CN101830830A - Method for extracting, distilling and separating acetonitrile-phenylmethane by utilizing dividing-wall rectifying tower - Google Patents
Method for extracting, distilling and separating acetonitrile-phenylmethane by utilizing dividing-wall rectifying tower Download PDFInfo
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Abstract
The invention discloses a method for extracting, distilling and separating acetonitrile-phenylmethane by utilizing dividing-wall rectifying tower, which belongs to separation techniques for an acetonitrile-phenylmethane azeotropic mixture. In the method, durene (1,2,4,5-durene) is preferably used as an extracting agent, the adopted device is an extractive rectifying tower provided with a dividing wall, and a dividing wall is installed in the vertical direction of a common rectifying tower to divide the tower into four parts. Region I is an extractive rectifying region, and the main body of the region I is provided with a tower tray and a filler; a sealing plate is arranged between region II and region III; the region II is an extracting agent recovery region; and since the extracting agent can be more easily separated in general and the extracting agent recovery region requires a smaller number of theoretical plates as compared with the extractive rectifying region, the position of the sealing plate can be adjusted by controlling the quantity of the tower trays or the filler. Region III is not additionally provided with any tower tray or filler. Region IV is the common stripping section of the region I and the region II. The invention can separate out high-purity acetonitrile and phenylmethane by using accessible, cheap and efficient extracting agent through extractive rectification with a dividing wall. The method reduces the equipment investment and energy consumption by more than 20% as compared with the conventional continuous extractive rectification.
Description
Technical field
The present invention relates to a kind of dividing wall extraction and rectification separation method of acetonitrile-methylbenzene azeotropic mixture, belong to the isolation technique of acetonitrile-methylbenzene azeotropic mixture.
Background technology
Extracting rectifying is a kind of extraordinary rectifying separation technology, is fit to separating of the azeotropic and the system of closely boiling.Add extraction agent continuously by the top toward rectifying tower and reach the separation purpose with the relative volatility that changes between stock blend, selection of Extractant is the key of extracting rectifying.The dividing wall rectifying tower is a kind of novel tower, can realize extracting rectifying and extraction agent reclaimed to be incorporated in the tower carrying out.Acetonitrile and toluene are extraction agents commonly used in the pharmaceutical industry, the acetonitrile-methylbenzene mixture of Chan Shenging in process of production, owing to forming azeotrope, acetonitrile-methylbenzene is difficult to separate, as not reclaiming, not only pollute the environment, and the increase production cost, it is significant therefore to develop the acetonitrile-methylbenzene azeotropic separating mixture.
ZL200510014635.8 and ZL200510014636.2 use batch extracting rectified respectively and method separating acetonitrile-methylbenzene azeotropic mixture continuous extraction rectifying, the employing extraction agent is propyl benzene, n-butyl benzene, Isobuytel Benzene, sec-butylbenzene, tert.-butylbenzene, p-diethylbenzene or p-tert-butyltoluene, in these extraction agents, propyl benzene separates than difficult in the high density section with acetonitrile, therefore obtaining highly purified acetonitrile product energy consumption can be very high, except that p-diethylbenzene, remaining extraction agent is mainly from building-up process, and cost is very high.Batch extracting rectified technological operation is flexible, and cost of equipment is low, can realize the separation of acetonitrile, toluene and the recovery of extraction agent in a batch fractionating tower, but interim fraction is many, and energy consumption is very big, and products obtained therefrom purity is not high.Continuous extraction rectification process products obtained therefrom purity height, energy consumption is relatively low, but the facility investment height.
Summary of the invention
The object of the present invention is to provide a kind of energy-conservation, equipment to drop into low acetonitrile-methylbenzene azeotropic mixture separation processes.
A kind of method of utilizing dividing wall rectifying tower extracting rectifying separating acetonitrile-toluene, it is characterized in that the device that adopts is the rectifying tower that has dividing wall, be one dividing wall to be installed in the vertical direction of common rectifying tower, tower is divided into four parts, wherein the I zone is the extracting rectifying district, main body is installed tower tray and filler, one sealing plate is arranged between II and the III zone, how many positions of sealing plate can adjusting by tower tray or filler, the II zone is the extraction agent recovery zone, the III zone is not added and is adorned any tower tray or filler, and the IV zone is the public stripping section in I zone and II zone; The method of separating acetonitrile-toluene is: be lower than or the acetonitrile-methylbenzene mixture formed near azeotropic and extraction agent enter the regional extracting rectifying of I district from opening for feed separately respectively, under normal pressure, operate, acetonitrile-methylbenzene mixture feeding temperature is 50～80 ℃, the extractant feed temperature is 80～100 ℃, I zone tower top temperature is controlled at 80～83 ℃, and high-purity acetonitrile product is from the cat head extraction of I zone; II zone head temperature is controlled at 109～111 ℃, and the toluene product is from II zone top extraction; Extraction agent extraction at the bottom of the tower recycles after heat exchange, and extraction agent is controlled at 0.5～3.0 with acetonitrile-methylbenzene mixture quality ratio, I zone control of reflux ratio at 0.5～3, the II zone control of reflux ratio 0.5～5.
Extraction agent of the present invention is selected from a kind of in propyl benzene, n-butyl benzene, Isobuytel Benzene, sec-butylbenzene, tert.-butylbenzene, p-diethylbenzene, p-tert-butyltoluene or the durol (1), preferred durol.Durol is one of component that content is the highest in the reformation C10 heavy aromatics, is crucial fine chemical material, obtains high-purity durol product by Crystallization Separation, with respect to other extraction agent, and low price and good separating effect.
Compare with traditional continuous extraction rectification process, the dividing wall rectifying tower is thermally coupled to extractive distillation column and extraction agent recovery tower together, reduces the energy expenditure that back-mixing caused owing to toluene, and only needs a tower and a reboiler, reduces facility investment.
Advantage of the present invention be adopt be easy to get, cheaply, efficient extracting agent, isolate high-purity acetonitrile and toluene product by the dividing wall extracting rectifying, adopt this method, the more conventional continuous extraction rectifying of facility investment and energy consumption reduces more than 20%.
Description of drawings
Fig. 1 is apparatus of the present invention and schematic flow sheet.The 1-condenser, 2-sealing plate, 3-condenser, 4-dividing wall, 5-dividing wall rectifying tower, 6-reboiler, a-acetonitrile-methylbenzene incoming flow thigh, b-extractant feed stream thigh, c-acetonitrile product flow thigh, d-toluene product flow thigh.
Fig. 2 is traditional extracting rectifying schematic flow sheet.The 7-extractive distillation column, 8-solvent recovery tower, a-acetonitrile-methylbenzene incoming flow thigh, b-extractant feed stream thigh, c-acetonitrile product flow thigh, d-toluene product flow thigh.
Embodiment
Further specify effect of the present invention with embodiment below, the extraction agent that is adopted in embodiment and the Comparative Examples there is no particular requirement, is the commercially available prod.The solvent ratio of the following stated is the mass ratio of extraction agent and acetonitrile-methylbenzene mixture.
Embodiment 1:
Raw material (mass ratio: acetonitrile 80%, toluene 20%), extraction agent durol (99.9m%)
As shown in Figure 1,50 theoretical stages in I zone, 30 theoretical stages in II zone, 10 theoretical stages in IV zone, raw material enters dividing wall rectifying tower I zone after heating, and feed entrance point is the 30th theoretical stage, the extraction agent durol enters the 6th theoretical stage after heating, high-purity acetonitrile is from the cat head extraction of I zone, and toluene is from II zone top extraction, and extraction agent extraction at the bottom of the tower recycles.
Operational condition is as follows:
Pressure: 0.1MPa
I zone reflux ratio: 1.5: 1
II zone reflux ratio: 2: 1
Solvent ratio: 1: 1
Acetonitrile toluene feed temperature: 60 ℃
Durol feeding temperature: 90 ℃
The overhead product stratographic analysis shows: by mass: acetonitrile is 99.0% in the cat head acetonitrile product, and toluene is 1.0%; Toluene is 95.9% in the toluene product, and acetonitrile is 4.1%; Durol is 99.9% in the bottom product, and toluene is 0.1%.
Comparative Examples 1:
Raw material (mass ratio: acetonitrile 80%, toluene 20%), extraction agent durol (99.9m%)
The operating parameters of Comparative Examples 1 and the extraction agent that is adopted are identical with embodiment 1, but adopt the traditional extraction rectification process, as shown in Figure 2,60 theoretical stages of extractive distillation column, 40 theoretical stages of solvent recovery tower, raw material enters extractive distillation column after heating, feed entrance point is the 30th theoretical stage, and the extraction agent n-butyl benzene enters the 6th theoretical stage after heating, and high-purity acetonitrile is from the extraction of extracting rectifying column overhead, toluene is from the extraction of solvent recuperation column overhead, and extraction agent extraction at the bottom of the tower recycles.
Operational condition is as follows:
Extractive distillation column
Pressure: 0.1MPa
Reflux ratio: 1.5: 1
Solvent ratio: 1: 1
Acetonitrile toluene feed temperature: 60 ℃
Durol feeding temperature: 90 ℃
Solvent recovery tower
Pressure: 0.1MPa
Reflux ratio: 2: 1
The overhead product stratographic analysis shows: by mass: acetonitrile is 98.7% in the cat head acetonitrile product, and toluene is 1.2%, and durol is 0.1%; Toluene is 94.6% in the toluene product, and acetonitrile is 5.4%; Durol is 99.9% at the bottom of the tower, and toluene is 0.1%.
Comparative Examples 1 is compared with embodiment 1, products obtained therefrom purity is lower than the result of embodiment 1, and energy consumption is high 8.4 percentage points, from Comparative Examples 1 as can be seen, the more traditional extraction rectification technique of dividing wall extraction rectification technique is saved energy consumption, if reach the purity of embodiment 1, will increase solvent ratio, energy consumption will be bigger.
Embodiment 2:
Raw material (mass ratio: acetonitrile 80%, toluene 20%), extraction agent is propyl benzene (99.9m%)
As shown in Figure 1,50 theoretical stages in I zone, 30 theoretical stages in II zone, 10 theoretical stages in IV zone, raw material enters dividing wall rectifying tower I zone after heating, and feed entrance point is the 30th theoretical stage, the extraction agent propyl benzene enters the 6th theoretical stage after heating, high-purity acetonitrile is from the cat head extraction of I zone, and toluene is from II zone top extraction, and extraction agent extraction at the bottom of the tower recycles.
Operational condition is as follows:
Pressure: 0.1MPa
I zone reflux ratio: 3: 1
II zone reflux ratio: 5: 1
Solvent ratio: 3: 1
Acetonitrile toluene feed temperature: 50 ℃
Propyl benzene feeding temperature: 80 ℃
The overhead product stratographic analysis shows: by mass: acetonitrile is 95.3% in the cat head acetonitrile product, and propyl benzene is 4.7%; Toluene is 81.4% in the toluene product, and acetonitrile is 18.6%; Propyl benzene is 98.8% at the bottom of the tower, and toluene is 1.2%.
Comparative Examples 2:
Raw material (mass ratio: acetonitrile 80%, toluene 20%), extraction agent is propyl benzene (99.9m%)
The operating parameters of Comparative Examples 2 and the extraction agent that is adopted are identical with embodiment 2, but adopt the traditional extraction rectification process, as shown in Figure 2,60 theoretical stages of extractive distillation column, 40 theoretical stages of solvent recovery tower, raw material enters extractive distillation column after heating, feed entrance point is the 30th theoretical stage, and the extraction agent propyl benzene enters the 6th theoretical stage after heating, and high-purity acetonitrile is from the extraction of extracting rectifying column overhead, toluene is from the extraction of solvent recuperation column overhead, and extraction agent extraction at the bottom of the tower recycles.
Operational condition is as follows:
Extractive distillation column
Pressure: 0.1MPa
Reflux ratio: 3: 1
Solvent ratio: 3: 1
Acetonitrile toluene feed temperature: 50 ℃
Durol feeding temperature: 80 ℃
Solvent recovery tower
Pressure: 0.1MPa
Reflux ratio: 5: 1
The overhead product stratographic analysis shows: by mass: acetonitrile is 94.0% in the cat head acetonitrile product, and propyl benzene is 6.0%; Toluene is 76.2% in the toluene product, and acetonitrile is 23.8%; Propyl benzene is 98.4% at the bottom of the tower, and toluene is 1.6%.
Comparative Examples 2 is compared with embodiment 2, and products obtained therefrom purity is lower than the result of embodiment 2, and energy consumption is high 8.2 percentage points, and from Comparative Examples 2 and embodiment 2 as can be seen, the more traditional extraction rectification technique of dividing wall extraction rectification technique is saved energy consumption.
Embodiment 3:
Raw material (mass ratio: acetonitrile 50%, toluene 50%), extraction agent durol (99.9m%)
As shown in Figure 1,40 theoretical stages in I zone, 20 theoretical stages in II zone, 10 theoretical stages in IV zone, raw material enters dividing wall rectifying tower I zone after heating, and feed entrance point is the 25th theoretical stage, the extraction agent durol enters the 5th theoretical stage after heating, high-purity acetonitrile is from the cat head extraction of I zone, and toluene is from II zone top extraction, and extraction agent extraction at the bottom of the tower recycles.
Operational condition is as follows:
Pressure: 0.1MPa
I zone reflux ratio: 0.5: 1
II zone reflux ratio: 0.6: 1
Solvent ratio: 0.8: 1
Acetonitrile toluene feed temperature: 60 ℃
Durol feeding temperature: 90 ℃
The overhead product stratographic analysis shows: by mass: acetonitrile is 99.5% in the cat head acetonitrile product, and durol is 0.5%; Toluene is 99.5% in the toluene product, and acetonitrile is 0.5%; Durol is 99.7% in the bottom product, and toluene is 0.3%.
Comparative Examples 3:
Raw material (mass ratio: acetonitrile 50%, toluene 50%), extraction agent is durol (99.9m%)
Comparative Examples 3 adopts the traditional extraction rectification process, as shown in Figure 2,50 theoretical stages of extractive distillation column, 30 theoretical stages of solvent recovery tower, raw material enters extractive distillation column after heating, and feed entrance point is the 25th theoretical stage, the extraction agent propyl benzene enters the 5th theoretical stage after heating, high-purity acetonitrile is from the extraction of extracting rectifying column overhead, and toluene is from the extraction of solvent recuperation column overhead, and extraction agent extraction at the bottom of the tower recycles.
Operational condition is as follows:
Extractive distillation column
Pressure: 0.1MPa
Reflux ratio: 0.5: 1
Solvent ratio: 0.8: 1
Acetonitrile toluene feed temperature: 60 ℃
Durol feeding temperature: 90 ℃
Solvent recovery tower
Pressure: 0.1MPa
Reflux ratio: 0.6: 1
The overhead product stratographic analysis shows: by mass: acetonitrile is 99.4% in the cat head acetonitrile product, and durol is 0.6%; Toluene is 99.5% in the toluene product, and acetonitrile is 0.5%; Durol is 99.6% in the bottom product, and toluene is 0.4%.
Comparative Examples 3 is compared with embodiment 3, and products obtained therefrom purity is lower than the result of embodiment 3, but energy consumption is high 14.2 percentage points, and from above two examples as can be seen, the more traditional extraction rectification technique of dividing wall extraction rectification technique is saved energy consumption.
Embodiment 4:
With the n-butyl benzene is extraction agent, and technology and parameter are consistent with embodiment 1.
The overhead product stratographic analysis shows: by mass: acetonitrile is 98.7% in the cat head acetonitrile product, and toluene is 1.1%, and durol is 0.2%; Toluene is 94.7% in the toluene product, and acetonitrile is 5.3%; Durol is 99.8% in the bottom product, and toluene is 0.2%.
Embodiment 5:
Raw material (mass ratio: acetonitrile 50%, toluene 50%), extraction agent tert.-butylbenzene (99.9m%)
As shown in Figure 1,40 theoretical stages in I zone, 20 theoretical stages in II zone, 10 theoretical stages in IV zone, raw material enters dividing wall rectifying tower I zone after heating, and feed entrance point is the 25th theoretical stage, the extraction agent tert.-butylbenzene enters the 5th theoretical stage after heating, high-purity acetonitrile is from the cat head extraction of I zone, and toluene is from II zone top extraction, and extraction agent extraction at the bottom of the tower recycles.
Operational condition is as follows:
Pressure: 0.1MPa
I zone reflux ratio: 1: 1
II zone reflux ratio: 0.6: 1
Solvent ratio: 0.8: 1
Acetonitrile toluene feed temperature: 60 ℃
Durol feeding temperature: 90 ℃
The overhead product stratographic analysis shows: by mass: acetonitrile is 97.8% in the cat head acetonitrile product, and toluene is 0.1%, and tert.-butylbenzene is 2.1%; Toluene is 97.8% in the toluene product, and acetonitrile is 2.2%; Tert.-butylbenzene is 98.7% in the bottom product, and toluene is 1.3%.
Claims (3)
1. method of utilizing dividing wall rectifying tower extracting rectifying separating acetonitrile-toluene, it is characterized in that the device that adopts is the rectifying tower that has dividing wall, promptly one dividing wall is installed in the vertical direction of common rectifying tower, tower is divided into four parts, wherein the I zone is the extracting rectifying district, main body is installed tower tray and filler, one sealing plate is arranged between II and the III zone, how many positions of sealing plate can adjusting by tower tray or filler, the II zone is the extraction agent recovery zone, the III zone is not added and is adorned any tower tray or filler, and the IV zone is the public stripping section in I zone and II zone; The method of separating acetonitrile-toluene is: be lower than or the acetonitrile-methylbenzene mixture formed near azeotropic and extraction agent enter the regional extracting rectifying of I district from opening for feed separately respectively, under normal pressure, operate, acetonitrile-methylbenzene mixture feeding temperature is 50～80 ℃, the extractant feed temperature is 80～100 ℃, I zone tower top temperature is controlled at 80～83 ℃, and high-purity acetonitrile product is from the cat head extraction of I zone; II zone head temperature is controlled at 109～111 ℃, and the toluene product is from II zone top extraction; Extraction agent extraction at the bottom of the tower recycles after heat exchange, and extraction agent is controlled at 0.5～3.0 with acetonitrile-methylbenzene mixture quality ratio, I zone control of reflux ratio at 0.5～3, the II zone control of reflux ratio 0.5～5.
2. the method for extracting rectifying separating acetonitrile-toluene as claimed in claim 1 is characterized in that the extraction agent that is adopted is selected from a kind of in propyl benzene, n-butyl benzene, Isobuytel Benzene, sec-butylbenzene, tert.-butylbenzene, p-diethylbenzene, p-tert-butyltoluene, the durol.
3. the method for extracting rectifying separating acetonitrile-toluene as claimed in claim 1 or 2 is characterized in that the extraction agent that is adopted is a durol.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102432460A (en) * | 2011-10-12 | 2012-05-02 | 潍坊市元利化工有限公司 | Method for purifying diacid dimethyl esters by plate distillation separation |
| CN105001055A (en) * | 2015-07-17 | 2015-10-28 | 济南大学 | Isopropanol-acetonitrile azeotrope rectification separation method based on mixed solvent as extracting agent |
| CN109320431A (en) * | 2018-10-24 | 2019-02-12 | 福建师范大学福清分校 | A method of N-METHYLFORMAMIDE and diethylene glycol monomethyl ether in recycling paint stripper waste liquid |
| CN109663379A (en) * | 2017-10-13 | 2019-04-23 | 抚顺伊科思新材料有限公司 | A kind of energy conservation acetonitrile method cracking c_5 separation method |
| CN111362831A (en) * | 2020-04-25 | 2020-07-03 | 青岛科技大学 | Heterogeneous batch rectification separation process of cyclohexane-acetonitrile-toluene azeotrope |
| CN113461568A (en) * | 2021-06-24 | 2021-10-01 | 索闻特环保科技(上海)有限公司 | Method for treating toluene in acetonitrile waste liquid |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1736530A (en) * | 2005-07-26 | 2006-02-22 | 天津大学 | Method for separating acetonitrile-methylbenzene azeotropic mixture by continuous extractive distillation |
| CN1736529A (en) * | 2005-07-26 | 2006-02-22 | 天津大学 | Batch extractive distillation separating method of acetonitrile-methylbenzene azeotropic mixtrue |
-
2009
- 2009-03-13 CN CN 200910079963 patent/CN101830830B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1736530A (en) * | 2005-07-26 | 2006-02-22 | 天津大学 | Method for separating acetonitrile-methylbenzene azeotropic mixture by continuous extractive distillation |
| CN1736529A (en) * | 2005-07-26 | 2006-02-22 | 天津大学 | Batch extractive distillation separating method of acetonitrile-methylbenzene azeotropic mixtrue |
Non-Patent Citations (1)
| Title |
|---|
| 崔现宝等: "间歇萃取精馏分离乙腈-甲苯共沸体系", 《化学工业与工程》 * |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102432460A (en) * | 2011-10-12 | 2012-05-02 | 潍坊市元利化工有限公司 | Method for purifying diacid dimethyl esters by plate distillation separation |
| CN102432460B (en) * | 2011-10-12 | 2014-01-08 | 山东元利科技股份有限公司 | Method for purifying diacid dimethyl esters by plate distillation separation |
| CN105001055A (en) * | 2015-07-17 | 2015-10-28 | 济南大学 | Isopropanol-acetonitrile azeotrope rectification separation method based on mixed solvent as extracting agent |
| CN109663379A (en) * | 2017-10-13 | 2019-04-23 | 抚顺伊科思新材料有限公司 | A kind of energy conservation acetonitrile method cracking c_5 separation method |
| CN109320431A (en) * | 2018-10-24 | 2019-02-12 | 福建师范大学福清分校 | A method of N-METHYLFORMAMIDE and diethylene glycol monomethyl ether in recycling paint stripper waste liquid |
| CN111362831A (en) * | 2020-04-25 | 2020-07-03 | 青岛科技大学 | Heterogeneous batch rectification separation process of cyclohexane-acetonitrile-toluene azeotrope |
| CN111362831B (en) * | 2020-04-25 | 2022-06-28 | 青岛科技大学 | Heterogeneous batch rectification separation process of cyclohexane-acetonitrile-toluene azeotrope |
| CN113461568A (en) * | 2021-06-24 | 2021-10-01 | 索闻特环保科技(上海)有限公司 | Method for treating toluene in acetonitrile waste liquid |
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