CN107501085A - A kind of method that economic benefits and social benefits are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures - Google Patents
A kind of method that economic benefits and social benefits are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures Download PDFInfo
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/43—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation
- C07C51/44—Separation; Purification; Stabilisation; Use of additives by change of the physical state, e.g. crystallisation by distillation
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention discloses a kind of method that economic benefits and social benefits are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, its extractant used is N methylacetamides；Separation equipment used includes extractive distillation column, heat exchanger and extractant recovery tower；In separation process, the condensed rear extraction of water vapour of the extracting rectifying top of tower generation, it is divided into circulation logistics and output streams after acetic acid and the extractant extraction of the extracting rectifying tower bottom；Recycle stream backs into the extractive distillation column after heat exchanger heating；Output streams enter the extractant recovery tower, and the extractant recovery tower bottom extraction extractant, the acetic acid steam that the extractant recovery tower top generates is after heat exchanger condensation by default reflux ratio extraction.Methods described employs economic benefits and social benefits and is thermally integrated technique, treats that boiling logistics again provides heat, realizes the secondary use of energy with extractant recovery column overhead logistics to be condensed for extractive distillation column bottom of towe, effectively reduces energy consumption and saves equipment cost.
Description
Technical field
The invention belongs to separation of extractive distillation technical field, it is related to the method for separating acetic acid and aqueous mixtures, more particularly to
A kind of method that economic benefits and social benefits are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures.
Background technology
Acetic acid, also referred to as acetic acid, it is extremely important synthesis material and organic solvent in chemical industry, is most widely used
One of organic carboxyl acid.As raw material, for producing the industrial products such as vinyl acetate, aceticanhydride, acetate, acetate fiber.As molten
Agent, for the purification of organic compound (terephthalic acid (TPA) etc.), and have extensively in the industries such as pharmacy, printing and dyeing, rubber and food
Using.
In above Chemical Manufacture, the mixture of a large amount of acetic acid and water can be produced, to reduce production cost, it is dirty to reduce environment
Dye, the acetic acid in acetic acid aqueous solution is reclaimed to reuse, can not only turn waste into wealth, can also improve the economic benefit of enterprise.But
It is that acetic acid and water belong to the difficult separation homogeneous mixture of low boiling, their relative volatility is close to 1, it is achieved that point of the two
From very difficult.
On the separation of extractive distillation process of acetic acid and water, have some document reports, such as Hu Xinglan (natural gases at present
Chemical industry, 2004,9 (1), 37), Li Xinli etc. (Sichuan chemical industry, 2006,9 (2), 40), Zhu Denglei etc. (computer and applied chemistry,
2010,27 (6), 791), Han Shucui etc. (Guangdong chemical industry, 2012,39 (9), 177).But reported above merely relate to conventional extraction
The design of distillation process is taken, is not related to being thermally integrated for extracting rectifying process, and generally existing reflux ratio is big, process high energy consumption, production
The shortcomings that product purity and relatively low yield.
Economic benefits and social benefits on acetic acid and aqueous mixtures are thermally integrated separation of extractive distillation, have not yet to see document report.
The content of the invention
It is therefore an object of the present invention to for overcome the deficiencies in the prior art, there is provided a kind of economic benefits and social benefits are thermally integrated extracting rectifying
The method of separating acetic acid and aqueous mixtures, realize that energy economic benefits and social benefits utilize, reach the purpose of energy-saving and emission-reduction, reduce separation costs.
Economic benefits and social benefits of the present invention are thermally integrated in the method for separation of extractive distillation acetic acid and aqueous mixtures,
Extractant used is N- methylacetamides；
Separation equipment used includes extractive distillation column, heat exchanger and extractant recovery tower, and the extractive distillation column is equipped with 25-
50 pieces of theoretical plates, the extractant recovery tower are equipped with 20-40 block theoretical plates；
In separation process, the mixture of acetic acid and water to be separated enters the extractive distillation column by 10-25 blocks theoretical plate,
Extractant enters the extractive distillation column by 3-15 blocks theoretical plate, and the water vapour of the extracting rectifying top of tower generation is condensed
Produced afterwards by default reflux ratio, be divided into circulation logistics after acetic acid and the extractant extraction of the extracting rectifying tower bottom and go out material
Stream；Recycle stream backs into the extractive distillation column after heat exchanger heating；Output streams are theoretical by 3-12 blocks
Plate enters the extractant recovery tower, the extractant that the extractant recovery tower bottom extraction can be recycled, the extractant
The acetic acid steam of generation is produced after heat exchanger condensation by default reflux ratio at the top of recovery tower；The behaviour of the extractive distillation column
Make the operating pressure that pressure is less than the extractant recovery tower, the tower top temperature of the extractant recovery tower is higher than extractive distillation column
Column bottom temperature.
Preferably, the extractive distillation column is equipped with 30-45 block theoretical plates, the mixture of acetic acid and water to be separated is by 14-
20 pieces of theoretical plates enter, and extractant is entered by 3-10 blocks theoretical plate.
Preferably, acetic acid content is 20%-80% in the mixture of the acetic acid to be separated and water.
Preferably, the ratio between mixture flow rate of extractant and the acetic acid to be separated and water is 0.1-1.0.Based on liquid phase
Balance test data, calculated by strict gas-liquid phase equilibrium, when N- methyl vinyls amine content is 0.1, water is to the relative of acetic acid
Volatility can reach more than 2, it is sufficient to meet separation water and the purpose of acetic acid.
Preferably, the reflux ratio of the extractive distillation column is 0.2-1.2.
Preferably, the reflux ratio of the extractant recovery tower is 1-6.
Preferably, the operating pressure of the extractive distillation column is 0.1-1atm.
Preferably, the operating pressure of the extractant recovery tower is 1.5-5atm.
Preferably, the extracting rectifying column overhead temperatures, at 45-100 DEG C, column bottom temperature is at 120-160 DEG C.
Preferably, the extractant reclaims column overhead temperatures at 130-180 DEG C, column bottom temperature is at 220-280 DEG C.
Preferably, the recycle stream by the heat exchanger heating after can also through supplement reboiler heating, return again into
Enter the extractive distillation column.
The positive effect of the present invention is：
Methods described not only can effectively be reduced Solvent quantity, be used simultaneously using N- methylacetamides as extractant
Economic benefits and social benefits are thermally integrated technique, and extractive distillation column is different with the operating pressure of extractant recovery tower, the tower of corresponding extractant recovery tower
The column bottom temperature of extractive distillation column can be higher than by pushing up temperature, therefore, can be treated by the heat exchanger with extractant recovery column overhead
Condensate flow (i.e. described acetic acid steam) is that extractive distillation column bottom of towe treats that boiling logistics (i.e. described circulation logistics) again provides heat, real
The secondary use of existing energy.And the heat exchanger is by the tower bottom reboiler of original extractive distillation column and extractant recovery tower
The function of both overhead condensers is combined into one, and can largely save equipment investment cost.To sum up, using methods described separating acetic acid
During with water, extractant is low with the ratio between mixture flow rate, and acetic acid and aqueous mixtures compositing range are wide, and energy consumption is low, and equipment investment is small, production
Product purity and high income, process safety, environmental protection, pollution-free, achievable clean manufacturing.
Brief description of the drawings
Fig. 1 is the flow chart that economic benefits and social benefits are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures.
Embodiment
In order to further illustrate the present invention, following serial specific embodiment is provided, but the present invention is not specific real by these
The limitation of example is applied, any understanding person skilled in art will can reach similar result to the few modifications of the present invention, this
A little changes are also contained among the present invention.
Fig. 1 show the flow chart that economic benefits and social benefits of the invention are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures.It is to be separated
Acetic acid and aqueous mixtures 1 enter extractive distillation column 2, obtain the water logistics 3 of high-purity in the tower top of extractive distillation column 2, bottom of towe obtains
The mixture stream passes 4 of acetic acid and extractant, logistics 4 divides circulates logistics 5 and output streams 6 for extractive distillation column bottom of towe, wherein following
The logistics 10 that ring logistics 5 enters in heat exchanger 7 with coming from extractant recovery column overhead carries out heat exchange, by mending after heat exchange
Fill reboiler 8 and supply heat Posterior circle time extractive distillation column bottom of towe.The bottom of towe output streams 6 of extractive distillation column 2 enter extractant
Recovery tower 9, high-purity acetic acid steam logistics 10 is obtained in the tower top of extractant recovery tower 9, logistics 10 enters in heat exchanger 7 with coming
From after the progress of circulation logistics 5 heat exchange of extractive distillation column bottom of towe is cooled to saturated liquid, it is divided into extractant recovery column overhead
Output streams 11 and circulation logistics 12, circulation logistics 12 back into extractant recovery tower.Extractant recovery tower bottom of towe goes out material
Stream 13 mixes with extractant supplement logistics 14 after supercooling, enters after mixing in extractive distillation column 2, realize following for extractant
Ring utilizes.
Embodiment 1
So that 19517.0kg/h acetic acid content is 76.9wt% acetic acid and water mixed liquid as an example：
Extractive distillation column totally 41 blocks of column plates, reflux ratio 0.73, operating pressure 0.2atm, fresh material is from the 16th piece of tower
Plate enters extractive distillation column, speed (mol ratio 0.45) of the extractant (N- methylacetamides) using flow as 16321.8kg/h
Enter extractive distillation column from the 6th block of column plate.Extracting rectifying column overhead temperatures are 60.4 DEG C, condenser heat load 5.10MW, tower
Bottom temperature is 131.7 DEG C, supplement reboiler heat duty 2.79MW.Extractant recovery tower totally 28 blocks of column plates, reflux ratio 1.17, behaviour
It is that 1.8atm, acetic acid and extractant mixed solution enter extractant recovery tower, extractant recovery tower tower from the 7th block of column plate to make pressure
It is 138.3 DEG C to push up temperature, and column bottom temperature is 233.6 DEG C, reboiler heat duty 4.99MW.It is without required thermic load when being thermally integrated
11.45MW, it is 3.67MW to have the heat being secondary use when being thermally integrated, energy-conservation 32.1%.Extracting rectifying column overhead obtains purity
For 99.9% water, extractant recovery column overhead obtains the acetic acid that purity is 99.91%.
Embodiment 2
So that 19517.0kg/h acetic acid content is 76.9wt% acetic acid and water mixed liquid as an example：
Extractive distillation column totally 41 blocks of column plates, reflux ratio 0.72, operating pressure 0.1atm, fresh material is from the 19th piece of tower
Plate enters extractive distillation column, speed (mol ratio 0.49) of the extractant (N- methylacetamides) using flow as 17885.0kg/h
Enter extractive distillation column from the 4th block of column plate.Extracting rectifying column overhead temperatures are 46.1 DEG C, condenser heat load 5.16MW, tower
Bottom temperature is 126.7 DEG C, supplement reboiler heat duty 1.59MW.Extractant recovery tower totally 28 blocks of column plates, reflux ratio 1.89, behaviour
It is that 1.5atm, acetic acid and extractant mixed solution enter extractant recovery tower, extractant recovery column overhead from 8 blocks of column plates to make pressure
Temperature is 131.7 DEG C, and column bottom temperature is 226.4 DEG C, reboiler heat duty 6.20MW.It is without required thermic load when being thermally integrated
12.61MW, it is 4.82MW to have the heat being secondary use when being thermally integrated, energy-conservation 38.2%.Extracting rectifying column overhead obtains purity
For 99.9% water, extractant recovery column overhead obtains the acetic acid that purity is 99.9%.
Embodiment 3
So that 19517.0kg/h acetic acid content is 76.9wt% acetic acid and water mixed liquid as an example：
Extractive distillation column totally 41 blocks of column plates, reflux ratio 0.8, operating pressure 0.4atm, fresh material is from the 16th piece of tower
Plate enters extractive distillation column, speed (mol ratio 0.41) of the extractant (N- methylacetamides) using flow as 15049.5kg/h
Enter extractive distillation column from the 4th block of column plate.Extracting rectifying column overhead temperatures are 76.2 DEG C, condenser heat load 4.90MW, tower
Bottom temperature is 141.0 DEG C, supplement reboiler heat duty 2.85MW.Extractant recovery tower totally 28 blocks of column plates, reflux ratio 1.13, behaviour
It is that 3atm, acetic acid and extractant mixed solution enter extractant recovery tower, extractant recovery column overhead temperature from 9 blocks of column plates to make pressure
Spend for 157.9 DEG C, column bottom temperature is 256.0 DEG C, reboiler heat duty 5.11MW.It is without required thermic load when being thermally integrated
11.57MW, it is 3.61MW to have the heat being secondary use when being thermally integrated, energy-conservation 31.2%.Extracting rectifying column overhead obtains purity
For 99.9% water, extractant recovery column overhead obtains the acetic acid that purity is 99.9%.
Embodiment 4
So that 9188.0kg/h acetic acid content is 58.8wt% acetic acid and water mixed liquid as an example：
Extractive distillation column totally 41 blocks of column plates, reflux ratio 0.30, operating pressure 0.5atm, fresh material is from the 18th piece of tower
Plate enters extractive distillation column, extractant (N- methylacetamides) using flow as 7904.7kg/h speed (mol ratio 0.36) from
6th block of column plate enters extractive distillation column.Extracting rectifying column overhead temperatures are 81.7 DEG C, condenser heat load 3.16MW, bottom of towe
Temperature is 156.4 DEG C, supplement reboiler heat duty 1.67MW.Extractant recovery tower totally 28 blocks of column plates, reflux ratio 1.47, operation
Pressure is that 4.0atm, acetic acid and extractant mixed solution enter extractant recovery tower, extractant recovery column overhead temperature from 5 blocks of column plates
Spend for 169.9 DEG C, column bottom temperature is 270.0 DEG C, reboiler heat duty 2.26MW.It is without required thermic load when being thermally integrated
6.34MW, it is 1.51MW to have the heat being secondary use when being thermally integrated, energy-conservation 23.8%.Extracting rectifying column overhead obtains purity
99.9% water, extractant recovery column overhead obtain the acetic acid that purity is 99.9%.
Embodiment 5
So that 9188.0kg/h acetic acid content is 58.8wt% acetic acid and water mixed liquid as an example：
Extractive distillation column totally 38 blocks of column plates, reflux ratio 0.30, operating pressure 0.2atm, fresh material is from the 18th piece of tower
Plate enters extractive distillation column, extractant (N- methylacetamides) using flow as 8036.1kg/h speed (mol ratio 0.37) from
7th block of column plate enters extractive distillation column.Extracting rectifying column overhead temperatures are 60.4 DEG C, condenser heat load 3.25MW, bottom of towe
Temperature is 137.7 DEG C, supplement reboiler heat duty 0.82MW.Extractant recovery tower totally 23 blocks of column plates, reflux ratio 4.10, operation
Pressure is that 2atm, acetic acid and extractant mixed solution enter extractant recovery tower, extractant recovery column overhead temperatures from 6 blocks of column plates
For 141.6 DEG C, column bottom temperature is 238.0 DEG C, reboiler heat duty 3.71MW.It is without required thermic load when being thermally integrated
7.63MW, it is 3.10MW to have the heat being secondary use when being thermally integrated, energy-conservation 40.6%.Extracting rectifying column overhead obtains purity
99.9% water, extractant recovery column overhead obtain the acetic acid that purity is 99.9%.
Embodiment 6
So that 9188.0kg/h acetic acid content is 58.8wt% acetic acid and water mixed liquid as an example：
Extractive distillation column totally 45 blocks of column plates, reflux ratio 0.33, operating pressure 0.2atm, fresh material is from the 19th piece of tower
Plate enters extractive distillation column, extractant (N- methylacetamides) using flow as 7692.8kg/h speed (mol ratio 0.35) from
6th block of column plate enters extractive distillation column.Extracting rectifying column overhead temperatures are 60.4 DEG C, condenser heat load 3.31MW, bottom of towe
Temperature is 141.0 DEG C, supplement reboiler heat duty 0.95MW.Extractant recovery tower totally 32 blocks of column plates, reflux ratio 4.05, operation
Pressure is that 2.5atm, acetic acid and extractant mixed solution enter extractant recovery tower, extractant recovery column overhead temperature from 7 blocks of column plates
Spend for 150.6 DEG C, column bottom temperature is 248.2 DEG C, reboiler heat duty 3.70MW.It is without required thermic load when being thermally integrated
7.69MW, it is 3.04MW to have the heat being secondary use when being thermally integrated, energy-conservation 39.5%.Extracting rectifying column overhead obtains purity
99.9% water, extractant recovery column overhead obtain the acetic acid that purity is 99.9%.
Embodiment 7
So that 7296.3kg/h acetic acid content is 37.0wt% acetic acid and water mixed liquid as an example：
Extractive distillation column totally 35 blocks of column plates, reflux ratio 0.33, operating pressure 0.2atm, fresh material is from the 17th piece of tower
Plate enters extractive distillation column, extractant (N- methylacetamides) using flow as 3717.9kg/h speed (mol ratio 0.17) from
4th block of column plate enters extractive distillation column.Extracting rectifying column overhead temperatures are 60.4 DEG C, condenser heat load 4.02MW, bottom of towe
Temperature is 135.4 DEG C, supplement reboiler heat duty 3.22MW.Extractant recovery tower totally 23 blocks of column plates, reflux ratio 2.82, operation
Pressure is that 2.5atm, acetic acid and extractant mixed solution enter extractant recovery tower, extractant recovery column overhead temperature from 6 blocks of column plates
Spend for 150.6 DEG C, column bottom temperature is 247.0 DEG C, reboiler heat duty 1.49MW.It is without required thermic load when being thermally integrated
5.86MW, it is 1.15MW to have the heat being secondary use when being thermally integrated, energy-conservation 19.6%.Extracting rectifying column overhead obtains purity
99.9% water, extractant recovery column overhead obtain the acetic acid that purity is 99.9%.
Embodiment 8
So that 9188kg/h acetic acid content is 58.8wt% acetic acid and water mixed liquid as an example：
Extractive distillation column totally 33 blocks of column plates, reflux ratio 0.40, operating pressure 0.5atm, fresh material is from the 15th piece of tower
Plate enters extractive distillation column, extractant (N- methylacetamides) using flow as 6538.5kg/h speed (mol ratio 0.30) from
4th block of column plate enters extractive distillation column.Extracting rectifying column overhead temperatures are 81.7 DEG C, condenser heat load 3.41MW, bottom of towe
Temperature is 148.4 DEG C, supplement reboiler heat duty 0.38MW.Extractant recovery tower totally 20 blocks of column plates, reflux ratio 5.33, operation
Pressure is that 3.3atm, acetic acid and extractant mixed solution enter extractant recovery tower, extractant recovery column overhead temperature from 4 blocks of column plates
Spend for 161.7 DEG C, column bottom temperature is 259.7 DEG C, reboiler heat duty 4.41MW.It is without required thermic load when being thermally integrated
8.59MW, it is 3.80MW to have the heat being secondary use when being thermally integrated, energy-conservation 44.2%.Extracting rectifying column overhead obtains purity
99.9% water, extractant recovery column overhead obtain the acetic acid that purity is 99.9%.
Embodiment 9
So that 9188kg/h acetic acid content is 58.8wt% acetic acid and water mixed liquid as an example：
Extractive distillation column totally 33 blocks of column plates, reflux ratio 0.45, operating pressure 0.8atm, fresh material is from the 14th piece of tower
Plate enters extractive distillation column, extractant (N- methylacetamides) using flow as 5726.6kg/h speed (mol ratio 0.26) from
5th block of column plate enters extractive distillation column.Extracting rectifying column overhead temperatures are 93.9 DEG C, condenser heat load 3.48MW, bottom of towe
Temperature is 156.9 DEG C, supplement reboiler heat duty 2.29MW.Extractant recovery tower totally 22 blocks of column plates, reflux ratio 2.40, operation
Pressure is that 4.2atm, acetic acid and extractant mixed solution enter extractant recovery tower, extractant recovery column overhead temperature from 4 blocks of column plates
Spend for 171.9 DEG C, column bottom temperature is 272.1 DEG C, reboiler heat duty 2.61MW.It is without required thermic load when being thermally integrated
6.94MW, it is 2.04MW to have the heat being secondary use when being thermally integrated, energy-conservation 29.4%.Extracting rectifying column overhead obtains purity
99.9% water, extractant recovery column overhead obtain the acetic acid that purity is 99.9%.
From the various embodiments described above, because the operating pressure of extractive distillation column and extractant recovery tower is different, accordingly
The tower top temperature of extractant recovery tower can be higher than the column bottom temperature of extractive distillation column, therefore, can reclaim column overhead with extractant
Logistics to be condensed treats that boiling logistics again provides heat for extractive distillation column bottom of towe, realizes the secondary use of energy, energy-conservation is up to 20%
~44%.At the same time, heat exchanger 7 had both served as the tower bottom reboiler of extractive distillation column, while acted also as extractant recovery tower
Overhead condenser, the two function is combined into one, equivalent to a condenser is saved, can largely save equipment investment cost.
And using the method for the present invention, extractant is low with the ratio between mixture flow rate, and acetic acid and aqueous mixtures compositing range are wide, energy consumption
Low, product purity and high income, the product purity of acetic acid and water after separation is more than 99.9%, process safety, environmental protection, nothing
Pollution, clean manufacturing can be achieved.
The preferred embodiment to the invention is illustrated above, but the invention be not limited to it is described
Embodiment, those skilled in the art can also make a variety of equivalent on the premise of without prejudice to the invention spirit
Modification or replacement, these equivalent modifications or replacement are all contained in the application claim limited range.
Claims (9)
1. a kind of method that economic benefits and social benefits are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, it is characterised in that
Extractant used is N- methylacetamides；
Separation equipment used includes extractive distillation column, heat exchanger and extractant recovery tower, and the extractive distillation column is equipped with 25-50 blocks
Theoretical plate, the extractant recovery tower are equipped with 20-40 block theoretical plates；
In separation process, the mixture of acetic acid and water to be separated enters the extractive distillation column by 10-25 blocks theoretical plate, extraction
Agent enters the extractive distillation column by 3-15 blocks theoretical plate, is pressed after the water vapour that the extracting rectifying top of tower generates is condensed
Default reflux ratio extraction, it is divided into circulation logistics and output streams after acetic acid and the extractant extraction of the extracting rectifying tower bottom；
Recycle stream backs into the extractive distillation column after heat exchanger heating；Output streams are entered by 3-12 block theoretical plates
Enter the extractant recovery tower, the extractant that the extractant recovery tower bottom extraction can be recycled, the extractant recovery
The acetic acid steam of top of tower generation is produced after heat exchanger condensation by default reflux ratio；The operation pressure of the extractive distillation column
Power is less than the operating pressure of the extractant recovery tower, and the tower top temperature of the extractant recovery tower is higher than the tower of extractive distillation column
Bottom temperature.
2. the method that economic benefits and social benefits as claimed in claim 1 are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, it is characterised in that
Acetic acid content is 20%-80% in the mixture of the acetic acid to be separated and water.
3. the method that economic benefits and social benefits as claimed in claim 1 are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, it is characterised in that
The ratio between mixture flow rate of extractant and the acetic acid to be separated and water is 0.1-1.0.
4. the method that economic benefits and social benefits as claimed in claim 1 are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, it is characterised in that
The reflux ratio of the extractive distillation column is 0.2-1.2.
5. the method that economic benefits and social benefits as claimed in claim 1 are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, it is characterised in that
The reflux ratio of the extractant recovery tower is 1-6.
6. the method that economic benefits and social benefits as claimed in claim 1 are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, it is characterised in that
The operating pressure of the extractive distillation column is 0.1-1atm.
7. the method that economic benefits and social benefits as claimed in claim 1 are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, it is characterised in that
The operating pressure of the extractant recovery tower is 1.5-5atm.
8. the method that economic benefits and social benefits as claimed in claim 1 are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, it is characterised in that
The extracting rectifying column overhead temperatures are at 45-100 DEG C, and column bottom temperature is at 120-160 DEG C.
9. the method that economic benefits and social benefits as claimed in claim 1 are thermally integrated separation of extractive distillation acetic acid and aqueous mixtures, it is characterised in that
The extractant reclaims column overhead temperatures at 130-180 DEG C, and column bottom temperature is at 220-280 DEG C.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109232482A (en) * | 2018-10-31 | 2019-01-18 | 重庆大学 | A kind of economic benefits and social benefits are thermally integrated abstraction distillation separation of tetrahydrofuran-methanol-water azeotropic mixture method |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1919821A (en) * | 2006-09-13 | 2007-02-28 | 西南化工研究设计院 | Method of recovery acetic acid from acetic acid containing waste water |
| CN102267889A (en) * | 2011-06-03 | 2011-12-07 | 华东理工大学 | Method for recovering spirit of vinegar by combining extraction with azeotropic distillation |
| CN104447275A (en) * | 2014-11-28 | 2015-03-25 | 浙江新和成药业有限公司 | Method for purifying acetic acid from acetic acid wastewater |
-
2017
- 2017-09-25 CN CN201710875376.0A patent/CN107501085A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1919821A (en) * | 2006-09-13 | 2007-02-28 | 西南化工研究设计院 | Method of recovery acetic acid from acetic acid containing waste water |
| CN102267889A (en) * | 2011-06-03 | 2011-12-07 | 华东理工大学 | Method for recovering spirit of vinegar by combining extraction with azeotropic distillation |
| CN104447275A (en) * | 2014-11-28 | 2015-03-25 | 浙江新和成药业有限公司 | Method for purifying acetic acid from acetic acid wastewater |
Non-Patent Citations (3)
| Title |
|---|
| ZHIGANG LEI 等: "Separation of acetic acid and water by complex extractive distillation", 《SEPARATION AND PURIFICATION TECHNOLOGY 》 * |
| 梁凯: "能量节约型萃取精馏过程的研究：设计与优化", 《中国优秀硕士学位论文全文数据库 工程科技Ⅰ辑》 * |
| 韩淑萃 等: "NMP 萃取精馏分离醋酸和水的过程模拟", 《广东化工》 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109232482A (en) * | 2018-10-31 | 2019-01-18 | 重庆大学 | A kind of economic benefits and social benefits are thermally integrated abstraction distillation separation of tetrahydrofuran-methanol-water azeotropic mixture method |
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