CN103923136B - A kind of production method of ascorbic acid glucoside - Google Patents
A kind of production method of ascorbic acid glucoside Download PDFInfo
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Abstract
The invention discloses a kind of production methods of ascorbic acid glucoside, include the following steps: step 1: ascorbic acid glucoside reaction solution passes through nanofiltration separation, and remaining VC in elimination reaction liquid obtains nanofiltration concentrate；Step 2: nanofiltration concentrate being separated by continuous fluid separator, removes the glucose in VC glucoside reaction solution；Step 3: from continuous fluid separator come out VC glucoside solution first pass through positive resin adjust pH after, be concentrated using nanofiltration membrane, the inorganic salts in elimination reaction liquid, obtain VC glucoside concentrate；Step 4: VC glucoside concentrate being subjected to vacuum distillation concentration, the concentration of VC glucoside is further increased, then crystallized, VC glucoside can be obtained.The production method of ascorbic acid glucoside of the present invention, have the advantages that it is environmentally protective, reduce pollution, reduce cost, increase yield, improve quality and simplify operation.
Description
Technical field
The present invention relates to ascorbic acid glucoside production field, in particular to a kind of producer of ascorbic acid glucoside
Method.
Background technique
Vitamin C (abbreviation VC) is one of nutrient needed by human, is clinically mainly used to treat bad hematic acid disease,
Therefore chemical name is ascorbic acid (Vitamin C, AA).In addition, the distinctive chemical structure of VC and physiological activity allow to make
It is widely applied and the fields such as cosmetics, food and medicine for acid, reducing agent, antioxidant, bleaching agent and stabilizer.However
There is also a series of intrinsic drawbacks by VC: it is extremely unstable in aqueous solution；It is easily oxidizing with other by the oxygen in air；
It is exposed to meeting fast degradation etc. under neutral pH, heat, light and heavy metal, to limit its application in certain fields.Therefore,
The VC derivative for developing high added value becomes the hot spot of recent domestic scholar research.
VC glucoside, scientific name O-a-D- glucopyranosyl-L-AA (2-O-a-D-
Glucopyranosyl-L-ascorbic acid, is abbreviated as AA-2G), it is a kind of derivative of VC, relative molecular mass is
338.27, fusing point is 158.5~159.5 DEG C.Since VC has stability poor, the disadvantages of being oxidized easily, therefore derive VC's
Product-VC glucoside is substituted, VC can be replaced as acid, reducing agent, antioxidant, bleaching agent and stabilizer, extensively
Applied to fields such as cosmetics, food and medicines.
The method of current VC glucoside industrially processed mainly passes through after biotransformation method synthesizes VC glucoside, then
Product is obtained by subsequent extraction and purification process, shown in main method process attached drawing 1；Since bed is being fixed in the technique
Inorganic salts can be generated in purification process, yield is low, and the water consume of fixed bed, regenerative agent consumption are high, lead to processing cost
It is larger.
Summary of the invention
It is an object of the invention to generate inorganic salts for current VC glucoside production method, yield is low, and cost
The disadvantages of big, is based on the advanced separation method of continuous fluid separator, provides a kind of VC glucoside production method of improvement, with
Reach reduction production cost, simplified production method, the purpose for shortening the production cycle, improving total recovery.
In order to achieve the above objectives, technical solution proposed by the present invention is: a kind of production method of ascorbic acid glucoside,
It is characterized in that, includes the following steps:
Step 1: ascorbic acid glucoside reaction solution passes through nanofiltration separation, and it is dense to obtain nanofiltration by remaining VC in elimination reaction liquid
Contracting liquid；
Step 2: nanofiltration concentrate being separated by continuous fluid separator, removes the Portugal in VC glucoside reaction solution
Grape sugar；
Step 3: from continuous fluid separator come out VC glucoside solution first pass through positive resin adjust pH after, then
It is concentrated by nanofiltration membrane, the inorganic salts in elimination reaction liquid, obtains VC glucoside concentrate；
Step 4: VC glucoside concentrate is subjected to vacuum distillation concentration, further increases the concentration of VC glucoside,
It is crystallized again, VC glucoside can be obtained.
Preferably, 30 separative units built in continuous fluid separator described in step 2, the interior filling of each separative unit
Weak base type anion exchange resin, and 30 separative unit designs are as follows::
Adsorption zone: including 8 separative units, the 1st and the 2nd separative unit series connection of 8 separative units connects in the region
It connects, VC glucoside reaction solution initially enters the 1st separative unit of adsorption zone, and material liquid passes through separative unit, VC glucoside
Partially exchanged on resin, from the 2nd separative unit efflux with absorption water wash zone water lotion mix together enter back into
The 3rd to the 8th separative unit connecting of modes of three and three strings, wherein the 7th, the 8th separative unit efflux be absorption
Extraction raffinate；
Adsorb water wash zone: including 3 separative units, after absorption, each separative unit is washed, 3 in the region
A separative unit connects in a series arrangement, and after being located at adsorption zone, using adverse current into pure water mode, separative unit rotates to absorption water
After washing area, the feed liquid being entrained between resin is ejected by water, and efflux mixes together with the efflux of the 2nd separative unit of adsorption zone
Into the 3rd, 4 separative units of adsorption zone；
It parses area: including 7 separative units, be divided into two sections, leading portion includes 3 separative units, and back segment includes that 4 separation are single
Member, after entering 3 separative units of leading portion using the series connection of 0.2mol/L sodium chloride forward direction, after efflux and parsing in water wash zone
Positive series connection collects the last one separative unit and goes out liquid, obtain VC grape into 4 separative units of back segment again for efflux mixing
Glucosides；
Water wash zone after parsing: including 4 separative units, using series connection adverse current into pure water mode, by sodium chloride solution
After analysis, resin is all washed out sodium chloride remaining in separative unit, the outflow after parsing in water wash zone by the flushing of pure water
Liquid is mixed with preceding 3 separative unit effluxes in parsing area；
Renewing zone: including 4 units, it is divided into alkali renewing zone and diluted alkaline renewing zone, pans is set before alkali and diluted alkaline, using inverse
Flow regeneration principle step by step, the lye that regenerated liquid is 4% or so；
Regeneration water wash zone: including 3 units, alkali of the wash residual in resin container, and it is returned directly to the back segment of renewing zone
In the pans of diluted alkaline renewing zone；
Anti- top drying zone: including 1 separative unit, uses the product VC glucoside in parsing area as the charging in the area, and
Using backward feed, to replace the water being entrained between resin.
Preferably, the feature of nanofiltration membrane used by nanofiltration described in step 3 be polysulfones, it is polyether sulfone, compound reverse osmosis
Film, operating condition are temperature at 20~35 DEG C, 2.0~4.0Mpa of operating pressure.
Preferably, in evaporative crystallization technique described in step 4, by vacuum distillation, so that the content of VC glucoside
Reach 50% or more, methanol is added after then cooling down, VC glucoside crystal can be precipitated.
Above-mentioned is the elaboration of Method And Principle, is related to the specific scale of system: such as the height of separative unit size, unit/
Diameter is then more associated with the initial parameter of actual requirement design than flow velocity in, each separative unit etc..
By adopting the above technical scheme, the production method of ascorbic acid glucoside of the present invention, with traditional VC grape
Glucosides production method is compared, the method for the present invention have it is environmentally protective, reduce pollution, reduce cost, increase yield, improve quality and
The advantages of simplifying operation；What specific tool had the advantage that:
One, the method for the present invention is carried out using nanofiltration membrane except VC and inorganic salts, the advantage is that:
(1) use nanofiltration membrane, can effectively catching VC glucoside, and remove most of VC and inorganic salts, improve
The yield and purity of VC glucoside；
(2) during processing, operating cost is low for nanofiltration membrane, and certain concentration has been carried out to VC glucoside, belongs to
It is concentrated in room temperature, does not destroy effective component.
Two, VC glucoside and glucose effectively divide by the method for the present invention using continuous fluid isolation technics
From, the advantage is that:
(1) since continuous operation, product composition and concentration keep stablizing, convenient for the mating of downstream section；
(2) because of continuous production, transfer tank and mating very little, facility compact, be easily installed in any position, easily with old life
Production process and equipment matching, land occupation are only 10% or so of identical scale；
(3) relatively fixed bed system, amount of resin can reduce about 85%；Due to using counter-current regeneration mode and close to equivalent
The dosage of regenerative agent is greatly reduced in the regenerative agent of ratio, and the dosage highest of washing water can save 50-60%；
(4) it can remove or separate simultaneously the substance with different characteristics, therefore can be by complicated methods simplification；
(5) rotation speed can be automatically adjusted with the quality of incoming fluid and the variation of flow according to the needs of production process；
Therefore it can guarantee and run under economically optimum state；
(6) it is required according to production process, the flow direction of fluid can be connected into adverse current or cocurrent mode；
(7) due to using multiple separative units, production method process can flexibly be changed.
Detailed description of the invention
Fig. 1 is VC glucoside production technological process described in the prior art；
Fig. 2 is VC glucoside production method flow chart of the present invention；
Fig. 3 is continuous fluid separator separation method flow chart of the present invention.
Specific embodiment
With reference to the accompanying drawings and detailed description, the present invention will be further described.
As shown in Fig. 2, the reaction solution of the glucoside containing VC is first passed through nanofiltration membrane, a large amount of VC in reaction solution are removed,
Nanofiltration concentrate carries out continuous ionic exchange removal glucose using continuous fluid separator, and obtained VC glucoside is molten
Liquid removes inorganic salts through nanofiltration membrane again after positive resin tune pH, and nanofiltration concentrate carries out vacuum distillation concentration, and concentrate carries out
Crystallize (see figure 1).Specific operation process is as follows:
Step 1: nanofiltration removes VC
Feed liquid used is VC glucoside reaction solution, 30 DEG C of temperature, pressure 2.6Mpa, has carried out the experiment of 3 batches altogether, specifically
As a result such as table 1:
1 nanofiltration filtration experiment data of table
From experimental data it can be seen that carrying out removing VC using nanofiltration membrane, in concentrate product purity can achieve 93% with
On, nanofiltration removing VC technique has many advantages, such as high-efficient, pollutes small.
Step 2: continuous fluid adsorption-desorption
Resin used by this example is weak base type negative resin, according to the characteristic of VC glucoside itself, every resin
Loading is 450ml.It is divided into following segment identifier (see attached drawing 2):
Adsorption zone: including 8 separative units, the 1st and the 2nd separative unit series connection of 8 separative units connects in the region
It connects, VC glucoside reaction solution initially enters the 1st separative unit of adsorption zone, and material liquid passes through separative unit, VC glucoside
Partially exchanged on resin, from the 2nd separative unit efflux with absorption water wash zone water lotion mix together enter back into
The 3rd to the 8th separative unit connecting of modes of three and three strings, wherein the 7th, the 8th separative unit efflux be absorption
Extraction raffinate；
Adsorb water wash zone: including 3 separative units, after absorption, each separative unit is washed, 3 in the region
A separative unit connects in a series arrangement, and after being located at adsorption zone, using adverse current into pure water mode, pillar rotates to absorption water wash zone
Afterwards, the feed liquid being entrained between resin is ejected by water, and efflux is mixed with the efflux of the 2nd separative unit of adsorption zone to be entered together
3rd, the 4th separative unit of adsorption zone；
It parses area: including 7 separative units, be divided into two sections, leading portion includes 3 separative units, and back segment includes that 4 separation are single
Member, after entering 3 separative units of leading portion using the series connection of 0.2mol/L sodium chloride forward direction, after efflux and parsing in water wash zone
Positive series connection collects the last one separative unit and goes out liquid, obtain VC grape into 4 separative units of back segment again for efflux mixing
Glucosides；
Water wash zone after parsing: including 4 separative units, using series connection adverse current into pure water mode, by sodium chloride solution
After analysis, resin is all washed out sodium chloride remaining in separative unit, the outflow after parsing in water wash zone by the flushing of pure water
Liquid is mixed with preceding 3 separative unit effluxes in parsing area；
Renewing zone: including 4 units, it is divided into alkali renewing zone and diluted alkaline renewing zone, pans is set before alkali and diluted alkaline, using inverse
Flow regeneration principle step by step, the lye that regenerated liquid is 4% or so；
Regeneration water wash zone: including 3 units, alkali of the wash residual in resin container, and it is returned directly to the back segment of renewing zone
In the pans of diluted alkaline renewing zone；
Anti- top drying zone: including a separative unit, uses the product VC glucoside in parsing area as the charging in the area, and
Using backward feed, to replace the water being entrained between resin.
Embodiment: material liquid is the feed liquid after nanofiltration removes VC, and feed liquid is in yellow, and wherein the content of VC glucoside exists
5% or so, glucose content 20% or so.Equipment rotation period is 2100s, that is, 35min.Flow=450/35 of resin=12.8mL/
Min, and reaction solution inlet amount is 138mL or so.Amount of resin can be characterized with resin volume with input material volume ratio, i.e.,
12.8:138=1:10.8, when 2100S/ turns, the accessible reduction of feed volume of per resin are as follows: 10.8ml feed liquid/ml resin；
The result for carrying out the production of VC glucoside using the above method is as follows:
2 continuous fluid adsorption and desorption experiment data of table
It should be noted that the present embodiment is only implemented with using the continuous ionic exchange system of 30 separative units
Example is illustrated the present invention using continuous ionic exchange system and produces the attainable technical effect of colistine sulfate institute, for
For those skilled in the art, the separative unit of different data is set as needed to realize the present invention, is of the invention
Protection scope.
Step: 3: nanofiltration membrane removes inorganic salts
Feed liquid used is the VC glucoside solution that continuous fluid device comes out, after first adjusting pH using positive resin, temperature
Control has carried out the experiment of 3 batches, concrete outcome such as table 1 at 20-30 DEG C, pressure 2Mpa altogether:
3 nanofiltration membrane of table removes inorganic salts experimental data
From experimental data it can be seen that carrying out removing inorganic salts using nanofiltration membrane, inorganic salt content in product can be made to obtain
To reduction, many burdens are alleviated for later crystallization technique, the yield in nanofiltration process can achieve 98% or more.
Step 4: VC glucoside concentrate is subjected to vacuum distillation concentration, further increases the concentration of VC glucoside,
It is crystallized again, VC glucoside can be obtained.The step is the prior art, is not described in detail again.
In the above-described embodiments, exemplary description only has been carried out to the present invention, but those skilled in the art are reading this
The present invention can be carry out various modifications without departing from the spirit and scope of the present invention after patent application.
Claims (3)
1. a kind of production method of ascorbic acid glucoside, which comprises the steps of:
Step 1: ascorbic acid glucoside reaction solution passes through nanofiltration separation, and remaining VC in elimination reaction liquid obtains nanofiltration concentrate；
Step 2: nanofiltration concentrate being separated by continuous fluid separator, removes the grape in VC glucoside reaction solution
Sugar；
Step 3: the VC glucoside solution come out from continuous fluid separator first passes through cation exchange resin and adjusts pH
Afterwards, it is concentrated using nanofiltration membrane, the inorganic salts in elimination reaction liquid, obtains VC glucoside concentrate；
Step 4: VC glucoside concentrate is subjected to vacuum distillation concentration, further increases the concentration of VC glucoside, then into
Row crystallization, can be obtained VC glucoside；
30 separative units built in continuous fluid separator described in step 2, in each separative unit filling weak base type yin from
Sub-exchange resin, and 30 separative unit designs are as follows:
Adsorption zone: including 8 separative units, the 1st and the 2nd separative unit of 8 separative units is connected in series in the region, VC
Glucoside reaction solution initially enters the 1st separative unit of adsorption zone, and material liquid passes through separative unit, and VC glucoside is by part
It exchanges on resin, mixes and enter back into three and three together with the water lotion of absorption water wash zone from the 2nd separative unit efflux
The 3rd to the 8th separative unit that the mode of string connects, wherein the 7th, the 8th separative unit efflux be absorption extraction raffinate；
Adsorb water wash zone: including 3 separative units, after absorption, each separative unit is washed, 3 points in the region
It is connected in a series arrangement from unit, after being located at adsorption zone, using adverse current into pure water mode, separative unit rotates to absorption water wash zone
Afterwards, the feed liquid being entrained between resin is ejected by water, and efflux is mixed with the efflux of the 2nd separative unit of adsorption zone to be entered together
3rd, 4 separative units of adsorption zone；
It parsing area: including 7 separative units, be divided into two sections, leading portion includes 3 separative units, and back segment includes 4 separative units,
Stream after entering 3 separative units of leading portion using the series connection of 0.2mol/L sodium chloride forward direction, after efflux and parsing in water wash zone
Positive series connection collects the last one separative unit and goes out liquid, obtain VC glucose into 4 separative units of back segment again for liquid mixing out
Glycosides；
Water wash zone after parsing: including 4 separative units, using series connection adverse current into pure water mode, after sodium chloride parses,
Resin is all washed out by the flushing of pure water, by sodium chloride remaining in separative unit, the efflux after parsing in water wash zone with
Parse preceding 3 separative unit effluxes mixing in area；
Renewing zone: including 4 units, being divided into alkali renewing zone and diluted alkaline renewing zone, set pans before alkali and diluted alkaline, using adverse current by
Grade regeneration principle, the lye that regenerated liquid is 4%；
Regeneration water wash zone: including 3 units, alkali of the wash residual in resin container, and it is returned directly to the back segment diluted alkaline of renewing zone
In the pans of renewing zone；
Anti- top drying zone: including 1 separative unit, uses the product VC glucoside in parsing area as the charging in the area, and use
Backward feed, to replace the water being entrained between resin.
2. a kind of production method of ascorbic acid glucoside according to claim 1, which is characterized in that described in step 3
Nanofiltration used by nanofiltration membrane feature be polysulfones, polyether sulfone, complex reverse osmosis membrane, operating condition be temperature 20~35
DEG C, 2.0~4.0Mpa of operating pressure.
3. a kind of production method of ascorbic acid glucoside according to claim 1 or 2, which is characterized in that institute in step 4
In the evaporative crystallization technique stated, by vacuum distillation, so that the content of VC glucoside reaches 50% or more, add after then cooling down
Enter methanol, VC glucoside crystal can be precipitated.
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| CN105506037B (en) * | 2016-01-29 | 2019-05-17 | 长兴制药股份有限公司 | A kind of L-Ascorbic acid glucoside crystalline powder and its manufacturing method |
| CN111111260A (en) * | 2020-01-15 | 2020-05-08 | 福州三合元生物科技有限公司 | Continuous fluid separation device for ascorbic acid glucoside production |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0539196A1 (en) * | 1991-10-23 | 1993-04-28 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | Process for preparing high 2-O-alpha-D-glucopyranosyl-L-ascorbic acid content product |
| EP1162205A2 (en) * | 2000-06-08 | 2001-12-12 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | Process for producing 2-O-Alpha-D-Glucopyranosyl-L-ascorbic acid in high content |
| CN102093448A (en) * | 2009-09-03 | 2011-06-15 | 株式会社林原生物化学研究所 | Particulate composition containing anhydrous crystalline 2-O-alpha -D-glucosyl-L-ascorbic acid, process for producing the same, and uses thereof |
| CN103265622A (en) * | 2013-05-05 | 2013-08-28 | 厦门世达膜科技有限公司 | Colistin sulfate production method |
-
2014
- 2014-04-20 CN CN201410158461.1A patent/CN103923136B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0539196A1 (en) * | 1991-10-23 | 1993-04-28 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | Process for preparing high 2-O-alpha-D-glucopyranosyl-L-ascorbic acid content product |
| EP1162205A2 (en) * | 2000-06-08 | 2001-12-12 | Kabushiki Kaisha Hayashibara Seibutsu Kagaku Kenkyujo | Process for producing 2-O-Alpha-D-Glucopyranosyl-L-ascorbic acid in high content |
| CN102093448A (en) * | 2009-09-03 | 2011-06-15 | 株式会社林原生物化学研究所 | Particulate composition containing anhydrous crystalline 2-O-alpha -D-glucosyl-L-ascorbic acid, process for producing the same, and uses thereof |
| CN103265622A (en) * | 2013-05-05 | 2013-08-28 | 厦门世达膜科技有限公司 | Colistin sulfate production method |
Non-Patent Citations (2)
| Title |
|---|
| Production of ascorbic acid glucoside by alginate-entrapped mycelia of Aspergillus niger;Hsin-Ju Hsieh，等;《Appl. Microbiol. Biotechnol.》;20071130;第77卷(第1期);第53–60页 |
| 连续逆流离子交换技术及其在抗生素生产中的应用;吴粦华，等;《福建化工》;20030331(第1期);第13-19页 |
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Application publication date: 20140716 Assignee: Xiamen Shida membrane Engineering Co.,Ltd. Assignor: XIAMEN STARMEM TECHNOLOGY CO.,LTD. Contract record no.: X2021980014823 Denomination of invention: A production method of ascorbic acid glucoside Granted publication date: 20190118 License type: Exclusive License Record date: 20211221 |
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