CN104560707A - Technological method and system for enzymatically synthesizing L-ascorbic acid 2-glucoside - Google Patents
Technological method and system for enzymatically synthesizing L-ascorbic acid 2-glucoside Download PDFInfo
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Abstract
The invention provides a technological system and method for enzymatically synthesizing L-ascorbic acid 2-glucoside. The technological system comprises reaction kettles (1), an enzyme storage tank (2), a storage tank (3), centrifuges (4), a first filter device (5), a first resin column (6), a second resin column (7), a second filter device (8), a falling film concentration device (9) and a third filter device (10). The technological method comprises the steps of enzyme reaction, preparation of the crude product of L-ascorbic acid 2-glucoside and crude product refining. The technological system and the technological method have the technical effects that impurities are effectively removed, thus improving the purity of a finished product; the requirements for equipment are simple; the yield is high, after-treatment is simple to carry out, and the cost is low.
Description
Technical field
The present invention relates to a kind of processing method and the process system of preparing AA 2G, specifically a kind of processing method of Enzyme catalyzed synthesis AA 2G and process system.
Background technology
AA 2G is (also known as vitamins C glucoside, be called for short AA-2G, L-VCG), chemistry 2-oxygen-α-D-glucopyranosyl xitix by name, it is ascorbic carbohydrate derivative, becoming ascorbic best substitute because having the following advantages: 1) good non-reduced activity, stablizing in aqueous; 2) good thermotolerance and photostabilization; 3) in born of the same parents, vitamins C and glucose are produced in hydrolysis, have the biological activity equal with vitamins C.
AA 2G is that Department of Health announces one of 6 kinds of whitening additives of accreditation.It directly can discharge the melanochrome (add speed in reversed direction by established melanochrome and be reduced to initial form) formed in epidermal area, whitening effect, therefore all has a wide range of applications more obviously with quick than other additives in multiple high-end skin-lightening cosmetic.Existingly prepare in AA 2G technique, impurity difficulty is removed, and AA 2G purity is not high, and yield is low.
Summary of the invention
In order to solve the problem, first object of the present invention is to provide a kind of process system improving AA 2G purity.
Second object of invention is to provide a kind of processing method improving AA 2G purity.
Maltose 4-glucosyltransferase provided by the invention (abbreviation CGT enzyme) adopts the patent No. to provide prepared by the preparation method of 201410236224.2 cyclodextrin glycosyltransferases.
Technical scheme of the present invention:
A process system for Enzyme catalyzed synthesis AA 2G, comprises reactor (1), enzyme basin (2), basin (3), whizzer (4), the first filtration unit (5), the first resin column (6), the second resin column (7), the second filtration unit (8), falling film concentrating device (9), the 3rd filtration unit (10); Described the first filtration unit (5) is positioned at the upstream of described first resin column (6), the downstream of this first resin column (6) is described the second resin column (7), described second filtration unit (8) is positioned at the downstream of this second resin column (7), and described falling film concentrating device (9) is positioned at the downstream of this second filtration unit (8); Described 3rd filtration unit (10) is positioned at the downstream of this falling film concentrating device (9); Described whizzer (4) has many groups, respectively in the upstream of described the first filtration unit (5), the described upstream of the 3rd filtration unit (10) and the downstream of described falling film concentrating device (9);
As preferably, described the first filtration unit (5) is ultrafilter, and described second filtration unit (8) is collecting and filtering apparatus, and described filtration unit (10) is titanium rod filtration unit, forms in this titanium rod filtration unit by organizing titanium rod filter core more.
As preferably, described the first resin column (6) is positive resin post, and described the second resin column (7) is negative resin post, and described whizzer (4) is butterfly centrifugal machine.
As preferably, described production line has three, and between the resin column (6) in every bar production line, pipeline is connected in parallel.
As preferably, described basin (3) has many groups, is positioned over the downstream of described reactor (1), the first filtration unit (5), the first resin column (6), the second resin column (7), the second filtration unit (8), falling film concentrating device (9), the 3rd filtration unit (10) respectively.
A processing method for Enzyme catalyzed synthesis AA 2G as claimed in claim 1, is characterized by: comprise the following steps:
Step one: enzyme reaction
(1) in reactor (1), add tap water, then add vitamins C, open and stir;
(2) hot water controls temperature 37 DEG C in described reactor (1), adjusts pH to 5.50 ± 0.10 with 30%NaOH solution;
(3) in described reactor (1), beta-cyclodextrin is added;
(4) add Maltose 4-glucosyltransferase again, add tap water and make system quantitative;
(5) the interior temperature in the kettle of this reactor (1) 37 ± 2 DEG C is controlled, lucifuge reaction 10-12h;
(6) after reacting 1 end, saccharifying enzyme (enzyme liquid 750,000 U/ml) is added, temperature control 37 ± 2 DEG C, lucifuge reaction 10-14h;
Step 2: prepared by AA 2G crude product
(1) react complete, blowing, with tap water washing reaction still (1), reaction solution and kettle washing water are merged, weighs, and centrifugal by whizzer (4), again wash whizzer (4) with tap water;
(2) filtrate obtained is carried out ultrafiltration by the first filtration unit (5), with tap water in ultra-filtration process, and wash with tap water top, control temperature is lower than 30 DEG C;
(3) ultrafiltrated is passed through the first resin column, resin elution liquid is adsorbed in the second resin column;
(4) rinse the first resin column with tap water, and elutriant is adsorbed in the second resin column;
(5) with NaCl solution wash-out resin, by elutriant by the first resin column, and be eluted to product-free outflow with tap water, merge all elutriants;
(6) elutriant merged is passed through the second filtration unit, then with tap water washing, finally concentrate, wash with tap water top; Transferred to by nanofiltration liquid in reactor (1), reduce pressure during temperature≤50 DEG C, vacuum tightness≤-0.1MPa, concentrated, being concentrated into AA 2G content is 55%-60%;
(7) in concentrated solution, methyl alcohol is added, stirring and dissolving; Then be cooled to 10-15 DEG C, and in 10-15 insulated and stirred 4-5 hour, continue at 1-2 hour and cool to 0-5 DEG C, then in 0-5 DEG C of insulated and stirred 4-5 hour;
(8) crystallization is complete, and blowing is centrifugal, centrifugal to dripless outflow, by methanol wash, centrifugal to dripless outflow, continues centrifugal, obtains AA 2G crude product;
Step 3: AA 2G crude product refining
(1) in reactor (1), add purified water, then add AA 2G crude product, open and stir;
Hot water controls warm 35-45 DEG C in still, and stirring and dissolving, adds gac, insulated and stirred 30min;
(2) solution in reactor (1) is passed through the 3rd filtration unit while hot, filtrate is weighed, censorship AA 2G content;
(3) AA 2G filtrate is added in reactor (1), concentrating under reduced pressure, temperature control≤50 DEG C, vacuum tightness≤-0.09Mpa; Being concentrated into AA 2G content in solution is 67% ± 1%;
(4) concentrated complete, control still temperature 38-45 DEG C, add crystal seed, stir, then leave standstill slow crystallization, slow cooling 5h, after temperature is down to 35 DEG C, programmed cooling, to 5-10 DEG C, is opened and is stirred, then 5-10 DEG C of insulation crystallization;
(5) crystallization is complete, and blowing is centrifugal, centrifugally to spray drip washing with frozen water after dripless flows out, and continues centrifugal, centrifugally after dripless flows out, continues centrifugal 30min, and discharging obtains AA 2G fine work wet product;
(6) centrifugal complete gained AA 2G wet product is placed in vacuum drying oven drying, temperature control≤50 DEG C, vacuum tightness <-0.1Mpa; Dry complete, obtain AA 2G fine work.
Advantageous Effects of the present invention:
The invention provides a kind of process system of Enzyme catalyzed synthesis AA 2G, employing ultrafilter can remove the enzyme in reaction solution, positive resin post is adopted to remove sodium ion, with negative resin post adsorption production, concentrating through nanofiltration through wash-out, elutriant, can molecular weight cut-off be the products molecule of 300-400 again.The present invention adopts collecting and filtering apparatus, can remove the impurity such as vitamins C, glucose.The present invention avoids using high temperature concentration method, and due to long-time high temperature, product can be degraded affects quality, and the present invention adopts falling film concentrating device, can rapid concentration at a lower temperature, guarantees quality product.The present invention adopts methanol plus water mixed solvent as AA 2G crystallization solvent, and Crystallization Process adopts program crystallization, and the AA 2G crystal habit stable and uniform of precipitation, impurity is few, and product purity is high.
Accompanying drawing explanation
Fig. 1 is schematic diagram of the present invention.
Embodiment
Below in conjunction with specific embodiment, set forth the present invention further.Should be understood that these embodiments are only not used in for illustration of the present invention to limit the scope of the invention.
Embodiment 1
As Fig. 1, a process system for Enzyme catalyzed synthesis AA 2G, is characterized by: comprise reactor 1, enzyme basin 2, basin 3, whizzer 4, first filtration unit 5, first resin column 6, second resin column 7, second filtration unit 8, falling film concentrating device 9, the 3rd filtration unit 10, discharge port 11; The first described filtration unit 5 is positioned at the described upstream of the first resin column 6, the downstream of this first resin column 6 is the second described resin column 7, described second filtration unit 8 is positioned at the downstream of this second resin column 7, and described falling film concentrating device 9 is positioned at the downstream of this second filtration unit 8; Described 3rd filtration unit 10 is positioned at the downstream of this falling film concentrating device 9; Described whizzer 4 has many groups, respectively in the upstream of the first described filtration unit 5, the described upstream of the 3rd filtration unit 10 and the downstream of described falling film concentrating device 9;
In the present embodiment, the first filtration unit 5 adopts ultrafilter, and described second filtration unit 8 adopts collecting and filtering apparatus, and described filtration unit (10) is titanium rod filtration unit, forms in this titanium rod filtration unit by organizing titanium rod filter core more.Described the first resin column (6) is positive resin post, and described the second resin column (7) is negative resin post, and described whizzer (4) is butterfly centrifugal machine.Described production line has three, and between the resin column (6) in every bar production line, pipeline is connected in parallel.Described basin (3) has many groups, is positioned over the downstream of described reactor (1), the first filtration unit (5), the first resin column (6), the second resin column (7), the second filtration unit (8), falling film concentrating device (9), the 3rd filtration unit (10) respectively.
Embodiment 2
In 1000L reactor, add tap water 20KG, then add vitamins C 6.5KG, stir; Temperature 37 DEG C in reactor is controlled with hot water; PH to 5.4 is adjusted with 30%NaOH solution; In reactor, add beta-cyclodextrin 14KG, then add CGT enzyme 4.0KG, add tap water and make system quantitatively to 65KG; Control reactor temperature 37 ± 2 DEG C, lucifuge reaction 10h; Add saccharifying enzyme (enzyme liquid 750,000 U/ml) 70g, temperature control 37 ± 2 DEG C, lucifuge reaction 10h.
React complete, blowing, with tap water 2.0KG washing reaction still, reaction solution and kettle washing water are merged, weighs, and centrifugal by butterfly centrifugal machine, wash whizzer with tap water 2.0KG; The filtrate obtained is carried out ultrafiltration by ultrafilter, and with tap water 30.0KG ultrafiltration in ultra-filtration process, and wash with tap water 2.0KG top, control temperature is lower than 30 DEG C; By ultrafiltrated by positive resin post, positive resin elutriant is adsorbed in negative resin post; Rinse positive resin post with tap water, and elutriant is adsorbed in negative resin post; With 0.03mol/L sodium chloride solution 100.0KG wash-out negative resin; With 0.2mol/L sodium chloride solution 100.0KG wash-out negative resin, by elutriant by positive resin post, and be eluted to product-free outflow with tap water 100.0KG, merge all elutriants; The elutriant merged by collecting and filtering apparatus, then with tap water 30.0KG washing, be finally concentrated into 20KG, wash with tap water 2.0KG top; Transfer in reactor by nanofiltration liquid, temperature reduces pressure 50 DEG C time, and concentrated during vacuum tightness≤-0.1MPa, being concentrated into product content is 55%; In concentrated solution, add methyl alcohol 30.0KG, stirring and dissolving, be then cooled to 10 DEG C, and in 10 DEG C of insulated and stirred 4 hours, be cooled to 0 DEG C, insulated and stirred carried out crystallization in 4 hours; Crystallization is complete, and blowing is centrifugal, centrifugal to dripless flow out after, wash with methyl alcohol 5.0KG, centrifugal to dripless outflow after, continue centrifugal 30min, obtain AA 2G wet product 4.0KG.
In 20L reactor, add purified water 8.0KG, then add AA 2G wet product 4.0KG, open and stir; Control temperature 40 DEG C in reactor with hot water, stirring and dissolving, adds gac 60.0g, insulated and stirred 30min; By solution in reactor while hot by titanium rod filtration unit, AA 2G filtrate is added in 20L falling film concentrating device, concentrating under reduced pressure, temperature control≤50 DEG C, vacuum tightness-0.09MPa; Being concentrated into AA 2G content in solution is 67% ± 1%; Concentrated complete, control temperature 40 DEG C in falling film concentrating device, add 25g crystal seed, stir 0.5min, then leave standstill slow crystallization, after temperature is down to 35 DEG C, programmed cooling to 5 DEG C, opens and stirs, then 5 DEG C of insulation crystallization 1h; Crystallization is complete, and blowing is centrifugal, centrifugal flow out to dripless after with 0.25KG frozen water spraying drip washing, continue centrifugal, centrifugally after dripless flows out, continue centrifugal 30min, discharging obtains AA 2G fine work wet product; AA 2G fine work wet product is placed in vacuum drying oven dry, temperature control≤50 DEG C, vacuum tightness-0.09MPa, dry complete, obtain AA 2G fine work 1.65KG.
Embodiment 3
In 1000L reactor, add tap water 20KG, then add vitamins C 6.5KG, stir; Temperature 37 DEG C in reactor is controlled with hot water; PH to 5.4 is adjusted with 30%NaOH solution; In reactor, add beta-cyclodextrin 14KG, then add CGT enzyme 4.0KG, add tap water and make system quantitatively to 65KG; Control reactor temperature 37 ± 2 DEG C, lucifuge reaction 10h; Add saccharifying enzyme (enzyme liquid 750,000 U/ml) 70g, temperature control 37 ± 2 DEG C, lucifuge reaction 14h.
React complete, blowing, with tap water 2.0KG washing reaction still, reaction solution and kettle washing water are merged, weighs, and centrifugal by butterfly centrifugal machine, wash whizzer with tap water 2.0KG; The filtrate obtained is carried out ultrafiltration by ultrafilter, and with tap water 30.0KG ultrafiltration in ultra-filtration process, and wash with tap water 2.0KG top, control temperature is lower than 30 DEG C; By ultrafiltrated by positive resin post, positive resin elutriant is adsorbed in negative resin post; Rinse positive resin post with tap water, and elutriant is adsorbed in negative resin post; With 0.03mol/L sodium chloride solution 100.0KG wash-out negative resin; With 0.2mol/L sodium chloride solution 100.0KG wash-out negative resin, by elutriant by positive resin post, and be eluted to product-free outflow with tap water 100.0KG, merge all elutriants; The elutriant merged by collecting and filtering apparatus, then with tap water 30.0KG washing, be finally concentrated into 40KG, wash with tap water 2.0KG top; Transfer in reactor by nanofiltration liquid, temperature reduces pressure 50 DEG C time, and concentrated during vacuum tightness≤-0.01MPa, being concentrated into product content is 60%; In concentrated solution, add methyl alcohol 30.0KG, stirring and dissolving, be then cooled to 10 DEG C, and in 10 DEG C of insulated and stirred 4 hours, be cooled to 5 DEG C, insulated and stirred carried out crystallization in 5 hours; Crystallization is complete, and blowing is centrifugal, centrifugal to dripless flow out after, wash with methyl alcohol 5.0KG, centrifugal to dripless outflow after, continue centrifugal 30min, obtain AA 2G wet product 4.0KG.
In 20L reactor, add purified water 8.0KG, then add AA 2G wet product 4.0KG, open and stir; Control temperature 40 DEG C in reactor with hot water, stirring and dissolving, adds gac 60.0g, insulated and stirred 30min; By solution in reactor while hot by titanium rod filtration unit, AA 2G filtrate is added in 20L falling film concentrating device, concentrating under reduced pressure, temperature control≤50 DEG C, vacuum tightness-0.09MPa; Being concentrated into AA 2G content in solution is 67% ± 1%; Concentrated complete, control temperature 40 DEG C in falling film concentrating device, add 25g crystal seed, stir 0.5min, then leave standstill slow crystallization, after temperature is down to 35 DEG C, programmed cooling to 10 DEG C, opens and stirs, then 5 DEG C of insulation crystallization 1h; Crystallization is complete, and blowing is centrifugal, centrifugal flow out to dripless after with 0.25KG frozen water spraying drip washing, continue centrifugal, centrifugally after dripless flows out, continue centrifugal 30min, discharging obtains AA 2G fine work wet product; AA 2G fine work wet product is placed in vacuum drying oven dry, temperature control≤50 DEG C, vacuum tightness≤-0.09MPa, dry complete, obtain AA 2G fine work 2.0KG.
Embodiment 4
In 1000L reactor, add tap water 20KG, then add vitamins C 6.5KG, stir; Temperature 37 DEG C in reactor is controlled with hot water; PH to 5.4 is adjusted with 30%NaOH solution; In reactor, add beta-cyclodextrin 14KG, then add CGT enzyme 4.0KG, add tap water and make system quantitatively to 65KG; Control reactor temperature 37 ± 2 DEG C, lucifuge reaction 11h; Add saccharifying enzyme (enzyme liquid 750,000 U/ml) 70g, temperature control 37 ± 2 DEG C, lucifuge reaction 12h.
React complete, blowing, with tap water 2.0KG washing reaction still, reaction solution and kettle washing water are merged, weighs, and centrifugal by butterfly centrifugal machine, wash whizzer with tap water 2.0KG; The filtrate obtained is carried out ultrafiltration by ultrafilter, and with tap water 30.0KG ultrafiltration in ultra-filtration process, and wash with tap water 2.0KG top, control temperature is lower than 30 DEG C; By ultrafiltrated by positive resin post, positive resin elutriant is adsorbed in negative resin post; Rinse positive resin post with tap water, and elutriant is adsorbed in negative resin post; With 0.03mol/L sodium chloride solution 100.0KG wash-out negative resin; With 0.2mol/L sodium chloride solution 100.0KG wash-out negative resin, by elutriant by positive resin post, and be eluted to product-free outflow with tap water 100.0KG, merge all elutriants; The elutriant merged by collecting and filtering apparatus, then with tap water 30.0KG washing, be finally concentrated into 35KG, wash with tap water 2.0KG top; Transfer in reactor by nanofiltration liquid, temperature reduces pressure 50 DEG C time, and concentrated during vacuum tightness≤-0.01MPa, being concentrated into product content is 60%; In concentrated solution, add methyl alcohol 30.0KG, stirring and dissolving, be then cooled to 10 DEG C, and in 10 DEG C of insulated and stirred 4 hours, be cooled to 8 DEG C, insulated and stirred carried out crystallization in 5 hours; Crystallization is complete, and blowing is centrifugal, centrifugal to dripless flow out after, wash with methyl alcohol 5.0KG, centrifugal to dripless outflow after, continue centrifugal 30min, obtain AA 2G wet product 4.0KG.
In 20L reactor, add purified water 8.0KG, then add AA 2G wet product 4.0KG, open and stir; Control temperature 40 DEG C in reactor with hot water, stirring and dissolving, adds gac 60.0g, insulated and stirred 30min; By solution in reactor while hot by titanium rod filtration unit, AA 2G filtrate is added in 20L falling film concentrating device, concentrating under reduced pressure, temperature control 48 DEG C, vacuum tightness-0.09MPa; Being concentrated into AA 2G content in solution is 67% ± 1%; Concentrated complete, control temperature 40 DEG C in falling film concentrating device, add 25g crystal seed, stir 0.5min, then leave standstill slow crystallization, after temperature is down to 38 DEG C, programmed cooling to 6 DEG C, opens and stirs, then 7 DEG C of insulation crystallization 1h; Crystallization is complete, and blowing is centrifugal, centrifugal flow out to dripless after with 0.25KG frozen water spraying drip washing, continue centrifugal, centrifugally after dripless flows out, continue centrifugal 30min, discharging obtains AA 2G fine work wet product; AA 2G fine work wet product is placed in vacuum drying oven dry, temperature control 48 DEG C, vacuum tightness-0.09MPa, dry complete, obtain AA 2G fine work 1.50KG.
Present specification describes some embodiments, but should be understood that those skilled in the art pass through to read this specification sheets and can know the various improvement not deviating from the spirit and scope of the present invention.Therefore, these other embodiments also should be included within the scope of appended claims.
Claims (6)
1. a process system for Enzyme catalyzed synthesis AA 2G, is characterized by: comprise reactor (1), enzyme basin (2), basin (3), whizzer (4), the first filtration unit (5), the first resin column (6), the second resin column (7), the second filtration unit (8), falling film concentrating device (9), the 3rd filtration unit (10); Described the first filtration unit (5) is positioned at the upstream of described first resin column (6), the downstream of this first resin column (6) is described the second resin column (7), described second filtration unit (8) is positioned at the downstream of this second resin column (7), and described falling film concentrating device (9) is positioned at the downstream of this second filtration unit (8); Described 3rd filtration unit (10) is positioned at the downstream of this falling film concentrating device (9); Described whizzer (4) has many groups, respectively in the upstream of described the first filtration unit (5), the described upstream of the 3rd filtration unit (10) and the downstream of described falling film concentrating device (9).
2. the process system of Enzyme catalyzed synthesis AA 2G according to claim 1, it is characterized in that, described the first filtration unit (5) is ultrafilter, described second filtration unit (8) is collecting and filtering apparatus, institute's three filtration units (10) is titanium rod filtration unit, forms in this titanium rod filtration unit by organizing titanium rod filter core more.
3. the process system of Enzyme catalyzed synthesis AA 2G according to claim 1, is characterized in that, described the first resin column (6) is positive resin post, and described the second resin column (7) is negative resin post; Described whizzer (4) is butterfly centrifugal machine.
4. the process system of Enzyme catalyzed synthesis AA 2G according to claim 1, is characterized by: described production line has three, and between the resin column (6) in every bar production line, pipeline is connected in parallel.
5. the process system of Enzyme catalyzed synthesis AA 2G according to claim 1, it is characterized by: described basin (3) has many groups, be positioned over the downstream of described reactor (1), the first filtration unit (5), the first resin column (6), the second resin column (7), the second filtration unit (8), falling film concentrating device (9), the 3rd filtration unit (10) respectively.
6. a processing method for Enzyme catalyzed synthesis AA 2G as claimed in claim 1, is characterized by: comprise the following steps:
Step one: enzyme reaction
(1) in reactor (1), add tap water, then add vitamins C, open and stir;
(2) hot water controls temperature 37 DEG C in described reactor (1), adjusts pH to 5.50 ± 0.10 with 30%NaOH solution;
(3) in described reactor (1), beta-cyclodextrin is added;
(4) add Maltose 4-glucosyltransferase again, add tap water and make system quantitative;
(5) the interior temperature in the kettle of this reactor (1) 37 ± 2 DEG C is controlled, lucifuge reaction 10-12h;
(6) after reacting 1 end, saccharifying enzyme (enzyme liquid 750,000 U/ml) is added, temperature control 37 ± 2 DEG C, lucifuge reaction 10-14h;
Step 2: prepared by AA 2G crude product
(1) react complete, blowing, with tap water washing reaction still (1), reaction solution and kettle washing water are merged, weighs, and centrifugal by whizzer (4), again wash whizzer (4) with tap water;
(2) filtrate obtained is carried out ultrafiltration by the first filtration unit (5), with tap water in ultra-filtration process, and wash with tap water top, control temperature is lower than 30 DEG C;
(3) ultrafiltrated is passed through the first resin column (6), elutriant is adsorbed in the second resin column (7);
(4) rinse the first resin column (6) with tap water, and elutriant is adsorbed in the second resin column (7);
(5) with sodium chloride solution wash-out resin, by elutriant by the first resin column (6), and be eluted to product-free outflow with tap water, merge all elutriants;
(6) elutriant merged is passed through the second filtration unit (8), then with tap water washing, finally concentrate, wash with tap water top; Transferred to by nanofiltration liquid in reactor (1), reduce pressure during temperature≤50 DEG C, concentrated during vacuum tightness≤-0.1MPa, being concentrated into AA 2G content is 55%-60%;
(7) in concentrated solution, methyl alcohol is added, stirring and dissolving; Then be cooled to 10-15 DEG C, and in 10-15 insulated and stirred 4-5 hour, continue at 1-2 hour and cool to 0-5 DEG C, then in 0-5 DEG C of insulated and stirred 4-5 hour;
(8) crystallization is complete, and blowing is centrifugal, centrifugal to dripless outflow, by methanol wash, centrifugal to dripless outflow, continues centrifugal, obtains AA 2G crude product;
Step 3: AA 2G crude product refining
(1) in reactor (1), add purified water, then add AA 2G crude product, open and stir;
Hot water controls warm 35-45 DEG C in still, and stirring and dissolving, adds gac, insulated and stirred 30min;
(2) solution in reactor (1) is passed through the 3rd filtration unit (10) while hot, filtrate is weighed, censorship AA 2G content;
(3) AA 2G filtrate is added in reactor (1), concentrating under reduced pressure, temperature control≤50 DEG C, vacuum tightness >=-0.09Mpa; Being concentrated into AA 2G content in solution is 67% ± 1%;
(4) concentrated complete, control still temperature 38-45 DEG C, add crystal seed, stir, then leave standstill slow crystallization, slow cooling 5h, after temperature is down to 35 DEG C, programmed cooling, to 5-10 DEG C, is opened and is stirred, then 5-10 DEG C of insulation crystallization;
(5) crystallization is complete, and blowing is centrifugal, centrifugally to spray drip washing with frozen water after dripless flows out, and continues centrifugal, centrifugally after dripless flows out, continues centrifugal 30min, and discharging obtains AA 2G fine work wet product;
(6) centrifugal complete gained AA 2G wet product is dry, temperature control≤50 DEG C, vacuum tightness <-0.1Mpa; Dry complete, obtain AA 2G fine work.
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