CN102838498A - Method for converting sodium amino propionate into amino propionic acid - Google Patents
Method for converting sodium amino propionate into amino propionic acid Download PDFInfo
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- CN102838498A CN102838498A CN2012103641658A CN201210364165A CN102838498A CN 102838498 A CN102838498 A CN 102838498A CN 2012103641658 A CN2012103641658 A CN 2012103641658A CN 201210364165 A CN201210364165 A CN 201210364165A CN 102838498 A CN102838498 A CN 102838498A
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Abstract
The invention discloses a method for converting sodium amino propionate into amino propionic acid. The method is characterized in that a continuous ion exchange system is adopted, wherein 20 separation units are arranged in the system; each separation unit is filled with macroporous strong acid resin; and the continuous ion exchange system is divided into five regions, i.e., a conversion region, a conversion and washing region, an acid regeneration region, a regeneration and washing region and a material top water region. The average content of the amino propionic acid obtained by using the method for converting the sodium amino propionate into the amino propionic acid reaches 9.9 percent, the purity is greater than 98 percent, the chlorine ion content does not exceed standard, and the reverse yield of a product is close to 100 percent. The method has the advantages of compact equipment, simplified system, reduced pipelines, small floor area, reduced resin consumption, reduced consumption of chemical agents such as a regenerant and wash water, basically stable composition and concentration of the product, good operation flexibility and capabilities of automatically adjusting the rotation speed according to variation in production load and reducing the operation cost and the equipment investment.
Description
Technical field
The present invention relates to ion-exchange field, particularly relate to the method that a kind of alanine sodium changes into alanine.
Background technology
Alanine is a kind of white or flaxen crystalline powder, and main users synthetic pantothenic acid, VA, carnosine, Sodium Pamidronate, Balsalazide etc. are widely used in fields such as medicine, feed, food.At present alanine sodium is changed into shortcomings such as often to exist operation in the process of alanine longer, and the production cycle is long, and total recovery is relatively low.
Summary of the invention
To the problems referred to above, the objective of the invention is to design the method that a kind of yield is high, operation is simple, changing effect is good alanine sodium changes into alanine.
For achieving the above object; Technical scheme proposed by the invention is: a kind of alanine sodium changes into the method for alanine; It is characterized in that: adopt the continuous ionic exchange system, fill large porous strong acid type resin in built-in 20 separating units of system, each separating unit; Described continuous ionic exchange system is divided into five zones, and each zone is formed as follows:
Zone of transformation: comprise 7 separating units, be divided into two sections, leading portion comprises 3 separating units; Back segment comprises 4 separating units; After the liquid stock forward was connected and got into 3 separating units of leading portion, its effluent was mixed in the tundish with the effluent that transforms in the water wash zone, and the feed liquid in the tundish is 4 separating units of forward series connection entering back segment again; Collect last separating unit fluid, get alanine solution;
Transform water wash zone: comprise 4 separating units, the separating unit after transforming through zone of transformation gets into and transforms water wash zone, adopts reverse series connection to advance pure water, washes, and collects the feed liquid that transforms water wash zone and gets in the tundish;
The acid regeneration district: comprise 4 separating units, be divided into two sections, leading portion comprises a separating unit; Back segment comprises 3 separating units; Transform the separating unit after water wash zone is washed, leading portion one separating unit forward advances 10% regeneration of hydrochloric acid, and the leading portion effluent gets into the diluted acid jar to be mixed with the reuse water washing lotion of regeneration water wash zone; Diluted acid, the diluted acid regeneration in the diluted acid jar into of connecting of 3 separating unit forwards of back segment;
The regeneration water wash zone: comprise 4 separating units, the separating unit after the regeneration of acid regeneration district adopts the reflux type that is connected in series to advance the pure water washing;
Pool, material top: comprise 1 separating unit; Adopt the backward feed mode; The water that to stay in the separating unit as charging with the alanine solution that obtains after transforming directly comes out on the top with product, and to improve the concentration of product, the water that is ejected can be back to use this system; Separating unit after handle in pool, material top gets into the zone of transformation circular treatment.
Further, need the pH value of control zone of transformation to be in the conversion process: 5.8≤pH≤7.0.
Further, the pH value that needs control to transform water wash zone in the conversion process is: pH≤10.5.
Further, the amount of resin of loading in described each separating unit is 150mL.
Further, described continuous ionic exchange system rotating speed is 420s/ time.
Preferably, the leading portion feed liquid flow velocity of zone of transformation is 30L/h, and the flow velocity of back segment is 117L/h; The flow velocity that transforms water wash zone is 85L/h, and the flow velocity of acid regeneration district leading portion is 36L/h, and the flow velocity of back segment is 1800L/h; The flow velocity of regeneration water wash zone is 1440L/h, and the flow velocity in pool, material top is 40L/h.
Further, described liquid stock is a concentration preferred concentration 30%, the alanine sodium solution of pH=14.
The alanine average content that adopts alanine sodium of the present invention to change into the method gained of alanine reaches 9.9%, purity＞98%, and chloride ion content does not exceed standard, and product yield is near 100%, and the advantage that has is:
1) facility compact, system simplification, pipeline reduction and floor space are few;
2) the resin consumption reduces, and pharmaceutical chemicalss such as regenerator, wash-down water consumption reduce; Reduce wastewater discharge;
3) owing to the continuous operation under the non-intermittent operation, the composition of product, concentration keep basic stablizing;
4) have good turndown ratio, can regulate speed of rotation automatically according to the variation of producing load; Reduce running cost and facility investment;
5) good operability, the valve switching frequency is low, the error that can avoid human factor to cause.
Description of drawings
Fig. 1 is a continuous ionic exchange system synoptic diagram of the present invention.
Embodiment
Below in conjunction with accompanying drawing and embodiment, the present invention is further specified.
As shown in Figure 1, alanine sodium changes into the method for alanine, adopts the continuous ionic exchange system, fills large porous strong acid type resin in built-in 20 separating units of system, each separating unit; Described continuous ionic exchange system is divided into five zones, and each zone is formed as follows:
Zone of transformation (5#-11#): comprise 7 separating units, be divided into two sections, leading portion comprises the 5#-7# separating unit, and charging is a liquid stock, and back segment comprises the 8#-11# separating unit, and charging is the mixed solution of middle batch can; After the series connection of liquid stock forward gets into the 5#-7# separating unit; Its effluent is mixed in the tundish with the effluent that transforms in the water wash zone; Feed liquid in the tundish is the 8#-11# separating unit of forward series connection entering back segment again, collects last separating unit fluid, gets alanine solution;
Transform water wash zone (1#-4#): comprise 4 separating units, the separating unit after transforming through zone of transformation gets into and transforms water wash zone, adopts reverse series connection to advance pure water, washes, and collects the feed liquid that transforms water wash zone and gets in the tundish;
Acid regeneration district (17#-20#): comprise 4 separating units, be divided into two sections, leading portion comprises the 17# separating unit; Back segment comprises 18-20# separating unit; Transform the separating unit after water wash zone is washed, 17# separating unit forward advances 10% regeneration of hydrochloric acid, and 17# separating unit effluent gets into the diluted acid jar to be mixed with the reuse water washing lotion of regeneration water wash zone; Diluted acid, the diluted acid regeneration in the diluted acid jar into of connecting of back segment 18-20# separating unit forward;
Regeneration water wash zone (13#-16#): comprise 4 separating units, the separating unit after the regeneration of acid regeneration district adopts the reflux type that is connected in series to advance the pure water washing;
Pool (12#), material top: comprise 1 separating unit; Adopt the backward feed mode; The water that to stay in the separating unit as charging with the alanine solution that obtains after transforming directly comes out on the top with product, and to improve the concentration of product, the water that is ejected can be back to use this system; Separating unit after handle in pool, material top gets into the zone of transformation circular treatment.
Adopt aforesaid method, be used for pilot scale structure such as following table that alanine sodium changes into alanine, the amount of resin of wherein loading in each separating unit is 150mL; Continuous ionic exchange system rotating speed is 420s/ time, and the pH value of control zone of transformation is in the conversion process: 5.8≤pH≤7.0, and the pH value that control transforms water wash zone is: pH≤10.5; The feed liquid flow velocity of zone of transformation leading portion is 30L/h, and the flow velocity of back segment is 117L/h, and the flow velocity that transforms water wash zone is 85L/h; The flow velocity of acid regeneration district leading portion is 36L/h; The flow velocity of back segment is 1800L/h, and the flow velocity of regeneration water wash zone is 1440L/h, and the flow velocity in pool, material top is 40L/h.
Need to prove; Present embodiment is embodiment with the continuous ionic exchange system that adopts 20 separating units only; Describing the present invention adopts the continuous ionic exchange system that alanine sodium is changed into the technique effect that alanine can reach; For a person skilled in the art, the separating unit that different pieces of information is set is as required realized the present invention, is protection scope of the present invention.
Claims (6)
1. an alanine sodium changes into the method for alanine, it is characterized in that: adopt the continuous ionic exchange system, fill large porous strong acid type resin in built-in 20 separating units of system, each separating unit; Described continuous ionic exchange system is divided into five zones, and each zone is formed as follows:
Zone of transformation: comprise 7 separating units, be divided into two sections, leading portion comprises 3 separating units; Back segment comprises 4 separating units; After the liquid stock forward was connected and got into 3 separating units of leading portion, its effluent was mixed in the tundish with the effluent that transforms in the water wash zone, and the feed liquid in the tundish is 4 separating units of forward series connection entering back segment again; Collect last separating unit fluid, get alanine solution;
Transform water wash zone: comprise 4 separating units, the separating unit after transforming through zone of transformation gets into and transforms water wash zone, adopts reverse series connection to advance pure water and washes, and collects the feed liquid that transforms water wash zone and gets in the tundish;
The acid regeneration district: comprise 4 separating units, be divided into two sections, leading portion comprises a separating unit; Back segment comprises 3 separating units; Transform the separating unit after water wash zone is washed, leading portion one separating unit forward advances 10% regeneration of hydrochloric acid, and the leading portion effluent gets into the diluted acid jar to be mixed with the reuse water washing lotion of regeneration water wash zone; Diluted acid, the diluted acid regeneration in the diluted acid jar into of connecting of 3 separating unit forwards of back segment;
The regeneration water wash zone: comprise 4 separating units, the separating unit after the regeneration of acid regeneration district adopts the reflux type that is connected in series to advance the pure water washing;
Pool, material top: comprise 1 separating unit; Adopt the backward feed mode; The water that to stay in the separating unit as charging with the alanine solution that obtains after transforming directly comes out on the top with product, and to improve the concentration of product, the water that is ejected can be back to use this system; Separating unit after handle in pool, material top gets into the zone of transformation circular treatment.
2. a kind of alanine sodium according to claim 1 changes into the method for alanine, it is characterized in that: the pH value of control zone of transformation is in the conversion process: 5.8≤pH≤7.0.
3. a kind of alanine sodium according to claim 1 changes into the method for alanine, it is characterized in that: the pH value of control conversion water wash zone is in the conversion process: pH≤10.5.
4. a kind of alanine sodium according to claim 1 changes into the method for alanine, it is characterized in that: the amount of resin of loading in described each separating unit is 150mL.
5. a kind of alanine sodium according to claim 1 changes into the method for alanine, it is characterized in that: described continuous ionic exchange system rotating speed is 420s/ time.
6. a kind of alanine sodium according to claim 1 changes into the method for alanine; It is characterized in that: the leading portion feed liquid flow velocity of zone of transformation is 30L/h, and the flow velocity of back segment is 117L/h, and the flow velocity that transforms water wash zone is 85L/h; The flow velocity of acid regeneration district leading portion is 36L/h; The flow velocity of back segment is 1800L/h, and the flow velocity of regeneration water wash zone is 1440L/h, and the flow velocity in pool, material top is 40L/h.
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| CN201210364165.8A CN102838498B (en) | 2012-09-24 | 2012-09-24 | A kind of alanine sodium changes into the method for alanine |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19857690A1 (en) * | 1998-12-14 | 2000-06-15 | Consortium Elektrochem Ind | Isolation of 2-methyl-thiazolidine-2,4-dicarboxylic acid from a reaction mixture by adding selected divalent metal ions to precipitate the corresponding metal salt and treating the salt with a strong acid cation exchanger |
| CN101643409A (en) * | 2009-08-31 | 2010-02-10 | 厦门世达膜科技有限公司 | Production method for converting sodium tartrate into tartaric acid |
| CN101671324A (en) * | 2009-09-24 | 2010-03-17 | 厦门世达膜科技有限公司 | Production method of glucolactone |
-
2012
- 2012-09-24 CN CN201210364165.8A patent/CN102838498B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE19857690A1 (en) * | 1998-12-14 | 2000-06-15 | Consortium Elektrochem Ind | Isolation of 2-methyl-thiazolidine-2,4-dicarboxylic acid from a reaction mixture by adding selected divalent metal ions to precipitate the corresponding metal salt and treating the salt with a strong acid cation exchanger |
| CN101643409A (en) * | 2009-08-31 | 2010-02-10 | 厦门世达膜科技有限公司 | Production method for converting sodium tartrate into tartaric acid |
| CN101671324A (en) * | 2009-09-24 | 2010-03-17 | 厦门世达膜科技有限公司 | Production method of glucolactone |
Non-Patent Citations (2)
| Title |
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| 吴春江等: "连续交换工艺和设备在VC生产转化工序的改造", 《机电信息》 * |
| 罗积杏等: "β-氨基丙酸的合成与应用", 《氨基酸和生物资源》 * |
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Application publication date: 20121226 Assignee: Xiamen Shida membrane Engineering Co.,Ltd. Assignor: XIAMEN STARMEM TECHNOLOGY CO.,LTD. Contract record no.: X2021980014823 Denomination of invention: Method for converting sodium aminopropionate into aminopropionic acid Granted publication date: 20160106 License type: Exclusive License Record date: 20211221 |
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