阅读说明：本技术 一种双氧水法制环氧氯丙烷水相中溶剂回收的方法 (Method for recovering solvent in aqueous phase of epoxy chloropropane prepared by hydrogen peroxide method ) 是由 黄杰军 徐林 丁克鸿 徐志斌 徐文轩 胡金良 黄文嵘 王东哲 于 2021-01-12 设计创作，主要内容包括：本发明提供一种双氧水法制环氧氯丙烷水相中溶剂回收的方法,所述方法通过三级精馏,并将所述第二溶剂馏分与第三精馏的塔釜循环液换热；所述第三溶剂馏分与双氧水法制环氧氯丙烷水相换热,使能量得到充分利用,显著降低了热负荷的蒸汽消耗量,从而降低了双氧水法制环氧氯丙烷的成本,应用前景广阔。(The invention provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which comprises the following steps of carrying out three-stage rectification, and carrying out heat exchange on a second solvent fraction and a tower kettle circulating liquid of a third rectification; the third solvent fraction exchanges heat with the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method, so that energy is fully utilized, and the steam consumption of heat load is obviously reduced, thereby reducing the cost of the epoxy chloropropane prepared by the hydrogen peroxide method and having wide application prospect.)

1. A method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method is characterized by comprising the following steps:

(1) performing heat exchange on the aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, and performing first rectification to obtain a first fraction containing 3-chloropropene and an organic solvent and a first kettle liquid;

(2) performing second rectification on the first part of the first kettle liquid to obtain a second solvent fraction; performing third rectification on a second part of the first kettle liquid to obtain a third solvent fraction;

the second solvent fraction exchanges heat with tower kettle circulating liquid of the third rectification;

and exchanging heat between the third solvent fraction and the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method.

2. The method as claimed in claim 1, wherein the aqueous phase of epichlorohydrin prepared by hydrogen peroxide solution process contains organic solvent, 3-chloropropene and water;

preferably, the content of the organic solvent in the aqueous phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 1-50 wt%;

preferably, the content of water in the aqueous phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 46-99 wt%;

preferably, the content of 3-chloropropene in the aqueous phase of epoxy chloropropane prepared by the hydrogen peroxide method is 0.1-4 wt%.

3. The method according to claim 1 or 2, wherein the organic solvent in step (1) comprises an alcohol having 6 or less carbon atoms or an organic substance having a boiling point lower than that of water;

preferably, the organic solvent comprises any one of methanol, ethanol, acetonitrile or acetone, preferably methanol;

preferably, the content of 3-chloropropene in the first kettle liquid is less than 0.1 wt%.

4. The process according to any one of claims 1 to 3, wherein the first rectification in step (1) is a first atmospheric rectification;

preferably, the absolute pressure of the first atmospheric distillation is 0.09-0.12 MPa;

preferably, the temperature of a tower kettle of the first atmospheric distillation is 85-100 ℃;

preferably, the tower top temperature of the first atmospheric distillation is 40-50 ℃;

preferably, the theoretical plate number of the first atmospheric distillation is 15-30;

preferably, the tower top reflux ratio of the first atmospheric distillation is 1-3.

5. The method according to any one of claims 1 to 3, wherein the first rectification in step (1) is a first negative pressure rectification;

preferably, the temperature of a tower kettle of the first negative pressure rectification is 40-80 ℃;

preferably, the tower top temperature of the first negative pressure rectification is 30-45 ℃;

preferably, the theoretical plate number of the first negative pressure rectification is 15-30;

preferably, the tower top reflux ratio of the first negative pressure rectification is 1-3;

preferably, the absolute pressure of the first negative pressure rectification is 60-760 mmHg.

6. The method according to any one of claims 1 to 5, wherein the temperature of the bottom of the second rectification column in the step (2) is 120 to 180 ℃;

preferably, the tower top temperature of the second rectification is 100-150 ℃;

preferably, the theoretical plate number of the second rectification is 5-45;

preferably, the tower top reflux ratio of the second rectification is 1-3;

preferably, the second rectification is a pressurized operation;

preferably, the absolute pressure of the second rectification is 0.2-1.5 MPa.

7. The process according to any one of claims 1 to 6, wherein the third rectification in step (2) is a third atmospheric rectification;

preferably, the temperature of a tower kettle of the third atmospheric distillation is 80-100 ℃;

preferably, the tower top temperature of the third atmospheric distillation is 55-65 ℃;

preferably, the theoretical plate number of the third atmospheric distillation is 5-45;

preferably, the tower top reflux ratio of the third atmospheric distillation is 1-3.

8. The method according to any one of claims 1 to 7, wherein the third rectification in the step (2) is a third negative pressure rectification;

preferably, the absolute pressure of the third negative pressure rectification is 60-760 mmHg;

preferably, the temperature of a tower kettle of the third negative pressure rectification is 60-80 ℃;

preferably, the tower top temperature of the third negative pressure rectification is 40-60 ℃;

preferably, the theoretical plate number of the third negative pressure rectification is 5-45;

preferably, the tower top reflux ratio of the third negative pressure rectification is 1-3.

9. The method of any one of claims 1 to 8, wherein the first portion of the first still liquor comprises 2 to 60 wt% of the total mass of the first still liquor;

preferably, the second solvent fraction is 2 to 60 wt% of the total amount of the second solvent fraction and the third solvent fraction.

10. A method according to any one of claims 1 to 9, characterized in that the method comprises the steps of:

(1) performing first rectification on an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method to obtain a first fraction containing 3-chloropropene and an organic solvent and a first kettle liquid; the content of 3-chloropropene in the first kettle liquid is less than 0.1 wt%;

the content of the organic solvent in the aqueous phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 1-50 wt%, the content of water is 46-99 wt%, and the content of 3-chloropropene is 0.1-4 wt%;

the first rectification is first atmospheric rectification, the temperature of a tower kettle is 85-100 ℃, the temperature of a tower top is 40-50 ℃, the number of theoretical plates is 15-30, and the reflux ratio of the tower top is 1-3; or the first rectification is first negative pressure rectification, the temperature of a tower kettle is 40-80 ℃, the temperature of a tower top is 30-45 ℃, the number of theoretical plates is 15-30, the reflux ratio of the tower top is 1-3, and the absolute pressure is 60-760 mmHg;

(2) performing second rectification on the first part of the first kettle liquid to obtain a second solvent fraction; performing third rectification on a second part of the first kettle liquid to obtain a third solvent fraction;

the temperature of a tower kettle of the second rectification is 120-180 ℃, the temperature of a tower top is 100-150 ℃, the number of theoretical plates is 5-45, the reflux ratio of the tower top is 1-3, and the absolute pressure is 0.2-1.5 MPa;

the third rectification is third atmospheric rectification, the temperature of a tower kettle is 80-100 ℃, the temperature of a tower top is 55-65 ℃, the number of theoretical plates is 5-45, and the reflux ratio of the tower top is 1-3; or the third rectification is third negative pressure rectification, the absolute pressure is 60-760 mmHg, the temperature of a tower kettle is 60-80 ℃, the temperature of a tower top is 40-60 ℃, the number of theoretical plates is 5-45, and the reflux ratio of the tower top is 1-3;

the second solvent fraction accounts for 2-60 wt% of the total amount of the second solvent fraction and the third solvent fraction, and the second solvent fraction exchanges heat with tower kettle circulating liquid of the third rectification.

Technical Field

The invention relates to the technical field of resource recovery treatment, in particular to a method for recovering a solvent in an aqueous phase of epoxy chloropropane by a hydrogen peroxide method.

Background

Epichlorohydrin is also known as epichlorohydrin, is a volatile and unstable colorless liquid, is mainly used for preparing epoxy resin, epichlorohydrin rubber and the like, and can also be used as an organic solvent. The epoxy resin prepared by using the epoxy resin as a raw material has the characteristics of strong cohesiveness, chemical medium corrosion resistance, low shrinkage, good chemical stability, high impact strength, excellent dielectric property and the like.

The method for producing epichlorohydrin by a direct oxidation method is to prepare epichlorohydrin by catalyzing chloropropene and hydrogen peroxide epoxidation by using a titanium-silicon molecular sieve, and directly synthesize the epichlorohydrin by the chloropropene in one step. The process generally adopts a large amount of solvents including low-carbon alcohols such as methanol and the like as solvents, and dissolves excessive 3-chloropropene in a methanol solution to react with hydrogen peroxide, so that the higher conversion rate of the hydrogen peroxide and the selectivity of epoxy chloropropane are ensured.

Although the direct epoxidation reaction of chloropropene and hydrogen peroxide has high selectivity and conversion rate, a large amount of circulating methanol exists in the reaction product, so that the energy consumption for separating the product of the direct epoxidation process is high. If the methanol recovery in the epichlorohydrin refining is finished by adopting a common rectification method, the method is only suitable for the condition of small production scale of the epichlorohydrin. When the production scale of the epichlorohydrin is enlarged, the amount of the solvent required for refining is increased sharply, and the energy consumption is obviously too high.

Therefore, it is urgently needed to develop a method for reducing the energy consumption of solvent recovery and promoting the large-scale industrialization of the direct oxidation process.

Disclosure of Invention

In view of the problems in the prior art, the invention provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method.

In order to achieve the purpose, the invention adopts the following technical scheme:

the invention provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which comprises the following steps:

(1) performing heat exchange on the aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, and performing first rectification to obtain a first fraction containing 3-chloropropene and an organic solvent and a first kettle liquid;

(2) performing second rectification on the first part of the first kettle liquid to obtain a second solvent fraction; performing third rectification on a second part of the first kettle liquid to obtain a third solvent fraction;

the second solvent fraction exchanges heat with tower kettle circulating liquid of the third rectification;

and exchanging heat between the third solvent fraction and the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method.

In the method for recovering the solvent in the aqueous phase of the epoxy chloropropane prepared by the hydrogen peroxide method, because the aqueous phase has relatively more water content and the purity of the organic solvent is not high, a large amount of heat is consumed when the purification and recovery are carried out by adopting the rectification process. And moreover, the heat of the third solvent fraction is further used for preheating the raw materials, so that the heat is fully utilized, and the application prospect is wide.

Preferably, the aqueous phase of the epoxy chloropropane prepared by the hydrogen peroxide method contains an organic solvent, 3-chloropropene and water.

Preferably, the content of the organic solvent in the aqueous phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 1 to 50 wt%, for example, 1 wt%, 7 wt%, 12 wt%, 18 wt%, 23 wt%, 29 wt%, 34 wt%, 40 wt%, 45 wt% or 50 wt%, etc., but not limited to the recited values, and other values not recited in the range are also applicable.

Preferably, the content of water in the aqueous phase of the epichlorohydrin prepared by the hydrogen peroxide method is 46 to 99 wt%, for example, 46 wt%, 52 wt%, 58 wt%, 64 wt%, 70 wt%, 76 wt%, 82 wt%, 88 wt%, 94 wt% or 99 wt%, etc., but not limited to the recited values, and other values not recited in the range are also applicable.

Preferably, the content of 3-chloropropene in the aqueous phase of epoxy chloropropane prepared by the hydrogen peroxide method is 0.1 to 4 wt%, for example, 0.1 wt%, 0.6 wt%, 1 wt%, 1.4 wt%, 1.9 wt%, 2.3 wt%, 2.7 wt%, 3.2 wt%, 3.6 wt%, or 4 wt%, etc., but not limited to the recited values, and other values not recited in the range are also applicable.

Preferably, the organic solvent in the step (1) comprises alcohol with the number of carbon atoms being less than or equal to 6 or organic matters with the boiling point being less than that of water.

Preferably, the organic solvent comprises any one of methanol, ethanol, acetonitrile or acetone, preferably methanol.

Preferably, the content of 3-chloropropene in the first kettle liquid is less than 0.1 wt%, and may be, for example, 0.09 wt%, 0.08 wt%, 0.07 wt%, 0.06 wt%, 0.05 wt%, 0.04 wt%, 0.03 wt%, 0.02 wt%, 0.01 wt%, or the like.

Preferably, the first rectification in step (1) is a first atmospheric rectification.

Preferably, the absolute pressure of the first atmospheric distillation is 0.09 to 0.12MPa, for example, 0.09MPa, 0.1MPa, 0.11MPa or 0.12MPa, but not limited to the values listed, and other values not listed in this range are also applicable.

Preferably, the column bottom temperature of the first atmospheric distillation is 85 to 100 ℃, for example, 85 ℃, 87 ℃, 89 ℃, 90 ℃, 92 ℃, 94 ℃, 95 ℃, 97 ℃, 99 ℃ or 100 ℃, etc., but not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the first atmospheric distillation has a top temperature of 40 to 50 ℃, for example, 40 ℃, 42 ℃, 43 ℃, 44 ℃, 45 ℃, 46 ℃, 47 ℃, 48 ℃, 49 ℃ or 50 ℃, but not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the theoretical plate number of the first atmospheric distillation is 15 to 30, for example, 15, 17, 19, 20, 22, 24, 25, 27, 29 or 30, etc., but is not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the overhead reflux ratio of the first atmospheric distillation is 1 to 3, and may be, for example, 1, 1.3, 1.5, 1.7, 1.9, 2.2, 2.4, 2.6, 2.8 or 3, etc., but is not limited to the values listed, and other values not listed in this range are also applicable.

Preferably, the first rectification in step (1) is a first negative pressure rectification.

Preferably, the first negative pressure distillation column bottom temperature is 40 ~ 80 ℃, for example can be 40 ℃, 45 ℃, 49 ℃, 54 ℃, 58 ℃, 63 ℃, 67 ℃, 72 ℃, 76 ℃ or 80 ℃, but not limited to the number, in the range of other values are also applicable.

Preferably, the temperature at the top of the first negative pressure distillation column is 30 to 45 ℃, and may be, for example, 30 ℃, 32 ℃, 34 ℃, 35 ℃, 37 ℃, 39 ℃, 40 ℃, 42 ℃, 44 ℃ or 45 ℃, but is not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the theoretical plate number of the first negative pressure distillation is 15 to 30, for example, 15, 17, 19, 20, 22, 24, 25, 27, 29 or 30, etc., but is not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the overhead reflux ratio of the first negative pressure distillation is 1 to 3, and may be, for example, 1, 1.3, 1.5, 1.7, 1.9, 2.2, 2.4, 2.6, 2.8 or 3, but not limited to the values listed, and other values not listed in this range are also applicable.

Preferably, the absolute pressure of the first negative pressure distillation is 60 to 760mmHg, for example, 60mmHg, 138mmHg, 216mmHg, 294mmHg, 372mmHg, 449mmHg, 527mmHg, 605mmHg, 683mmHg or 760mmHg, etc., but is not limited to the recited values, and other values not recited in the range are also applicable.

Preferably, the column bottom temperature of the second rectification in the step (2) is 120 to 180 ℃, for example, 120 ℃, 127 ℃, 134 ℃, 140 ℃, 147 ℃, 154 ℃, 160 ℃, 167 ℃, 174 ℃ or 180 ℃, etc., but not limited to the recited values, and other values not recited in the range are also applicable.

Preferably, the overhead temperature of the second rectification is 100 to 150 ℃, and may be, for example, 100 ℃, 106 ℃, 112 ℃, 117 ℃, 123 ℃, 128 ℃, 134 ℃, 139 ℃, 145 ℃ or 150 ℃, but is not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the theoretical plate number of the second rectification is 5 to 45, for example, 5, 10, 14, 19, 23, 28, 32, 37, 41 or 45, etc., but is not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the overhead reflux ratio of the second rectification is 1 to 3, and may be, for example, 1, 1.3, 1.5, 1.7, 1.9, 2.2, 2.4, 2.6, 2.8 or 3, etc., but is not limited to the values listed, and other values not listed in this range are also applicable.

Preferably, the second rectification is a pressurized operation.

In the invention, in order to realize that the temperature of the second fraction of the second rectification has higher heat quality, the second rectification is pressurized, so that the second fraction is more favorable for providing heat for a tower kettle of the third rectification.

Preferably, the absolute pressure of the second distillation is 0.2 to 1.5MPa, and for example, 0.2MPa, 0.4MPa, 0.5MPa, 0.7MPa, 0.8MPa, 1MPa, 1.1MPa, 1.3MPa, 1.4MPa or 1.5MPa may be used.

Preferably, the third rectification in step (2) is a third atmospheric rectification.

Preferably, the column bottom temperature of the third atmospheric distillation is 80 to 100 ℃, for example, 80 ℃, 83 ℃, 85 ℃, 87 ℃, 89 ℃, 92 ℃, 94 ℃, 96 ℃, 98 ℃ or 100 ℃, etc., but not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the top temperature of the third atmospheric distillation is 55 to 65 ℃, and may be, for example, 55 ℃, 57 ℃, 58 ℃, 59 ℃, 60 ℃, 61 ℃, 62 ℃, 63 ℃, 64 ℃ or 65 ℃, but is not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the theoretical plate number of the third atmospheric distillation is 5 to 45, for example, 5, 10, 14, 19, 23, 28, 32, 37, 41 or 45, etc., but not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the overhead reflux ratio of the third atmospheric distillation is 1 to 3, and may be, for example, 1, 1.3, 1.5, 1.7, 1.9, 2.2, 2.4, 2.6, 2.8 or 3, etc., but is not limited to the values listed, and other values not listed in this range are also applicable.

Preferably, the third rectification in step (2) is a third negative pressure rectification.

Preferably, the absolute pressure of the third negative pressure rectification is 60-760 mmHg.

Preferably, the temperature of the bottom of the third negative pressure distillation column is 60 to 80 ℃, and may be, for example, 60 ℃, 63 ℃, 65 ℃, 67 ℃, 69 ℃, 72 ℃, 74 ℃, 76 ℃, 78 ℃ or 80 ℃, but not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the temperature at the top of the third negative pressure distillation column is 40 to 60 ℃, and may be, for example, 40 ℃, 43 ℃, 45 ℃, 47 ℃, 49 ℃, 52 ℃, 54 ℃, 56 ℃, 58 ℃ or 60 ℃, but is not limited to the values listed, and other values not listed in this range are also applicable.

Preferably, the theoretical plate number of the third negative pressure distillation is 5 to 45, for example, 5, 10, 14, 19, 23, 28, 32, 37, 41 or 45, etc., but is not limited to the values listed, and other values not listed in the range are also applicable.

Preferably, the overhead reflux ratio of the third negative pressure distillation is 1 to 3, and may be, for example, 1, 1.3, 1.5, 1.7, 1.9, 2.2, 2.4, 2.6, 2.8 or 3, but not limited to the values listed, and other values not listed in this range are also applicable.

Preferably, the first part of the first still solution accounts for 2 to 60 wt% of the total mass of the first still solution, and may be, for example, 2 wt%, 9 wt%, 15 wt%, 22 wt%, 28 wt%, 35 wt%, 41 wt%, 48 wt%, 54 wt%, or 60 wt%, etc., but is not limited to the enumerated values, and other values not enumerated within this range are also applicable, and preferably 10 to 60 wt%.

Preferably, the second solvent fraction is 2 to 60 wt% of the total amount of the second solvent fraction and the third solvent fraction, and may be, for example, 2 wt%, 9 wt%, 15 wt%, 22 wt%, 28 wt%, 35 wt%, 41 wt%, 48 wt%, 54 wt%, or 60 wt%, and the like, but is not limited to the recited values, and other values not recited in this range are also applicable.

According to the invention, the first part of the first kettle liquid accounts for the total mass of the first kettle liquid, so that the second solvent fraction accounts for 2-60 wt% of the total amount of the second solvent fraction and the third solvent fraction, preferably 10-60 wt% of the total amount of the second solvent fraction and the third solvent fraction, the heat can be more fully utilized, and the overall heat load is reduced.

As a preferred technical scheme of the invention, the method comprises the following steps:

(1) performing heat exchange on the aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, and performing first rectification to obtain a first fraction containing 3-chloropropene and an organic solvent and a first kettle liquid; the content of 3-chloropropene in the first kettle liquid is less than 0.1 wt%;

the content of the organic solvent in the aqueous phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 1-50 wt%, the content of water is 46-99 wt%, and the content of 3-chloropropene is 0.1-4 wt%;

the first rectification is first atmospheric rectification, the temperature of a tower kettle is 85-100 ℃, the temperature of a tower top is 40-50 ℃, the number of theoretical plates is 15-30, and the reflux ratio of the tower top is 1-3; or the first rectification is first negative pressure rectification, the temperature of a tower kettle is 40-80 ℃, the temperature of a tower top is 30-45 ℃, the number of theoretical plates is 15-30, the reflux ratio of the tower top is 1-3, and the absolute pressure is 60-760 mmHg;

(2) performing second rectification on the first part of the first kettle liquid to obtain a second solvent fraction; performing third rectification on a second part of the first kettle liquid to obtain a third solvent fraction;

the temperature of a tower kettle of the second rectification is 120-180 ℃, the temperature of a tower top is 100-150 ℃, the number of theoretical plates is 5-45, the reflux ratio of the tower top is 1-3, and the absolute pressure is 0.2-1.5 MPa;

the third rectification is third atmospheric rectification, the temperature of a tower kettle is 80-100 ℃, the temperature of a tower top is 55-65 ℃, the number of theoretical plates is 5-45, and the reflux ratio of the tower top is 1-3; or the third rectification is third negative pressure rectification, the absolute pressure is 60-760 mmHg, the temperature of a tower kettle is 60-80 ℃, the temperature of a tower top is 40-60 ℃, the number of theoretical plates is 5-45, and the reflux ratio of the tower top is 1-3;

the second solvent fraction accounts for 2-60 wt% of the total amount of the second solvent fraction and the third solvent fraction, and the second solvent fraction exchanges heat with tower kettle circulating liquid of the third rectification; and exchanging heat between the third solvent fraction and the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method.

Compared with the prior art, the invention has at least the following beneficial effects:

(1) according to the method for recovering the solvent in the aqueous phase of epoxy chloropropane prepared by using the hydrogen peroxide method, the solvent is recovered by separating the kettle liquid of the first rectification by adopting the two-tower rectification, so that the heat at the tower top of the second rectification tower can be supplied to the third rectification tower, and the energy consumption of the rectification is greatly reduced;

(2) the method for recovering the solvent in the aqueous phase of epoxy chloropropane by using the hydrogen peroxide method adopts a mode of parallel connection of the second rectification and the third rectification, is convenient to operate, and avoids the problem of unstable gas-liquid balance of series connection of the second rectification and the third rectification;

(3) the method for recovering the solvent in the aqueous phase of the epoxy chloropropane prepared by the hydrogen peroxide method also fully utilizes the heat of the third solvent fraction to preheat the aqueous phase of the epoxy chloropropane prepared by the hydrogen peroxide method, the energy consumption of the integral rectification process is obviously reduced, the total heat load steam consumption is less than or equal to 0.1t/h, the total heat load steam consumption is less than or equal to 0.07t/h under the better condition and the heat load steam consumption of the aqueous phase of the epoxy chloropropane is less than or equal to 0.07t/h aiming at 222kg/h of the aqueous phase feed≤0.46×10^-3t/(kg of epoxy chloropropane aqueous phase), and compared with a direct epoxidation process only adopting a direct rectification method, the energy consumption can be reduced by more than 35 percent.

Detailed Description

For the purpose of facilitating an understanding of the present invention, the present invention will now be described by way of examples. It should be understood by those skilled in the art that the examples are only for the understanding of the present invention and should not be construed as the specific limitations of the present invention.

First, an embodiment

Example 1

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which comprises the following steps:

(1) feeding 222kg/h of water phase of epoxy chloropropane prepared by a hydrogen peroxide method into a first rectifying tower for first rectification, wherein the number of theoretical plates is 25, the pressure at the top of the tower is normal pressure (101.325kPa), the temperature at the top of the tower is 45 ℃, the temperature at the bottom of the tower is 95 ℃, the reflux ratio is 1, and the water phase of epoxy chloropropane prepared by the hydrogen peroxide method is fed from a 10 th theoretical plate to obtain 9.9kg/h (90 wt% of methanol and 10%) of first fraction containing 3-chloropropene and methanol and 212.1kg/h of first kettle liquid serving as methanol water solution (46.6 wt% of methanol, 51.3 wt% of water and the balance of impurities);

the content of methanol in the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 45 wt%, the content of water is 49 wt%, the content of 3-chloropropene is 4 wt%, and the balance is impurities;

(2) feeding 112.1kg/h of the first still liquid into a second rectifying tower for second rectification, wherein the number of theoretical plates is 45, the first still liquid is fed from a 15 th theoretical plate, the pressure at the top of the tower is 1.0MPa, the temperature of the bottom of the tower is 175 ℃, the reflux ratio is 2, and the temperature at the top of the tower is 130 ℃ to obtain a second solvent fraction;

feeding a second part of the first kettle liquid into a third rectifying tower for third rectification, wherein the number of theoretical plates is 45, the second part of the first kettle liquid is fed from a 15 th theoretical plate, the pressure at the top of the tower is normal pressure (101.325kPa), the temperature at the bottom of the tower is 100 ℃, the temperature at the top of the tower is 65 ℃, and the reflux ratio is 3, so as to obtain a third solvent fraction;

the second solvent fraction is methanol vapor with the discharge temperature of 130 ℃ and the purity of 99.5 wt%, enters a reboiler of a tower kettle of a third rectifying tower to be used as all heat sources to exchange heat with circulating liquid of the tower kettle of the third rectifying tower, after the second solvent fraction is condensed, part of the second solvent fraction reflows, and part of the second solvent fraction returns to an epoxidation reaction system for preparing epoxy chloropropene through epoxidation reaction as circulating methanol;

the third solvent fraction is methanol vapor with the discharge temperature of 65 ℃ and the purity of 99.5 wt%, and the methanol vapor exchanges heat with the first rectified feed stream (the aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method) to be used as a partial heat source; and after the third solvent fraction is condensed, partially refluxing, and returning part of the third solvent fraction to an epoxidation reaction system for preparing epoxy chloropropene by using cyclic methanol.

Example 2

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which comprises the following steps:

(1) feeding 222kg/h of water phase of epoxy chloropropane prepared by a hydrogen peroxide method into a first rectifying tower for first rectification, wherein the number of theoretical plates is 15, the pressure at the top of the tower is normal pressure (101.325kPa), the temperature at the top of the tower is 50 ℃, the temperature at the bottom of the tower is 85 ℃, the reflux ratio is 2, and the water phase of epoxy chloropropane prepared by the hydrogen peroxide method is fed from a 10 th theoretical plate to obtain 10.5kg/h (85 wt% of methanol and 15%) of first fraction containing 3-chloropropene and methanol and 211.5kg/h of first kettle liquid serving as a methanol water solution (46.5 wt% of methanol, 51.4 wt% of water and the balance of impurities);

the content of methanol in the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 45 wt%, the content of water is 49 wt%, the content of 3-chloropropene is 4 wt%, and the balance is impurities;

(2) feeding 111.5kg/h of the first still liquid into a second rectifying tower for second rectification, wherein the number of theoretical plates is 5, feeding the first still liquid from a 3 rd theoretical plate, separating at the tower top pressure of 1.5MPa, the tower kettle temperature of 180 ℃, the reflux ratio of 3 and the tower top temperature of 150 ℃ to obtain a second solvent fraction;

feeding a second part of the first kettle liquid into a third rectifying tower for third rectification, wherein the number of theoretical plates is 30, the second part of the first kettle liquid is fed from a 15 th theoretical plate, the pressure at the top of the tower is normal pressure (101.325kPa), the temperature at the bottom of the tower is 90 ℃, the temperature at the top of the tower is 60 ℃, and the reflux ratio is 2, so as to obtain a third solvent fraction;

the second solvent fraction is methanol vapor with the discharge temperature of 150 ℃ and the purity of 99.5 wt%, enters a reboiler of a tower kettle of a third rectifying tower to be used as all heat sources to exchange heat with circulating liquid of the tower kettle of the third rectifying tower, after the second solvent fraction is condensed, part of the second solvent fraction reflows, and part of the second solvent fraction returns to an epoxidation reaction system for preparing epoxy chloropropene through epoxidation reaction as circulating methanol;

the third solvent fraction is methanol vapor with the discharge temperature of 90 ℃ and the purity of 99.5 wt%, and the methanol vapor exchanges heat with the first rectified feed stream (the aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method) to be used as a partial heat source; and after the third solvent fraction is condensed, partially refluxing, and returning part of the third solvent fraction to an epoxidation reaction system for preparing epoxy chloropropene by using cyclic methanol.

Example 3

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which comprises the following steps:

(1) feeding 222kg/h of water phase of epoxy chloropropane prepared by a hydrogen peroxide method into a first rectifying tower for first rectification, wherein the number of theoretical plates is 30, the pressure at the top of the tower is normal pressure (101.325kPa), the temperature at the top of the tower is 40 ℃, the temperature at the bottom of the tower is 100 ℃, the reflux ratio is 3, and the water phase of epoxy chloropropane prepared by the hydrogen peroxide method is fed from a 10 th theoretical plate to obtain 11.1kg/h (80 wt% of methanol and 20%) of first fraction containing 3-chloropropene and methanol and 210.9kg/h of first kettle liquid serving as a methanol water solution (46.3 wt% of methanol, 51.6 wt% of water and the balance of impurities);

the content of methanol in the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 45 wt%, the content of water is 49 wt%, the content of 3-chloropropene is 4 wt%, and the balance is impurities;

(2) feeding 110.9kg/h of the first still liquid into a second rectifying tower for second rectification, wherein the number of theoretical plates is 30, feeding the first still liquid from a 15 th theoretical plate, separating at the tower top pressure of 0.2MPa, the tower kettle temperature of 120 ℃, the reflux ratio of 1 and the tower top temperature of 100 ℃ to obtain a second solvent fraction;

feeding a second part of the first kettle liquid into a third rectifying tower for third rectification, wherein the number of theoretical plates is 5, the second part of the first kettle liquid is fed from a 3 rd theoretical plate, the pressure at the top of the tower is normal pressure (101.325kPa), the temperature at the bottom of the tower is 80 ℃, the temperature at the top of the tower is 55 ℃, and the reflux ratio is 2, so as to obtain a third solvent fraction;

the second solvent fraction is methanol vapor with the discharge temperature of 100 ℃ and the purity of 99.5 wt%, enters a reboiler of a tower kettle of a third rectifying tower to be used as all heat sources to exchange heat with circulating liquid of the tower kettle of the third rectifying tower, after the second solvent fraction is condensed, part of the second solvent fraction reflows, and part of the second solvent fraction returns to an epoxidation reaction system for preparing epoxy chloropropene through epoxidation reaction as circulating methanol;

the third solvent fraction is methanol vapor with the discharge temperature of 55 ℃ and the purity of 98 wt%, and the methanol vapor exchanges heat with the first rectified feed stream (the aqueous phase of epoxy chloropropane prepared by the hydrogen peroxide method) to serve as a partial heat source; and after the third solvent fraction is condensed, partially refluxing, and returning part of the third solvent fraction to an epoxidation reaction system for preparing epoxy chloropropene by using cyclic methanol.

Example 4

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which comprises the following steps:

(1) feeding 222kg/h of water phase of epoxy chloropropane prepared by a hydrogen peroxide method into a first rectifying tower for first rectification, wherein the number of theoretical plates is 30, the pressure at the top of the tower is negative pressure (700mmHg), the temperature at the top of the tower is 40 ℃, the temperature at the bottom of the tower is 80 ℃, the reflux ratio is 3, and the water phase of epoxy chloropropane prepared by the hydrogen peroxide method is fed from a 10 th theoretical plate to obtain 11.1kg/h (80 wt% of methanol and 20%) of first fraction containing 3-chloropropene and methanol and 210.9kg/h of first residue serving as a methanol water solution (46.3 wt% of methanol, 51.6 wt% of water and the balance of impurities);

the content of methanol in the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 45 wt%, the content of water is 49 wt%, the content of 3-chloropropene is 4 wt%, and the balance is impurities;

(2) feeding 110.9kg/h of the first still liquid into a second rectifying tower for second rectification, wherein the number of theoretical plates is 30, feeding the first still liquid from a 15 th theoretical plate, separating at the tower top pressure of 0.2MPa, the tower kettle temperature of 120 ℃, the reflux ratio of 1 and the tower top temperature of 100 ℃ to obtain a second solvent fraction;

feeding a second part of the first still liquid of 100.0kg/h into a third rectifying tower for third rectification, wherein the number of theoretical plates is 5, feeding the second part of the first still liquid from a 3 rd theoretical plate, and separating under the conditions that the overhead pressure is negative pressure (650mmHg), the temperature of the bottom of the tower is 70 ℃, the temperature of the top of the tower is 50 ℃ and the reflux ratio is 3 to obtain a third solvent fraction;

the second solvent fraction is methanol vapor with the discharge temperature of 100 ℃ and the purity of 99.5 wt%, enters a reboiler of a tower kettle of a third rectifying tower to be used as all heat sources to exchange heat with circulating liquid of the tower kettle of the third rectifying tower, after the second solvent fraction is condensed, part of the second solvent fraction reflows, and part of the second solvent fraction returns to an epoxidation reaction system for preparing epoxy chloropropene through epoxidation reaction as circulating methanol;

the third solvent fraction is methanol vapor with the discharge temperature of 50 ℃ and the purity of 98 wt%, and the methanol vapor exchanges heat with the first rectified feed stream (the aqueous phase of epoxy chloropropane prepared by the hydrogen peroxide method) to be used as a partial heat source; and after the third solvent fraction is condensed, partially refluxing, and returning part of the third solvent fraction to an epoxidation reaction system for preparing epoxy chloropropene by using cyclic methanol.

Example 5

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which comprises the following steps:

(1) feeding 222kg/h of water phase of epoxy chloropropane prepared by a hydrogen peroxide method into a first rectifying tower for first rectification, wherein the number of theoretical plates is 15, the pressure at the top of the tower is negative pressure (60mmHg), the temperature at the top of the tower is 50 ℃, the temperature at the bottom of the tower is 60 ℃, the reflux ratio is 3, and the water phase of epoxy chloropropane prepared by the hydrogen peroxide method is fed from a 10 th theoretical plate to obtain 10.5kg/h (85 wt% of methanol and 15%) of first fraction containing 3-chloropropene and methanol and 211.5kg/h of first kettle liquid serving as a methanol water solution (46.5 wt% of methanol, 51.4 wt% of water and the balance of impurities);

the content of methanol in the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 45 wt%, the content of water is 49 wt%, the content of 3-chloropropene is 4 wt%, and the balance is impurities;

(2) feeding 111.5kg/h of the first still liquid into a second rectifying tower for second rectification, wherein the number of theoretical plates is 5, feeding the first still liquid from a 3 rd theoretical plate, separating at the tower top pressure of 1.5MPa, the tower kettle temperature of 180 ℃, the reflux ratio of 3 and the tower top temperature of 150 ℃ to obtain a second solvent fraction;

feeding a second part of the first still liquid of 100.0kg/h into a third rectifying tower for third rectification, wherein the number of theoretical plates is 30, feeding the second part of the first still liquid from a 15 th theoretical plate, and separating under the tower top pressure of negative pressure (200mmHg), the tower bottom temperature of 65 ℃, the tower top temperature of 50 ℃ and the reflux ratio of 2 to obtain a third solvent fraction;

the second solvent fraction is methanol vapor with the discharge temperature of 150 ℃ and the purity of 99.5 wt%, enters a reboiler of a tower kettle of a third rectifying tower to be used as all heat sources to exchange heat with circulating liquid of the tower kettle of the third rectifying tower, after the second solvent fraction is condensed, part of the second solvent fraction reflows, and part of the second solvent fraction returns to an epoxidation reaction system for preparing epoxy chloropropene through epoxidation reaction as circulating methanol;

the third solvent fraction is methanol vapor with the discharge temperature of 50 ℃ and the purity of 99.5 wt%, and the methanol vapor exchanges heat with the first rectified feed stream (the aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method) to be used as a partial heat source; and after the third solvent fraction is condensed, partially refluxing, and returning part of the third solvent fraction to an epoxidation reaction system for preparing epoxy chloropropene by using cyclic methanol.

Example 6

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which comprises the following steps:

(1) feeding 222kg/h of water phase of epoxy chloropropane prepared by a hydrogen peroxide method into a first rectifying tower for first rectification, wherein the number of theoretical plates is 45, the pressure at the top of the tower is negative pressure (300mmHg), the temperature at the top of the tower is 45 ℃, the temperature at the bottom of the tower is 70 ℃, the reflux ratio is 3, and the water phase of epoxy chloropropane prepared by the hydrogen peroxide method is fed from a 10 th theoretical plate to obtain 10.0kg/h (91 wt% of methanol and 9%) of first fraction containing 3-chloropropene and methanol and 212kg/h of first kettle liquid serving as a methanol water solution (46.6 wt% of methanol, 51.3 wt% of water and the balance of impurities);

the content of methanol in the water phase of the epoxy chloropropane prepared by the hydrogen peroxide method is 45 wt%, the content of water is 49 wt%, the content of 3-chloropropene is 4 wt%, and the balance is impurities;

(2) feeding 112.0kg/h of the first still liquid into a second rectifying tower for second rectification, wherein the number of theoretical plates is 45, feeding the first still liquid from a 15 th theoretical plate, separating at the tower top pressure of 1.0MPa, the tower kettle temperature of 175 ℃, the reflux ratio of 2 and the tower top temperature of 130 ℃ to obtain a second solvent fraction;

feeding a second part of the first kettle liquid into a third rectifying tower for third rectification, wherein the number of theoretical plates is 45, the second part of the first kettle liquid is fed from a 15 th theoretical plate, the pressure at the top of the tower is normal pressure (101.325kPa), the temperature at the bottom of the tower is 100 ℃, the temperature at the top of the tower is 65 ℃, and the reflux ratio is 3, so as to obtain a third solvent fraction;

the second solvent fraction is methanol vapor with the discharge temperature of 130 ℃ and the purity of 99.5 wt%, enters a reboiler of a tower kettle of a third rectifying tower to be used as all heat sources to exchange heat with circulating liquid of the tower kettle of the third rectifying tower, after the second solvent fraction is condensed, part of the second solvent fraction reflows, and part of the second solvent fraction returns to an epoxidation reaction system for preparing epoxy chloropropene through epoxidation reaction as circulating methanol;

the third solvent fraction is methanol vapor with the discharge temperature of 65 ℃ and the purity of 98 wt%, and the methanol vapor exchanges heat with the first rectified feed stream (the aqueous phase of epoxy chloropropane prepared by the hydrogen peroxide method) to serve as a partial heat source; and after the third solvent fraction is condensed, partially refluxing, and returning part of the third solvent fraction to an epoxidation reaction system for preparing epoxy chloropropene by using cyclic methanol.

Example 7

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which is the same as that in embodiment 1 except that the first part of the first kettle liquid is 125kg/h, and the second part of the first kettle liquid is 87.1 kg/h.

Example 8

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which is the same as that in embodiment 1 except that the first part of the first kettle liquid is 45kg/h, and the second part of the first kettle liquid is 167.1 kg/h. The second solvent fraction of this example serves only as part of the heat source for the third distillation.

Example 9

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which is the same as that in embodiment 1 except that the first part of the first kettle liquid is 20kg/h, and the second part of the first kettle liquid is 192.1 kg/h. The second solvent fraction of this example serves only as part of the heat source for the third distillation.

Example 10

The embodiment provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, which is the same as that in embodiment 1 except that the first part of the first kettle liquid is 160kg/h, and the second part of the first kettle liquid is 52.1 kg/h.

Comparative example 1

The comparative example provides a method for recovering a solvent in an aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method, wherein the method directly performs second rectification on all the first kettle liquid without performing third rectification, and the rest is the same as that in example 1, specifically, the step (2):

(2) feeding the first kettle liquid into a second rectifying tower for second rectification, wherein the number of theoretical plates is 45, feeding the first kettle liquid from a 15 th theoretical plate, separating at the tower top pressure of normal pressure (101.325kPa), the tower kettle temperature of 100 ℃, the reflux ratio of 3 and the tower top temperature of 65 ℃ to obtain a second solvent fraction;

the third solvent fraction is methanol vapor with the discharge temperature of 65 ℃ and the purity of 99.5 wt%, and the methanol vapor exchanges heat with the first rectified feed stream (the aqueous phase of epoxy chloropropane prepared by a hydrogen peroxide method) to be used as a partial heat source; and after the third solvent fraction is condensed, partially refluxing, and returning part of the third solvent fraction to an epoxidation reaction system for preparing epoxy chloropropene by using cyclic methanol.

The flow in examples 1-6 and comparative example 1 were simulated using the rectification module in AspenPlus and the heat load of the overall rectification process was calculated and the results are shown in table 1.

TABLE 1

	Total heat load steam consumption (t/h)
		Example 1	0.069
Example 2	0.089
		Example 3	0.070
Example 4	0.075
		Example 5	0.085
Example 6	0.091
		Example 7	0.071
Example 8	0.076
		Example 9	0.089
Example 10	0.099
		Comparative example 1	0.139

From table 1, the following points can be seen:

(1) it can be seen from the comprehensive examples 1 to 10 that the total heat load steam consumption of the recovered solvent is less than or equal to 0.1t/h by adopting the parallel connection mode of the second rectification and the third rectification for the 222kg/h hydrogen peroxide method for preparing the aqueous phase of epoxy chloropropane, namely the heat load steam consumption of the aqueous phase of epoxy chloropropane by the method provided by the invention is less than or equal to 0.46 × 10^-3t/(kg of epoxy chloropropane aqueous phase), the energy consumption is obviously reduced, and the economic value of the whole process is improved;

(2) by combining the example 1 and the comparative example 1, it can be seen that the third rectification is arranged in the example 1, and the second rectification and the third rectification are connected in parallel, compared with the arrangement of only the second rectification in the comparative example 1, the heat of the tower top of the second rectification can be fully utilized in the example 1, and the problem of unstable gas-liquid balance in series connection is solved, the total heat load steam consumption is only 0.069t/h, while the gas-liquid balance in the comparative example 1 is unstable, and the total heat load steam consumption is 0.139 t/h;

(3) it can be seen from the comprehensive results of example 1 and examples 7 to 10 that the present invention can further reduce the total heat load steam consumption by controlling the ratio of the first part of the first kettle liquid to the total mass of the first kettle liquid within a specific range, specifically, the ratio of the first part of the first kettle liquid to 52.85 wt%, 58.93 wt% and 21.22 wt% of the first kettle liquid in examples 1 and 7 to 8 is 9.43 wt% and 75.44 wt% respectively, wherein the total heat load steam consumption in examples 1 and 7 to 8 is 0.069t/h, 0.071t/h and 0.076t/h respectively, and the total heat load steam consumption in examples 9 to 10 is 0.089t/h and 0.099t/h respectively.

In conclusion, the invention adopts the mode of connecting the second rectification and the third rectification in parallel and fully utilizes the heat of the second rectification, so that the energy is fully utilized, the steam consumption of the heat load is obviously reduced, and the steam consumption of the heat load aiming at the water phase of the epichlorohydrin is less than or equal to 0.46 multiplied by 10^-3t/(kg of epoxy chloropropane water phase), reduces the cost of preparing epoxy chloropropane by using a hydrogen peroxide method, and has wide application prospect.

The applicant states that the present invention is illustrated by the above examples to show the detailed process equipment and process flow of the present invention, but the present invention is not limited to the above detailed process equipment and process flow, i.e. it does not mean that the present invention must rely on the above detailed process equipment and process flow to be implemented. It should be understood by those skilled in the art that any modification of the present invention, equivalent substitutions of the raw materials of the product of the present invention, addition of auxiliary components, selection of specific modes, etc., are within the scope and disclosure of the present invention.