CN107382713A - A kind of technique of purification of lactic acid - Google Patents
A kind of technique of purification of lactic acid Download PDFInfo
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- CN107382713A CN107382713A CN201710762389.7A CN201710762389A CN107382713A CN 107382713 A CN107382713 A CN 107382713A CN 201710762389 A CN201710762389 A CN 201710762389A CN 107382713 A CN107382713 A CN 107382713A
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
- C07C51/42—Separation; Purification; Stabilisation; Use of additives
- C07C51/47—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
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Abstract
The invention discloses a kind of technique of purification of lactic acid, for object be calcium salt method production L lactic fermentation liquids, step is：（1）The lactic fermentation liquid for removing thalline and solia particle is concentrated, acidolysis；（2）Lactic acid feed liquid after acidolysis filtering enters continuous moving column system, is decolourized and removes calcium sulfate and other foreign ions；（3）Lactic acid feed liquid is concentrated to give fine purification of lactic acid through nanofiltration membrane.The technique of the present invention, using continuous moving column technology, can effectively solve the blockage problem of NF membrane, the step of avoiding the rapid wear consumptive material matter filtration residue calcium sulfate such as micro-filtration, milipore filter, reduce production process.Compared with traditional ion-exchange process, the dosage of resin reduces 50%~80%, and washing water consumption can reduce 50%~70%, regenerant consumption is also accordingly reduced, production cost and the pollution to environment are greatly reduced, obtained lactic product purity is up to more than 95%, and the rate of recovery is up to more than 90%.
Description
Technical field
The present invention relates to breast in a kind of technique of purification of lactic acid, more particularly to the Pfansteihl zymotic fluid of purification calcium salt method production
The technique of acid, belongs to lactic acid extractive technique field.
Background technology
In the lactic fermentation liquid of fermentation method production, due to containing various inorganic salts, residual sugar, other small molecular organic acids, amino
The impurity such as acid, protein, pigment, colloid, it is more difficult to separate.And nanofiltration is pressure-actuated membrane separating process, membrane aperture model
Be trapped among several rans, can the impurity such as deproteination, polypeptide, divalent salts, be precisely separated monose and polysaccharide, monovalent salt and multivalence
Salt, the effect that traditional handicraft is unable to reach is realized, and energy consumption is low, floor space is small, and operating procedure is simple, environmentally friendly.But
The fermentation overwhelming majority of Pfansteihl is using calcium carbonate as nertralizer, and a small amount of sulfuric acid still can be remained after product acidolysis filtering
Calcium.The bad phenomenon of refining effect is caused in order to avoid blocking NF membrane, generally there are two methods, first, applying traditional ion
Switching equipment directly removes the calcium sulfate of residual, and the method can consume a large amount of resins, and resin regeneration can produce a large amount of waste water simultaneously；
Second, micro-filtration or the film combination of ultrafiltration and nanofiltration, add production process, and film belongs to loss material, it is necessary to periodically more
Change；It can be seen that both approaches all improve cost.In addition, in patent CN101234962A, lactic fermentation liquid is directly connected
Continuous anion exchange procedures, can not effectively remove the calcium ion of fermentation process introducing, and can equally consume the consumption such as a large amount of resins
Material, cost greatly improve, and are not particularly suited for calcium salt method production Pfansteihl.Therefore, a kind of low cost is found, the lactic acid of low stain carries
Pure technique is that current needs urgently solve the problems, such as.
The content of the invention
For above-mentioned prior art, the invention provides a kind of technique of purification of lactic acid, for object be calcium salt method life
The Pfansteihl zymotic fluid of production.
The present invention is achieved by the following technical solutions：
A kind of technique of purification of lactic acid, comprises the following steps：
（1）The Pfansteihl zymotic fluid of calcium salt method production, centrifuges or filters off except thalline and solia particle（Conventional method）, carry out dense
Contracting, acidolysis, decolouring（Conventional method）, the lactic acid feed liquid after must decolourizing；
（2）Lactic acid feed liquid after above-mentioned decolouring enters continuous moving column system, and calcium sulfate and its are remained to remove after acidolysis is filtered
Its foreign ion；
（3）Lactic acid feed liquid after above-mentioned processing, through nanofiltration membrane, concentration, obtain fine purification of lactic acid.
Further, the step（2）In, continuous moving column system is composed in series by 30 resin columns, previous resin
The bottom of post at the top of latter resin column with being serially connected；Resin pole unit（The resin column of 30 series connection）One is put into turn
On disk, switching is realized by the rotation of rotating disk, and material is controlled by an automatic rotary distributor, and resin column is divided into exchange
The functional areas such as area, water wash zone, renewing zone, elution area, corresponding technical process is carried out when resin unit reaches designated area；
After filtrate enters exchange area, exchanged by one-level, efflux is lactic acid solution, and the salt ion in filtrate is adsorbed on resin
It is interior；Now resin pole unit is moved into water wash zone and washed, and remaining lactic acid feed liquid is ejected inside resin column, and efflux is with handing over
Change region effluent together into exchange area two, three, level Four exchange, so guarantee feed liquid foreign ion all adsorbed；Inhaled
The resin unit of attached saturation is washed by two level, ensures that feed liquid is washed with water totally；Resin column is now moved into renewing zone, pickling again
Or alkali cleaning carries out resin regeneration, regenerated by three-level and cause resin to recover switching performance completely；Resin by regeneration is through filtering
Wash and enter exchange area, the circulation synchronous that so goes round and begins again switching is carried out, and in time by resin regeneration, is improved the utilization rate of resin, is prevented
Only resin aging, regeneration are difficult, while washings and regenerant consumption greatly reduce, and greatly reduce production of lactic acid cost.
Further, resin is filled with the resin column, wherein, 15 load styrene or acrylic acid（Ester）It is strong acid
Cationic ion-exchange resin, 15 load styrene or acrylic acid in addition（Ester）It is strong basic anion-exchange resin, particle diameter is 0.4~
0.6mm, particle voids rate 50%；Cationic ion-exchange resin water content 40%~60%, it is wet regarding 0.60~0.86g/mL of index, it is wet true
1.05~1.30g/mL of index, expansion rate 10%~15%；Anion exchange resin water content 40%~60%, it is wet regard index 0.56~
0.74g/mL, 1.05~1.21g/mL of wet true index, expansion rate 20%~25%.
Further, the specific workflow of " lactic acid feed liquid enters continuous moving column system " is：First pass through and be filled with by force
The resin column of acid positive resin, discharge by the resin column for being filled with strong basicity negative resin, then discharging is continued back to filling
The resin column for having highly acid sulphur resin continues to remove cation impurity, and discharging again returns to the resin for being filled with strong basicity negative resin
Post continues to remove anionic impurity, you can reaches the purity of the lactic acid feed liquid subsequent technique required in production.In cation exchange
In the resin container of system, for the cation such as sodium, magnesium, calcium with the hydrogen ion on resin by exchanging, effluent enters anion exchange
In the resin container of system, chlorion, sulfate radical plasma are with the hydroxide ion on resin by exchanging.
Further, the input concentration of lactic acid feed liquid is 18%~27%（Mass concentration）, positive resin lactic acid material handling capacity
For 6~8 times of resin volume；Negative resin lactic acid material handling capacity is 20~25 times of resin volume；Resin used in pickling is again
Raw liquid is concentration 30%（Mass concentration）HCl solution, dosage be lactic acid feed liquid treating capacity 2%~3%；Resin used in alkali cleaning
Regenerated liquid is concentration 32%（Mass concentration）NaOH solution, dosage be lactic acid feed liquid treating capacity 1%~2%；Washing water consumption is
The 40%~55% of lactic acid feed liquid treating capacity.
Further, the step（3）In, lactic acid feed liquid concentrates after nanofiltration membrane to filtrate, in evaporator
100~120 DEG C, 8000~12000Pa of absolute pressure of portion's temperature, in the condensed Posterior circle of acid solution that this process portion is distillated extremely
Continuous moving post exchange system.Resulting lactic product after concentration detects through HPLC, the final purity of lactic acid 95.3%~
96.7%, the lactic acid rate of recovery is up to 91.2%~92.7%.
The technique of the present invention, using continuous moving column technology, can effectively solve the blockage problem of NF membrane, avoid calcium salt
While method produces L lactic acid application NF membranes, the step of the rapid wear consumptive material matter filtration residue calcium sulfate such as micro-filtration, milipore filter need to be used
Suddenly, production process is reduced.The technique of the present invention compared with traditional ion-exchange process, the dosage of resin reduces 50%~
80%, washing water consumption can reduce 50%~70%, and regenerant consumption is also accordingly reduced, and greatly reduces production cost and to ring
The pollution in border, obtained lactic product purity is up to more than 95%, and the rate of recovery is up to more than 90%.
Brief description of the drawings
Fig. 1：The process flow diagram of the purification of lactic acid of the present invention.
Fig. 2：Standard lactic acid reference substance HPLC analysis detection figures.
Fig. 3：Outturn sample HPLC analysis detection figures.
Fig. 4：Standard lactic acid reference substance HPLC analysis detection figures.
Fig. 5：Outturn sample HPLC analysis detection figures.
Fig. 6：Standard lactic acid reference substance HPLC analysis detection figures.
Fig. 7：Outturn sample HPLC analysis detection figures.
Embodiment
With reference to embodiment, the present invention is further illustrated.
Involved instrument, reagent, material etc. in following embodiments, it is existing in the prior art unless otherwise noted
Conventional instrument, reagent, material etc., can be obtained by regular commercial sources.Involved experimental method in following embodiments, inspection
Survey method etc., it is existing normal experiment method, detection method etc. in the prior art unless otherwise noted.
The purification of the Pfansteihl Lactic Acid from Fermentation Broth of the calcium salt method of embodiment 1 production
By the lactic fermentation liquid for using calcium salt method fermenting and producing through centrifuging or filtering off except thalline and solia particle, zymotic fluid warp
The concentration of lactic acid is set to rise to 20%~30% after concentration, subsequently into acid hydrolysis tank, the sulfuric acid of addition 30% under conditions of 70~80 DEG C
Acidolysis is carried out, using ammonium oxalate and barium chloride reagent as indicator, after reaction terminates, stirs 4~5 hours, is formed to calcium sulfate
Flaky crystal, start using band filter or flame filter press filtering, washing.Feed liquid after acidolysis is sent into decolorizing column, taken off
Feed liquid after color is with 10m3/ h sloughs foreign ion into continuous moving post, and simultaneously removes the calcium sulfate remained in feed liquid
Remove；Lactic acid feeding liquid concentration is 21%, and resin used is styrene or acrylic acid（Ester）It is strong-acid cation-exchange resin and benzene second
Alkene or acrylic acid（Ester）It is strong basic anion-exchange resin, particle diameter 0.5mm, particle voids rate 50%.Cationic ion-exchange resin contains
Water 50%, it is wet regarding index 0.86g/mL, wet true index 1.30g/mL, expansion rate 15%；Anion exchange resin water content 55%,
It is wet to regard index 0.74g/mL, wet true index 1.21g/mL, expansion rate 25%.The flow for the HCl that resin regeneration liquid concentration is 30% is
230L/h, the flow that concentration is 32%NaOH are 110L/h, and washing water-carrying capacity is 5.2m3/h.Lactic acid feed liquid needs to use 2 sets
Continuous moving column system is used with, and each 15 of negative and positive post, idiographic flow, which first passes through, is filled with strong acid positive resin, and discharging passes through filling
There is strong basicity negative resin, then discharging continued back to and is filled with highly acid sulphur resin and continues to remove cation impurity, discharging is again
Strong basicity negative resin is returned to continue to can reach the lactic acid feed liquid subsequent technique for producing and requiring after removing anionic impurity
Purity.In the resin container of cation exchange system, the cation such as sodium, magnesium, calcium, by exchanging, flows out with the hydrogen ion on resin
Thing enters in the resin container of anion exchange system, and chlorion, sulfate radical plasma are with the hydroxide ion on resin by handing over
Change.Feed liquid after the processing of continuous moving post filters through nano filter membrance device, and NF membrane is usually rolling, and molecular cut off is
250D, operating pressure 0.3bar, it is 3.0MPa to enter film pressure, and it is 2.8Mpa, membrane flux 16L/m to go out film pressure2.h.Through nanofiltration
Lactic acid feed liquid after film is refined is sent into evaporator and concentrated, absolute pressure 8000Pa, and temperature is 120 DEG C, the acid solution distillated
Condensed Posterior circle is to continuous moving post exchange system.Resulting lactic product after concentration detects through HPLC, and lactic acid is finally pure
Degree is 95.3%, and the lactic acid rate of recovery is up to 91.2%.
Product HPLC analysis detection figures are shown in Fig. 2, Fig. 3.
Embodiment 2
By the lactic fermentation liquid for using calcium salt method fermenting and producing through centrifuging or filtering off except thalline and solia particle, zymotic fluid warp
The concentration of lactic acid is set to rise to 20%~30% after concentration, subsequently into acid hydrolysis tank, the sulfuric acid of addition 30% under conditions of 70~80 DEG C
Acidolysis is carried out, using ammonium oxalate and barium chloride reagent as indicator, after reaction terminates, stirs 4~5 hours, is formed to calcium sulfate
Flaky crystal, start using band filter or flame filter press filtering, washing.Feed liquid after acidolysis is sent into decolorizing column, taken off
Feed liquid after color is with 13m3/ h sloughs foreign ion into continuous moving post, and simultaneously removes the calcium sulfate remained in feed liquid
Remove；Lactic acid feeding liquid concentration is 21%, and resin used is styrene or acrylic acid（Ester）It is strong-acid cation-exchange resin and benzene second
Alkene or acrylic acid（Ester）It is strong basic anion-exchange resin, particle diameter 0.5mm, particle voids rate 50%.Cationic ion-exchange resin contains
Water 50%, it is wet regarding index 0.86g/mL, wet true index 1.30g/mL, expansion rate 15%；Anion exchange resin water content 55%,
It is wet to regard index 0.74g/mL, wet true index 1.21g/mL, expansion rate 25%.The flow for the HCl that resin regeneration liquid concentration is 30% is
260L/h, the flow that concentration is 32%NaOH are 170L/h, and washing water-carrying capacity is 7.2m3/h.Lactic acid feed liquid needs to use 2 sets
Continuous moving column system is used with, and each 15 of negative and positive post, idiographic flow, which first passes through, is filled with strong acid positive resin, and discharging passes through filling
There is strong basicity negative resin, then discharging continued back to and is filled with highly acid sulphur resin and continues to remove cation impurity, discharging is again
Strong basicity negative resin is returned to continue to can reach the lactic acid feed liquid subsequent technique for producing and requiring after removing anionic impurity
Purity.In the resin container of cation exchange system, the cation such as sodium, magnesium, calcium, by exchanging, flows out with the hydrogen ion on resin
Thing enters in the resin container of anion exchange system, and chlorion, sulfate radical plasma are with the hydroxide ion on resin by handing over
Change.Feed liquid after the processing of continuous moving post filters through nano filter membrance device, and NF membrane is rolling, molecular cut off 250D, is grasped
It is 0.3bar to make pressure, and it is 3.0MPa to enter film pressure, and it is 2.8Mpa, membrane flux 16L/m to go out film pressure2.h.Refined through NF membrane
Lactic acid feed liquid afterwards is sent into evaporator and concentrated, absolute pressure 8000Pa, and temperature is 120 DEG C, and the acid solution distillated is condensed
Posterior circle is to continuous moving post exchange system.Resulting lactic product after concentration detects through HPLC to be surveyed, and the final purity of lactic acid exists
95.6%, the lactic acid rate of recovery is up to 91.7%.
Product HPLC analysis detection figures are shown in Fig. 4, Fig. 5.
Embodiment 3
By the lactic fermentation liquid for using calcium salt method fermenting and producing through centrifuging or filtering off except thalline and solia particle, zymotic fluid warp
The concentration of lactic acid is set to rise to 20%~30% after concentration, subsequently into acid hydrolysis tank, the sulfuric acid of addition 30% under conditions of 70~80 DEG C
Acidolysis is carried out, using ammonium oxalate and barium chloride reagent as indicator, after reaction terminates, 3-4 hours is stirred, piece is formed to calcium sulfate
Shape crystallizes, and starts using band filter or flame filter press filtering, washing.Feed liquid after acidolysis is sent into decolorizing column, decolourized
Feed liquid afterwards is with 15m3/ h sloughs foreign ion into continuous moving post, and simultaneously removes the calcium sulfate remained in feed liquid；
Lactic acid feeding liquid concentration is 21%, and resin used is styrene or acrylic acid（Ester）It is strong-acid cation-exchange resin and styrene
Or acrylic acid（Ester）It is strong basic anion-exchange resin, particle diameter 0.5mm, particle voids rate 50%.Cationic ion-exchange resin is aqueous
Amount 50%, it is wet regarding index 0.86g/mL, wet true index 1.30g/mL, expansion rate 15%；Anion exchange resin water content 55%, it is wet
Depending on index 0.74g/mL, wet true index 1.21g/mL, expansion rate 25%.The flow for the HCl that resin regeneration liquid concentration is 30% is
300L/h, the flow that concentration is 32%NaOH are 110L/h, and washing water-carrying capacity is 8.3m3/h.Lactic acid feed liquid needs to use 2 sets
Continuous moving column system is used with, and each 15 of negative and positive post, idiographic flow, which first passes through, is filled with strong acid positive resin, and discharging passes through filling
There is strong basicity negative resin, then discharging continued back to and is filled with highly acid sulphur resin and continues to remove cation impurity, discharging is again
Strong basicity negative resin is returned to continue to can reach the lactic acid feed liquid subsequent technique for producing and requiring after removing anionic impurity
Purity.In the resin container of cation exchange system, the cation such as sodium, magnesium, calcium, by exchanging, flows out with the hydrogen ion on resin
Thing enters in the resin container of anion exchange system, and chlorion, sulfate radical plasma are with the hydroxide ion on resin by handing over
Change.Feed liquid after the processing of continuous moving post filters through nano filter membrance device, and NF membrane is usually rolling, and molecular cut off is
250D, operating pressure 0.3bar, it is 3.0MPa to enter film pressure, and it is 2.8Mpa, membrane flux 16L/m to go out film pressure2.h.Through nanofiltration
Lactic acid feed liquid after film is refined is sent into evaporator and concentrated, absolute pressure 8000Pa, and temperature is 120 DEG C, the acid solution distillated
Condensed Posterior circle is to continuous moving post exchange system.Resulting lactic product after concentration detects through HPLC to be surveyed, and lactic acid is final
Purity is 96.3%, and the lactic acid rate of recovery is up to 92.2%.
Product analysis detection figure is shown in Fig. 6, Fig. 7.
Claims (6)
- A kind of 1. technique of purification of lactic acid, it is characterised in that：Comprise the following steps：（1）The Pfansteihl zymotic fluid of calcium salt method production, centrifuges or filters off except thalline and solia particle, is concentrated, be acidolysis, de- Color, the lactic acid feed liquid after must decolourizing；（2）Lactic acid feed liquid after above-mentioned decolouring enters continuous moving column system, and calcium sulfate and other is remained later to remove acidolysis Foreign ion；（3）Lactic acid feed liquid after above-mentioned processing, through nanofiltration membrane, concentration, obtain fine purification of lactic acid.
- 2. the technique of purification of lactic acid according to claim 1, it is characterised in that：The step（2）In, continuous moving post system System is composed in series by 30 resin columns, and the bottom of previous resin column at the top of latter resin column with being serially connected；Resin Pole unit is put on a rotating disk, and switching is realized by the rotation of rotating disk, and material is controlled by an automatic rotary distributor, Resin column is divided into the functional areas such as exchange area, water wash zone, renewing zone, elution area, just held when resin unit reaches designated area The corresponding technical process of row；After filtrate enters exchange area, exchanged by one-level, efflux is lactic acid solution, in filtrate Salt ion is adsorbed in resin；Now resin pole unit is moved into water wash zone and washed, remaining lactic acid material inside resin column Liquid is ejected, efflux with exchange region effluent together into exchange area two, three, level Four exchange, so guarantee feed liquid impurity Ion is all adsorbed；The resin unit of adsorbed saturation is washed by two level, ensures that feed liquid is washed with water totally；Now again will tree Fat post moves into renewing zone, and pickling or alkali cleaning carry out resin regeneration, regenerated by three-level and cause resin to recover switching performance completely；Through Cross regeneration resin it is scrubbed enter exchange area, the circulation synchronous that so goes round and begins again switching progress.
- 3. the technique of purification of lactic acid according to claim 2, it is characterised in that：Resin is filled with the resin column, its In, 15 load styrene or acrylic acid（Ester）It is strong-acid cation-exchange resin, 15 load styrene or acrylic acid in addition （Ester）It is strong basic anion-exchange resin, particle diameter is 0.4~0.6mm, particle voids rate 50%；Cationic ion-exchange resin water content 40%~60%, it is wet to regard 0.60~0.86g/mL of index, 1.05~1.30g/mL of wet true index, expansion rate 10%~15%；Anion Exchanger resin water content 40%~60%, it is wet to regard 0.56~0.74g/mL of index, 1.05~1.21g/mL of wet true index, expansion rate 20%~25%.
- 4. the technique of purification of lactic acid according to claim 2, it is characterised in that：" lactic acid feed liquid enters continuous moving post system System " specific workflow be：The resin column for being filled with strong acid positive resin is first passed through, is discharged by being filled with the cloudy tree of strong basicity The resin column of fat, then discharging continued back to and is filled with the resin column of highly acid sulphur resin and continues to remove cation impurity, go out Expect that again returning to the resin column for being filled with strong basicity negative resin continues to remove anionic impurity, you can reach the breast required in production The purity of sour feed liquid subsequent technique；In the resin container of cation exchange system, the cation such as sodium, magnesium, calcium and the hydrogen on resin By exchanging, effluent enters in the resin container of anion exchange system ion, on chlorion, sulfate radical plasma and resin Hydroxide ion is by exchanging.
- 5. the technique of purification of lactic acid according to claim 2, it is characterised in that：The input concentration of lactic acid feed liquid be 18%~ 27%, positive resin lactic acid material handling capacity is 6~8 times of resin volume；Negative resin lactic acid material handling capacity is the 20 of resin volume ~25 times；Resin regeneration liquid used in pickling is the HCl solution of concentration 30%, and dosage is the 2%~3% of lactic acid feed liquid treating capacity；Alkali The NaOH solution that resin regeneration liquid used is concentration 32% is washed, dosage is the 1%~2% of lactic acid feed liquid treating capacity；Wash water consumption For the 40%~55% of lactic acid feed liquid treating capacity.
- 6. the technique of purification of lactic acid according to claim 1, it is characterised in that：The step（3）In, lactic acid feed liquid is through receiving After membrane filtration, filtrate is concentrated, 100~120 DEG C, 8000~12000Pa of absolute pressure of evaporator internal temperature, herein The condensed Posterior circle of acid solution that process portion is distillated is to continuous moving post exchange system.
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| CN111269107A (en) * | 2020-04-09 | 2020-06-12 | 安徽固德生物工程有限公司 | L-lactic acid purification and refining method |
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| CN114181070A (en) * | 2021-12-28 | 2022-03-15 | 普立思生物科技有限公司 | Method for extracting high-purity L-lactic acid by using molecular distillation heavy phase and nanofiltration membrane concentrated solution |
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| CN107988274A (en) * | 2017-11-30 | 2018-05-04 | 沈阳金博地生态环保科技有限公司 | The method that fermented maize stalk produces Pfansteihl and ethanol |
| CN109956859B (en) * | 2017-12-22 | 2021-10-19 | 广州中国科学院先进技术研究所 | Method for separating and purifying lactic acid from lactic acid fermentation liquor |
| CN109956859A (en) * | 2017-12-22 | 2019-07-02 | 广州中国科学院先进技术研究所 | A method of the separating-purifying lactic acid from lactic fermentation liquid |
| CN107986956A (en) * | 2017-12-28 | 2018-05-04 | 九江科院生物化工有限公司 | A kind of method for preparing calcium lactate crystal and the method by the calcium lactate crystal production lactic acid of resistance to thermal level |
| CN111269107A (en) * | 2020-04-09 | 2020-06-12 | 安徽固德生物工程有限公司 | L-lactic acid purification and refining method |
| CN111592458A (en) * | 2020-05-25 | 2020-08-28 | 中粮营养健康研究院有限公司 | Method for separating lactic acid |
| CN111592458B (en) * | 2020-05-25 | 2022-12-23 | 中粮营养健康研究院有限公司 | Method for separating lactic acid |
| CN111773749A (en) * | 2020-07-13 | 2020-10-16 | 青岛海湾精细化工有限公司 | Vacuum concentration system for dilute sulfuric acid |
| CN113880710A (en) * | 2021-10-22 | 2022-01-04 | 万华化学集团股份有限公司 | Lactic acid purification method |
| CN113880710B (en) * | 2021-10-22 | 2023-10-20 | 万华化学集团股份有限公司 | Purification method of lactic acid |
| CN114605254A (en) * | 2021-11-01 | 2022-06-10 | 欧尚元(天津)有限公司 | Refining and purifying method and device for crude L-lactic acid |
| CN114605254B (en) * | 2021-11-01 | 2022-08-23 | 欧尚元(天津)有限公司 | Refining and purifying method and purifying device for crude L-lactic acid |
| CN114181070A (en) * | 2021-12-28 | 2022-03-15 | 普立思生物科技有限公司 | Method for extracting high-purity L-lactic acid by using molecular distillation heavy phase and nanofiltration membrane concentrated solution |
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