CN103086930A - Method for extracting 2-acrylamide-2-methylpropanesulfonic acid from recrystallization filtrate - Google Patents
Method for extracting 2-acrylamide-2-methylpropanesulfonic acid from recrystallization filtrate Download PDFInfo
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- CN103086930A CN103086930A CN2013100166464A CN201310016646A CN103086930A CN 103086930 A CN103086930 A CN 103086930A CN 2013100166464 A CN2013100166464 A CN 2013100166464A CN 201310016646 A CN201310016646 A CN 201310016646A CN 103086930 A CN103086930 A CN 103086930A
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- acrylamide
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Abstract
The invention discloses a method for extracting 2-acrylamide-2-methylpropanesulfonic acid from recrystallization filtrate. The method comprises the following steps of: adding the recrystallization filtrate into a distillation kettle for heating distillation; adding a stabilizing agent the weight of which is 0.001%-0.005% of that of the recrystallization filtrate into the distillation kettle, wherein the distillation temperature inside the distillation kettle is 55-70 DEG G, the vacuum degree inside the distillation kettle is not less than 0.08Mpa, and the distillation extraction ratio takes 55-65% of the weight of the recrystallization filtrate; and after the distillation is finished, reducing the temperature to 15-20 DEG C, centrifugating the resulting product, and drying the centrifugated product to obtain a 2-acrylamide-2-methylpropanesulfonic acid product. By virtue of the method provided by the invention, the 2-acrylamide-2-methylpropanesulfonic acid can be scientifically and reasonably recycled and extracted from the recrystallization filtrate, the obtained product is high in quality, the product loss is prevented, and the economical benefit is improved.
Description
Technical field
The recrystallization filtrate that the present invention relates to from the preparation of 2-acrylamide-2-methylpro panesulfonic acid reclaims the method for extracting the 2-acrylamide-2-methylpro panesulfonic acid.
Background technology
2-acrylamide-2-methylpro panesulfonic acid (being called for short AMPS) is a kind of vinyl monomer with sulfonic acid group, and its structural formula is:
Can find out from its structure, it contains strong anionic property, water miscible sulfonic acid group, and the amide group of shielding and unsaturated double-bond make it have good performance.Sulfonic acid group makes it have the dyeing affinity, electroconductibility, ion exchangeable and to the good tolerance of divalent cation; Amide group makes it that good stability to hydrolysis be arranged, and is antiacid, alkali resistant and thermostability; And active two keys make it have addition, polymerization.Therefore, the 2-acrylamide-2-methylpro panesulfonic acid has been widely used in weaving (spinning, dyeing), plastics, papermaking, coating, in the industrial production such as sewage disposal and oil production, produced the static inhibitor of excellent property, staining agent, dispersion agent, water-retaining agent, wadding is doubted agent, suds-stabilizing agent, speciality coating, Oilfield Chemicals etc. are a kind of organic compound that has development potentiality.
Interrupter method is adopted in the production of producing the 2-acrylamide-2-methylpro panesulfonic acid at present more, for generating the pulpous state product take vinyl cyanide and oleum as main raw material reacts, get crude product 2-acrylamide-2-methylpro panesulfonic acid after separating drying, then adopt recrystallizing technology that crude product 2-acrylamide-2-methylpro panesulfonic acid is dissolved in the aqueous acetic acid system and carry out recrystallizing and refining through operations such as centrifugations, finally obtain highly purified 2-acrylamide-2-methylpro panesulfonic acid finished product.This operational path raw material is easy to get, reaction conditions gentle, and the yield of product and quality are comparatively stable, so this route is adopted by numerous manufacturers.due to the reasons such as solvability of the limitation of recrystallizing technology and 2-acrylamide-2-methylpro panesulfonic acid product, in recrystallization filtrate in recrystallizing technology after centrifugation, because recrystallization filtrate is that crude product 2-acrylamide-2-methylpro panesulfonic acid is through the solvent after recrystallization, so in the conventional recrystallization filtrate of producing in the 2-acrylamide-2-methylpro panesulfonic acid, do not separate out fully except also having retained a considerable amount of 2-acrylamide-2-methylpro panesulfonic acids, it is numerous that composition has also been dissolved in the inside, impurity thing such as acetic acid that content is larger, vinyl cyanide and some other reaction are residual, and this recrystallization filtrate has passed through for a long time, heating and cooling operation frequently, the phenomenons such as polymerization is rotten have occured in the residual product of the inside greatly, material easily is clamminess, as the simple distillation and extraction method that adopts routine, 2-acrylamide-2-methylpro panesulfonic acid in recrystallization filtrate can't be extracted operations such as carrying out drying, even the 2-acrylamide-2-methylpro panesulfonic acid in recrystallization filtrate extracts, because the existence of other compositions makes the quality level of products obtained therefrom relatively poor.Therefore never effectively extract the method for 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate, cause this part the 2-acrylamide-2-methylpro panesulfonic acid that remains in recrystallization filtrate to be wasted, increased the difficulty that reclaims, be unfavorable for the environmental requirement of producing, and caused the unnecessary loss of product, affected the raising of economic benefit.
Summary of the invention
Technical problem to be solved by this invention is: provide a kind of can be scientific and reasonable reclaim from routine is produced the recrystallization filtrate of 2-acrylamide-2-methylpro panesulfonic acid extract the 2-acrylamide-2-methylpro panesulfonic acid and obtain quality product high, avoided product loss, improved the method for 2-acrylamide-2-methylpro panesulfonic acid of extracting of economic benefit from recrystallization filtrate.
For solving the problems of the technologies described above, technical scheme of the present invention is: the method for extracting the 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate, recrystallization filtrate is added add thermal distillation in still kettle, and add the stablizer of relative recrystallization filtrate weight 0.001%-0.005%, interior distillation temperature 55-70 ℃ of still kettle, vacuum tightness 〉=0.08Mpa, the relative recrystallization filtrate weight of distillation extraction ratio 55-65%, distill complete, be cooled to 15-20 ℃, carry out afterwards centrifugal, the dry 2-acrylamide-2-methylpro panesulfonic acid product that gets.
Wherein said stablizer is MEHQ or Resorcinol.The preferred MEHQ of described stablizer.
In still kettle distillation temperature 60-65 ℃ will be controlled well and the highlyest be not more than 70 ℃.And recrystallization filtrate adds the thermal recovery hot water bath and heats in still kettle, and described hot water bath is 80 ℃-90 ℃.
The preferred recrystallization filtrate weight 60% relatively of distillation extraction ratio.
This extracts the method for 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate, to extract the 2-acrylamide-2-methylpro panesulfonic acid in the recrystallization filtrate from routine production 2-acrylamide-2-methylpro panesulfonic acid, wherein distillation adopts hot water bath to heat, interior distillation temperature 55-70 ℃ of still kettle, preferred 60-65 ℃, vacuum tightness 〉=0.08Mpa has avoided the decomposition of material system under hot environment rotten; And by having added stablizer, effectively avoided the polymerization of material in the filtrate distillation extraction process phenomenon that is clamminess, make whole recovery extraction process realizing smoothly, and also greatly improved thus the quality level of extracting product, purity and the turbidity index of product are significantly improved, more than product purity reaches 96wt%.Whole operational path science, reasonable, easy, easy row can be implemented on producing smoothly, extracts high-quality 2-acrylamide-2-methylpro panesulfonic acid product from recrystallization filtrate.
Description of drawings
The following drawings only is intended to the present invention is done and schematically illustrates and explain, not delimit the scope of the invention.Wherein:
Fig. 1 is that this extracts the method process flow diagram of 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate.
Embodiment
Embodiment one:
as shown in Figure 1, the recrystallization filtrate 5000Kg that routine is produced the recrystallizing technology centrifugation in the 2-acrylamide-2-methylpro panesulfonic acid adds in still kettle, employing hot water is that the hot water bath of 80 ℃ is heated, open and stir, add 0.05kg stablizer Resorcinol, 65 ℃ of distillation temperatures in still kettle, carry out the vacuum decompression distillation, vacuum tightness 〉=0.08Mpa, the distillation Produced Liquid enters temporary tank stores after condensation, the relative recrystallization filtrate weight 60% of distillation extraction ratio, distill complete, close hot water circulation, close vacuum, uniform decrease in temperature is to 15-16 ℃, centrifugal afterwards, filtrate recovery enters temporary tank stores after condensation, wet product is dry, pack to get 2-acrylamide-2-methylpro panesulfonic acid product 152.5kg, purity 96.32wt%.
Embodiment two:
as shown in Figure 1, the recrystallization filtrate 5000Kg that routine is produced the recrystallizing technology centrifugation in the 2-acrylamide-2-methylpro panesulfonic acid adds in still kettle, employing hot water is that the hot water bath of 90 ℃ is heated, open and stir, add 0.05kg stablizer MEHQ, 69.5 ℃ of distillation temperatures in still kettle, carry out the vacuum decompression distillation, vacuum tightness 〉=0.08Mpa, the distillation Produced Liquid enters temporary tank stores after condensation, the relative recrystallization filtrate weight 60% of distillation extraction ratio, distill complete, close hot water circulation, close vacuum, uniform decrease in temperature is to 15-16 ℃, centrifugal afterwards, material is little sticking, filtrate recovery enters temporary tank stores after condensation, wet product is dry, the 2-acrylamide-2-methylpro panesulfonic acid product 157.2kg that is packaged to be, purity 95.67wt%.
The comparative example one:
as shown in Figure 1, the recrystallization filtrate 5000Kg that routine is produced the recrystallizing technology centrifugation in the 2-acrylamide-2-methylpro panesulfonic acid adds in still kettle, employing hot water is that the hot water bath of 95 ℃ is heated, open and stir, add 0.05kg stablizer MEHQ, 75 ℃ of distillation temperatures in still kettle, carry out the vacuum decompression distillation, vacuum tightness 〉=0.08Mpa, the distillation Produced Liquid enters temporary tank stores after condensation, the relative recrystallization filtrate weight 60% of distillation extraction ratio, distill complete, close hot water circulation, close vacuum, uniform decrease in temperature is to 15-16 ℃, the material that obtains is thickness very, centrifugal afterwards, centrifugal very difficult, filtrate recovery enters temporary tank stores after condensation, wet product is dry, after dry, material has caking phenomenon, the 2-acrylamide-2-methylpro panesulfonic acid product 161.5kg that obtains, purity 93.72%.
Embodiment three
as shown in Figure 1, the recrystallization filtrate 5000Kg that routine is produced the recrystallizing technology centrifugation in the 2-acrylamide-2-methylpro panesulfonic acid adds in still kettle, employing hot water is that the hot water bath of 80 ℃ is heated, open and stir, add 0.25kg stablizer Resorcinol, distillation temperature in still kettle keeps 65 ℃, vacuum tightness 〉=0.08Mpa, the distillation Produced Liquid enters temporary tank stores after condensation, the relative recrystallization filtrate weight 60% of distillation extraction ratio, distill complete, close hot water circulation, close vacuum, uniform decrease in temperature to 18 ℃, centrifugal afterwards, filtrate recovery enters temporary tank stores after condensation, wet product is dry, the 2-acrylamide-2-methylpro panesulfonic acid product purity 96.56wt% that obtains.
Embodiment four
as shown in Figure 1, the recrystallization filtrate that routine is produced in the 2-acrylamide-2-methylpro panesulfonic acid adds in still kettle, employing hot water is that the hot water bath of 85 ℃ is heated, open and stir, the stablizer Resorcinol that adds relative recrystallization filtrate weight 0.005%, begin the vacuum decompression distillation when being warming up to 60 ℃, distillation temperature in still kettle keeps 60-65 ℃ afterwards, vacuum tightness 〉=0.08Mpa, the distillation Produced Liquid enters temporary tank stores after condensation, the relative recrystallization filtrate weight 60% of distillation extraction ratio, distill complete, close hot water circulation, close vacuum, uniform decrease in temperature is to 15-16 ℃, centrifugal afterwards, filtrate recovery enters temporary tank stores after condensation, wet product is dry, the 2-acrylamide-2-methylpro panesulfonic acid product purity 96.32wt% that obtains.
Embodiment five
as shown in Figure 1, the recrystallization filtrate that routine is produced in the 2-acrylamide-2-methylpro panesulfonic acid adds in still kettle, employing hot water is that the hot water bath of 80 ℃ is heated, open and stir, the stablizer MEHQ that adds relative recrystallization filtrate weight 0.005%, begin the vacuum decompression distillation when being warming up to 60 ℃, distillation temperature in still kettle keeps 60-65 ℃ afterwards, vacuum tightness 〉=0.08Mpa, the distillation Produced Liquid enters temporary tank stores after condensation, the relative recrystallization filtrate weight 60% of distillation extraction ratio, distill complete, close hot water circulation, close vacuum, uniform decrease in temperature to 18 ℃, centrifugal afterwards, filtrate recovery enters temporary tank stores after condensation, wet product is dry, the 2-acrylamide-2-methylpro panesulfonic acid product purity 96.32wt% that obtains.
The comparative example two
as shown in Figure 1, the recrystallization filtrate that routine is produced in the 2-acrylamide-2-methylpro panesulfonic acid adds in still kettle, employing hot water is that the hot water bath of 80 ℃ is heated, open and stir, the stablizer MEHQ that adds relative recrystallization filtrate weight 0.0002%, begin the vacuum decompression distillation when being warming up to 60 ℃, distillation temperature in still kettle keeps 60-65 ℃ afterwards, vacuum tightness 〉=0.08Mpa, the distillation Produced Liquid enters temporary tank stores after condensation, the relative recrystallization filtrate weight 60% of distillation extraction ratio, distill complete, close hot water circulation, close vacuum, uniform decrease in temperature to 18 ℃, centrifugal afterwards, material has the whizzer of being stained with phenomenon, centrifugation time is longer, filtrate recovery enters temporary tank stores after condensation, wet product is dry, the 2-acrylamide-2-methylpro panesulfonic acid product purity 95.82wt% that obtains, material is in small, broken bits.
Can be drawn by above-mentioned comparative example one and comparative example two for comparing with embodiments of the invention, distillation temperature when distillation in still reaches 75 ℃ greater than 70 ℃, exceed distillation temperature of the present invention, and the usage quantity of stablizer is when reducing lower than stablizer usage quantity of the present invention, the material that obtains after distillation is thickness very, and centrifugal very difficult, during centrifugation, material has the whizzer of being stained with phenomenon, the purity that obtains equally product is lower, and is second-rate.
Description of the invention provides for example with for the purpose of describing, and is not exhaustively or limit the invention to disclosed form.Many modifications and variations are obvious for the ordinary skill in the art.Selecting and describing embodiment is for better explanation principle of the present invention and practical application, thereby and makes those of ordinary skill in the art can understand the various embodiment with various modifications that the present invention's design is suitable for specific end use.
Claims (6)
1. extract the method for 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate, it is characterized in that: recrystallization filtrate is added add thermal distillation in still kettle, and add the stablizer of relative recrystallization filtrate weight 0.001%-0.005%, interior distillation temperature 55-70 ℃ of still kettle, vacuum tightness 〉=0.08Mpa, the relative recrystallization filtrate weight of distillation extraction ratio 55-65%, distill complete, be cooled to 15-20 ℃, carry out afterwards centrifugal, the dry 2-acrylamide-2-methylpro panesulfonic acid product that gets.
2. the method for extracting the 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate as claimed in claim 1, it is characterized in that: described stablizer is MEHQ or Resorcinol.
3. the method for extracting the 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate as claimed in claim 2, is characterized in that: the preferred MEHQ of described stablizer.
4. the method for extracting the 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate as claimed in claim 1 is characterized in that: in still kettle distillation temperature 60-65 ℃.
5. the method for extracting the 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate as claimed in claim 1, it is characterized in that: recrystallization filtrate adds the thermal recovery hot water bath and heats in still kettle, and described hot water bath is 80 ℃-90 ℃.
6. the method for extracting the 2-acrylamide-2-methylpro panesulfonic acid from recrystallization filtrate as described in arbitrary claim in claim 1 to 5, is characterized in that: the relative recrystallization filtrate weight 60% of distillation extraction ratio.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114195685A (en) * | 2020-09-18 | 2022-03-18 | Spcm股份公司 | Purification method of 2-acrylamide-2-methylpropanesulfonic acid |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1482252A (en) * | 1975-11-05 | 1977-08-10 | Lubrizol Corp | Salts of acrylamidoalkanesulphonic acids and polymers thereof |
| JPH05125037A (en) * | 1991-11-05 | 1993-05-21 | Mitsubishi Kasei Corp | Production of high-purity 2-acrylamido-2-methylpropanesulfonic acid |
| US6331647B1 (en) * | 1991-06-03 | 2001-12-18 | The Lubrizol Corporation | Process for the preparation of a purified acrylamido sulfonic acid monomer derivative |
| CN102452965A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Method for removing polymerization inhibitor in AMPS (2-acrylamide-2-methyl propanesulfonic acid) raw material |
-
2013
- 2013-01-17 CN CN2013100166464A patent/CN103086930A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1482252A (en) * | 1975-11-05 | 1977-08-10 | Lubrizol Corp | Salts of acrylamidoalkanesulphonic acids and polymers thereof |
| US6331647B1 (en) * | 1991-06-03 | 2001-12-18 | The Lubrizol Corporation | Process for the preparation of a purified acrylamido sulfonic acid monomer derivative |
| JPH05125037A (en) * | 1991-11-05 | 1993-05-21 | Mitsubishi Kasei Corp | Production of high-purity 2-acrylamido-2-methylpropanesulfonic acid |
| CN102452965A (en) * | 2010-10-22 | 2012-05-16 | 中国石油化工股份有限公司 | Method for removing polymerization inhibitor in AMPS (2-acrylamide-2-methyl propanesulfonic acid) raw material |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114195685A (en) * | 2020-09-18 | 2022-03-18 | Spcm股份公司 | Purification method of 2-acrylamide-2-methylpropanesulfonic acid |
| CN114195685B (en) * | 2020-09-18 | 2024-02-06 | 爱森集团 | Purification method of 2-acrylamido-2-methylpropanesulfonic acid |
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Application publication date: 20130508 |