WO2023272949A1 - 一种十六碳双酯的连续化生产工艺 - Google Patents

一种十六碳双酯的连续化生产工艺 Download PDF

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WO2023272949A1
WO2023272949A1 PCT/CN2021/117985 CN2021117985W WO2023272949A1 WO 2023272949 A1 WO2023272949 A1 WO 2023272949A1 CN 2021117985 W CN2021117985 W CN 2021117985W WO 2023272949 A1 WO2023272949 A1 WO 2023272949A1
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hexadecyl
tower
butyl ester
esterification
ester
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PCT/CN2021/117985
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English (en)
French (fr)
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张世元
宋文国
卢小松
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润泰新材料股份有限公司
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/08—Preparation of carboxylic acid esters by reacting carboxylic acids or symmetrical anhydrides with the hydroxy or O-metal group of organic compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/48—Separation; Purification; Stabilisation; Use of additives
    • C07C67/52—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation
    • C07C67/54—Separation; Purification; Stabilisation; Use of additives by change in the physical state, e.g. crystallisation by distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C67/00—Preparation of carboxylic acid esters
    • C07C67/48—Separation; Purification; Stabilisation; Use of additives
    • C07C67/58—Separation; Purification; Stabilisation; Use of additives by liquid-liquid treatment

Definitions

  • the invention relates to the technical field of fine chemicals, in particular to a continuous production process of hexadecyl diester.
  • Hexadecyl diester is hexadecyl n-butyl or hexadecyl isobutyl
  • hexadecyl n-butyl or hexadecyl isobutyl is a multi-purpose plasticizer without benzene ring, not only compatible with all Compatible with general-purpose primary and secondary plasticizers, especially when used in conjunction with DOP, it can exert the best effect; it is also a fluid viscosity reducer, with good light resistance, excellent hardening, high transparency, balanced lubricity, and Oxygen, low odor and other characteristics.
  • the traditional hexadecyl n-/isobutyl ester (alcohol ester sixteen) adopts the batch method still-type production process, which has unstable batches, long esterification time of more than 30 hours, many by-products, and low production efficiency, etc. weakness.
  • the purpose of the present invention is to overcome the deficiencies in the prior art, provide a continuous production process of hexadecanyl diester, shorten the esterification time, reduce by-products, and improve production efficiency.
  • a continuous production process of hexadecyl diester comprises the following steps:
  • Esterification Add n-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and catalyst continuously into the The esterification tower carries out the esterification reaction at normal pressure to generate hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product, and the crude product is extracted from the bottom of the tower;
  • Alkali washing the deacidified hexadecyl n-butyl ester or hexadecyl isobutyl ester primary product enters the alkali washing tower, and neutralizes a small amount of isobutyric acid or n-butyric acid through a weak alkali solution;
  • the odor mainly comes from isobutyric acid or n-butyric acid, isobutanol (from the light component of the previous step reaction), etc., and the hexadecyl n-butyl ester or hexadecyl isobutyl of the heavy component is removed
  • the ester enters the fourth rectification tower to further remove light components under negative pressure, and the light components at the top of the tower return to the esterification tower for esterification, and hexadecyl n-butyl ester or hexadecyl isobutyl ester is extracted from the bottom of the tower to obtain the finished product Hexadecyl n-butyl ester or hexadecyl isobutyl ester.
  • the continuous production process of hexadecyl diester wherein: the temperature of the bottom of the esterification tower in the step S1 is 165°C-175°C.
  • the continuous production process of hexadecyl diester wherein: the negative pressure of the first rectification tower in the step S2 is -0.090 ⁇ -0.095MPa, and the temperature of the bottom of the first rectification tower is 155°C ⁇ 165°C.
  • the continuous production process of cetyl diester wherein: the weak base in step S3 is sodium bicarbonate or potassium hydroxide.
  • the continuous production process of hexadecyl diester wherein: the negative pressure of the light removal tower in the step S4 is -0.085 ⁇ -0.09MPa, and the temperature of the tower bottom is 158°C ⁇ 162°C.
  • the continuous production process of hexadecyl diester wherein: the negative pressure of the second rectification tower in the step S5 is -0.096 ⁇ -0.099MPa, and the temperature of the bottom of the second rectification tower is 162°C ⁇ 168°C.
  • the continuous production process of hexadecyl diester wherein: the negative pressure of the third rectification tower in the step S6 is -0.1 ⁇ -0.105MPa, and the temperature of the bottom of the third rectification tower is 172°C ⁇ 178°C.
  • the continuous production process of hexadecyl diester wherein: the negative pressure of the fourth rectification tower in step S7 is -0.096 ⁇ -0.099MPa, and the temperature of the bottom of the fourth rectification tower is 175°C ⁇ 180°C.
  • the continuous production process of hexadecyl diester wherein: the catalyst in step S1 is BO 3 3- /ZrO 2 /Ce 4+ , and the BO 3 3- /ZrO 2 /Ce 4 + is prepared as follows:
  • the continuous production process of cetyl diester wherein: the concentration of the boric acid solution is 1 to 3 mol/L, the concentration of the Ce 4+ solution is 0.05 to 0.1 mol/L, the The calcination temperature is 500-600° C., and the calcination time is 2-4 hours.
  • the esterification reaction is generally carried out according to the reaction process of breaking the acyl-oxygen bond.
  • n-butyric acid or isobutyric acid is first combined with H + , so that the carbon atom in the carbonyl is positively charged and It is easy to combine with the alcohol oxygen atom to form a bond to generate hexadecyl n-butyl ester or hexadecyl isobutyl ester.
  • the active centers of solid superacid catalysts are protons and Lewis acids.
  • the formation of BO 3 3- /ZrO 2 solid superacid centers in this patent is mainly due to the coordination and adsorption of BO 3 3- on the surface, making the Zr-O bond
  • the electron cloud is strongly shifted, which strengthens the Lewis acid center, and makes it easier to dissociate and adsorb H 2 O to generate a proton acid center.
  • BO 3 3- /ZrO 2 /Ce 4+ BO 3 3- /ZrO 2 Doped with a certain amount of Ce 4+ , so that BO 3 3- /ZrO 2 is modified, BO 3 3- , and a certain amount of Ce 4+ , Ce 4 + itself is a Lewis acid.
  • the continuous production process of hexadecyl diester of the present invention esterifies n-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and a catalyst React to obtain hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product, the crude product is sequentially deacidified, alkali washed, dehydrated, delightened, deheavy, and deodorized to obtain hexadecyl n-butyl ester or hexadecyl isobutyl ester , improve the stability of the product, shorten the esterification reaction time, reduce the ratio of by-products, and improve the product yield and production efficiency.
  • the side reaction is the reaction of dodecyl alcohol ester with n-butyric acid as follows:
  • the side reaction between octanediol and n-butyric acid is mainly monoester, as shown below:
  • a continuous production process of hexadecyl diester comprises the following steps:
  • Esterification N-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and catalyst are continuously entered into the esterification tower according to the mass ratio of 4:7:0.01 for esterification Normal pressure reaction, the tower still temperature of esterification tower is 165 °C, generates hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product, and described crude product is extracted from the bottom of the tower;
  • the catalyst is BO 3 3- /ZrO 2 /Ce 4+
  • the preparation method of the BO 3 3- /ZrO 2 /Ce 4+ is as follows: Dissolve CeO 2 in 1mol/L boric acid solution to prepare 0.05mol/L Ce 4+ solution, then add ZrO 2 into the Ce 4+ solution for 10 hours, filter with suction, dry, and roast at 500°C for 4 hours.
  • the esterified hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the first rectification tower to remove n-butyric acid or isobutyric acid under negative pressure, and the first rectification tower is under negative pressure It is -0.090MPa, the temperature of the first rectifying tower is 155°C, the removed n-butyric acid or isobutyric acid is returned from the top of the tower to the esterification tower to further participate in the reaction, and the hexadecyl n-butyl ester is produced from the tower Or the initial product of hexadecyl isobutyl ester;
  • Alkali washing the deacidified hexadecyl n-butyl ester or hexadecyl isobutyl ester primary product enters the alkali washing tower, and neutralizes a small amount of isobutyric acid or n-butyric acid through sodium bicarbonate solution;
  • the dehydrated hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the second rectification tower to remove light components under negative pressure.
  • the negative pressure of the second rectification tower is -0.096MPa, so The temperature in the bottom of the second rectification tower is 162°C, the light components are returned to the esterification tower for esterification, and hexadecyl n-butyl ester or hexadecyl isobutyl ester is extracted from the bottom of the tower;
  • a continuous production process of hexadecyl diester comprises the following steps:
  • Esterification N-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and catalyst are continuously entered into the esterification tower according to the mass ratio of 5:8:0.02 for esterification Normal pressure reaction, the tower still temperature of esterification tower is 170 °C, generates hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product, and described crude product is extracted from the bottom of the tower;
  • the catalyst is BO 3 3- /ZrO 2 /Ce 4+
  • the preparation method of the BO 3 3- /ZrO 2 /Ce 4+ is as follows: Dissolve CeO 2 in 2mol/L boric acid solution to prepare 0.08mol/L C e 4+ solution, then add ZrO 2 into the Ce 4+ solution for 15 hours, filter with suction, dry, and roast at 550°C for 3 hours.
  • the esterified hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the first rectification tower to remove n-butyric acid or isobutyric acid under negative pressure, and the first rectification tower is under negative pressure is 0.092MPa, the temperature of the first rectifying tower bottom is 160°C, the removed n-butyric acid or isobutyric acid is returned from the top of the tower to the esterification tower to further participate in the reaction, and the tower bottom takes out hexadecyl n-butyl ester or Hexadecyl isobutyl ester primary product;
  • Alkali washing the deacidified hexadecyl n-butyl ester or hexadecyl isobutyl ester primary product enters the alkali washing tower, and neutralizes a small amount of isobutyric acid or n-butyric acid through potassium hydroxide weak alkali solution;
  • the dehydrated hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the second rectification tower to remove light components under negative pressure.
  • the negative pressure of the second rectification tower is -0.098MPa, so
  • the temperature at the bottom of the second rectification tower is 164°C, the light components are returned to the esterification tower for esterification, and hexadecyl n-butyl ester or hexadecyl isobutyl ester is extracted from the bottom of the tower;
  • a continuous production process of hexadecyl diester comprises the following steps:
  • Esterification N-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and catalyst are continuously entered into the esterification tower according to the mass ratio of 6:10:0.03 for esterification Normal pressure reaction, the tower still temperature of esterification tower is 175 °C, generates hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product, and described crude product is extracted from the bottom of the tower;
  • the catalyst is BO 3 3- /ZrO 2 /Ce 4+
  • the preparation method of the BO 3 3- /ZrO 2 /Ce 4+ is as follows: dissolve CeO 2 in a 3mol/L boric acid solution to prepare a 0.1mol/L Ce 4+ solution, then add ZrO 2 into the Ce 4+ solution for 20h, filter with suction, dry, and roast, the roasting temperature is 600°C, and the roasting time is 2h.
  • the esterified hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the first rectification tower to remove n-butyric acid or isobutyric acid under negative pressure, and the first rectification tower is under negative pressure It is -0.095MPa, the temperature of the first rectification tower is 165°C, the removed n-butyric acid or isobutyric acid is returned from the top of the tower to the esterification tower to further participate in the reaction, and the hexadecyl n-butyl ester is produced from the tower Or the initial product of hexadecyl isobutyl ester;
  • the dehydrated hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the second rectification tower to remove light components under negative pressure, and the negative pressure of the second rectification tower is -0.099MPa, so The temperature in the bottom of the second rectification tower is 168°C, the light components are returned to the esterification tower for esterification, and hexadecyl n-butyl ester or hexadecyl isobutyl ester is extracted from the bottom of the tower;
  • a continuous production process of hexadecyl diester comprises the following steps:
  • Esterification N-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and catalyst are continuously entered into the esterification tower according to the mass ratio of 4:7:0.01 for esterification Normal pressure reaction, the tower still temperature of esterification tower is 165 °C, generates hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product, and described crude product is extracted from the bottom of the tower;
  • the catalyst is BO 3 3- /ZrO 2 /Ce 4+
  • the preparation method of the BO 3 3- /ZrO 2 /Ce 4+ is as follows: Dissolve CeO 2 in 1mol/L boric acid solution to prepare 0.05mol/L Ce 4+ solution, then add ZrO 2 into the Ce 4+ solution for 10 hours, filter with suction, dry, and roast at 500°C for 4 hours.
  • the esterified hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the first rectification tower to remove n-butyric acid or isobutyric acid under negative pressure, and the first rectification tower is under negative pressure It is -0.090MPa, the temperature of the first rectifying tower is 155°C, the removed n-butyric acid or isobutyric acid is returned from the top of the tower to the esterification tower to further participate in the reaction, and the hexadecyl n-butyl ester is produced from the tower Or the initial product of hexadecyl isobutyl ester;
  • Alkali washing the deacidified hexadecyl n-butyl ester or hexadecyl isobutyl ester primary product enters the alkali washing tower, and neutralizes a small amount of isobutyric acid or n-butyric acid through sodium bicarbonate solution;
  • the dehydrated hexadecyl n-butyl ester or hexadecyl isobutyl ester enters the third rectification tower under negative pressure to remove heavy components, and the third rectification tower has a negative pressure of -0.1MPa.
  • the temperature of the bottom of the rectification tower is 172°C, and the hexadecanyl n-/isobutyl ester is withdrawn from the top of the tower;
  • a continuous production process of hexadecyl diester comprises the following steps:
  • Esterification N-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and catalyst are continuously entered into the esterification tower according to the mass ratio of 5:8:0.02 for esterification Normal pressure reaction, the tower still temperature of esterification tower is 170 °C, generates hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product, and described crude product is extracted from the bottom of the tower;
  • the catalyst is BO 3 3- /ZrO 2 /Ce 4+
  • the preparation method of the BO 3 3- /ZrO 2 /Ce 4+ is as follows: Dissolve CeO 2 in 2mol/L boric acid solution to prepare 0.08mol/L Ce 4+ solution, then add ZrO 2 into the Ce 4+ solution for 15 hours, suction filter, dry, and roast at 550°C for 3 hours.
  • the esterified hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the first rectification tower to remove n-butyric acid or isobutyric acid under negative pressure, and the first rectification tower is under negative pressure It is -0.092MPa, the temperature of the first rectification tower is 160°C, the removed n-butyric acid or isobutyric acid is returned from the top of the tower to the esterification tower to further participate in the reaction, and the hexadecyl n-butyl ester is produced from the tower Or the initial product of hexadecyl isobutyl ester;
  • Alkali washing the deacidified hexadecyl n-butyl ester or hexadecyl isobutyl ester primary product enters the alkali washing tower, and neutralizes a small amount of isobutyric acid or n-butyric acid through potassium hydroxide weak alkali solution;
  • the dehydrated hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the second rectification tower to remove light components under negative pressure.
  • the negative pressure of the second rectification tower is -0.098MPa, so
  • the temperature at the bottom of the second rectification tower is 164°C, the light components are returned to the esterification tower for esterification, and hexadecyl n-butyl ester or hexadecyl isobutyl ester is extracted from the bottom of the tower;
  • a continuous production process of hexadecyl diester comprises the following steps:
  • Esterification N-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and catalyst are continuously entered into the esterification tower according to the mass ratio of 6:10:0.03 for esterification Normal pressure reaction, the tower still temperature of esterification tower is 175 °C, generates hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product, and described crude product is extracted from the bottom of the tower;
  • the catalyst is BO 3 3- /ZrO 2 /Ce 4+
  • the preparation method of the BO 3 3- /ZrO 2 /Ce 4+ is as follows: dissolve CeO 2 in a 3mol/L boric acid solution to prepare a 0.1mol/L Ce 4+ solution, then add ZrO 2 into the Ce 4+ solution for 20h, filter with suction, dry, and roast, the roasting temperature is 600°C, and the roasting time is 2h.
  • the esterified hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the first rectification tower to remove n-butyric acid or isobutyric acid under negative pressure, and the first rectification tower is under negative pressure It is -0.095MPa, the temperature of the first rectification tower is 165°C, the removed n-butyric acid or isobutyric acid is returned from the top of the tower to the esterification tower to further participate in the reaction, and the hexadecyl n-butyl ester is produced from the tower Or the initial product of hexadecyl isobutyl ester;
  • Alkali washing the deacidified hexadecyl n-butyl ester or hexadecyl isobutyl ester primary product enters the alkali washing tower, and neutralizes a small amount of isobutyric acid or n-butyric acid through potassium hydroxide weak alkali solution;
  • the dehydrated hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the second rectification tower to remove light components under negative pressure, and the negative pressure of the second rectification tower is -0.099MPa, so The temperature in the bottom of the second rectification tower is 168°C, the light components are returned to the esterification tower for esterification, and hexadecyl n-butyl ester or hexadecyl isobutyl ester is extracted from the bottom of the tower;
  • a continuous production process of hexadecyl diester comprises the following steps:
  • Esterification N-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and catalyst are continuously entered into the esterification tower according to the mass ratio of 6:10:0.03 for esterification Normal pressure reaction, the tower still temperature of esterification tower is 175 °C, generates hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product, and described crude product is extracted from the bottom of the tower;
  • the catalyst is BO 3 3- /ZrO 2
  • the preparation method of the BO 3 3- /ZrO 2 is as follows: dissolve ZrO 2 in a 3mol/L boric acid solution for 20 hours, filter with suction, dry, and roast at 600°C. The roasting time is 2h.
  • the esterified hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the first rectification tower to remove n-butyric acid or isobutyric acid under negative pressure, and the first rectification tower is under negative pressure It is -0.095MPa, the temperature of the first rectification tower is 165°C, the removed n-butyric acid or isobutyric acid is returned from the top of the tower to the esterification tower to further participate in the reaction, and the hexadecyl n-butyl ester is produced from the tower Or the initial product of hexadecyl isobutyl ester;
  • Alkali washing the deacidified hexadecyl n-butyl ester or hexadecyl isobutyl ester primary product enters the alkali washing tower, and neutralizes a small amount of isobutyric acid or n-butyric acid through potassium hydroxide weak alkali solution;
  • the dehydrated hexadecyl n-butyl ester or hexadecyl isobutyl ester crude product enters the second rectification tower to remove light components under negative pressure, and the negative pressure of the second rectification tower is -0.099MPa, so The temperature in the bottom of the second rectification tower is 168°C, the light components are returned to the esterification tower for esterification, and hexadecyl n-butyl ester or hexadecyl isobutyl ester is extracted from the bottom of the tower;
  • n-butyric acid or isobutyric acid, 2,2,4-trimethyl-1,3-pentanediol and a catalyst are subjected to esterification reaction to obtain hexadecyl
  • the crude product of n-butyl ester or hexadecyl isobutyl ester is deacidified, alkali washed, dehydrated, delightened, deweighted and deodorized to obtain hexadecyl n-butyl ester or hexadecyl isobutyl ester in order to improve the stability of the product It shortens the esterification reaction time, reduces by-products, and improves product yield and production efficiency.

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Abstract

一种十六碳双酯的连续化生产工艺，包括以下步骤：S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂连续进入酯化塔进行酯化常压反应，生成粗品；S2.脱酸：粗品进入第一精馏塔在负压下脱除正丁酸或异丁酸；S3.碱洗：初品进入碱洗塔，中和掉微量异丁酸或正丁酸；S4.脱水：十六碳正丁酯或十六碳异丁酯进入脱轻塔脱水；S5.脱轻：十六碳正丁酯或十六碳异丁酯进入第二精馏塔脱除轻组分；S6.脱重：十六碳正丁酯或十六碳异丁酯进入第三精馏塔脱除重组分；S7.脱气味：十六碳正丁酯或十六碳异丁酯进入第四精馏塔脱除轻组分，得到成品。该工艺缩短了酯化反应时间，减少了副产物，提高了产品收率和生产效率。

Description

一种十六碳双酯的连续化生产工艺 技术领域
本发明涉及精细化工技术领域，特别涉及一种十六碳双酯的连续化生产工艺。
背景技术
十六碳双酯为十六碳正丁酯或十六碳异丁酯，十六碳正丁酯或十六碳异丁酯是一种不含苯环的多用途增塑剂，不仅与所有通用的一、二级增塑剂相溶，尤其是与DOP配合使用时可以发挥最佳效果；还是流动性降粘剂，具有抗光性佳，硬化性优良，透明度高、润滑性均衡、抗氧、气味小等特性。
传统的十六碳正/异丁酯(醇酯十六)采用间歇法釜式生产工艺，存在批次不稳定，酯化时间较长，30小时以上，副产物较多，生产效率偏低等弱点。
发明内容
本发明的目的是克服现有技术中存在的不足，提供一种十六碳双酯的连续化生产工艺，缩短酯化时间，减少副产物，提高生产效率。
为了解决上述技术问题，本发明的技术方案为：
一种十六碳双酯的连续化生产工艺，其中：包括以下步骤：
S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂按照质量比为4～6∶7～10∶0.01～0.03连续进入酯化塔进行酯化常压反应，生成十六碳正丁酯或十六碳异丁酯粗品，所述粗品从塔底采出；
S2.脱酸：酯化后的十六碳正丁酯或十六碳异丁酯粗品进入第一精馏塔在负压下脱除正丁酸或异丁酸，脱除的正丁酸或异丁酸从塔顶返回酯化塔进一步参与反应，塔釜采出十六碳正丁酯或十六碳异丁酯初品；
S3.碱洗：脱酸后的十六碳正丁酯或十六碳异丁酯初品进入碱洗塔，通过弱碱溶液中和掉微量异丁酸或正丁酸；
S4.脱水：碱洗后的十六碳正丁酯或十六碳异丁酯进入脱轻塔负压脱水，脱水后十六碳正丁酯或十六碳异丁酯从塔釜采出；
S5.脱轻：脱水后的十六碳正丁酯或十六碳异丁酯粗品进入第二精馏塔进行负压脱除轻组分，轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔釜采出；
S6.脱重：脱除轻组分的十六碳正丁酯或十六碳异丁酯进入第三精馏塔负压脱除重组分，十六碳正丁酯或十六碳异丁酯从塔顶采出；
S7.脱气味：气味主要来源于异丁酸或正丁酸，异丁醇(来自于上一步反应的轻组分)等，脱除重组分的十六碳正丁酯或十六碳异丁酯进入第四精馏塔进一步负压脱除轻组分，塔顶轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔底采出，得到成品十六碳正丁酯或十六碳异丁酯。
优选的是，所述的十六碳双酯的连续化生产工艺，其中：所述步骤S1酯化塔的塔釜温度为165℃～175℃。
优选的是，所述的十六碳双酯的连续化生产工艺，其中：所述步骤S2第一精馏塔负压为-0.090～-0.095MPa，所述第一精馏塔塔釜温度为155℃～165℃。
优选的是，所述的十六碳双酯的连续化生产工艺，其中：所述步骤S3弱碱为碳酸氢钠或氢氧化钾。
优选的是，所述的十六碳双酯的连续化生产工艺，其中：所述步骤S4脱轻塔负压为-0.085～-0.09MPa，塔釜温度为158℃～162℃。
优选的是，所述的十六碳双酯的连续化生产工艺，其中：所述步骤S5第二精馏塔负压为-0.096～-0.099MPa，第二精馏塔塔釜温度为162℃～168℃。
优选的是，所述的十六碳双酯的连续化生产工艺，其中：所述步骤S6第三精馏塔负压为-0.1～-0.105MPa，第三精馏塔塔釜温度为172℃～178℃。
优选的是，所述的十六碳双酯的连续化生产工艺，其中：所述步骤S7第四精馏塔负压为-0.096～-0.099MPa，第四精馏塔塔釜温度为175℃～180℃。
优选的是，所述的十六碳双酯的连续化生产工艺，其中：所述步骤S1催化剂为BO 3 3-/ZrO 2/Ce 4+，所述BO 3 3-/ZrO 2/Ce 4+的制备方法如下：
将CeO 2溶于硼酸溶液中，配成Ce 4+溶液，再将ZrO 2加入Ce 4+溶液中10～20h，抽滤，干燥，焙烧，得到BO 3 3-/ZrO 2/Ce 4+。
优选的是，所述的十六碳双酯的连续化生产工艺，其中：所述硼酸溶液的浓度为1～3mol/L，所述Ce 4+溶液的浓度为0.05～0.1mol/L，所述焙烧温度为500～600℃，焙烧时间为2～4h。
在酸的作用下，酯化反应一般是按照酰氧键断裂的反应历程进行，正丁酸或异丁酸在强 酸的作用下，首先与H +结合，使得羰基中的碳原子带正电荷而易和醇氧原子结合成键生成十六碳正丁酯或十六碳异丁酯。
固体超强酸催化剂其活性中心就是质子算和路易斯酸，本专利中BO 3 3-/ZrO 2固体超强酸中心的形成主要是源于BO 3 3-在表面配位吸附，使得Zr-O键上电子云强烈偏移，强化了路易斯酸中心，同时更易使H 2O发生解离吸附而产生质子酸中心，对于BO 3 3-/ZrO 2/Ce 4+来说，BO 3 3-/ZrO 2掺杂了一定量的Ce 4+，使得BO 3 3-/ZrO 2进行了改性，BO 3 3-/ZrO 2表面吸附了BO 3 3-，又吸附了一定量的Ce 4+，Ce 4+本身就是路易斯酸，通过BO 3 3-的吸附，不但增加了Ce 4+的路易斯酸强度，又使得该催化剂比BO 3 3-/ZrO 2多了一部分路易斯酸中心，正是由此BO 3 3-/ZrO 2/Ce 4+比BO 3 3-/ZrO 2具有更高的酸强度，从而提高酯化催化的活性。
采用上述技术方案，本发明的十六碳双酯的连续化生产工艺，将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂进行酯化反应得到十六碳正丁酯或十六碳异丁酯粗品，粗品依次经过脱酸、碱洗、脱水、脱轻、脱重、脱气味得到十六碳正丁酯或十六碳异丁酯，提高产品的稳定性，缩短了酯化反应时间，减少了副产较，提高了产品收率和生产效率。
具体实施方式
下面结合实施例对本发明的具体实施方式作进一步说明。在此需要说明的是，对于这些实施方式的说明用于帮助理解本发明，但并不构成对本发明的限定。此外，下面所描述的本发明各个实施方式中所涉及的技术特征只要彼此之间未构成冲突就可以相互组合。
异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂通过酯化反应，生成十六碳异丁酯，反应式如下：
Figure PCTCN2021117985-appb-000001
副反应就是十二碳醇酯与正丁酸的反应，如下所示：
Figure PCTCN2021117985-appb-000002
辛二醇与正丁酸的副反应主要就是单酯，如下所示：
Figure PCTCN2021117985-appb-000003
通过本发明的连续化生产十六碳双酯的生产工艺缩短酯化时间，减少副产较，提高生产效率。
实施例1
一种十六碳双酯的连续化生产工艺，其中：包括以下步骤：
S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂按照质量比为4∶7∶0.01连续进入酯化塔进行酯化常压反应，酯化塔的塔釜温度为165℃，生成十六碳正丁酯或十六碳异丁酯粗品，所述粗品从塔底采出；
催化剂为BO 3 3-/ZrO 2/Ce 4+，所述BO 3 3-/ZrO 2/Ce 4+的制备方法如下：将CeO 2溶于1mol/L硼酸溶液中，配成0.05mol/L Ce 4+溶液，再将ZrO 2加入Ce 4+溶液中10h，抽滤，干燥，焙烧，焙烧温度为500℃，焙烧时间为4h。
S2.脱酸：酯化后的十六碳正丁酯或十六碳异丁酯粗品进入第一精馏塔在负压下脱除正丁酸或异丁酸，第一精馏塔负压为-0.090MPa，所述第一精馏塔塔釜温度为155℃，脱除的正丁酸或异丁酸从塔顶返回酯化塔进一步参与反应，塔釜采出十六碳正丁酯或十六碳异丁酯初品；
S3.碱洗：脱酸后的十六碳正丁酯或十六碳异丁酯初品进入碱洗塔，通过碳酸氢钠溶液中和掉微量异丁酸或正丁酸；
S4.脱水：碱洗后的十六碳正丁酯或十六碳异丁酯进入脱轻塔负压脱水，脱轻塔负压为-0.085MPa，塔釜温度为158℃，脱水后十六碳正丁酯或十六碳异丁酯从塔釜采出；
S5.脱轻：脱水后的十六碳正丁酯或十六碳异丁酯粗品进入第二精馏塔进行负压脱除轻组分，第二精馏塔负压为-0.096MPa，所述第二精馏塔塔釜温度为162℃，轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔釜采出；
S6.脱重：脱除轻组分的十六碳正丁酯或十六碳异丁酯进入第三精馏塔负压脱除重组分，第三精馏塔负压为-0.1MPa，所述第三精馏塔塔釜温度为172℃，十六碳正/异丁酯从塔顶采出；
S7.脱气味：脱除重组分的十六碳正丁酯或十六碳异丁酯进入第四精馏塔进一步负压脱除轻组分，第四精馏塔负压为-0.096MPa，所述第四精馏塔塔釜温度为175℃，塔顶轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔底采出，得到成品十六碳正丁酯或十六碳异丁酯。
实施例2
一种十六碳双酯的连续化生产工艺，其中：包括以下步骤：
S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂按照质量比为5∶8∶0.02连续进入酯化塔进行酯化常压反应，酯化塔的塔釜温度为170℃，生成十六碳正丁酯或十六碳异丁酯粗品，所述粗品从塔底采出；
催化剂为BO 3 3-/ZrO 2/Ce 4+，所述BO 3 3-/ZrO 2/Ce 4+的制备方法如下：将CeO 2溶于2mol/L硼酸溶液中，配成0.08mol/L C e 4+溶液，再将ZrO 2加入Ce 4+溶液中15h，抽滤，干燥，焙烧，焙烧温度为550℃，焙烧时间为3h。
S2.脱酸：酯化后的十六碳正丁酯或十六碳异丁酯粗品进入第一精馏塔在负压下脱除正丁 酸或异丁酸，第一精馏塔负压为0.092MPa，所述第一精馏塔塔釜温度为160℃，脱除的正丁酸或异丁酸从塔顶返回酯化塔进一步参与反应，塔釜采出十六碳正丁酯或十六碳异丁酯初品；
S3.碱洗：脱酸后的十六碳正丁酯或十六碳异丁酯初品进入碱洗塔，通过氢氧化钾弱碱溶液中和掉微量异丁酸或正丁酸；
S4.脱水：碱洗后的十六碳正丁酯或十六碳异丁酯进入脱轻塔负压脱水，脱轻塔负压为-0.087MPa，塔釜温度为160℃，脱水后十六碳正丁酯或十六碳异丁酯从塔釜采出；
S5.脱轻：脱水后的十六碳正丁酯或十六碳异丁酯粗品进入第二精馏塔进行负压脱除轻组分，第二精馏塔负压为-0.098MPa，所述第二精馏塔塔釜温度为164℃，轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔釜采出；
S6.脱重：脱除轻组分的十六碳正丁酯或十六碳异丁酯进入第三精馏塔负压脱除重组分，第三精馏塔负压为-0.102MPa，所述第三精馏塔塔釜温度为174℃，十六碳正丁酯或十六碳异丁酯从塔顶采出；
S7.脱气味：脱除重组分的十六碳正丁酯或十六碳异丁酯进入第四精馏塔进一步负压脱除轻组分，第四精馏塔负压为-0.098MPa，所述第四精馏塔塔釜温度为177℃，塔顶轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔底采出，得到成品十六碳正丁酯或十六碳异丁酯。
实施例3
一种十六碳双酯的连续化生产工艺，其中：包括以下步骤：
S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂按照质量比为6∶10∶0.03连续进入酯化塔进行酯化常压反应，酯化塔的塔釜温度为175℃，生成十六碳正丁酯或十六碳异丁酯粗品，所述粗品从塔底采出；
催化剂为BO 3 3-/ZrO 2/Ce 4+，所述BO 3 3-/ZrO 2/Ce 4+的制备方法如下：将CeO 2溶于3mol/L硼酸溶液中，配成0.1mol/L Ce 4+溶液，再将ZrO 2加入Ce 4+溶液中20h，抽滤，干燥，焙烧，焙烧温度为600℃，焙烧时间为2h。
S2.脱酸：酯化后的十六碳正丁酯或十六碳异丁酯粗品进入第一精馏塔在负压下脱除正丁酸或异丁酸，第一精馏塔负压为-0.095MPa，所述第一精馏塔塔釜温度为165℃，脱除的正丁酸或异丁酸从塔顶返回酯化塔进一步参与反应，塔釜采出十六碳正丁酯或十六碳异丁酯初品；
S3.碱洗：脱酸后的十六碳正丁酯或十六碳异丁酯初品进入碱洗塔，通过氢氧化钾弱碱溶 液中和掉微量异丁酸或正丁酸；
S4.脱水：碱洗后的十六碳正丁酯或十六碳异丁酯进入脱轻塔负压脱水，脱轻塔负压为-0.09MPa，塔釜温度为162℃，脱水后十六碳正丁酯或十六碳异丁酯从塔釜采出；
S5.脱轻：脱水后的十六碳正丁酯或十六碳异丁酯粗品进入第二精馏塔进行负压脱除轻组分，第二精馏塔负压为-0.099MPa，所述第二精馏塔塔釜温度为168℃，轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔釜采出；
S6.脱重：脱除轻组分的十六碳正丁酯或十六碳异丁酯进入第三精馏塔负压脱除重组分，第三精馏塔负压为-0.105MPa，所述第三精馏塔塔釜温度为178℃，十六碳正/异丁酯从塔顶采出；
S7.脱气味：脱除重组分的十六碳正丁酯或十六碳异丁酯进入第四精馏塔进一步负压脱除轻组分，第四精馏塔负压为-0.099MPa，所述第四精馏塔塔釜温度为180℃，塔顶轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔底采出，得到成品十六碳正丁酯或十六碳异丁酯。
对比例1
一种十六碳双酯的连续化生产工艺，其中：包括以下步骤：
S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂按照质量比为4∶7∶0.01连续进入酯化塔进行酯化常压反应，酯化塔的塔釜温度为165℃，生成十六碳正丁酯或十六碳异丁酯粗品，所述粗品从塔底采出；
催化剂为BO 3 3-/ZrO 2/Ce 4+，所述BO 3 3-/ZrO 2/Ce 4+的制备方法如下：将CeO 2溶于1mol/L硼酸溶液中，配成0.05mol/L Ce 4+溶液，再将ZrO 2加入Ce 4+溶液中10h，抽滤，干燥，焙烧，焙烧温度为500℃，焙烧时间为4h。
S2.脱酸：酯化后的十六碳正丁酯或十六碳异丁酯粗品进入第一精馏塔在负压下脱除正丁酸或异丁酸，第一精馏塔负压为-0.090MPa，所述第一精馏塔塔釜温度为155℃，脱除的正丁酸或异丁酸从塔顶返回酯化塔进一步参与反应，塔釜采出十六碳正丁酯或十六碳异丁酯初品；
S3.碱洗：脱酸后的十六碳正丁酯或十六碳异丁酯初品进入碱洗塔，通过碳酸氢钠溶液中和掉微量异丁酸或正丁酸；
S4.脱水：碱洗后的十六碳正丁酯或十六碳异丁酯进入脱轻塔负压脱水，脱轻塔负压为-0.085MPa，塔釜温度为158℃，脱水后十六碳正丁酯或十六碳异丁酯从塔釜采出；
S5.脱重：脱水后的十六碳正丁酯或十六碳异丁酯进入第三精馏塔负压脱除重组分，第三精馏塔负压为-0.1MPa，所述第三精馏塔塔釜温度为172℃，十六碳正/异丁酯从塔顶采出；
S6.脱气味：脱除重组分的十六碳正丁酯或十六碳异丁酯进入第四精馏塔进一步负压脱除轻组分，第四精馏塔负压为-0.096MPa，所述第四精馏塔塔釜温度为175℃，塔顶轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔底采出，得到成品十六碳正丁酯或十六碳异丁酯。
对比例2
一种十六碳双酯的连续化生产工艺，其中：包括以下步骤：
S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂按照质量比为5∶8∶0.02连续进入酯化塔进行酯化常压反应，酯化塔的塔釜温度为170℃，生成十六碳正丁酯或十六碳异丁酯粗品，所述粗品从塔底采出；
催化剂为BO 3 3-/ZrO 2/Ce 4+，所述BO 3 3-/ZrO 2/Ce 4+的制备方法如下：将CeO 2溶于2mol/L硼酸溶液中，配成0.08mol/L Ce 4+溶液，再将ZrO 2加入Ce 4+溶液中15h，抽滤，干燥，焙烧，焙烧温度为550℃，焙烧时间为3h。
S2.脱酸：酯化后的十六碳正丁酯或十六碳异丁酯粗品进入第一精馏塔在负压下脱除正丁酸或异丁酸，第一精馏塔负压为-0.092MPa，所述第一精馏塔塔釜温度为160℃，脱除的正丁酸或异丁酸从塔顶返回酯化塔进一步参与反应，塔釜采出十六碳正丁酯或十六碳异丁酯初品；
S3.碱洗：脱酸后的十六碳正丁酯或十六碳异丁酯初品进入碱洗塔，通过氢氧化钾弱碱溶液中和掉微量异丁酸或正丁酸；
S4.脱水：碱洗后的十六碳正丁酯或十六碳异丁酯进入脱轻塔负压脱水，脱轻塔负压为-0.087MPa，塔釜温度为160℃，脱水后十六碳正丁酯或十六碳异丁酯从塔釜采出；
S5.脱轻：脱水后的十六碳正丁酯或十六碳异丁酯粗品进入第二精馏塔进行负压脱除轻组分，第二精馏塔负压为-0.098MPa，所述第二精馏塔塔釜温度为164℃，轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔釜采出；
S7.脱气味：脱除轻组分的十六碳正丁酯或十六碳异丁酯进入第四精馏塔进一步负压脱除轻组分，第四精馏塔负压为-0.098MPa，所述第四精馏塔塔釜温度为177℃，塔顶轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔底采出，得到成品十六碳正丁酯或十六碳异丁酯。
对比例3
一种十六碳双酯的连续化生产工艺，其中：包括以下步骤：
S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂按照质量比为6∶10∶0.03连续进入酯化塔进行酯化常压反应，酯化塔的塔釜温度为175℃，生成十六碳正丁酯或十六碳异丁酯粗品，所述粗品从塔底采出；
催化剂为BO 3 3-/ZrO 2/Ce 4+，所述BO 3 3-/ZrO 2/Ce 4+的制备方法如下：将CeO 2溶于3mol/L硼酸溶液中，配成0.1mol/L Ce 4+溶液，再将ZrO 2加入Ce 4+溶液中20h，抽滤，干燥，焙烧，焙烧温度为600℃，焙烧时间为2h。
S2.脱酸：酯化后的十六碳正丁酯或十六碳异丁酯粗品进入第一精馏塔在负压下脱除正丁酸或异丁酸，第一精馏塔负压为-0.095MPa，所述第一精馏塔塔釜温度为165℃，脱除的正丁酸或异丁酸从塔顶返回酯化塔进一步参与反应，塔釜采出十六碳正丁酯或十六碳异丁酯初品；
S3.碱洗：脱酸后的十六碳正丁酯或十六碳异丁酯初品进入碱洗塔，通过氢氧化钾弱碱溶液中和掉微量异丁酸或正丁酸；
S4.脱水：碱洗后的十六碳正丁酯或十六碳异丁酯进入脱轻塔负压脱水，脱轻塔负压为-0.09MPa，塔釜温度为162℃，脱水后十六碳正丁酯或十六碳异丁酯从塔釜采出；
S5.脱轻：脱水后的十六碳正丁酯或十六碳异丁酯粗品进入第二精馏塔进行负压脱除轻组分，第二精馏塔负压为-0.099MPa，所述第二精馏塔塔釜温度为168℃，轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔釜采出；
S6.脱重：脱除轻组分的十六碳正丁酯或十六碳异丁酯进入第三精馏塔负压脱除重组分，第三精馏塔负压为-0.105MPa，所述第三精馏塔塔釜温度为178℃，十六碳正/异丁酯从塔顶采出，得到成品十六碳正丁酯或十六碳异丁酯。
对比例4
一种十六碳双酯的连续化生产工艺，其中：包括以下步骤：
S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂按照质量比为6∶10∶0.03连续进入酯化塔进行酯化常压反应，酯化塔的塔釜温度为175℃，生成十六碳正丁酯或十六碳异丁酯粗品，所述粗品从塔底采出；
催化剂为BO 3 3-/ZrO 2，所述BO 3 3-/ZrO 2的制备方法如下：将ZrO 2溶于3mol/L硼酸溶液中20h，抽滤，干燥，焙烧，焙烧温度为600℃，焙烧时间为2h。
S2.脱酸：酯化后的十六碳正丁酯或十六碳异丁酯粗品进入第一精馏塔在负压下脱除正丁 酸或异丁酸，第一精馏塔负压为-0.095MPa，所述第一精馏塔塔釜温度为165℃，脱除的正丁酸或异丁酸从塔顶返回酯化塔进一步参与反应，塔釜采出十六碳正丁酯或十六碳异丁酯初品；
S3.碱洗：脱酸后的十六碳正丁酯或十六碳异丁酯初品进入碱洗塔，通过氢氧化钾弱碱溶液中和掉微量异丁酸或正丁酸；
S4.脱水：碱洗后的十六碳正丁酯或十六碳异丁酯进入脱轻塔负压脱水，脱轻塔负压为-0.09MPa，塔釜温度为162℃，脱水后十六碳正丁酯或十六碳异丁酯从塔釜采出；
S5.脱轻：脱水后的十六碳正丁酯或十六碳异丁酯粗品进入第二精馏塔进行负压脱除轻组分，第二精馏塔负压为-0.099MPa，所述第二精馏塔塔釜温度为168℃，轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔釜采出；
S6.脱重：脱除轻组分的十六碳正丁酯或十六碳异丁酯进入第三精馏塔负压脱除重组分，第三精馏塔负压为-0.105MPa，所述第三精馏塔塔釜温度为178℃，十六碳正/异丁酯从塔顶采出；
S7.脱气味：脱除重组分的十六碳正丁酯或十六碳异丁酯进入第四精馏塔进一步负压脱除轻组分，第四精馏塔负压为-0.099MPa，所述第四精馏塔塔釜温度为180℃，塔顶轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔底采出，得到成品十六碳正丁酯或十六碳异丁酯。
下面列出实施例1-3和对比例1-3的测试结果：
  实施例1 实施例2 实施例3 对比例1 对比例2 对比例3 对比例4
转化率％ 99.0 99.5 99.7 99.2 99.4 96.2 78.2
收率％ 95.4 96.7 97.8 87.1 80.2 84.3 80.9
本发明的十六碳双酯的连续化生产工艺，将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂进行酯化反应得到十六碳正丁酯或十六碳异丁酯粗品，粗品依次经过脱酸、碱洗、脱水、脱轻、脱重、脱气味得到十六碳正丁酯或十六碳异丁酯，提高产品的稳定性，缩短了酯化反应时间，减少了副产较，提高了产品收率和生产效率。
以上结合实施例对本发明的实施方式作了详细说明，但本发明不限于所描述的实施方式。对于本领域的技术人员而言，在不脱离本发明原理和精神的情况下，对这些实施方式进行多种变化、修改、替换和变型，仍落入本发明的保护范围内。

Claims (10)

  1. 一种十六碳双酯的连续化生产工艺，其特征在于：包括以下步骤：
    S1.酯化：将正丁酸或异丁酸、2，2，4-三甲基-1，3-戊二醇以及催化剂按照质量比为4～6∶7～10∶0.01～0.03连续进入酯化塔进行酯化常压反应，生成十六碳正丁酯或十六碳异丁酯粗品，所述粗品从塔底采出；
    S2.脱酸：酯化后的十六碳正丁酯或十六碳异丁酯粗品进入第一精馏塔在负压下脱除正丁酸或异丁酸，脱除的正丁酸或异丁酸从塔顶返回酯化塔进一步参与反应，塔釜采出十六碳正丁酯或十六碳异丁酯初品；
    S3.碱洗：脱酸后的十六碳正丁酯或十六碳异丁酯初品进入碱洗塔，通过弱碱溶液中和掉微量异丁酸或正丁酸；
    S4.脱水：碱洗后的十六碳正丁酯或十六碳异丁酯进入脱轻塔负压脱水，脱水后十六碳正丁酯或十六碳异丁酯从塔釜采出；
    S5.脱轻：脱水后的十六碳正丁酯或十六碳异丁酯进入第二精馏塔进行负压脱除轻组分，轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔釜采出；
    S6.脱重：脱除轻组分的十六碳正丁酯或十六碳异丁酯进入第三精馏塔负压脱除重组分，十六碳正丁酯或十六碳异丁酯从塔顶采出；
    S7.脱气味：脱除重组分的十六碳正丁酯或十六碳异丁酯进入第四精馏塔进一步负压脱除轻组分，塔顶轻组分返回酯化塔酯化，十六碳正丁酯或十六碳异丁酯从塔底采出，得到成品十六碳正丁酯或十六碳异丁酯。
  2. 根据权利要求1所述的十六碳双酯的连续化生产工艺，其特征在于：所述步骤S1酯化塔的塔釜温度为165℃～175℃。
  3. 根据权利要求1所述的十六碳双酯的连续化生产工艺，其特征在于：所述步骤S2第一精馏塔负压为-0.090～-0.095MPa，所述第一精馏塔塔釜温度为155℃～165℃。
  4. 根据权利要求1所述的十六碳双酯的连续化生产工艺，其特征在于：所述步骤S3弱碱为碳酸氢钠或氢氧化钾。
  5. 根据权利要求1所述的十六碳双酯的连续化生产工艺，其特征在于：所述步骤S4脱轻塔负压为-0.085～-0.09MPa，塔釜温度为158℃～162℃。
  6. 根据权利要求1所述的十六碳双酯的连续化生产工艺，其特征在于：所述步骤S5第二精馏塔负压为-0.096～-0.099MPa，所述第二精馏塔塔釜温度为162℃～168℃。
  7. 根据权利要求1所述的十六碳双酯的连续化生产工艺，其特征在于：所述步骤S6第三精馏塔负压为-0.1～-0.105MPa，所述第三精馏塔塔釜温度为172℃～178℃。
  8. 根据权利要求1所述的十六碳双酯的连续化生产工艺，其特征在于：所述步骤S7第四精馏塔负压为-0.096～-0.099MPa，所述第四精馏塔塔釜温度为175℃～180℃。
  9. 根据权利要求1所述的十六碳双酯的连续化生产工艺，其特征在于：所述步骤S1催化剂为BO 3 3-/ZrO 2/Ce 4+，所述BO 3 3-/ZrO 2/Ce 4+的制备方法如下：
    将CeO 2溶于硼酸溶液中，配成Ce 4+溶液，再将ZrO 2加入Ce 4+溶液中10～20h，抽滤，干燥，焙烧，得到BO 3 3-/ZrO 2/Ce 4+。
  10. 根据权利要求9所述的十六碳双酯的连续化生产工艺，其特征在于：所述硼酸溶液的浓度为1～3mol/L，所述Ce 4+溶液的浓度为0.05～0.1mol/L，所述焙烧温度为500～600℃，焙烧时间为2～4h。
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