CN107382682B - Refining method and device of 2, 2-methoxypropane - Google Patents
Refining method and device of 2, 2-methoxypropane Download PDFInfo
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- CN107382682B CN107382682B CN201710774362.XA CN201710774362A CN107382682B CN 107382682 B CN107382682 B CN 107382682B CN 201710774362 A CN201710774362 A CN 201710774362A CN 107382682 B CN107382682 B CN 107382682B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
- C07C41/48—Preparation of compounds having groups
- C07C41/58—Separation; Purification; Stabilisation; Use of additives
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/146—Multiple effect distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/36—Azeotropic distillation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
- B01D3/40—Extractive distillation
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Abstract
The invention provides a refining method and a device of 2, 2-methoxy propane, and the refining method of the 2, 2-methoxy propane comprises the following steps: s1, primarily separating a raw material liquid containing 2, 2-dimethoxy propane, methanol, acetone and water through an azeotropic tower, and partially refluxing an azeotrope of the acetone and the methanol extracted from the top of the tower to the azeotropic tower; s2, introducing materials extracted from the bottom of the azeotropic tower into an extraction rectifying tower for extraction rectification, introducing materials extracted from the top of the extraction rectifying tower into a layering tank, and introducing materials extracted from the bottom of the extraction rectifying tower into a methanol tower; s3, introducing a water part from the bottom of the methanol tower into a layering tank as an extracting agent for recycling, introducing a water phase in the layering tank into an extraction rectifying tower as reflux, and introducing an oil phase into a product tower; s4, obtaining the 2, 2-dimethoxy propane from the bottom of the product tower. The refining method of 2, 2-methoxy propane has low energy consumption, and can obtain the 2, 2-dimethoxy propane product with the mass fraction of more than 99.5 percent.
Description
Technical Field
The invention belongs to the field of chemical separation, and particularly relates to a refining method and device of 2, 2-methoxypropane.
Background
2, 2-dimethoxy propane is the simplest and active ketal, and one carbon atom of the compound is connected with two methoxy groups, so that the compound has strong chemical activity and is extremely easy to absorb water and decompose due to larger steric hindrance, and the compound is widely applied to fine chemical industries such as medicines, pesticides and the like due to the high reaction activity, so that the compound has special significance for research on synthesis and application of the compound. The traditional 2, 2-dimethoxy propane synthesis method uses acetone and methanol as raw materials, and has the advantages of simple and easily obtained raw materials and simple production process, but has low yield and difficult separation and purification of products. The product mainly contains four components of methanol, acetone, water and 2, 2-methoxypropane, wherein four pairs of azeotropes are included, namely methanol-acetone, methanol-2, 2-methoxypropane, acetone-2, 2-methoxypropane and water-2, 2-methoxypropane, so that the separation and purification of the 2, 2-methoxypropane are difficult.
US4775447 provides a method for refining 2, 2-dimethoxypropane by first using azeotropic distillation to produce a methanol-acetone azeotrope, then distilling off the mixture of the product and methanol, finally adding acetone to the mixture, and using azeotropic distillation to produce an acetone-methanol azeotrope, and obtaining the product 2, 2-dimethoxypropane from the bottom of the column. The process comprises two steps of azeotropic distillation, and the amount of acetone added in the third step is large, so that the problem of high energy consumption is caused. In addition, the product quality fraction obtained by the process is only 98%, and the purity is not high.
Disclosure of Invention
In view of the above, the present invention aims to provide a refining method of 2, 2-methoxypropane, which overcomes the defects of the prior art, adopts water as an extractant to extract, rectify and separate an azeotrope of water-2, 2-dimethoxypropane, and then utilizes the principle of heterogeneous azeotropic rectification to obtain the product 2, 2-methoxypropane, wherein the energy consumption is low, the mass fraction of the 2, 2-dimethoxypropane product can reach more than 99.5%, and the yield reaches more than 97%.
In order to achieve the above purpose, the technical scheme of the invention is realized as follows:
a refining method of 2, 2-methoxy propane comprises the following steps:
s1, primarily separating a raw material liquid containing 2, 2-dimethoxy propane, methanol, acetone and water through an azeotropic tower, and partially refluxing an azeotrope of the acetone and the methanol extracted from the top of the tower to the azeotropic tower;
s2, introducing materials extracted from the bottom of the azeotropic tower into an extraction rectifying tower for extraction rectification, introducing materials extracted from the top of the extraction rectifying tower into a layering tank, and introducing materials extracted from the bottom of the extraction rectifying tower into a methanol tower;
s3, introducing a water part from the bottom of the methanol tower into a layering tank as an extracting agent for recycling, introducing a water phase in the layering tank into an extraction rectifying tower as reflux, and introducing an oil phase into a product tower;
s4, obtaining the 2, 2-dimethoxy propane with the mass fraction of more than 99.5% from the bottom of the product tower, feeding the extracted material at the top of the product tower into a layering tank, and extracting methanol from the top of the methanol tower.
Preferably, the materials extracted from the azeotropic tower, the extractive distillation tower, the product tower, the top of the methanol tower and the bottom of the methanol tower are subjected to condensation treatment.
Preferably, the product tower and the methanol tower are both rectifying towers; the azeotropic tower, the extractive distillation tower, the product tower and the methanol tower are one of decompression operation, normal pressure operation and pressurization operation; the operating pressures of the azeotropic column, the extractive distillation column, the product column and the methanol column are 0.02MPa to 0.8MPa in absolute pressure.
Preferably, the reflux ratio of the azeotropic column is controlled to be 6:1-15:1, the temperature of the top of the column is 54-56 ℃, and the temperature of the bottom of the column is 65-68 ℃.
Preferably, the operation reflux ratio of the extractive distillation column is controlled to be 2:1-4:1, the temperature of the top of the column is 63-66 ℃, and the temperature of the bottom of the column is 78-81 ℃.
Preferably, the operation reflux ratio of the product tower is controlled to be 2:1-4:1, the tower top temperature is 67-71 ℃, and the tower bottom temperature is 80-83 ℃.
Preferably, the operation reflux ratio of the methanol tower is controlled to be 1.2:1-3:1, the tower top temperature is 63-65 ℃, and the tower bottom temperature is 100-102 ℃.
Another object of the present invention is to provide a refining apparatus for 2, 2-methoxypropane, so as to obtain a 2, 2-methoxypropane product with a mass fraction of 99.5% or more and a yield of 97% or more.
In order to achieve the above purpose, the technical scheme of the invention is realized as follows:
the refining device of the 2, 2-methoxy propane comprises an azeotropic tower, an extraction rectifying tower, a product tower and a methanol tower, wherein the lower ends of the towers are provided with reboilers;
a feed liquid inlet is arranged in the middle of the azeotropic tower, and a feed outlet at the top of the azeotropic tower is sequentially communicated with a first condenser, a first reflux tank and a feed inlet at the upper end of the azeotropic tower; a material outlet at the bottom of the azeotropic tower is communicated with a middle feed inlet of the extraction rectifying tower;
a discharge port at the top of the extraction rectifying tower is sequentially communicated with a second condenser, a layering tank and a feed port at the upper end of the extraction rectifying tower; the bottom discharge port of the layering tank is communicated with the product tower; a discharge hole at the bottom of the product tower is communicated with a product collecting unit; a discharge port at the bottom of the extraction rectifying tower is communicated with a feed port in the middle of the methanol tower;
the material outlet at the bottom of the methanol tower is sequentially communicated with a third condenser and a layering tank.
Further, a discharge hole at the top of the product tower is communicated with a fourth condenser, and the fourth condenser is communicated with the layering tank and the first material discharging unit; a discharge hole at the top of the methanol tower is sequentially communicated with a fifth condenser and a second reflux tank, and a discharge hole of the second reflux tank is communicated with a feed hole at the upper end of the methanol tower and a first material discharge unit; the third condenser is communicated with the first material discharging unit; the first reflux tank is communicated with the second material discharging unit.
Further, reflux pumps are arranged between the first reflux tank and the azeotropic tower, between the layering tank and the extractive distillation tower and between the second reflux tank and the methanol tower; the product tower and the methanol tower are both rectifying towers.
Compared with the prior art, the refining method of the 2, 2-methoxy propane has the following advantages:
the refining method of 2, 2-methoxypropane fully utilizes the characteristic of low solubility of 2, 2-dimethoxypropane and water, adopts water as an extractant to extract, rectify and separate azeotrope of water-2, 2-dimethoxypropane, and then utilizes the principle of heterogeneous azeotropic rectification (water and 2, 2-methoxypropane are slightly dissolved in a product tower) to obtain the product 2, 2-methoxypropane. As the extractant of water, the gasification is little in the rectification process, so the energy consumption of the process is low. In addition, the process does not introduce other components and does not affect the quality of the product. The product quality fraction can reach more than 99.5%, and the yield reaches more than 97%.
The refining device of 2, 2-methoxypropane has the same advantages as the refining method of 2, 2-methoxypropane in the prior art, and is not described herein.
Drawings
FIG. 1 is a schematic view showing a simple structure of a 2, 2-methoxypropane purifying apparatus according to example 1 of the present invention.
Reference numerals:
1-an azeotropic column; 2-an extraction rectifying tower; 3-a product column; a 4-methanol column; 5-reboiler; 6-a first condenser; 7-a first reflux drum; 8-a second condenser; 9-layering tank; 10-a third condenser; 11-fourth condenser; 12-a product collection unit; 13-a first material discharge unit; 14-a fifth condenser; 15-a second reflux drum; 16-a second material discharge unit; 17-reflux pump.
Detailed Description
Unless defined otherwise, technical terms used in the following examples have the same meaning as commonly understood by one of ordinary skill in the art to which the present invention pertains. The test reagents used in the following examples, unless otherwise specified, are all conventional biochemical reagents; the experimental methods are conventional methods unless otherwise specified.
The present invention will be described in detail with reference to the following examples and drawings.
Example 1
As shown in figure 1, a refining device of 2, 2-methoxy propane comprises an azeotropic tower 1, an extraction rectifying tower 2, a product tower 3 and a methanol tower 4, wherein the lower ends of the towers are provided with reboilers 5;
a raw material liquid inlet is arranged in the middle of the azeotropic tower 1, and a material outlet at the top of the azeotropic tower 1 is sequentially communicated with a first condenser 6, a first reflux tank 7 and a feed inlet at the upper end of the azeotropic tower 1; the material outlet at the bottom of the azeotropic tower 1 is communicated with the middle feed inlet of the extraction rectifying tower 2;
the top discharge port of the extraction rectifying tower 2 is sequentially communicated with a second condenser 8, a layering tank 9 and the upper end feed port of the extraction rectifying tower 2; the bottom discharge port of the layering tank 9 is communicated with the product tower 3; a discharge hole at the bottom of the product tower 3 is communicated with a product collecting unit 12; a discharge port at the bottom of the extraction rectifying tower 2 is communicated with a feed port in the middle of the methanol tower 4;
the material outlet at the bottom of the methanol tower 4 is sequentially communicated with a third condenser 10 and a layering tank 9.
The discharge port at the top of the product tower 3 is communicated with a fourth condenser 11, and the fourth condenser 11 is communicated with the layering tank 9 and the first material discharging unit 13; a discharge port at the top of the methanol tower 4 is sequentially communicated with a fifth condenser 14 and a second reflux tank 15, and a discharge port of the second reflux tank 15 is communicated with a feed port at the upper end of the methanol tower 4 and the first material discharging unit 13; the third condenser 10 is communicated with the first material discharging unit 13; the first reflux drum 7 communicates with the second material discharging unit 16.
Reflux pumps 17 are arranged between the first reflux tank 7 and the azeotropic tower 1, between the layering tank 9 and the extraction rectifying tower 2 and between the second reflux tank 15 and the methanol tower 4; the product tower 3 and the methanol tower 4 are rectifying towers; the cooling medium of each condenser is water.
The method for purifying 2, 2-dimethoxypropane by using the apparatus for purifying 2, 2-dimethoxypropane is as follows:
the mass fractions of the 2, 2-dimethoxy propane, the methanol, the acetone and the water in the raw material liquid are respectively as follows: 15%, 54%, 24%, 7%, feeding the raw material liquid into an azeotropic tower 1, wherein the operating reflux ratio of the tower is 10:1, the temperature of the tower top is 54 ℃, the temperature of the tower bottom is 65 ℃, an azeotrope of acetone and methanol is extracted from the tower top of the tower, the azeotrope is partially refluxed to the azeotropic tower 1 after being condensed, the azeotropic tower 1 is a material which does not contain acetone basically, the material enters an extraction rectifying tower 2, the operating reflux ratio of the extraction rectifying tower 2 is 3:1, the temperature of the tower top is 63 ℃, the temperature of the tower bottom is 80 ℃, extractant water enters a layering tank 9, water phase generated by layering enters the extraction rectifying tower 2 as reflux, and the material consisting of methanol and water is extracted from the tower bottom. The oil phase generated at the upper part of the layering tank 9 enters a product tower 3, the operation reflux ratio of the product tower 3 is 2.5:1, the temperature of the top of the tower is 68 ℃, the temperature of the bottom of the tower is 80 ℃, the materials extracted from the top of the product tower 3 enter the layering tank 9 after being condensed, and the mass fraction of 2, 2-dimethoxy propane extracted from the bottom of the product tower 3 is 99.7%, so that the yield is 97.3%. The tower bottom material of the extraction rectifying tower 2 enters a methanol tower 4, the operation reflux ratio of the methanol tower 4 is 2:1, the tower top temperature is 64 ℃, the tower bottom temperature is 101 ℃, methanol is extracted from the tower top, the material extracted from the tower bottom is water, a part of the material is discharged after being cooled, and the material enters a layering tank 9 to be recycled as an extractant.
The materials extracted from the azeotropic tower 1, the extractive distillation tower 2, the product tower 3, the top of the methanol tower 4 and the bottom of the methanol tower 4 are subjected to condensation treatment.
The product tower 3 and the methanol tower 4 are rectifying towers; the azeotropic column 1, the extractive distillation column 2, the product column 3 and the methanol column 4 are all operated under normal pressure.
Example 2
This example is substantially the same as example 1, except that in the method for purifying 2, 2-dimethoxypropane: the operation reflux ratio of the azeotropic tower is 7:1, the temperature of the top of the tower is 55 ℃, and the temperature of the bottom of the tower is 66 ℃; the operation reflux ratio of the extraction rectifying tower is 2:1, the temperature of the top of the tower is 65 ℃, and the temperature of the bottom of the tower is 79 ℃; the operation reflux ratio of the product tower is 3:1, the temperature of the tower top is 70 ℃, and the temperature of the tower bottom is 81 ℃; the operating reflux ratio of the methanol tower was 1.5:1, the temperature at the top of the tower was 63℃and the temperature at the bottom of the tower was 102 ℃.
The operating pressures of the azeotropic column 1, the extractive distillation column 2, the product column 3 and the methanol column 4 are all normal pressures.
The 2, 2-dimethoxy propane with the mass fraction of 99.9% is extracted from the bottom of the product tower 3 of the embodiment, and the yield is 98.6%.
Example 3
This example is substantially the same as example 1, except that in the method for purifying 2, 2-dimethoxypropane: the operation reflux ratio of the azeotropic tower is 14.5:1, the temperature of the top of the tower is 56 ℃, and the temperature of the bottom of the tower is 68 ℃; the operation reflux ratio of the extraction rectifying tower is 3.7:1, the temperature of the top of the tower is 66 ℃, and the temperature of the bottom of the tower is 81 ℃; the operation reflux ratio of the product tower is 4:1, the temperature of the top of the tower is 71 ℃, and the temperature of the bottom of the tower is 83 ℃; the operating reflux ratio of the methanol tower was 2.4:1, the top temperature was 65℃and the bottom temperature was 101 ℃.
The operating pressures of the azeotropic column 1, the extractive distillation column 2, the product column 3 and the methanol column 4 are all normal pressures.
The 2, 2-dimethoxy propane with the mass fraction of 99.86% is extracted from the bottom of the product tower 3 of the embodiment, and the yield is 99.1%.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather is intended to cover all modifications, equivalents, alternatives, and improvements that fall within the spirit and scope of the invention.
Claims (8)
1. A refining method of 2, 2-methoxy propane is characterized in that: the method comprises the following steps:
s1, primarily separating a raw material liquid containing 2, 2-dimethoxypropane, methanol, acetone and water through an azeotropic tower (1), and partially refluxing an azeotrope of the acetone and the methanol extracted from the tower top to the azeotropic tower (1), wherein the operation pressure of the azeotropic tower (1) is 0.02MPa to 0.8MPa, the operation reflux ratio of the azeotropic tower (1) is 6:1-15:1, the temperature of the tower top is 54-56 ℃, and the temperature of the tower bottom is 65-68 ℃;
s2, introducing materials extracted from the bottom of the azeotropic tower (1) into an extraction rectifying tower (2) for extraction rectification, introducing materials extracted from the top of the extraction rectifying tower (2) into a layering tank (9), and introducing materials extracted from the bottom of the extraction rectifying tower (2) into a methanol tower (4);
s3, introducing a water part from the bottom of the methanol tower (4) into a layering tank (9) to be used as an extractant for recycling, introducing a water phase in the layering tank (9) into the extraction rectifying tower (2) to be used as reflux, and introducing an oil phase into the product tower (3);
s4, obtaining 2, 2-dimethoxy propane with the mass fraction of more than 99.5% from the bottom of the product tower (3), feeding the extracted material at the top of the product tower (3) into a layering tank (9), and extracting methanol at the top of the methanol tower (4).
2. The method for purifying 2, 2-methoxypropane as claimed in claim 1, wherein: the materials extracted from the top of the extraction rectifying tower (2), the product tower (3), the methanol tower (4) and the bottom of the methanol tower (4) are subjected to condensation treatment.
3. The method for purifying 2, 2-methoxypropane as claimed in claim 1, wherein: the product tower (3) and the methanol tower (4) are both rectifying towers; the azeotropic tower (1), the extractive distillation tower (2), the product tower (3) and the methanol tower (4) are one of decompression operation, normal pressure operation and pressurization operation; the operating pressures of the azeotropic column (1), the extractive distillation column (2), the product column (3) and the methanol column (4) are 0.02MPa to 0.8MPa in absolute pressure.
4. The method for purifying 2, 2-methoxypropane as claimed in claim 1, wherein: the operation reflux ratio of the extraction rectifying tower (2) is controlled to be 2:1-4:1, the temperature of the top of the tower is 63-66 ℃, and the temperature of the bottom of the tower is 78-81 ℃.
5. The method for purifying 2, 2-methoxypropane as claimed in claim 1, wherein: controlling the operation reflux ratio of the product tower (3) to be 2:1-4:1, the temperature of the top of the tower to be 67-71 ℃ and the temperature of the bottom of the tower to be 80-83 ℃.
6. The method for purifying 2, 2-methoxypropane as claimed in claim 1, wherein: the operation reflux ratio of the methanol tower (4) is controlled to be 1.2:1-3:1, the temperature of the top of the tower is 63-65 ℃, and the temperature of the bottom of the tower is 100-102 ℃.
7. A refining device of 2, 2-methoxy propane is characterized in that: comprises an azeotropic tower (1), an extraction rectifying tower (2), a product tower (3) and a methanol tower (4), wherein the lower ends of the towers are provided with reboilers (5);
a raw material liquid inlet is arranged in the middle of the azeotropic tower (1), and a material outlet at the top of the azeotropic tower (1) is sequentially communicated with a first condenser (6), a first reflux tank (7) and a feed inlet at the upper end of the azeotropic tower (1); a material outlet at the bottom of the azeotropic tower (1) is communicated with a middle feed inlet of the extractive distillation tower (2);
a top discharge port of the extraction rectifying tower (2) is sequentially communicated with a second condenser (8), a layering tank (9) and an upper end feed port of the extraction rectifying tower (2); the bottom discharge port of the layering tank (9) is communicated with the product tower (3); a discharge hole at the bottom of the product tower (3) is communicated with a product collecting unit (12); a discharge port at the bottom of the extraction rectifying tower (2) is communicated with a feed port in the middle of the methanol tower (4);
the material outlet at the bottom of the methanol tower (4) is sequentially communicated with a third condenser (10) and a layering tank (9),
a discharge hole at the top of the product tower (3) is communicated with a fourth condenser (11), and the fourth condenser (11) is communicated with the layering tank (9) and the first material discharging unit (13); a discharge hole at the top of the methanol tower (4) is sequentially communicated with a fifth condenser (14) and a second reflux tank (15), and a discharge hole of the second reflux tank (15) is communicated with a feed hole at the upper end of the methanol tower (4) and a first material discharge unit (13); the third condenser (10) is communicated with the first material discharging unit (13); the first reflux tank (7) is communicated with the second material discharging unit (16).
8. The apparatus for purifying 2, 2-methoxypropane as claimed in claim 7, wherein: reflux pumps (17) are arranged between the first reflux tank (7) and the azeotropic column (1), between the layering tank (9) and the extractive distillation column (2) and between the second reflux tank (15) and the methanol column (4); the product tower (3) and the methanol tower (4) are both rectifying towers.
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| DE2929827A1 (en) * | 1979-07-23 | 1981-02-26 | Basf Ag | 2,2-Di:methoxy-propane continuous prodn. - by ketalisation of acetone with methanol on an acidic ion-exchange column and sepn. of the reaction mixt. in distn. column |
| CN101914001A (en) * | 2010-08-05 | 2010-12-15 | 南京师范大学 | Method for extracting acetone from acetone-dichloromethane-methanol-water mixed liquor by azeotropy and composite extraction reditification integration and equipment thereof |
| CN103664516A (en) * | 2013-11-29 | 2014-03-26 | 中国五环工程有限公司 | Ethanediol separation process for preparing ethanediol from synthetic gas |
| CN103717564A (en) * | 2011-07-06 | 2014-04-09 | 帝斯曼知识产权资产管理有限公司 | Process for preparing acetals and ketals |
| CN103772167A (en) * | 2014-01-08 | 2014-05-07 | 浙江胡涂硅有限公司 | Preparation method of 2, 2-dimethoxypropane |
| CN104326888A (en) * | 2014-09-27 | 2015-02-04 | 安徽华甬新材料有限公司 | Preparation method of 2,2-dimethoxyl propane |
-
2017
- 2017-08-31 CN CN201710774362.XA patent/CN107382682B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2929827A1 (en) * | 1979-07-23 | 1981-02-26 | Basf Ag | 2,2-Di:methoxy-propane continuous prodn. - by ketalisation of acetone with methanol on an acidic ion-exchange column and sepn. of the reaction mixt. in distn. column |
| CN101914001A (en) * | 2010-08-05 | 2010-12-15 | 南京师范大学 | Method for extracting acetone from acetone-dichloromethane-methanol-water mixed liquor by azeotropy and composite extraction reditification integration and equipment thereof |
| CN103717564A (en) * | 2011-07-06 | 2014-04-09 | 帝斯曼知识产权资产管理有限公司 | Process for preparing acetals and ketals |
| CN103664516A (en) * | 2013-11-29 | 2014-03-26 | 中国五环工程有限公司 | Ethanediol separation process for preparing ethanediol from synthetic gas |
| CN103772167A (en) * | 2014-01-08 | 2014-05-07 | 浙江胡涂硅有限公司 | Preparation method of 2, 2-dimethoxypropane |
| CN104326888A (en) * | 2014-09-27 | 2015-02-04 | 安徽华甬新材料有限公司 | Preparation method of 2,2-dimethoxyl propane |
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