CN107382682A - A kind of process for purification and device of 2,2 methoxy propane - Google Patents
A kind of process for purification and device of 2,2 methoxy propane Download PDFInfo
- Publication number
- CN107382682A CN107382682A CN201710774362.XA CN201710774362A CN107382682A CN 107382682 A CN107382682 A CN 107382682A CN 201710774362 A CN201710774362 A CN 201710774362A CN 107382682 A CN107382682 A CN 107382682A
- Authority
- CN
- China
- Prior art keywords
- column
- methanol
- extractive distillation
- tower
- azeotrope
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- 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
-
- 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
-
- 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
- B01D3/34—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
-
- 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
- B01D3/34—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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention provides a kind of process for purification and device of 2,2 methoxy propanes, the process for purification of 2,2 methoxy propanes, comprise the following steps：S1. the material liquid that 2,2 dimethoxy propanes, methanol, acetone and water will be contained is partly refluxed to azeotrope column through azeotrope column initial gross separation, the azeotropic mixture of acetone and methanol from overhead extraction；S2. material azeotrope column bottom of towe produced introduces extractive distillation column and carries out extracting rectifying, and the material of extractive distillation column overhead extraction introduces layering tank, and extractive distillation column bottom of towe extraction material introduces methanol column；S3. the water section from methanol column bottom of towe is introduced into layering tank to recycle as extractant, the aqueous phase being layered in tank introduces extractive distillation column and introduces product tower as backflow, oil phase；S4. 2,2 dimethoxy propanes are obtained from product tower bottom.Of the present invention 2, the process for purification of 2 methoxy propanes, energy consumption is low, can obtain 2, the 2 dimethoxy propane products that mass fraction is more than 99.5%.
Description
Technical field
The invention belongs to chemical separating field, more particularly, to the process for purification and device of one kind 2,2- methoxy propanes.
Background technology
2,2-dimethoxypropane is a kind of most simple, active ketal, is connected with a carbon atom of the compound
Two methoxy groups, steric hindrance is larger to cause chemism very strong, and easily water suction is decomposed, because its reactivity is very high,
It is set to be widely used in the fine chemistry industry industry such as medicine, agricultural chemicals, therefore the research for synthesizing and applying to it has spy
Different meaning.Traditional 2,2-dimethoxypropane synthetic method is using acetone and methanol as raw material, although simply easy with raw material
, the advantages of simple production process, but yield is very low, product separation, purification difficult.Mainly contained in product methanol, acetone,
Water, 2,2- methoxy propanes, four kinds of components, wherein including four pairs of azeotropic mixtures, respectively methanol-acetone, methanol -2,2- methoxyl group
Propane, acetone -2,2- methoxy propane, water -2,2- methoxy propane, therefore come for separating-purifying 2,2- methoxy propanes
Say, have any problem.
US4775447 provides a kind of method of refined 2,2-dimethoxypropane, and first is produced first with azeotropic distillation
The azeotropic mixture of alcohol-acetone, the mixture of product and methanol is then steamed, the most backward mixture adds acetone, utilizes azeotropic
Rectifying produces the azeotropic mixture of acetone and methanol, and product 2,2-dimethoxypropane is obtained by bottom of towe.The process includes two step azeotropic
Rectifying, cause high energy consumption the problem of many in the amounts of acetone that the 3rd step adds.In addition, the product quality point that the process obtains
Number only 98%, purity is not high.
The content of the invention
In view of this, the present invention is directed to propose the process for purification of one kind 2,2- methoxy propanes, to overcome prior art
Defect, using azeotropic mixture of the water as extractant separation of extractive distillation water outlet -2,2-dimethoxypropane, recycle heterogeneous common
The principle of boiling rectifying obtains product 2, and 2- methoxy propanes, energy consumption is low, and 2,2-dimethoxypropane product quality fraction can reach
To more than 99.5%, yield reaches more than 97%.
To reach above-mentioned purpose, the technical proposal of the invention is realized in this way：
The process for purification of one kind 2,2- methoxy propanes, comprises the following steps：
S1. by the material liquid containing 2,2-dimethoxypropane, methanol, acetone and water through azeotrope column initial gross separation, from tower top
The acetone of extraction and the azeotropic mixture of methanol are partly refluxed to azeotrope column；
S2. material azeotrope column bottom of towe produced introduces extractive distillation column and carries out extracting rectifying, and extracting rectifying column overhead is adopted
The material gone out introduces layering tank, and extractive distillation column bottom of towe extraction material introduces methanol column；
S3. the water section from methanol column bottom of towe is introduced into layering tank to recycle as extractant, the water being layered in tank
Mutually introduce extractive distillation column and introduce product tower as backflow, oil phase；
S4. the 2,2-dimethoxypropane that mass fraction is more than 99.5%, product top of tower are obtained from product tower bottom
Produce material and enter layering tank, methanol is produced at the top of methanol column.
Preferably, the azeotrope column, extractive distillation column, product tower, methanol column top and methanol tower bottom production material are equal
Condensation process need to be first passed through.
Preferably, the product tower and methanol column are rectifying column；Azeotrope column, extractive distillation column, product tower and methanol column
It is one kind in decompression operation, atmospheric operation and pressurized operation；Azeotrope column, extractive distillation column, the behaviour of product tower and methanol column
It is absolute pressure 0.02MPa to 0.8MPa to make pressure.
Preferably, the operating reflux ratio for controlling azeotrope column is 6:1-15:1, tower top temperature is 54-56 DEG C, and column bottom temperature is
65-68℃。
Preferably, the operating reflux ratio for controlling extractive distillation column is 2:1-4:1, tower top temperature is 63-66 DEG C, column bottom temperature
For 78-81 DEG C.
Preferably, the operating reflux ratio for controlling product tower is 2:1-4:1, tower top temperature is 67-71 DEG C, and column bottom temperature is
80-83℃。
Preferably, the operating reflux ratio for controlling methanol column is 1.2:1-3:1, tower top temperature is 63-65 DEG C, and column bottom temperature is
100-102℃。
Another object of the present invention is to propose the refining plant of one kind 2,2- methoxy propanes, to refine 2,2- methoxyl groups
Propane, it is more than 99.5% to obtain mass fraction, 2,2- methoxy propane product of the high income up to more than 97%.
To reach above-mentioned purpose, the technical proposal of the invention is realized in this way：
The refining plant of one kind 2,2- methoxy propanes, including azeotrope column, extractive distillation column, product tower and methanol column, and
Each tower lower end is equipped with reboiler；
Be provided with material liquid import among azeotrope column, azeotrope column top material export be sequentially communicated the first condenser, first time
Flow tank and the upper end charging aperture of azeotrope column；The intermediate feed mouth of the material outlet connection extractive distillation column of azeotropic tower bottom；
Extractive distillation column top discharge mouth is sequentially communicated the upper endfeed of the second condenser, layering tank and extractive distillation column
Mouthful；The bottom discharge mouth of layering tank connects with product tower；The discharging opening connection product collector unit of product tower bottom；Extracting rectifying
Charging aperture among the discharging opening connection methanol column of tower bottom；
The material outlet of methanol column bottom of towe is sequentially communicated the 3rd condenser and layering tank.
Further, the product top of tower discharging opening connect the 4th condenser, the 4th condenser connection layering tank and
Unit is arranged outside first material；Methanol column top discharge mouth is sequentially communicated the 5th condenser and the second return tank, the second return tank
Unit is arranged outside the charging aperture and first material of discharging opening connection methanol column upper end；List is arranged outside 3rd condenser connection first material
Member；Unit is arranged outside first return tank connection second material.
Further, between the first return tank and azeotrope column, between layering tank and extractive distillation column, the second return tank and first
Reflux pump is equipped between alcohol tower；The product tower and methanol column are rectifying column.
Relative to prior art, a kind of process for purification of 2,2- methoxy propanes of the present invention has the advantage that：
A kind of process for purification of 2,2- methoxy propanes of the present invention, makes full use of 2,2-dimethoxypropane and water
The characteristics of solubility is not high, using azeotropic mixture of the water as extractant separation of extractive distillation water outlet -2,2-dimethoxypropane, then
Using the principle of heterogeneous azeotropic rectification product 2,2- methoxyl groups are obtained (in product tower reclaimed water and 2,2- methoxy propanes slightly soluble)
Propane.As the extractant of water, gasify in distillation process seldom, therefore the process energy consumption is relatively low.In addition, the technique is not drawn
Enter other components, product quality will not be impacted.Product quality fraction can reach more than 99.5%, and yield reaches 97%
More than.
A kind of refining plant of 2,2- methoxy propanes and a kind of above-mentioned process for purification phase of 2,2- methoxy propanes
It is same for Dominant Facies possessed by prior art, it will not be repeated here.
Brief description of the drawings
Fig. 1 is the simple structure schematic diagram of the refining plant of the 2,2- methoxy propanes described in the embodiment of the present invention 1.
Reference：
1- azeotrope columns；2- extractive distillation columns；3- product towers；4- methanol columns；5- reboilers；The condensers of 6- first；7- first
Return tank；The condensers of 8- second；9- is layered tank；The condensers of 10- the 3rd；The condensers of 11- the 4th；12- product collector units；13-
Unit is arranged outside first material；The condensers of 14- the 5th；The return tanks of 15- second；Unit is arranged outside 16- second materials；17- reflux pumps.
Embodiment
In addition to being defined, technical term used has universal with those skilled in the art of the invention in following examples
The identical meanings of understanding.Test reagent used, is routine biochemistry reagent unless otherwise specified in following examples；It is described
Experimental method, it is conventional method unless otherwise specified.
The present invention is described in detail with reference to embodiment and accompanying drawing.
Embodiment 1
As shown in figure 1, the refining plant of one kind 2,2- methoxy propanes, including azeotrope column 1, extractive distillation column 2, product tower
3 and methanol column 4, and each tower lower end is equipped with reboiler 5；
Material liquid import is provided among azeotrope column 1, the outlet of the top material of azeotrope column 1 is sequentially communicated the first condenser 6, first
The upper end charging aperture of return tank 7 and azeotrope column 1；The intermediate feed of the material outlet connection extractive distillation column 2 of the bottom of azeotrope column 1
Mouthful；
The upper end that the top discharge mouth of extractive distillation column 2 is sequentially communicated the second condenser 8, layering tank 9 and extractive distillation column 2 is entered
Material mouth；The bottom discharge mouth of layering tank 9 connects with product tower 3；The discharging opening connection product collector unit 12 of the bottom of product tower 3；
Charging aperture among the discharging opening connection methanol column 4 of the bottom of extractive distillation column 2；
The material outlet of the bottom of towe of methanol column 4 is sequentially communicated the 3rd condenser 10 and layering tank 9.
The discharging opening at the top of the said goods tower 3 connects the 4th condenser 11, the 4th condenser 11 connection layering tank 9 and first
Unit 13 is arranged outside material；The top discharge mouth of methanol column 4 is sequentially communicated the 5th condenser 14 and the second return tank 15, the second return tank
Unit 13 is arranged outside the charging aperture and first material of 15 discharging opening connection methanol column 4 upper end；3rd condenser 10 connects the first thing
The outer row's unit 13 of material；Unit 16 is arranged outside first return tank 7 connection second material.
Between first return tank 7 and azeotrope column 1, between layering tank 9 and extractive distillation column 2, the second return tank 15 and methanol
Reflux pump 17 is equipped between tower 4；The said goods tower 3 and methanol column 4 are rectifying column；The cooling medium of each condenser is
Water.
The method that 2,2- dimethoxy propanes are refined using the refining plant of above-mentioned 2,2- dimethoxy propanes is as follows：
2,2- dimethoxy propanes in material liquid, methanol, the mass fraction of acetone and water are respectively：15%th, 54%,
24%th, 7%, material liquid is initially entered into azeotrope column 1, the tower operating reflux ratio is 10:1, tower top temperature is 54 DEG C, column bottom temperature
For 65 DEG C, the azeotropic mixture of acetone and methanol is produced by the column overhead, azeotrope column 1 is partly refluxed to after the azeotropic mixture is condensed, altogether
Boiling tower 1 is the material for being substantially free of acetone, and the material enters extractive distillation column 2, and the operating reflux ratio of extractive distillation column 2 is 3:1, tower
It is 63 DEG C to push up temperature, and column bottom temperature is 80 DEG C, and extractant water enters layering tank 9, and aqueous phase caused by layering enters extractive distillation column 2
As backflow, the material of bottom of towe extraction first alcohol and water composition.Oil phase caused by layering tank 9 top enters product tower 3, product tower 3
Operating reflux ratio be 2.5:1, tower top temperature is 68 DEG C, and column bottom temperature is 80 DEG C, and the material of the overhead extraction of product tower 3 is condensed
Enter layering tank 9, the 2,2-dimethoxypropane that the bottom of towe of product tower 3 extraction mass fraction is 99.7%, yield 97.3% afterwards.
The materials at bottom of tower of extractive distillation column 2 enters methanol column 4, and the operating reflux ratio of methanol column 4 is 2:1, tower top temperature is 64 DEG C, bottom of towe
Temperature is 101 DEG C, overhead extraction methanol, and the material of bottom of towe extraction is water, and part discharge, is partly into layering after cooling
Tank 9 recycles as extractant.
Above-mentioned azeotrope column 1, extractive distillation column 2, product tower 3, the top of methanol column 4 and the bottom of methanol column 4 extraction material are both needed to
First pass through condensation process.
The said goods tower 3 and methanol column 4 are rectifying column；Azeotrope column 1, extractive distillation column 2, product tower 3 and methanol column 4 are equal
For atmospheric operation.
Embodiment 2
The present embodiment is substantially the same manner as Example 1, and difference is in the method in refined 2,2-dimethoxypropane：Altogether
The operating reflux ratio for boiling tower is 7:1, tower top temperature is 55 DEG C, and column bottom temperature is 66 DEG C；The operating reflux ratio of extractive distillation column is
2:1, tower top temperature is 65 DEG C, and column bottom temperature is 79 DEG C；The operating reflux ratio of product tower is 3:1, tower top temperature is 70 DEG C, bottom of towe
Temperature is 81 DEG C；The operating reflux ratio of methanol column is 1.5:1, tower top temperature is 63 DEG C, and column bottom temperature is 102 DEG C.
Azeotrope column 1, extractive distillation column 2, the operating pressure of product tower 3 and methanol column 4 are normal pressure.
The 2,2-dimethoxypropane that the bottom of towe of the present embodiment product tower 3 extraction mass fraction is 99.9%, yield are
98.6%.
Embodiment 3
The present embodiment is substantially the same manner as Example 1, and difference is in the method in refined 2,2-dimethoxypropane：Altogether
The operating reflux ratio for boiling tower is 14.5:1, tower top temperature is 56 DEG C, and column bottom temperature is 68 DEG C；The operating reflux ratio of extractive distillation column
For 3.7:1, tower top temperature is 66 DEG C, and column bottom temperature is 81 DEG C；The operating reflux ratio of product tower is 4:1, tower top temperature is 71 DEG C,
Column bottom temperature is 83 DEG C；The operating reflux ratio of methanol column is 2.4:1, tower top temperature is 65 DEG C, and column bottom temperature is 101 DEG C.
Azeotrope column 1, extractive distillation column 2, the operating pressure of product tower 3 and methanol column 4 are normal pressure.
The 2,2-dimethoxypropane that the bottom of towe of the present embodiment product tower 3 extraction mass fraction is 99.86%, yield are
99.1%.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all essences in the present invention
God any modification, equivalent substitution and improvements made etc., should be included in the scope of the protection with principle.
Claims (10)
1. one kind 2, the process for purification of 2- methoxy propanes, it is characterised in that：Comprise the following steps：
S1. the material liquid containing 2,2-dimethoxypropane, methanol, acetone and water is adopted through azeotrope column (1) initial gross separation from tower top
The acetone and the azeotropic mixture of methanol gone out is partly refluxed to azeotrope column (1)；
S2. the material of azeotrope column (1) bottom of towe extraction is introduced into extractive distillation column (2) and carries out extracting rectifying, extractive distillation column (2) tower
The material of top extraction introduces layering tank (9), and extractive distillation column (2) bottom of towe extraction material introduces methanol column (4)；
S3. the water section that methanol column (4) bottom of towe will be come from introduces layering tank (9) as extractant recycling, is layered in tank (9)
Aqueous phase introduce extractive distillation column (2) as backflow, oil phase introduce product tower (3)；
S4. the 2,2-dimethoxypropane that mass fraction is more than 99.5%, product tower (3) top are obtained from product tower (3) bottom
Portion's extraction material enters layering tank (9), and methanol is produced at the top of methanol column (4).
2. the process for purification of 2,2- methoxy propanes according to claim 1, it is characterised in that：The azeotrope column (1), extraction
Rectifying column (2), product tower (3), methanol column (4) top and methanol column (4) bottom extraction material is taken to be both needed to first pass through condensation process.
3. the process for purification of 2,2- methoxy propanes according to claim 1, it is characterised in that：The product tower (3) and
Methanol column (4) is rectifying column；Azeotrope column (1), extractive distillation column (2), product tower (3) and methanol column (4) be decompression operation,
One kind in atmospheric operation and pressurized operation；The operation of azeotrope column (1), extractive distillation column (2), product tower (3) and methanol column (4)
Pressure is absolute pressure 0.02MPa to 0.8MPa.
4. the process for purification of 2,2- methoxy propanes according to claim 1, it is characterised in that：Control azeotrope column (1)
Operating reflux ratio is 6:1-15:1, tower top temperature is 54-56 DEG C, and column bottom temperature is 65-68 DEG C.
5. the process for purification of 2,2- methoxy propanes according to claim 1, it is characterised in that：Control extractive distillation column
(2) operating reflux ratio is 2:1-4:1, tower top temperature is 63-66 DEG C, and column bottom temperature is 78-81 DEG C.
6. the process for purification of 2,2- methoxy propanes according to claim 1, it is characterised in that：Control product tower (3)
Operating reflux ratio is 2:1-4:1, tower top temperature is 67-71 DEG C, and column bottom temperature is 80-83 DEG C.
7. the process for purification of 2,2- methoxy propanes according to claim 1, it is characterised in that：Control methanol column (4)
Operating reflux ratio is 1.2:1-3:1, tower top temperature is 63-65 DEG C, and column bottom temperature is 100-102 DEG C.
8. one kind 2, the refining plant of 2- methoxy propanes, it is characterised in that：Including azeotrope column (1), extractive distillation column (2), production
Product tower (3) and methanol column (4), and each tower lower end is equipped with reboiler (5)；
Be provided with material liquid import among azeotrope column (1), azeotrope column (1) top material, which exports, is sequentially communicated the first condenser (6), the
The upper end charging aperture of one return tank (7) and azeotrope column (1)；The material outlet connection extractive distillation column (2) of azeotrope column (1) bottom
Intermediate feed mouth；
Extractive distillation column (2) top discharge mouth is sequentially communicated the upper of the second condenser (8), layering tank (9) and extractive distillation column (2)
Endfeed mouth；The bottom discharge mouth of layering tank (9) connects with product tower (3)；The discharging opening connection product of product tower (3) bottom is received
Collect unit (12)；Charging aperture among the discharging opening connection methanol column (4) of extractive distillation column (2) bottom；
The material outlet of methanol column (4) bottom of towe is sequentially communicated the 3rd condenser (10) and layering tank (9).
9. the refining plant of 2,2- methoxy propanes according to claim 8, it is characterised in that：Product tower (3) top
The discharging opening in portion connects the 4th condenser (11), and unit is arranged outside the 4th condenser (11) connection layering tank (9) and first material
(13)；Methanol column (4) top discharge mouth is sequentially communicated the 5th condenser (14) and the second return tank (15), the second return tank (15)
Discharging opening connection methanol column (4) upper end charging aperture and first material outside arrange unit (13)；3rd condenser (10) connection the
Unit (13) is arranged outside one material；Unit (16) is arranged outside first return tank (7) connection second material.
10. the refining plant of 2,2- methoxy propanes according to claim 9, it is characterised in that：First return tank (7) with
It is all provided between azeotrope column (1), between layering tank (9) and extractive distillation column (2), between the second return tank (15) and methanol column (4)
There is reflux pump (17)；The product tower (3) and methanol column (4) are rectifying column.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710774362.XA CN107382682B (en) | 2017-08-31 | 2017-08-31 | Refining method and device of 2, 2-methoxypropane |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710774362.XA CN107382682B (en) | 2017-08-31 | 2017-08-31 | Refining method and device of 2, 2-methoxypropane |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107382682A true CN107382682A (en) | 2017-11-24 |
| CN107382682B CN107382682B (en) | 2023-05-26 |
Family
ID=60349010
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710774362.XA Active CN107382682B (en) | 2017-08-31 | 2017-08-31 | Refining method and device of 2, 2-methoxypropane |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107382682B (en) |
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 |
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107382682B (en) | 2023-05-26 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105218315B (en) | A kind of method and device of the refined methyl alcohol of use divided-wall distillation column combination heat pump | |
| US8476464B2 (en) | Alkylene oxide purification systems | |
| CN101284762B (en) | Method for the production of very pure 1,4-butanediol | |
| CN101092337B (en) | Method for preparing methylal by combining reaction rectification and extraction | |
| CN101367710A (en) | Process and apparatus for preparing absolute ethyl alcohol | |
| CN105218305B (en) | A kind of byproduct recovery process of synthesis gas preparing ethylene glycol | |
| CN111675601B (en) | Novel process and device for separating and purifying industrial ethanol | |
| CN100395226C (en) | Method for mass producing butyl acetate by reactive distillation method and using sulfuric acid as catalyst | |
| CN105753649B (en) | A kind of method that isooctanol is reclaimed from the solvent slop of isooctyl thioglycolate production process | |
| CN106866366A (en) | Dihydroxylic alcohols or polyol impurities and the method for increasing production ethylene glycol in a kind of removal ethylene glycol | |
| CN107556172B (en) | Process method for producing ethylene glycol mono-tert-butyl ether | |
| EP2307111B1 (en) | Alkylene oxide purification columns | |
| CN211798889U (en) | Refining system for by-product hydrochloric acid in methane chloride process | |
| RU1829948C (en) | Method for separation of medium-boiling fraction from mixture of cyclohexanone and cyclohexanol with medium- and high-boiling products | |
| CN111377801B (en) | Method and system for refining low carbon alcohol | |
| CN107382682A (en) | A kind of process for purification and device of 2,2 methoxy propane | |
| CN207418632U (en) | A kind of refining plant of 2,2- methoxy propanes | |
| CN101177419A (en) | Method for separating N-ethylpiperazine-ethanolamine azeotropic mixture by azeotropic rectifying intermittent operation | |
| CN103864592B (en) | By side draw tower order post processing CDON/CDOL mixtures | |
| CN107162875B (en) | Process and system for extracting refined methanol and absolute ethanol from crude methanol | |
| EP2307114B1 (en) | Alkylene oxide purification column with two internal condensers | |
| CN107382743A (en) | A kind of method of extracting rectifying purification triethylamine | |
| CN110002960B (en) | Device and method for separating ABE fermentation pervaporation liquid | |
| RU2682330C1 (en) | Method of continuous unmixing mixture of ethyl chlorosilane | |
| CN113354605A (en) | Separation device and process for maleic anhydride hydrogenation product |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |