CN1035661A - The novel method that vinyl cyanide and acetonitrile reclaim - Google Patents
The novel method that vinyl cyanide and acetonitrile reclaim Download PDFInfo
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- CN1035661A CN1035661A CN 88105488 CN88105488A CN1035661A CN 1035661 A CN1035661 A CN 1035661A CN 88105488 CN88105488 CN 88105488 CN 88105488 A CN88105488 A CN 88105488A CN 1035661 A CN1035661 A CN 1035661A
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Abstract
The present invention has narrated a kind of novel method of recover acrylonitrile and acetonitrile in the aqueous solution that is obtained in the ammoxidating propylene to prepare acrylonitrile process, contain vinyl cyanide, prussic acid, acetonitrile and carbonyl compound etc. in this aqueous solution, employing be the technology that compound extracting desorb-conventional distillation combines with extracting rectifying.Cat head injects phegma, and aqueous solvent is sent into from several column plates below the cat head.In the crude acetonitrile that cat head obtains, ethane nitrile content is less than 100PPM.Acetonitrile is drawn with liquid state from side line, and wherein prussic acid content is 20-100PPM.Adopt the present invention that the purification schemes of acetonitrile is simplified, and significantly reduce the distillatory energy consumption.
Description
The invention belongs to the method for recover acrylonitrile and acetonitrile from the water absorption liquid that contains vinyl cyanide, prussic acid, acetonitrile and carbonyl compound.
The technology of production and recover acrylonitrile and acetonitrile is well-known.Report was once being arranged abroad aspect the vinyl cyanide separation and purification.For example United States Patent (USP) 4,377,444, introduced the isolating two kinds of typical process of vinyl cyanide and acetonitrile, a kind ofly form " flow process 1 " (see figure 1) by extraction desorption tower and acetonitrile desorption tower; Another kind is the mode of extracting acetonitrile with the gas phase side line out, extracting " flow process 2 " (see figure 2) that desorption tower and acetonitrile desorption tower are integrated.
Now two kinds of flow processs are summarized as follows respectively:
By shown in Figure 1, send into extraction desorption tower (1) from the water absorption liquid that contains vinyl cyanide, prussic acid, acetonitrile and carbonyl compound etc. of bottom, absorption tower, aqueous solvent adds from cat head, carry out extractive distillation, cat head steams crude acetonitrile and the prussic acid that contains acetonitrile hardly, through being condensate in oil-water separation tank (2), carry out liquid-liquid separation, form organic phase and water.Water is sent extraction desorption tower (1) back to and is done charging, and organic phase (crude acetonitrile) send the vinyl cyanide refining system to be for further processing.The still liquid that does not contain vinyl cyanide send acetonitrile desorption tower (3), steams the crude acetonitrile that contains a certain amount of prussic acid from cat head, refluxes and return cat head, rest part discharging in the condensation rear section.The tower still material that contains the heavy component all enters process tank (4) from the bottom tray of acetonitrile desorption tower (3), send circulation from middle storage tank (4) and absorb water and aqueous solvent, the remaining reboiler (5) of sending into, partly vaporization in reboiler is sent sewage disposal by the heavy component raffinate of enrichment by the discharge of tower still.
Fig. 2 is similar substantially to vinyl cyanide recovery process shown in Figure 1.Contain the water absorption liquid of vinyl cyanide, prussic acid, acetonitrile and carbonyl compound etc. from the absorption tower, send into the position on the upper side, add aqueous solvent, carry out extractive distillation from cat head from the middle part of extraction desorption tower (1).Cat head steams crude acetonitrile, the prussic acid that contains acetonitrile hardly, after condensation, in oil-water separation tank (2), carry out liquid-liquid separation, form organic phase and water, water returns extraction desorption tower (1) and does charging, and organic phase (crude acetonitrile) send the vinyl cyanide refining system to be for further processing.The characteristics of flow process 2 are from position on the lower side, extraction desorption tower (1) middle part, the gas phase side line is extracted the acetonitrile that contains a certain amount of prussic acid out, directly send into acetonitrile stripping tower (3), make acetonitrile, prussic acid and carbonyl compound be carried dense at the epimere of tower (3), the crude acetonitrile that steams from cat head, after condensation, partly reflux and return stripping tower (3) cat head, all the other partly send acetonitrile to reclaim refining system and are for further processing.Extracting out on the identical column plate in position from liquid stream at the bottom of the tower of stripping tower (3), returning extraction desorption tower (1).The dirty liquid of extraction desorption tower (1) is all discharged from bottom tray (first block of plate), send into process tank (4), return be equivalent to absorb the required Total Water circulation of water and aqueous solvent to absorption tower and extraction desorption tower cat head from middle storage tank (4), partly remaining, deliver to reboiler (5), partly vaporization in reboiler (5) is sent sewage disposal by the heavy component raffinate of enrichment by the discharge of tower still.
Above-mentioned two kinds of typical flow exist following shortcoming:
As " flow process 1 ", in the discharging of extraction desorb Tata still, a part of prussic acid and acetonitrile are emitted together, cause containing in the crude acetonitrile prussic acid of 500PPM, this has not only influenced the dense and further recovery of proposing of acetonitrile desorption tower cat head acetonitrile, and be easy to cause polymerization to stop up, influence the running period of equipment.In addition, because the rare acetonitrile liquid stream that contains big water gaging that extraction desorb Tata still is discharged during the desorb acetonitrile, need expend a large amount of heat energy.
As " flow process 2 ",, reduced acetonitrile desorb energy consumption partly to a certain extent owing to adopt the gas phase side line to extract acetonitrile technology out.But in the crude acetonitrile that the stripping tower cat head steams, still contain 5% prussic acid (in acetonitrile), also influenced acetonitrile and further reclaimed and carry dense.
The objective of the invention is to propose a kind of method that adds water extractive distillation at certain position, can change the distribution rule of prussic acid in the former extraction desorption technique, and be equipped with in stripping section acetonitrile enrichment district, the liquid phase side line is extracted acetonitrile technology out, can reduce the content of prussic acid in the acetonitrile effectively, thereby can save the purpose of dehydrogenation cyanic acid tower in the acetonitrile refining, and reduce the energy consumption of acetonitrile desorb, the flow process of acetonitrile removal process is simplified.
Specifically, on former extraction desorption tower rectifying section, add the combination tower of the preceding paragraph conventional distillation section, be called " compound extracting desorption tower ".Be exactly to add aqueous solvent in the position on the upper side from the rectifying section middle part, be equivalent to conventional distillation and " compound " technology of combining of extraction desorb, utilize both additions, changed the distribution rule of prussic acid in the former extraction desorption technique, steamed the crude acetonitrile of content less than 100PPM acetonitrile, most prussic acid and part water from compound extracting desorption tower cat head.And be equipped with at the middle part of tower position on the lower side, the liquid phase side line is extracted acetonitrile liquid stream out, wherein ethane nitrile content be the absorption liquid ethane nitrile content 2-4 doubly, prussic acid content is 20-100PPM, through the acetonitrile desorb, steam the crude acetonitrile that content is 60-84% from acetonitrile desorption tower cat head, wherein the content of prussic acid is less than 0.8%.
New technological process of the present invention (flow process 3) is shown in figure three:
From the water absorption liquid that contains vinyl cyanide, prussic acid, acetonitrile and carbonyl compound etc. on absorption tower, from having 65-125 piece column plate, the best is sent into the position on the upper side for the middle part of the compound extracting desorption tower (1) of 90-110 piece column plate.Aqueous solvent is from distance cat head 4-16 piece column plate, best for adding on the 6-12 piece column plate, the compound extracting desorption tower is divided into the conventional distillation section and the extracting rectifying section is carried out the compound extracting desorb, steam the crude acetonitrile of content from cat head less than 100PPM acetonitrile, most prussic acid and part water, after the condensation, carry out liquid-liquid separation at oil-water separation tank (2), form organic phase and water, the water that contains the saturation capacity vinyl cyanide returns compound extracting desorption tower (1) and does charging, organic phase (crude acetonitrile) partly refluxes and returns cat head, and rest part send refining system to handle.Simultaneously, 20-40 piece column plate on compound extracting desorb Tata still, the best is that the side line mouth of 25-35 piece column plate is extracted acetonitrile liquid stream out, wherein ethane nitrile content be the absorption liquid ethane nitrile content 2-4 doubly, prussic acid content is 20-100PPM, directly send acetonitrile desorption tower (3) with it, reclaims and carries dense acetonitrile.The material that compound extracting desorb Tata still contains the heavy component all enters process tank (4) from bottom tray, send required absorption water of circulation and part aqueous solvent from middle storage tank (4), the remaining reboiler (5) of partly sending into, partly vaporization in reboiler is sent sewage disposal by the heavy component raffinate of enrichment by the discharge of tower still.
Acetonitrile desorption tower (3) is a common rectifying tower, side line acetonitrile liquid stream from compound extracting desorption tower (1), send into the position on the upper side from the middle part of tower, steam the crude acetonitrile that content is 60-84% from cat head, concentration the best is 80%, and wherein the content of prussic acid is less than 0.8%, after the condensation, partly reflux and return cat head, all the other partly send acetonitrile to reclaim refining system and handle.Tower still material is all made the part aqueous solvent that aqueous solvent and process tank (4) send and is merged, and sends into compound extracting desorption tower (1) from distance cat head 4-16 piece column plate.
Compound extracting desorption tower and acetonitrile desorption tower can adopt sieve-tray tower, packing tower or valve tray column.
The novel method that vinyl cyanide provided by the present invention and acetonitrile reclaim, its operational condition is as follows:
The pressure of compound extracting desorption tower (1) is normal pressure, pushes up warm 65-67 ℃, 100-102 ℃ of still temperature, and it is 90-92 ℃ that the liquid phase side line is extracted a mouthful temperature out; The pressure of acetonitrile desorption tower (3) is normal pressure, and the top temperature is 75-77 ℃, 100-102 ℃ of still temperature.
In a word, the novel method that vinyl cyanide of the present invention and acetonitrile reclaim can reclaim the vinyl cyanide that contains on absorption tower cost-effectively.The water absorption liquid of prussic acid, acetonitrile and carbonyl compound etc.Test shows that the compound extracting desorption tower utilizes conventional distillation and the addition of extraction desorb to separation of hydrogen cyanic acid, can not produce significantly influence to separating of vinyl cyanide and acetonitrile, but can change the distribution rule of prussic acid.Under conditions such as the solvent water yield that does not change former extraction desorption tower technology, reflux ratio, only increase the conventional distillation section of 4-16 piece column plate, acetonitrile still can be less than the requirement of 100PPM in the crude acetonitrile that cat head steams.If adopt flow process 1 or 2 extraction desorption techniques, the content of the prussic acid in the acetonitrile is up to 500PPM, and employing compound extracting desorption tower and liquid phase side line are extracted acetonitrile technology out, and prussic acid content can be reduced to 20-100PPM.Make acetonitrile simplify the separation of prussic acid in reclaiming, prolonged condenser running period, reduce the facility investment expense, can improve acetonitrile concentration again, reduce the required energy consumption of acetonitrile desorb.
[example one]
The vinyl cyanide water absorption liquid that contains vinyl cyanide 3.4%, prussic acid 0.4%, acetonitrile 0.2%, other impurity 0.1% and big water gaging, sending into internal diameter with the flow of 12000ml/hr is the compound extracting desorption tower that 57mm is filled with 85 blocks of column plates, aqueous solvent is with the flow of 6000ml/hr, add from the 5th block of column plate of distance cat head, its operational condition is a normal pressure, the top temperature is 67 ℃, and the still temperature is to carry out the compound extracting desorb under 101 ℃.And on the 20th block of column plate of distance tower still with the flow of 4000ml/hr, the liquid phase side line is extracted a mouthful temperature out when being 91 ℃, extracts the liquid phase side line out acetonitrile, directly is sent to the acetonitrile desorption tower and reclaims acetonitrile, its operational condition is a normal pressure, the top temperature is 76 ℃, the still temperature is 101 ℃.
Test-results, from the crude acetonitrile that compound extracting desorption tower cat head steams, ethane nitrile content is less than 100PPM, acrylonitrile content 75%, prussic acid content 11%.Vinyl cyanide, ethane nitrile content are all less than 20PPM in the still liquid.The liquid phase side line is extracted a mouthful ethane nitrile content 0.6%, prussic acid content 60PPM out.
From the crude acetonitrile that acetonitrile desorption tower cat head steams, ethane nitrile content 80%, prussic acid content 0.7%.
[example two]
The vinyl cyanide water absorption liquid that contains vinyl cyanide 3.4%, prussic acid 0.4%, acetonitrile 0.2%, other impurity 0.1% and big water gaging, sending into internal diameter with the flow of 12000ml/hr is the compound extracting desorption tower that 57mm is filled with 125 blocks of plates, aqueous solvent is with the flow of 6000ml/hr, add from the 15th block of column plate of distance cat head, carry out the compound extracting desorb.With the flow of 6000ml/hr, the liquid phase side line is extracted acetonitrile out on the 40th block of column plate of distance tower still, directly is sent to the acetonitrile desorption tower and reclaims acetonitrile.Operational condition is with example 1.
Test-results, from the crude acetonitrile that compound extracting desorption tower cat head steams, ethane nitrile content is less than 100PPM, acrylonitrile content 75%, prussic acid content 11%, vinyl cyanide, ethane nitrile content are less than 20PPM in the still liquid, the liquid phase side line is extracted a mouthful ethane nitrile content 0.4%, prussic acid content 40PPM out.
From the crude acetonitrile that acetonitrile desorption tower cat head steams, ethane nitrile content 80%, prussic acid content 0.7%.
[example three]
The vinyl cyanide water absorption liquid that contains vinyl cyanide 4.7%, prussic acid 0.7%, acetonitrile 0.2% and big water gaging, under similar process conditions, acetonitrile recovery to " flow process 1 ", " flow process 2 " and " flow process 3 " provided by the invention is partly tested, and the results are shown in following table.
| | Flow process | 1 | Flow process 2 | |
|
| Crude acetonitrile is formed (wt%) | ACN | 20 | 50 | 80 | |
| |
4 | 2－2.5 | 0.8 | ||
| Reclaim one kilogram of acetonitrile thermal losses (Kcal/ kilogram ACN) | 48790 | 9303 | 5750 | ||
From the data shown in the table, the method that adopts " flow process 3 " acrylonitrile provided by the invention and acetonitrile to reclaim, can reach the requirement (ethane nitrile content 80% of acetonitrile refining Central Plains dehydrogenation cyanic acid tower isolation technics index, hydrogen cyanide content 0.8%), thereby can save in the past required dehydrogenation cyanic acid tower in the acetonitrile refining flow process, not only saved investment, simplified technology, and can cut down the consumption of energy significantly.
Claims (5)
1, a kind of water absorption liquid that contains vinyl cyanide, prussic acid, acetonitrile and carbonyl compound that from the process of ammoxidating propylene to prepare acrylonitrile, is obtained, by top Jia Shui, the extraction desorption tower, the method of acetonitrile desorption tower recover acrylonitrile and acetonitrile, it is characterized in that solution water adds from distance cat head 4-16 piece column plate, compound extracting desorption tower with 65-125 piece column plate is divided into conventional distillation section and extracting rectifying section with tower, carries out the compound extracting desorb.Steam the acetonitrile of content from cat head less than 100PPM, the crude acetonitrile of most of prussic acid and part water, send refining system to handle, extracting out partly mutually from tower bottoms, the circulation of material do absorbs water and aqueous solvent, the still raffinate that contains the heavy component send sink drainage to handle, 20-40 piece column plate place on compound extracting desorb Tata still simultaneously, the liquid phase side line is extracted acetonitrile liquid stream out, wherein ethane nitrile content be the absorption liquid ethane nitrile content 2-4 doubly, prussic acid content is 20-100PPM, it is sent to the acetonitrile desorption tower, steam the crude acetonitrile that content is 60-84% from cat head, wherein the content of prussic acid send refining system to handle it less than 0.8%, extract tower bottoms out and do the solvent water circulation use, send into the compound extracting desorption tower.
2,, it is characterized in that aqueous solvent is incorporated as the best from distance cat head 6-12 piece column plate according to the method for described recover acrylonitrile of claim 1 and acetonitrile.
3,, it is characterized in that it is best that the liquid phase side line is extracted acetonitrile liquid stream 25-35 piece place on the tower still out according to the method for described recover acrylonitrile of claim 1 and acetonitrile.
4, according to the method for described recover acrylonitrile of claim 1 and acetonitrile, the best stage number that it is characterized in that the compound extracting desorption tower is the 90-110 piece.
5, according to the method for described recover acrylonitrile of claim 1 and acetonitrile, it is characterized in that the crude acetonitrile that acetonitrile desorption tower cat head steams, its concentration the best is 80%(weight %).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88105488 CN1014888B (en) | 1988-03-10 | 1988-03-10 | Recovery technique of acrylonitrile and acetonitrile |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88105488 CN1014888B (en) | 1988-03-10 | 1988-03-10 | Recovery technique of acrylonitrile and acetonitrile |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1035661A true CN1035661A (en) | 1989-09-20 |
| CN1014888B CN1014888B (en) | 1991-11-27 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 88105488 Expired CN1014888B (en) | 1988-03-10 | 1988-03-10 | Recovery technique of acrylonitrile and acetonitrile |
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| Country | Link |
|---|---|
| CN (1) | CN1014888B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1098836C (en) * | 1999-03-30 | 2003-01-15 | 中国石油化工总公司 | Decompression side stream gas-phase productions of finished product acrylonitrile |
| CN104667556A (en) * | 2015-01-22 | 2015-06-03 | 宜兴市阳洋塑料助剂有限公司 | Rectification equipment for producing plasticizer |
| CN105367449A (en) * | 2014-08-27 | 2016-03-02 | 中国石油化工股份有限公司 | Method for absorbing acrylonitrile |
| CN106892843A (en) * | 2015-12-17 | 2017-06-27 | 英尼奥斯欧洲股份公司 | Recovery tower is controlled |
| CN106892842A (en) * | 2015-12-17 | 2017-06-27 | 英尼奥斯欧洲股份公司 | Recovery tower |
| CN106892838A (en) * | 2015-12-17 | 2017-06-27 | 英尼奥斯欧洲股份公司 | Recovery tower is controlled |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1298405C (en) * | 2005-07-26 | 2007-02-07 | 天津大学 | Method for separating acetonitrile-methylbenzene azeotropic mixture by continuous extractive distillation |
-
1988
- 1988-03-10 CN CN 88105488 patent/CN1014888B/en not_active Expired
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1098836C (en) * | 1999-03-30 | 2003-01-15 | 中国石油化工总公司 | Decompression side stream gas-phase productions of finished product acrylonitrile |
| CN105367449A (en) * | 2014-08-27 | 2016-03-02 | 中国石油化工股份有限公司 | Method for absorbing acrylonitrile |
| CN105367449B (en) * | 2014-08-27 | 2018-01-09 | 中国石油化工股份有限公司 | Absorb the method for acrylonitrile |
| CN104667556A (en) * | 2015-01-22 | 2015-06-03 | 宜兴市阳洋塑料助剂有限公司 | Rectification equipment for producing plasticizer |
| CN106892843A (en) * | 2015-12-17 | 2017-06-27 | 英尼奥斯欧洲股份公司 | Recovery tower is controlled |
| CN106892842A (en) * | 2015-12-17 | 2017-06-27 | 英尼奥斯欧洲股份公司 | Recovery tower |
| CN106892838A (en) * | 2015-12-17 | 2017-06-27 | 英尼奥斯欧洲股份公司 | Recovery tower is controlled |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1014888B (en) | 1991-11-27 |
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