CN105418467A - Clear production technology for converting sodium camphorsulfonate into camphorsulfonic acid - Google Patents
Clear production technology for converting sodium camphorsulfonate into camphorsulfonic acid Download PDFInfo
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- CN105418467A CN105418467A CN201510961121.7A CN201510961121A CN105418467A CN 105418467 A CN105418467 A CN 105418467A CN 201510961121 A CN201510961121 A CN 201510961121A CN 105418467 A CN105418467 A CN 105418467A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C303/00—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides
- C07C303/02—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof
- C07C303/22—Preparation of esters or amides of sulfuric acids; Preparation of sulfonic acids or of their esters, halides, anhydrides or amides of sulfonic acids or halides thereof from sulfonic acids, by reactions not involving the formation of sulfo or halosulfonyl groups; from sulfonic halides by reactions not involving the formation of halosulfonyl groups
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Abstract
The invention discloses a clear production technology for converting sodium camphorsulfonate into camphorsulfonic acid. The clear production technology comprises the following steps of step one, carrying out ceramic membrane filtration on a feed solution, and obtaining ceramic membrane dialysate; step two, enabling the ceramic membrane dialysate to enter a bipolar membrane electrodialysis system to carry out bipolar membrane electrodialysis, and obtaining a crude camphorsulfonic acid solution; step three, enabling the ceramic membrane dialysate to enter a continuous ion exchange system to carry out continuous ion exchange, and obtaining a camphorsulfonic acid solution; step four, carrying out reverse osmosis concentration on the camphorsulfonic acid solution, and obtaining a camphorsulfonic acid concentrated solution; step 5, obtaining camphorsulfonic acid crystals through crystallizing, centrifugal separation and crystal drying after carrying out mechanical vapor recompression concentration on the camphorsulfonic acid concentrated solution. According to the camphorsulfonic acid crystals produced by adopting the clear production technology disclosed by the invention, the purity can be more than 99.5 percent, and the crystals reach the pharmaceutical-grade camphorsulfonic acid level; meanwhile, a one-step recovery rate of materials can be more than 95 percent, the cycling volume is reduced, and energy consumption is reduced.
Description
Technical field
The present invention relates to camphorsulfonic acid production field, particularly relate to a kind of process for cleanly preparing being changed into camphorsulfonic acid by sodium camphorsulfonate.
Background technology
Camphor is mainly present in camphor tree plant camphorwood material, zingiberaceous plant alpinia japonica seed, is medical, daily and the indispensable raw material of national defense industry.According to the difference in its source, camphor is mainly divided into natural and synthesis two large classes.Natural camphor mainly extracts and obtains from canella essential oil, generally has right-handed rotation activity; Artificial camphor makes from turps through main chemical reactions processes such as isomerization, acetic acid addition esterification, hydrolysis and dehydrogenations, is raceme.
Camphorsulfonic acid is the derivative of camphor, has the corresponding body structure of chirality, can be divided into and left and rightly revolve structure, be widely used in the industries such as medicine, light industry and daily use chemicals according to its optical characteristics.At present, chemical industry artificial camphor sulfonic acid, mainly by first artificial camphor sodium sulfonate or camphorsulfonic acid sodium solution, then obtains camphorsulfonic acid solution carrying out continuous ionic exchange system by fixed bed; Often there is the production cycle long, total recovery is relatively low, and product purity difference also needs the shortcomings such as further separation and purification.
Summary of the invention
For the problems referred to above, the object of the invention is to design the process for cleanly preparing being changed into camphorsulfonic acid by sodium camphorsulfonate that a kind of yield is high, operation is simple, changing effect is good, product purity is high.
For achieving the above object, technical scheme proposed by the invention is: a kind of process for cleanly preparing being changed into camphorsulfonic acid by sodium camphorsulfonate, is characterized in that, comprise the steps:
Step 1: stock liquid carries out ceramic membrane filter, obtains ceramic membrane dialyzate;
Step 2: ceramic membrane dialyzate enters bipolar membrane electrodialysis system and carries out bipolar membrane electrodialysis, the thick solution of camphorsulfonic acid;
Step 3: the thick solution of camphorsulfonic acid enters in continuous ionic exchange system and carries out continuous ionic exchange, obtains camphorsulfonic acid solution, fills strongly acidic cation-exchange in the separating unit of described continuous ionic exchange system;
Step 4: camphorsulfonic acid solution carries out reverse osmosis concentration, obtains camphorsulfonic acid concentrated solution;
Step 5: after camphorsulfonic acid concentrated solution carries out mechanical steam recompression concentrated (MVR concentrates), then by crystallization, centrifugation, crystal dry camphorsulfonic acid crystal.
Preferably, built-in 30 separating units of described continuous ionic exchange system, described continuous ionic exchange system is divided into five regions, and each region is composed as follows:
Zone of transformation: comprise 6 separating units, be divided into two sections, leading portion comprises 3 separating units, back segment comprises 3 separating units, after the series connection of stock liquid forward enters leading portion 3 separating units, its effluent liquid is mixed in tundish with the effluent liquid transformed in water wash zone, and the feed liquid in tundish again forward series connection enters 3 separating units of back segment, collect last separating unit fluid, obtain camphorsulfonic acid solution;
Transform water wash zone: comprise 4 separating units, the separating unit after zone of transformation transforms enters and transforms water wash zone, adopts forward to connect into pure water, washes, and collects the feed liquid transforming water wash zone and enters in tundish;
Alkali breeding blanket: comprise 6 separating units, be divided into two sections, leading portion comprises 3 separating units, back segment comprises 3 separating units, transform the separating unit after the washing of water wash zone, leading portion 3 separating unit forward enters alkaline solution regeneration, and leading portion effluent liquid enters diluted alkaline tank and mixes with the reuse water washing lotion of regeneration water wash zone, obtain sig water, back segment 3 separating unit forwards are connected into the sig water regeneration in diluted alkaline tank;
Alkali regeneration water wash zone: comprise 4 separating units, the separating unit after the regeneration of alkali breeding blanket, adopt forward series system to enter pure water washing, reuse water washing lotion enters in diluted alkaline tank;
Acid regeneration district: comprise 6 separating units, be divided into two sections, leading portion comprises 3 separating units, back segment comprises 3 separating units, separating unit after alkali regeneration water wash zone washing, leading portion 3 separating unit forward enters acid solution regeneration, and leading portion effluent liquid enters diluted acid tank and mixes with the reuse water washing lotion of acid regeneration water wash zone, obtain diluted acid, back segment 3 separating unit forwards are connected into the diluted acid regeneration in diluted acid tank;
Acid regeneration water wash zone: comprise 3 separating units, the separating unit after the regeneration of acid regeneration district, adopt forward series system to enter pure water washing, reuse water washing lotion enters in diluted acid tank;
Pool, material top: comprise 1 separating unit, adopt backward feed mode, the water camphorsulfonic acid solution immediate roof stayed in separating unit come out as charging with the camphorsulfonic acid solution obtained after conversion, to improve the concentration of product, the water be ejected can be back to use this system; Separating unit after the pool process of material top, enters zone of transformation circular treatment.
Preferably, the camphorsulfonic acid sodium solution of described stock liquid to be concentration be 15-30%.
Preferably, the pore size filter of the ceramic membrane that described ceramic membrane filter adopts is 50-200nm.
Adopt the camphorsulfonic acid crystal that the process for cleanly preparing changing into camphorsulfonic acid by sodium camphorsulfonate of the present invention is produced, purity can reach more than 99.7%, reach the camphorsulfonic acid level of pharmaceutical grade, the disposable rate of recovery of material can reach more than 95% simultaneously, reduce circulation volume, energy efficient.
Accompanying drawing explanation
Fig. 1 is the process for cleanly preparing schematic flow sheet being changed into camphorsulfonic acid by sodium camphorsulfonate of the present invention;
Fig. 2 is continuous ionic exchange system schematic diagram of the present invention.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention will be further described.
As shown in Figure 1 and Figure 2, the process for cleanly preparing being changed into camphorsulfonic acid by sodium camphorsulfonate of the present invention, comprises the steps:
Step 1: stock liquid carries out ceramic membrane filter, removes insoluble matter and suspended substance with ceramic membrane filter, reduces the pollution of resin and the regeneration frequency, obtains ceramic membrane dialyzate; The camphorsulfonic acid sodium solution of stock liquid to be concentration be 15-30%; The pore size filter of the ceramic membrane that ceramic membrane filter adopts is 50-200nm;
Step 2: ceramic membrane dialyzate enters bipolar membrane electrodialysis system and carries out bipolar membrane electrodialysis, the thick solution of camphorsulfonic acid; Bipolar membrane electrodialysis can change into camphorsulfonic acid sodium camphorsulfonate, yield can reach more than 98%, concentration 10-25%, the by product of bipolar membrane electrodialysis is sodium hydroxide solution, sodium hydroxide solution directly can turn back to the neutralization that former process carries out resulting solution, and this transformation efficiency is 90%;
Step 3: the thick solution of camphorsulfonic acid enters in continuous ionic exchange system and carries out continuous ionic exchange, removes sodium ion further, obtains camphorsulfonic acid solution, fills strongly acidic cation-exchange in the separating unit of described continuous ionic exchange system;
Concrete, as shown in Figure 2, built-in 30 separating units of described continuous ionic exchange system, described continuous ionic exchange system is divided into five regions, and each region is composed as follows:
Zone of transformation (5#-10#): comprise 6 separating units, be divided into two sections, leading portion comprises 3 separating units (5#-7#), back segment comprises 3 separating units (8#-10#), after the series connection of stock liquid forward enters leading portion 3 separating units, its effluent liquid is mixed in tundish with the effluent liquid transformed in water wash zone, and the feed liquid in tundish again forward series connection enters 3 separating units of back segment, collect last separating unit fluid, obtain camphorsulfonic acid solution;
Transform water wash zone (1#-4#): comprise 4 separating units, the separating unit after zone of transformation transforms enters and transforms water wash zone, adopts forward to connect into pure water, washes, and collects the feed liquid transforming water wash zone and enters in tundish;
Alkali breeding blanket (25#-30#): comprise 6 separating units, be divided into two sections, leading portion comprises 3 separating units (25#-27#), back segment comprises 3 separating units (28#-30#), transform the separating unit after the washing of water wash zone, leading portion 3 separating unit forwards enter alkaline solution regeneration, and leading portion effluent liquid enters diluted alkaline tank and mixes with the reuse water washing lotion of regeneration water wash zone, obtain sig water, back segment 3 separating unit forwards are connected into the sig water regeneration in diluted alkaline tank;
Alkali regeneration water wash zone (21#-24#): comprise 4 separating units, the separating unit after the regeneration of alkali breeding blanket, adopt forward series system to enter pure water washing, reuse water washing lotion enters in diluted alkaline tank;
Acid regeneration district (15#-20#): comprise 6 separating units, be divided into two sections, leading portion comprises 3 separating units (15#-17#), back segment comprises 3 separating units (18#-20#), separating unit after alkali regeneration water wash zone washing, leading portion 3 separating unit forward enters acid solution regeneration, and leading portion effluent liquid enters diluted acid tank and mixes with the reuse water washing lotion of acid regeneration water wash zone, obtain diluted acid, back segment 3 separating unit forwards are connected into the diluted acid regeneration in diluted acid tank;
Acid regeneration water wash zone (12#-14#): comprise 3 separating units, the separating unit after the regeneration of acid regeneration district, adopt forward series system to enter pure water washing, reuse water washing lotion enters in diluted acid tank;
Material pool, top (11#): comprise 1 separating unit, adopt backward feed mode, the water camphorsulfonic acid solution immediate roof stayed in separating unit is come out as charging with the camphorsulfonic acid solution obtained after conversion, to improve the concentration of product, the water be ejected can be back to use this system; Separating unit after the pool process of material top, enters zone of transformation circular treatment;
Step 3: camphorsulfonic acid solution carries out reverse osmosis concentration, obtains camphorsulfonic acid concentrated solution;
Step 4: after camphorsulfonic acid concentrated solution carries out mechanical steam recompression concentrated (MVR concentrates), then by crystallization, centrifugation, crystal dry camphorsulfonic acid crystal.
Embodiment 1
Wherein: the stock liquid in step 1 adopts the camphorsulfonic acid sodium solution of 25%, aperture is adopted to be the ceramic membrane of 50nm; Strongly acidic cation-exchange in step 2 is 732 strongly acidic cation-exchanges, hydrochloric acid to be concentration be 5% hydrochloric acid, sodium hydroxide be concentration be 4% sodium hydroxide;
Embodiment 2
Wherein: the stock liquid in step 1 adopts the camphorsulfonic acid sodium solution of 15%, aperture is adopted to be the ceramic membrane of 100nm; Strongly acidic cation-exchange in step 2 is 732 strongly acidic cation-exchanges, hydrochloric acid to be concentration be 5% hydrochloric acid, sodium hydroxide be concentration be 4% sodium hydroxide;
Embodiment 3
Wherein: the stock liquid in step 1 adopts the camphorsulfonic acid sodium solution of 30%, aperture is adopted to be the ceramic membrane of 200nm; Strongly acidic cation-exchange in step 2 is 732 strongly acidic cation-exchanges, and acid is 4% sodium hydroxide for hydrochloric acid, alkali that concentration is 5% are concentration.
Result is as follows:
As can be seen from the above table, the just calculation yield of three batches of experiments, all more than 100%, is got rid of the error on weighing, can be found out that product does not lose substantially, also can find out the very thorough of conversion from the color of resin variation phenomenon at scene simultaneously.
The camphorsulfonic acid solution that continuous ionic clearing house obtains is camphorsulfonic acid crystal after, crystallization concentrated through reverse osmosis concentration, MVR successively, centrifugation, crystal drying again, can more than 99.7% be reached through inspection camphorsulfonic acid crystal purity, reach the camphorsulfonic acid level of pharmaceutical grade.
Every technician's notice: although the present invention describes according to above-mentioned embodiment, invention thought of the present invention is not limited in this invention, and the repacking of any utilization inventive concept, all will include in this patent scope of patent protection.
Claims (4)
1. changed into a process for cleanly preparing for camphorsulfonic acid by sodium camphorsulfonate, it is characterized in that, comprise the steps:
Step 1: stock liquid carries out ceramic membrane filter, obtains ceramic membrane dialyzate;
Step 2: ceramic membrane dialyzate enters bipolar membrane electrodialysis system and carries out bipolar membrane electrodialysis, the thick solution of camphorsulfonic acid;
Step 3: the thick solution of camphorsulfonic acid enters in continuous ionic exchange system and carries out continuous ionic exchange, obtains camphorsulfonic acid solution, fills strongly acidic cation-exchange in the separating unit of described continuous ionic exchange system;
Step 4: camphorsulfonic acid solution carries out reverse osmosis concentration, obtains camphorsulfonic acid concentrated solution;
Step 5: camphorsulfonic acid concentrated solution carry out mechanical steam recompression concentrated after, then by crystallization, centrifugation, crystal dry camphorsulfonic acid crystal.
2. a kind of process for cleanly preparing being changed into camphorsulfonic acid by sodium camphorsulfonate according to claim 1, it is characterized in that, built-in 30 separating units of described continuous ionic exchange system, described continuous ionic exchange system is divided into five regions, and each region is composed as follows:
Zone of transformation: comprise 6 separating units, be divided into two sections, leading portion comprises 3 separating units, back segment comprises 3 separating units, after the series connection of stock liquid forward enters leading portion 3 separating units, its effluent liquid is mixed in tundish with the effluent liquid transformed in water wash zone, and the feed liquid in tundish again forward series connection enters 3 separating units of back segment, collect last separating unit fluid, obtain camphorsulfonic acid solution;
Transform water wash zone: comprise 4 separating units, the separating unit after zone of transformation transforms enters and transforms water wash zone, adopts forward to connect into pure water, washes, and collects the feed liquid transforming water wash zone and enters in tundish;
Alkali breeding blanket: comprise 6 separating units, be divided into two sections, leading portion comprises 3 separating units, back segment comprises 3 separating units, transform the separating unit after the washing of water wash zone, leading portion 3 separating unit forward enters alkaline solution regeneration, and leading portion effluent liquid enters diluted alkaline tank and mixes with the reuse water washing lotion of regeneration water wash zone, obtain sig water, back segment 3 separating unit forwards are connected into the sig water regeneration in diluted alkaline tank;
Alkali regeneration water wash zone: comprise 4 separating units, the separating unit after the regeneration of alkali breeding blanket, adopt forward series system to enter pure water washing, reuse water washing lotion enters in diluted alkaline tank;
Acid regeneration district: comprise 6 separating units, be divided into two sections, leading portion comprises 3 separating units, back segment comprises 3 separating units, separating unit after alkali regeneration water wash zone washing, leading portion 3 separating unit forward enters acid solution regeneration, and leading portion effluent liquid enters diluted acid tank and mixes with the reuse water washing lotion of acid regeneration water wash zone, obtain diluted acid, back segment 3 separating unit forwards are connected into the diluted acid regeneration in diluted acid tank;
Acid regeneration water wash zone: comprise 3 separating units, the separating unit after the regeneration of acid regeneration district, adopt forward series system to enter pure water washing, reuse water washing lotion enters in diluted acid tank;
Pool, material top: comprise 1 separating unit, adopt backward feed mode, the water camphorsulfonic acid solution immediate roof stayed in separating unit come out as charging with the camphorsulfonic acid solution obtained after conversion, to improve the concentration of product, the water be ejected can be back to use this system; Separating unit after the pool process of material top, enters zone of transformation circular treatment.
3. a kind of process for cleanly preparing being changed into camphorsulfonic acid by sodium camphorsulfonate according to claim 1 and 2, is characterized in that, the camphorsulfonic acid sodium solution of described stock liquid to be concentration be 15-30%.
4. a kind of process for cleanly preparing being changed into camphorsulfonic acid by sodium camphorsulfonate according to claim 1 and 2, is characterized in that, the pore size filter of the ceramic membrane that described ceramic membrane filter adopts is 50-200nm.
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Cited By (5)
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| CN106496077A (en) * | 2016-09-30 | 2017-03-15 | 厦门欣赛科技有限公司 | A kind of method for reclaiming camphorsulfonic acid from camphorsulfonic acid synthesis mother liquid |
| CN106518732A (en) * | 2016-09-30 | 2017-03-22 | 厦门欣赛科技有限公司 | Recycling method for camphorsulfonic acid synthesized mother liquor |
| CN106565550A (en) * | 2016-11-02 | 2017-04-19 | 河北美邦工程科技股份有限公司 | Method for concentrating and dewatering camphor sulfonic acid solution in production process of L-phenylglycine |
| CN109134317A (en) * | 2018-09-10 | 2019-01-04 | 合肥科佳高分子材料科技有限公司 | A kind of method that bipolar membrane electrodialysis prepares L-10- camphorsulfonic acid |
| CN112174856A (en) * | 2020-10-26 | 2021-01-05 | 湖北吉和昌化工科技有限公司 | Purification production process of organic sulfonic acid |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106496077A (en) * | 2016-09-30 | 2017-03-15 | 厦门欣赛科技有限公司 | A kind of method for reclaiming camphorsulfonic acid from camphorsulfonic acid synthesis mother liquid |
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| CN106565550A (en) * | 2016-11-02 | 2017-04-19 | 河北美邦工程科技股份有限公司 | Method for concentrating and dewatering camphor sulfonic acid solution in production process of L-phenylglycine |
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| CN109134317A (en) * | 2018-09-10 | 2019-01-04 | 合肥科佳高分子材料科技有限公司 | A kind of method that bipolar membrane electrodialysis prepares L-10- camphorsulfonic acid |
| CN109134317B (en) * | 2018-09-10 | 2021-11-12 | 合肥科佳高分子材料科技有限公司 | Method for preparing L-10-camphorsulfonic acid by bipolar membrane electrodialysis |
| CN112174856A (en) * | 2020-10-26 | 2021-01-05 | 湖北吉和昌化工科技有限公司 | Purification production process of organic sulfonic acid |
| CN112174856B (en) * | 2020-10-26 | 2023-03-24 | 湖北吉和昌化工科技有限公司 | Purification production process of organic sulfonic acid |
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