acid treatment
    • 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
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/40—Special temperature treatment, i.e. other than just for template removal
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency

Definitions

  • the invention relates to a preparation method of isosorbide and belongs to the technical field of fine chemicals.
  • isosorbide and its derivatives are widely used in the fields of food, cosmetics, medicine, and polymer materials.
  • Isosorbide is commonly obtained by catalytic dehydration of sorbitol, and its raw material sorbitol can be produced in large quantities through catalytic hydrogenation of glucose, making the source of isosorbide raw materials very abundant and the price very low.
  • Catalytic dehydration of sorbitol usually uses liquid acid (such as H 2 SO 4 , etc.) as a catalyst.
  • Liquid acid catalysts not only corrode equipment, pollute the environment, and are difficult to separate from the product, but also have many side reactions and dark color of the resulting product. To avoid the above problems with liquid acid catalysts, researchers in this field have developed many methods to avoid the use of liquid acid catalysts.
  • Chinese patent CN108117560A discloses a method for preparing isosorbide. This method first adds phosphorus-modified HZSM-5 molecular sieve to the sorbitol solution, performs a dehydration reaction to obtain a solid-liquid mixture, and then filters it to obtain a filtrate.
  • the filtrate is then processed Decolorize the activated carbon and filter again to obtain the filtrate; then pass the filtrate through D301 anion resin, 001 ⁇ 7 cation resin, and D301 anion resin for ion exchange to obtain an ion exchange liquid; reduce the ion exchange liquid to a Brix of 75 ⁇ 90%, carry out one cooling crystallization; after centrifugation, obtain crude isosorbide crystals; add water to the crude isosorbide crystals, and heat and dissolve them to make the Brix 70 ⁇ 85%, carry out two cooling crystallizations; centrifuge and dry , to obtain the isosorbide crystal product.
  • the patented preparation process is cumbersome, the operation is complex, the yield of isosorbide is low, the dehydration reaction temperature is 150-300°C, the reaction pressure is 3-10MPa, the conditions are harsh, and the energy consumption is high.
  • Chinese patent CN101492457A discloses a method for preparing isosorbide, using sorbitol as raw material, H 3 PO 4 modified tetravalent metal oxide as catalyst, and preparing isosorbide through dehydration reaction.
  • the patented isosorbide selectivity is 63.49%, the yield is 62.23%, and the dehydration reaction temperature is 250-300°C. It can be seen that the preparation method disclosed in the patent has high reaction temperature, high energy consumption, and relatively low product selectivity and yield. .
  • the present invention provides a preparation method of isosorbide, achieving the following invention objectives: developing a method with mild reaction conditions, simple operation, high sorbitol conversion rate, high isosorbide selectivity and yield. High preparation method.
  • a method for preparing isosorbide including molecular sieve cleaning, molecular sieve modification, active material adsorption and calcination, and isosorbide synthesis.
  • the mass concentration of the concentrated sulfuric acid is 98wt%
  • the mass ratio of the molecular sieve to the strong oxidizing solution is 20-50:100;
  • the molecular sieve is spherical in shape, has a particle size of 1.6 ⁇ 2.5mm, a pore diameter of 10 ⁇ 40nm, a bulk density of 0.64g/mL, an abrasion rate of 0.1%, a compressive strength of 35N, and a silicon-aluminum ratio of 1:1;
  • the mass ratio of the molecular sieve to the mixed liquid is 15-40:100;
  • the mixed solution is composed of bis(2-hydroxyethyl)dimethylammonium chloride, tetramethylammonium hydroxide, potassium hydroxide, and deionized water;
  • the mass ratio of bis(2-hydroxyethyl)dimethylammonium chloride, tetramethylammonium hydroxide, potassium hydroxide, and deionized water is 1 ⁇ 7:2 ⁇ 8:1 ⁇ 6:70 ⁇ 100 .
  • the mass ratio of the cleaned molecular sieve to the acid solution is 20-35:100;
  • the mass ratio of citric acid, ethylenediaminetetraacetic acid, trifluoroacetic acid, and deionized water is 10 to 19:5 to 9:1 to 6:80 to 110.
  • Put the modified molecular sieve into the mixed salt solution soak it for 30 to 50 hours, take it out, and dry it at 80 to 110°C for 2 to 5 hours.
  • Transfer to a muffle furnace raise the temperature to 280-380°C at a heating rate of 2-4°C/min, calcine at a constant temperature for 1-3.5 hours, then cool to room temperature to obtain the catalyst;
  • the mass ratio of the modified molecular sieve to the mixed salt solution is 20 to 36:100;
  • the mass ratio of ammonium metavanadate, zirconium sulfate, and deionized water is 12-18:13-20:80-100.
  • the reactant sorbitol aqueous solution passes through the preheating section of the reactor and is preheated to 100 to 130°C. After vaporization, it is sent to the constant temperature section.
  • the reacted gas-liquid mixture is cooled in an ice-water bath and separated from gas and liquid.
  • the liquid obtained is collected into a crude product tank. After the reaction is stable, the liquid collected in the crude product tank within 3 hours is sampled and analyzed;
  • the mass concentration of sorbitol in the sorbitol aqueous solution is 10 to 14 wt%.
  • the present invention achieves the following beneficial effects:
  • the preparation method of isosorbide according to the present invention has mild reaction conditions, simple operation, high conversion rate of reactant sorbitol, and high selectivity and high yield of product isosorbide;
  • the preparation method of isosorbide according to the present invention is 130-230°C, the conversion rate of sorbitol is 95.32-97.93%, the selectivity of isosorbide is 75.47-77.43%, and the yield of isosorbide is 72.89-72.89%. 75.74%.
  • Example 1 A preparation method of isosorbide
  • the mass concentration of the concentrated sulfuric acid is 98wt%
  • the mass ratio of the molecular sieve to the strong oxidizing solution is 40:100;
  • the molecular sieve has a spherical shape, a particle diameter of 2mm, a pore diameter of 30nm, a bulk density of 0.64g/mL, an abrasion rate of 0.1%, a compressive strength of 35N, and a silicon-to-aluminum ratio of 1:1;
  • the mass ratio of the molecular sieve to the mixed liquid is 25:100;
  • the mixed solution is composed of bis(2-hydroxyethyl)dimethylammonium chloride, tetramethylammonium hydroxide, potassium hydroxide, and deionized water; the bis(2-hydroxyethyl)dimethylammonium chloride
  • the mass ratio of ammonium chloride, tetramethylammonium hydroxide, potassium hydroxide, and deionized water is 5:6:4:90.
  • the mass ratio of the cleaned molecular sieve to the acid solution is 30:100;
  • the mass ratio of citric acid, ethylenediaminetetraacetic acid, trifluoroacetic acid, and deionized water is 13:7:4:100.
  • Put the modified molecular sieve into the mixed salt solution soak it for 40 hours, take it out, dry it at 100°C for 4 hours, and then transfer it to a muffle furnace. , heated to 320°C at a heating rate of 3°C/min, calcined at a constant temperature for 2 hours, then cooled to room temperature to obtain the catalyst;
  • the mass ratio of the modified molecular sieve to the mixed salt solution is 30:100;
  • the mass ratio of ammonium metavanadate, zirconium sulfate, and deionized water is 15:17:90.
  • the catalyst is loaded into the constant temperature section of the tubular fixed bed reactor. Under nitrogen protection, the temperature of the constant temperature section is controlled at 180°C.
  • the reactant sorbitol aqueous solution is preheated to 120°C through the preheating section of the reactor, and is vaporized before being sent to the reactor.
  • the reacted gas-liquid mixture is cooled in an ice-water bath and separated from gas-liquid, and the liquid obtained is collected into the crude product tank. After the reaction is stable, the liquid collected in the crude product tank within 3 hours is sampled and analyzed;
  • the mass concentration of sorbitol in the sorbitol aqueous solution is 13wt%.
  • Example 2 A preparation method of isosorbide
  • the mass concentration of the concentrated sulfuric acid is 98wt%
  • the mass ratio of the molecular sieve to the strong oxidizing solution is 20:100;
  • the molecular sieve has a spherical shape, a particle diameter of 1.6mm, a pore diameter of 10nm, a bulk density of 0.64g/mL, an abrasion rate of 0.1%, a compressive strength of 35N, and a silicon-aluminum ratio of 1:1;
  • the mass ratio of the molecular sieve to the mixed liquid is 15:100;
  • the mixed solution is composed of bis(2-hydroxyethyl)dimethylammonium chloride, tetramethylammonium hydroxide, potassium hydroxide, and deionized water;
  • the mass ratio of bis(2-hydroxyethyl)dimethylammonium chloride, tetramethylammonium hydroxide, potassium hydroxide, and deionized water is 1:2:1:70.
  • the mass ratio of the cleaned molecular sieve to the acid solution is 20:100;
  • the mass ratio of citric acid, ethylenediaminetetraacetic acid, trifluoroacetic acid, and deionized water is 10:5:1:80.
  • Put the modified molecular sieve into the mixed salt solution soak it for 30 hours, take it out, dry it at 80°C for 2 hours, and then transfer it to a muffle furnace. , heated to 280°C at a heating rate of 2°C/min, calcined at a constant temperature for 1 hour, then cooled to room temperature to obtain the catalyst;
  • the mass ratio of the modified molecular sieve to the mixed salt solution is 20:100;
  • the mass ratio of ammonium metavanadate, zirconium sulfate, and deionized water is 12:13:80.
  • the catalyst is loaded into the constant temperature section of the tubular fixed bed reactor. Under nitrogen protection, the temperature of the constant temperature section is controlled at 130°C.
  • the reactant sorbitol aqueous solution is preheated to 100°C through the preheating section of the reactor, and is vaporized before being sent to the reactor.
  • the reacted gas-liquid mixture is cooled in an ice-water bath and separated from gas-liquid, and the liquid obtained is collected into the crude product tank. After the reaction is stable, the liquid collected in the crude product tank within 3 hours is sampled and analyzed;
  • the mass concentration of sorbitol in the sorbitol aqueous solution is 10 wt%.
  • Example 3 A preparation method of isosorbide
  • the mass concentration of the concentrated sulfuric acid is 98wt%
  • the mass ratio of the molecular sieve to the strong oxidizing solution is 50:100;
  • the molecular sieve has a spherical shape, a particle diameter of 2.5mm, a pore diameter of 40nm, a bulk density of 0.64g/mL, an abrasion rate of 0.1%, a compressive strength of 35N, and a silicon-aluminum ratio of 1:1;
  • the mass ratio of the molecular sieve to the mixed liquid is 40:100;
  • the mixed solution is composed of bis(2-hydroxyethyl)dimethylammonium chloride, tetramethylammonium hydroxide, potassium hydroxide, and deionized water;
  • the mass ratio of bis(2-hydroxyethyl)dimethylammonium chloride, tetramethylammonium hydroxide, potassium hydroxide, and deionized water is 7:8:6:100.
  • the mass ratio of the cleaned molecular sieve to the acid solution is 35:100;
  • the mass ratio of citric acid, ethylenediaminetetraacetic acid, trifluoroacetic acid, and deionized water is 19:9:6:110.
  • Put the modified molecular sieve into the mixed salt solution soak it for 50 hours, take it out, dry it at 110°C for 5 hours, and then transfer it to a muffle furnace. , heated to 380°C at a heating rate of 4°C/min, calcined at a constant temperature for 3.5 hours, then cooled to room temperature to obtain the catalyst;
  • the mass ratio of the modified molecular sieve to the mixed salt solution is 36:100;
  • the mass ratio of ammonium metavanadate, zirconium sulfate, and deionized water is 18:20:100.
  • the catalyst is loaded into the constant temperature section of the tubular fixed bed reactor. Under nitrogen protection, the temperature of the constant temperature section is controlled at 230°C.
  • the reactant sorbitol aqueous solution is preheated to 130°C through the preheating section of the reactor, and is vaporized before being sent to the reactor.
  • the reacted gas-liquid mixture is cooled in an ice-water bath and separated from gas-liquid, and the liquid obtained is collected into the crude product tank. After the reaction is stable, the liquid collected in the crude product tank within 3 hours is sampled and analyzed;
  • the mass concentration of sorbitol in the sorbitol aqueous solution is 14wt%.
  • Comparative Example 1 Based on Example 1, the two steps of molecular sieve cleaning and molecular sieve modification are not performed.
  • step 1 Do not perform step 1 or step 2;
  • steps 3 and 4 are the same as those in Example 1.
  • Comparative Example 2 Based on Example 1, in the active material adsorption and calcination steps, equal amounts of ammonium metavanadate were replaced with zirconium sulfate. The operations of Steps 1 and 2 were the same as in Example 1;
  • step 3 replace 15 parts of ammonium metavanadate with 15 parts of zirconium sulfate in equal amounts, and the remaining operations are the same as in Example 1;
  • step 4 is the same as that of Example 1.
  • Comparative Example 3 Based on Example 1, in the active material adsorption and calcination steps, equal amounts of zirconium sulfate were replaced with ammonium metavanadate. The operations of Steps 1 and 2 were the same as in Example 1;
  • step 3 replace 17 parts of zirconium sulfate with 17 parts of ammonium metavanadate in equal amounts, and the remaining operations are the same as in Example 1;
  • step 4 is the same as that of Example 1.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Heterocyclic Carbon Compounds Containing A Hetero Ring Having Oxygen Or Sulfur (AREA)

Abstract

一种异山梨醇的制备方法，属于精细化工技术领域，包括分子筛清洗、分子筛改性、活性物质吸附和煅烧、异山梨醇的合成。本发明所述异山梨醇的制备方法，反应条件温和，操作简单，反应物山梨醇的转化率高，产物异山梨醇的选择性高、收率高，反应温度为130～230℃，山梨醇的转化率为95.32～97.93％，异山梨醇选择性为75.47～77.43％，异山梨醇收率为72.89～75.74％。

Description

一种异山梨醇的制备方法 技术领域
本发明涉及一种异山梨醇的制备方法，属于精细化工技术领域。
背景技术
基于功能性二元羟基、刚性结构以及手性中心等结构特征，异山梨醇及其衍生物被广泛用于食品、化妆品、医药及高分子材料等领域。异山梨醇常用山梨醇催化脱水得到，而其原料山梨醇可以通过葡萄糖催化加氢大量制备，使得异山梨醇的原料来源十分丰富，而且价格也十分低廉。山梨醇的催化脱水通常以液体酸(如H 2SO 4等)为催化剂，液体酸催化剂不仅腐蚀设备、污染环境、与产物难以分离，而且还存在副反应多、所得产物色泽深等弊端。为避免以上液体酸催化剂的问题，该领域的研究人员开发出很多方法来避免液体酸催化剂的使用。
中国专利CN108117560A公开了一种异山梨醇制备方法，该方法先向山梨醇溶液中加入磷改性HZSM-5分子筛，进行脱水反应得到固液混合物后进行过滤，得到过滤液，再将过滤液进行活性炭脱色，并再次过滤，得到滤过液；再将滤过液依次经过D301阴树脂、001×7阳树脂、D301阴树脂进行离子交换，得到离子交换液；将离子交换液缩至Brix为75～90％，进行一次降温结晶；离心后，得到粗异山梨醇晶体；向粗异山梨醇晶体中加水，并加热溶化，使其Brix为70～85％，二次降温结晶；离心并烘干，得到异山梨醇晶体产品。该专利制备工艺繁琐，操作复杂，异山梨醇的产率低，脱水反应温度150～300℃，反应压力3～10MPa，条件苛刻，能耗较高。
中国专利CN101492457A公开了一种异山梨醇的制备方法，以山梨醇为原料，H 3PO 4改性的四价金属氧化物为催化剂，通过脱水反应制备异山梨醇。该专利异山梨醇选择性为63.49％，收率为62.23％，脱水反应温度250～300℃，可见该专利所披露的制备方法，反应温度高，能耗高，产物选择性和收率比较低。
从上述专利可以看到，以山梨醇为原料，经催化脱水制备异山梨醇的制备方法中，尽管已开 发出了很多方法来避免使用液体酸催化剂，但仍存在反应条件苛刻，工艺操作复杂，异山梨醇选择性和收率低等问题。
发明内容
针对上述现有技术存在的不足，本发明提供一种异山梨醇的制备方法，实现以下发明目的：开发出反应条件温和，操作简单，山梨醇转化率高，异山梨醇选择性高、收率高的制备方法。
为实现上述发明目的，本发明采取以下技术方案：
一种异山梨醇的制备方法，包括分子筛清洗、分子筛改性、活性物质吸附和煅烧、异山梨醇的合成。
以下是对上述技术方案的进一步改进：
步骤1分子筛清洗
双氧水和浓硫酸按体积比3:7混合成强氧化溶液，将分子筛放入其中浸泡1～6分钟后取出，然后用去离子水将分子筛浸泡冲洗至洗出液呈中性，再将分子筛浸没入混合液中，控温50～80℃下，浸泡12～26小时后取出，用去离子水冲洗至洗出液呈中性后，于100～130℃下干燥1～3小时后得到清洗后的分子筛；
所述双氧水，其中过氧化氢质量浓度为30wt％；
所述浓硫酸的质量浓度为98wt％；
所述分子筛与强氧化溶液的质量比为20～50:100；
所述分子筛，形状为球形，粒径为1.6～2.5mm，孔径为10～40nm，堆积密度为0.64g/mL，磨耗率为0.1％，抗压强度为35N，硅铝比为1:1；
所述分子筛与混合液的质量比为15～40:100；
所述混合液，由双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水组成；
所述双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水的质量比为1～7:2～8:1～6:70～100。
步骤2分子筛改性
将柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水混合后得到酸液，将清洗后的分子筛浸没到酸液中，加热至80～110℃，浸泡2～4小时后，过滤出分子筛并用去离子水洗涤至洗出液呈中性后，于90～120℃下干燥1～4小时后得到改性分子筛；
所述清洗后的分子筛与酸液的质量比为20～35:100；
所述柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水的质量比为10～19:5～9:1～6:80～110。
步骤3活性物质吸附和煅烧
将偏钒酸铵、硫酸锆溶于去离子水中，得到混合盐溶液，将改性分子筛放入混合盐溶液中，浸渍30～50小时后取出，于80～110℃下干燥2～5小时后转移至马弗炉中，以2～4℃/min的升温速率升温至280～380℃，恒温煅烧1～3.5小时后，冷却至室温，得到催化剂；
所述改性分子筛与混合盐溶液的质量比为20～36:100；
所述混合盐溶液中，偏钒酸铵、硫酸锆、去离子水的质量比为12～18:13～20:80～100。
步骤4异山梨醇的合成
将催化剂装入管式固定床反应器的恒温段，通氮气保护下，将恒温段温度控制在130～230℃，反应物山梨醇水溶液经反应器预热段，预热至100～130℃，经汽化后送入恒温段，反应后的气液混合物经冰水浴冷却和气液分离后，得到的液体收集入粗品罐中，对反应平稳后，3小时内粗品罐内收集的液体进行取样分析；
所述山梨醇水溶液，山梨醇的质量浓度为10～14wt％。
与现有技术相比，本发明取得以下有益效果：
1、本发明所述异山梨醇的制备方法，反应条件温和，操作简单，反应物山梨醇的转化率高，产物异山梨醇的选择性高、收率高；
2、本发明所述异山梨醇的制备方法，反应温度为130～230℃，山梨醇的转化率95.32～97.93％，异山梨醇选择性为75.47～77.43％，异山梨醇收率为72.89～75.74％。
具体实施方式
以下对本发明的优选实施例进行说明，应当理解，此处所描述的优选实施例仅用于说明和解 释本发明，并不用于限定本发明。
实施例1：一种异山梨醇的制备方法
包括以下步骤：
1、分子筛清洗
双氧水和浓硫酸按体积比3:7混合成强氧化溶液，将分子筛放入其中浸泡4分钟后取出，然后用去离子水将分子筛浸泡冲洗至洗出液呈中性，再将分子筛浸没入混合液中，控温70℃下，浸泡20小时后取出，用去离子水冲洗至洗出液呈中性后，于120℃下干燥2小时后得到清洗后的分子筛；
所述双氧水，其中过氧化氢质量浓度为30wt％；
所述浓硫酸的质量浓度为98wt％；
所述分子筛与强氧化溶液的质量比为40:100；
所述分子筛，形状为球形，粒径为2mm，孔径为30nm，堆积密度为0.64g/mL，磨耗率为0.1％，抗压强度为35N，硅铝比为1:1；
所述分子筛与混合液的质量比为25:100；
所述混合液，由双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水组成；所述双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水的质量比为5:6:4:90。2、分子筛改性
将柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水混合后得到酸液，将清洗后的分子筛浸没到酸液中，加热至100℃，浸泡3小时后，过滤出分子筛并用去离子水洗涤至洗出液呈中性后，于110℃下干燥3小时后得到改性分子筛；
所述清洗后的分子筛与酸液的质量比为30:100；
所述柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水的质量比为13:7:4:100。
3、活性物质吸附和煅烧
将偏钒酸铵、硫酸锆溶于去离子水中，得到混合盐溶液，将改性分子筛放入混合盐溶液中， 浸渍40小时后取出，于100℃下干燥4小时后转移至马弗炉中，以3℃/min的升温速率升温至320℃，恒温煅烧2小时后，冷却至室温，得到催化剂；
所述改性分子筛与混合盐溶液的质量比为30:100；
所述混合盐溶液中，偏钒酸铵、硫酸锆、去离子水的质量比为15:17:90。
4、异山梨醇的合成
将催化剂装入管式固定床反应器的恒温段，通氮气保护下，将恒温段温度控制在180℃，反应物山梨醇水溶液经反应器预热段，预热至120℃，经汽化后送入恒温段，反应后的气液混合物经冰水浴冷却和气液分离后，得到的液体收集入粗品罐中，对反应平稳后，3小时内粗品罐内收集的液体进行取样分析；
所述山梨醇水溶液，山梨醇的质量浓度为13wt％。
实施例2：一种异山梨醇的制备方法
包括以下步骤：
1、分子筛清洗
双氧水和浓硫酸按体积比3:7混合成强氧化溶液，将分子筛放入其中浸泡1分钟后取出，然后用去离子水将分子筛浸泡冲洗至洗出液呈中性，再将分子筛浸没入混合液中，控温50℃下，浸泡12小时后取出，用去离子水冲洗至洗出液呈中性后，于100℃下干燥1小时后得到清洗后的分子筛；
所述双氧水，其中过氧化氢质量浓度为30wt％；
所述浓硫酸的质量浓度为98wt％；
所述分子筛与强氧化溶液的质量比为20:100；
所述分子筛，形状为球形，粒径为1.6mm，孔径为10nm，堆积密度为0.64g/mL，磨耗率为0.1％，抗压强度为35N，硅铝比为1:1；
所述分子筛与混合液的质量比为15:100；
所述混合液，由双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水组成；
所述双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水的质量比为1:2:1:70。
2、分子筛改性
将柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水混合后得到酸液，将清洗后的分子筛浸没到酸液中，加热至80℃，浸泡2小时后，过滤出分子筛并用去离子水洗涤至洗出液呈中性后，于90℃下干燥1小时后得到改性分子筛；
所述清洗后的分子筛与酸液的质量比为20:100；
所述柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水的质量比为10:5:1:80。
3、活性物质吸附和煅烧
将偏钒酸铵、硫酸锆溶于去离子水中，得到混合盐溶液，将改性分子筛放入混合盐溶液中，浸渍30小时后取出，于80℃下干燥2小时后转移至马弗炉中，以2℃/min的升温速率升温至280℃，恒温煅烧1小时后，冷却至室温，得到催化剂；
所述改性分子筛与混合盐溶液的质量比为20:100；
所述混合盐溶液中，偏钒酸铵、硫酸锆、去离子水的质量比为12:13:80。
4、异山梨醇的合成
将催化剂装入管式固定床反应器的恒温段，通氮气保护下，将恒温段温度控制在130℃，反应物山梨醇水溶液经反应器预热段，预热至100℃，经汽化后送入恒温段，反应后的气液混合物经冰水浴冷却和气液分离后，得到的液体收集入粗品罐中，对反应平稳后，3小时内粗品罐内收集的液体进行取样分析；
所述山梨醇水溶液，山梨醇的质量浓度为10wt％。
实施例3：一种异山梨醇的制备方法
包括以下步骤：
1、分子筛清洗
双氧水和浓硫酸按体积比3:7混合成强氧化溶液，将分子筛放入其中浸泡6分钟后取出，然后用去离子水将分子筛浸泡冲洗至洗出液呈中性，再将分子筛浸没入混合液中，控温80℃下， 浸泡26小时后取出，用去离子水冲洗至洗出液呈中性后，于130℃下干燥3小时后得到清洗后的分子筛；
所述双氧水，其中过氧化氢质量浓度为30wt％；
所述浓硫酸的质量浓度为98wt％；
所述分子筛与强氧化溶液的质量比为50:100；
所述分子筛，形状为球形，粒径为2.5mm，孔径为40nm，堆积密度为0.64g/mL，磨耗率为0.1％，抗压强度为35N，硅铝比为1:1；
所述分子筛与混合液的质量比为40:100；
所述混合液，由双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水组成；
所述双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水的质量比为7:8:6:100。
2、分子筛改性
将柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水混合后得到酸液，将清洗后的分子筛浸没到酸液中，加热至110℃，浸泡4小时后，过滤出分子筛并用去离子水洗涤至洗出液呈中性后，于120℃下干燥4小时后得到改性分子筛；
所述清洗后的分子筛与酸液的质量比为35:100；
所述柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水的质量比为19:9:6:110。
3、活性物质吸附和煅烧
将偏钒酸铵、硫酸锆溶于去离子水中，得到混合盐溶液，将改性分子筛放入混合盐溶液中，浸渍50小时后取出，于110℃下干燥5小时后转移至马弗炉中，以4℃/min的升温速率升温至380℃，恒温煅烧3.5小时后，冷却至室温，得到催化剂；
所述改性分子筛与混合盐溶液的质量比为36:100；
所述混合盐溶液中，偏钒酸铵、硫酸锆、去离子水的质量比为18:20:100。
4、异山梨醇的合成
将催化剂装入管式固定床反应器的恒温段，通氮气保护下，将恒温段温度控制在230℃，反应物山梨醇水溶液经反应器预热段，预热至130℃，经汽化后送入恒温段，反应后的气液混合物经冰水浴冷却和气液分离后，得到的液体收集入粗品罐中，对反应平稳后，3小时内粗品罐内收集的液体进行取样分析；
所述山梨醇水溶液，山梨醇的质量浓度为14wt％。
对比例1：实施例1基础上，不进行分子筛清洗、分子筛改性两个步骤
不进行步骤1、步骤2；
步骤3和步骤4操作同于实施例1。
对比例2：实施例1基础上，活性物质吸附和煅烧步骤中，偏钒酸铵等量替换为硫酸锆步骤1、步骤2的操作同于实施例1；
步骤3中，将15份偏钒酸铵等量替换为15份硫酸锆，其余操作同于实施例1；
步骤4操作同于实施例1。
对比例3：实施例1基础上，活性物质吸附和煅烧步骤中，硫酸锆等量替换为偏钒酸铵步骤1、步骤2的操作同于实施例1；
步骤3中，将17份硫酸锆等量替换为17份偏钒酸铵，其余操作同于实施例1；
步骤4操作同于实施例1。
实施例1、2、3和对比例1、2、3取样测试结果见表1：
表1
  山梨醇转化率(％) 异山梨醇选择性(％) 异山梨醇收率(％)
实施例1 97.93 77.34 75.74
实施例2 96.58 75.47 72.89
实施例3 95.32 77.43 73.81
对比例1 48.66 42.51 20.69
对比例2 54.91 61.94 34.01
对比例3 49.45 55.29 27.34

Claims (5)

  1. 一种异山梨醇的制备方法，其特征在于：
    包括分子筛清洗、分子筛改性、活性物质吸附和煅烧、异山梨醇的合成；
    所述分子筛清洗，其方法为将双氧水和浓硫酸按体积比3:7混合成强氧化溶液，将分子筛放入其中浸泡1～6分钟后取出，然后用去离子水将分子筛浸泡冲洗至洗出液呈中性，再将分子筛浸没入混合液中，控温50～80℃下，浸泡12～26小时后取出，用去离子水冲洗至洗出液呈中性后，于100～130℃下干燥1～3小时后得到清洗后的分子筛；
    所述分子筛，形状为球形，粒径为1.6～2.5mm，孔径为10～40nm，堆积密度为0.64g/mL，磨耗率为0.1％，抗压强度为35N，硅铝比为1:1；
    所述混合液，由双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水组成；所述双(2-羟乙基)二甲基氯化铵、四甲基氢氧化铵、氢氧化钾、去离子水的质量比为1～7:2～8:1～6:70～100；
    所述分子筛改性，其方法为将柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水混合后得到酸液，将清洗后的分子筛浸没到酸液中，加热至80～110℃，浸泡2～4小时后，过滤出分子筛并用去离子水洗涤至洗出液呈中性后，于90～120℃下干燥1～4小时后得到改性分子筛；
    所述清洗后的分子筛与酸液的质量比为20～35:100；
    所述柠檬酸、乙二胺四乙酸、三氟乙酸、去离子水的质量比为10～19:5～9:1～6:80～110；
    所述活性物质吸附和煅烧，其方法为将偏钒酸铵、硫酸锆溶于去离子水中，得到混合盐溶液，将改性分子筛放入混合盐溶液中，浸渍30～50小时后取出，于80～110℃下干燥2～5小时后转移至马弗炉中，升温至280～380℃，恒温煅烧1～3.5小时后，冷却至室温，得到催化剂；
    所述改性分子筛与混合盐溶液的质量比为20～36:100；
    所述混合盐溶液中，偏钒酸铵、硫酸锆、去离子水的质量比为12～18:13～20:80～100。
  2. 根据权利要求1所述的一种异山梨醇的制备方法，其特征在于：
    所述双氧水，其中过氧化氢质量浓度为30wt％；
    所述浓硫酸的质量浓度为98wt％；
    所述分子筛与强氧化溶液的质量比为20～50:100；
    所述分子筛与混合液的质量比为15～40:100。
  3. 根据权利要求1所述的一种异山梨醇的制备方法，其特征在于：
    所述活性物质吸附和煅烧步骤中，升温的速率为2～4℃/min。
  4. 根据权利要求1所述的一种异山梨醇的制备方法，其特征在于：
    所述异山梨醇的合成，其方法为将催化剂装入管式固定床反应器的恒温段，通氮气保护下，将恒温段温度控制在130～230℃，反应物山梨醇水溶液经反应器预热段，预热至100～130℃，经汽化后送入恒温段，反应后的气液混合物经冰水浴冷却和气液分离后，得到的液体收集入粗品罐中。
  5. 根据权利要求4所述的一种异山梨醇的制备方法，其特征在于：
    所述山梨醇水溶液，山梨醇的质量浓度为10～14wt％。
PCT/CN2022/129714 2022-04-08 2022-11-04 一种异山梨醇的制备方法 WO2023193430A1 (zh)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN202210362604.5A CN114437101B (zh) 2022-04-08 2022-04-08 一种异山梨醇的制备方法
CN202210362604.5 2022-04-08

Publications (1)

Publication Number Publication Date
WO2023193430A1 true WO2023193430A1 (zh) 2023-10-12

Family

ID=81360268

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2022/129714 WO2023193430A1 (zh) 2022-04-08 2022-11-04 一种异山梨醇的制备方法

Country Status (2)

Country Link
CN (1) CN114437101B (zh)
WO (1) WO2023193430A1 (zh)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114437101B (zh) * 2022-04-08 2022-05-31 山东天力药业有限公司 一种异山梨醇的制备方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1960963A (zh) * 2004-01-21 2007-05-09 康斯乔最高科学研究公司 多羟基醇单酯的制备方法
CN101492458A (zh) * 2009-02-27 2009-07-29 南京工业大学 一种采用四价金属磷酸盐作催化剂制备异山梨醇的方法
CN101691376A (zh) * 2009-09-22 2010-04-07 南京工业大学 以固载杂多酸为催化剂制备异山梨醇的方法
CN108675317A (zh) * 2018-08-22 2018-10-19 江西西林科新材料有限公司 一种低成本sapo-34分子筛的合成方法
CN109261202A (zh) * 2018-09-30 2019-01-25 中国科学院山西煤炭化学研究所 一种用于山梨醇脱水制备异山梨醇的催化剂及其制法和应用
CN113289672A (zh) * 2021-06-02 2021-08-24 南通大学 分子筛催化剂改进工艺
CN114437101A (zh) * 2022-04-08 2022-05-06 山东天力药业有限公司 一种异山梨醇的制备方法

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1960963A (zh) * 2004-01-21 2007-05-09 康斯乔最高科学研究公司 多羟基醇单酯的制备方法
CN101492458A (zh) * 2009-02-27 2009-07-29 南京工业大学 一种采用四价金属磷酸盐作催化剂制备异山梨醇的方法
CN101691376A (zh) * 2009-09-22 2010-04-07 南京工业大学 以固载杂多酸为催化剂制备异山梨醇的方法
CN108675317A (zh) * 2018-08-22 2018-10-19 江西西林科新材料有限公司 一种低成本sapo-34分子筛的合成方法
CN109261202A (zh) * 2018-09-30 2019-01-25 中国科学院山西煤炭化学研究所 一种用于山梨醇脱水制备异山梨醇的催化剂及其制法和应用
CN113289672A (zh) * 2021-06-02 2021-08-24 南通大学 分子筛催化剂改进工艺
CN114437101A (zh) * 2022-04-08 2022-05-06 山东天力药业有限公司 一种异山梨醇的制备方法

Also Published As

Publication number Publication date
CN114437101B (zh) 2022-05-31
CN114437101A (zh) 2022-05-06

Similar Documents

Publication Publication Date Title
CN109019691B (zh) 一种仲钨酸铵的制备工艺
US1840450A (en) Zeolite product
WO2023193430A1 (zh) 一种异山梨醇的制备方法
JPS6176470A (ja) 無水マレイン酸の製造法
CN114643050B (zh) 一种提高乳糖异构化产率的复合催化剂、制备方法及应用
CN110980759B (zh) 一种硅铟酸盐分子筛及其制备方法和应用
CN111072493B (zh) 一种一步法制备1,5-戊二胺的方法
CN103894188A (zh) 一种钯/树脂碳催化剂的制备方法及其应用
JP7041784B1 (ja) タウリンの製造方法
CN106380443A (zh) 一种2‑甲基吡啶的催化制备方法
CN100408688C (zh) 一种以淀粉为原料制取甘露醇的方法
DE3107756C2 (zh)
US1782353A (en) Zeolite
JP7186313B2 (ja) リンゴ酸の製造
CN107311839A (zh) 气相氟‑氯交换制备七氟环戊烯的方法
CN107501375A (zh) 一种醋酸甲地孕酮的制备方法
Joshi et al. Synthesis of monoesters and diesters using eco-friendly solid acid catalysts-M (IV) tungstates and phosphates
CN117229248B (zh) 一种使用固体碱制备提纯玻色因的方法
CN112851554A (zh) 一种硝酸胍的制备方法
CN108727184A (zh) 一种醋酸正丁酯的生产方法
CN111410602B (zh) 一种蒽醌的制备方法
CN112746136B (zh) 一种果糖的化学制备方法
US1886023A (en) Catalytic oxidation of anthracene
CN114539047B (zh) 一种1,2,3-连苯三甲酸的制备方法
US1582851A (en) Effecting catalytic reactions, particularly in catalytically producing hydrocyanic acid

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 22936358

Country of ref document: EP

Kind code of ref document: A1