CN105906688A - Technological system and technological method for extracting glutathione - Google Patents
Technological system and technological method for extracting glutathione Download PDFInfo
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- CN105906688A CN105906688A CN201610277269.3A CN201610277269A CN105906688A CN 105906688 A CN105906688 A CN 105906688A CN 201610277269 A CN201610277269 A CN 201610277269A CN 105906688 A CN105906688 A CN 105906688A
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- glutathion
- gsh
- resin column
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07K—PEPTIDES
- C07K5/00—Peptides containing up to four amino acids in a fully defined sequence; Derivatives thereof
- C07K5/02—Peptides containing up to four amino acids in a fully defined sequence; Derivatives thereof containing at least one abnormal peptide link
- C07K5/0215—Peptides containing up to four amino acids in a fully defined sequence; Derivatives thereof containing at least one abnormal peptide link containing natural amino acids, forming a peptide bond via their side chain functional group, e.g. epsilon-Lys, gamma-Glu
Abstract
The invention relates to a technological system for extracting glutathione. The technological system comprises devices which are arrayed from upstream to downstream and include a reaction kettle (1), a first material tank (2), a first centrifugal machine (3), a filter device (4), a second material tank (5), a resin column (6), a third material tank (7), a fourth material tank (8), a decolorization tank (9), a crystallization tank (10), a second centrifugal machine (11) and a fifth material tank (12), and further comprises an organic solvent tank (13). The organic solvent tank (13) is positioned on upstream of the resin column (6), upstream of the fourth material tank (8) and upstream of the crystallization tank (10) and is connected with the resin column (6), the fourth material tank (8) and the crystallization tank (10) by pipelines. The technological system has the advantage that the technological system is applicable to extracting the glutathione.
Description
Technical field
The present invention relates to the preparation technology of a kind of glutathion, belong to medicine and intermediate technical field thereof.
Background technology
Glutathion (glutathione, r-glutamyl cysteingl+glycine, GSH) is a kind of containing γ-acyl
Amine key and the tripeptides of sulfydryl, be made up of glutamic acid, cysteine and glycine.It is present in each cell of almost health.Paddy
The sweet Toplink of Guang assists in keeping normal immune function, and has antioxidation and integrate Detoxication, cysteine
On sulfydryl be its active group (therefore being often abbreviated as G-SH), easily and some drugs (such as acetaminophen), toxin (as free radical,
Iodoacetic acid, mustard gas, the heavy metal such as lead, hydrargyrum, arsenic) etc. combine, and there is integration Detoxication.
The production method of glutathion mainly has chemical synthesis, enzyme transforming process and fermentation method.At present, chemical synthesis and
Extraction method industrialization, chemical synthesis is relatively early applied to the production of glutathion, but the shortcoming that there is complicated and time consumption.Biological
Synthetic method includes enzyme transforming process and microbe fermentation method, and microbe fermentation method is our times for the production of glutathion
Main production method, and consume owing to avoiding the ATP of costliness, both economical practicality, the main product of external glutathion
Ground is in Japan, and application is Progress in Glutathione Production by Microbial Fermentation.Domestic produced glutathion by fermentable, adding
In the case of three kinds of amino acid precursors, fermentation unit is typically at 4-8g/L.Our main studying enzyme conversion method.Enzyme transforming process produces
Glutathion obtains related enzyme systems due to needs, needs to design ATP regenerating system for it, in addition it is also necessary to add precusor amino acids, because of
This technical difficulty is high.Use enzyme process to prepare in the technique of glutathion, reactant liquor has enzyme liquid residual, subsequent technique is had one
Fixing sound.
Summary of the invention
Goal of the invention: in order to overcome above-mentioned deficiency present in prior art, first purpose of the present invention is to provide
A kind of extraction process system preparing glutathion.
Second object of the present invention is to provide a kind of process for extracting preparing glutathion.
Technical scheme:
The extraction process system of a kind of glutathion, from upstream to the equipment of arranged downstream, including reactor (1), the first batch can
(2), the first centrifuge (3), filter plant (4), the second batch can (5), resin column (6), the 3rd batch can (7), the 4th batch can (8),
Bleacher (9), crystallize tank (10), the second centrifuge (11), the 5th batch can (12), also include organic solvent tank (13), and this is organic
Solvent tank (13) lays respectively at described tree and refers to post (6), the 4th batch can (8), the upstream of crystallize tank (10), and is connected by pipeline；
As preferably, described organic solvent tank (13) is the one in methanol tank, Ethanol tank, isopropanol tank, acetone tank.
The extraction process system of glutathion according to claim 1, it is characterised in that: described filter plant
(4) being ultrafiltration apparatus, the filter sizes of this ultrafiltration apparatus is 8000-10000 dalton.
As preferably, described bleacher (9) is activated carbon decolorizing tank.
As preferably, described resin column (6) is DA201-C type macroporous adsorptive resins.
The process of a kind of extraction process system using above-mentioned glutathion, comprises the steps:
1) prepared by GSH crude product: comprise the steps:
The enzymatic clarification glutathion complete material of reaction is carried out blowing by 1.1, and feed liquid is centrifuged off insoluble matter, collects filtrate；
The filtrate obtained is carried out ultrafiltration by ultrafiltration apparatus by 1.2, collects ultrafiltration dialysis liquid；
1.3 by resin column (4) upper after ultrafiltration dialysis liquid acid adjustment；The blade diameter length ratio of resin column (4) is 0.05-0.2, and loading pH value is
2.0-3.5, applied sample amount is 8-20mgGSH/ml resin, and loading flow velocity is 0.5-1.5bv/h；
1.4 rinse macroporous resin column by the purified water of 1-3bv with the speed of 0.5-1.5bv/h；
1.5 ethanol speed eluting desorption macroporous resin column with 0.5-2.0bv/h using 50%-95%, collect 1,2,3-indantrione monohydrate colour developing
Elution fractions；
The 1.6 eluent 30-50 DEG C decompressions that will collect, vacuum≤-0.09MPa, concentrate, being concentrated into GSH content is 15%-
30%；
1.7 add the one in the methanol of 0.5-1.5 times amount, ethanol, isopropanol or acetone in concentrated solution, under nitrogen protection,
0-25 DEG C of stirring and crystallizing 10-24h；
1.8 crystallizes are complete, and blowing is centrifuged, washing with alcohol, 30-50 DEG C of decompression, vacuum≤-0.09MPa, are dried 6-8h,
GSH crude product；
2) GSH crude product refining, comprises the steps:
2.1 GSH crude products add the water dissolution of 4-12 times amount, add the activated carbon decolorizing of 1%-3%；
2.2 filter, and add the one in the methanol of 2-10 times amount, ethanol, isopropanol or acetone in filtrate, under nitrogen protection,
0-25 DEG C of stirring and crystallizing 10-24h；
2.3 crystallizes are complete, and blowing is centrifuged, 30-50 DEG C, decompression, and vacuum≤-0.09MPa is dried 6-8h, obtains GSH fine work.
Beneficial effect: the present invention utilizes DA201-C type macroporous adsorbent resin desalination, purifies reactant liquor, it is to avoid use
Traditional mantoquita method (copper oxidule precipitation, hydrogen sulfide reduce), reduces environmental pollution, alleviates environmental protection pressure；And DA201-C type is big
Macroporous adsorbent resin adsorbance is big, and Sample Purification on Single disposal ability is strong.
Accompanying drawing explanation
Fig. 1 is this process system structural representation.
Specific embodiment
Below in conjunction with specific embodiment, the present invention is expanded on further.Should be understood that these embodiments are merely to illustrate the present invention
Rather than restriction the scope of the present invention.
Embodiment one
A kind of extraction process system of glutathion, from upstream to the equipment of arranged downstream, including reactor the 1, first batch can 2,
First centrifuge 3, filter plant the 4, second batch can 5, resin column the 6, the 3rd batch can the 7, the 4th batch can 8, bleacher 9, crystallize tank 10,
Second centrifuge the 11, the 5th batch can 12, also includes organic solvent tank 13, this organic solvent tank 13 lay respectively at described tree refer to post 6,
4th batch can 8, the upstream of crystallize tank 10, and connected by pipeline；
As preferably, described organic solvent tank 13 is the one in methanol tank, Ethanol tank, isopropanol tank, acetone tank.
The extraction process system of glutathion according to claim 1, it is characterised in that: described filter plant 4
For ultrafiltration apparatus, the filter sizes of this ultrafiltration apparatus is 8000-10000 dalton.In the present embodiment, described bleacher 9 is
Activated carbon decolorizing tank, described resin column 6 is DA201-C type macroporous adsorptive resins.
Embodiment two
The process of a kind of extraction process system using above-mentioned glutathion, comprises the steps:
1) prepared by GSH crude product: comprise the steps:
The enzymatic clarification glutathion complete material of reaction is carried out blowing by 1.1, and feed liquid is centrifuged off insoluble matter, collects filtrate
55kg；
The filtrate obtained is carried out ultrafiltration by ultrafiltration apparatus by 1.2, collects ultrafiltration dialysis liquid；
1.3 by resin column 6 upper after ultrafiltration dialysis liquid acid adjustment；The blade diameter length ratio of resin column 6 is 0.05, and loading pH value is 2.0, loading
Amount is 8mgGSH/ml resin, and loading flow velocity is 0.5bv/h；
1.4 rinse macroporous resin column by the purified water of 1bv with the speed of 0.5bv/h；
1.5 with 50%% ethanol with the speed eluting desorption macroporous resin column of 0.5bv/h, collect 1,2,3-indantrione monohydrate coloured moiety and wash
De-liquid；
The 1.6 eluent 30 DEG C decompressions that will collect, vacuum≤-0.09MPa, concentrate, being concentrated into GSH content is 15%；
1.7 toward adding the methanol 6 of 0.5 times amount in concentrated solution, under nitrogen protection, 0 DEG C of stirring and crystallizing 10h；
1.8 crystallizes are complete, and blowing is centrifuged, washing with alcohol, 30 DEG C of decompressions, vacuum≤-0.09MPa, are dried 6h, obtain GSH crude product
515g；
2) GSH crude product refining, comprises the steps:
2.1 GSH crude products add the water dissolution of 4 times amount, add the activated carbon decolorizing of 1%；
2.2 filter, and add the methanol 6 of 2 times amount toward filtrate in, under nitrogen is protected, 0 DEG C of stirring and crystallizing 10h；
2.3 crystallizes are complete, and blowing is centrifuged, 30-50 DEG C, decompression, and vacuum≤-0.09MPa is dried 6h, obtains GSH fine work 415g.
Embodiment 3
1) prepared by GSH crude product: comprise the steps:
The enzymatic clarification glutathion complete material of reaction is carried out blowing by 1.1, and feed liquid is centrifuged off insoluble matter, collects filtrate
55kg；
The filtrate obtained is carried out ultrafiltration by ultrafiltration apparatus by 1.2, collects ultrafiltration dialysis liquid；
1.3 by resin column upper after ultrafiltration dialysis liquid acid adjustment；The blade diameter length ratio of resin column is 0.2, and loading pH value is 3.5, and applied sample amount is
20mgGSH/ml resin, loading flow velocity is 1.5bv/h；
1.4 rinse macroporous resin column by the purified water of 3bv with the speed of 1.5bv/h；
1.5 with 95% ethanol with the speed eluting desorption macroporous resin column of 2.0bv/h, collect 1,2,3-indantrione monohydrate coloured moiety eluting
Liquid；
The 1.6 eluent 50 DEG C decompressions that will collect, vacuum≤-0.09MPa, concentrate, being concentrated into GSH content is 30%；
1.7 toward adding the ethanol of 1.5 times amount in concentrated solution, under nitrogen protection, 25 DEG C of stirring and crystallizing 24h；
1.8 crystallizes are complete, and blowing is centrifuged, washing with alcohol, 50 DEG C of decompressions, vacuum≤-0.09MPa, are dried 8h, obtain GSH crude product
580g；
2) GSH crude product refining, comprises the steps:
2.1 GSH crude products add the water dissolution of 12 times amount, add the activated carbon decolorizing of 3%；
2.2 filter, and add the ethanol of 10 times amount toward filtrate in, under nitrogen is protected, 25 DEG C of stirring and crystallizing 24h；
2.3 crystallizes are complete, and blowing is centrifuged, 50 DEG C, decompression, and vacuum≤-0.09MPa is dried 8h, obtains GSH fine work 460g.
Embodiment 4
1) prepared by GSH crude product: comprise the steps:
The enzymatic clarification glutathion complete material of reaction is carried out blowing by 1.1, and feed liquid is centrifuged off insoluble matter, collects filtrate
55kg；
The filtrate obtained is carried out ultrafiltration by ultrafiltration apparatus by 1.2, collects ultrafiltration dialysis liquid；
1.3 by resin column (4) upper after ultrafiltration dialysis liquid acid adjustment；The blade diameter length ratio of resin column (4) is 0.1, and loading pH value is 3.0, on
Sample amount is 15mgGSH/ml resin, and loading flow velocity is 1bv/h；
1.4 rinse macroporous resin column by the purified water of 2bv with the speed of 0.8bv/h；
1.5 with 80% ethanol with the speed eluting desorption macroporous resin column of 1.5v/h, collect 1,2,3-indantrione monohydrate coloured moiety eluting
Liquid；
The 1.6 eluent 40 DEG C decompressions that will collect, vacuum≤-0.09MPa, concentrate, being concentrated into GSH content is 20%；
1.7 toward adding the isopropanol of 1.2 times amount in concentrated solution, under nitrogen protection, 15 DEG C of stirring and crystallizing 15h；
1.8 crystallizes are complete, and blowing is centrifuged, washing with alcohol, 40 DEG C of decompressions, vacuum≤-0.09MPa, are dried 7h, obtain GSH crude product
650g；
2) GSH crude product refining, comprises the steps:
2.1 GSH crude products add the water dissolution of 8 times amount, add the activated carbon decolorizing of 1%-3%；
2.2 filter, and add the isopropanol of 6 times amount toward filtrate in, under nitrogen is protected, 15 DEG C of stirring and crystallizing 15h；
2.3 crystallizes are complete, and blowing is centrifuged, 40 DEG C, decompression, and vacuum≤-0.09MPa is dried 7h, obtains GSH fine work 480g.
Embodiment 5
1) prepared by GSH crude product: comprise the steps:
The enzymatic clarification glutathion complete material of reaction is carried out blowing by 1.1, and feed liquid is centrifuged off insoluble matter, collects filtrate
55kg；
The filtrate obtained is carried out ultrafiltration by ultrafiltration apparatus by 1.2, collects ultrafiltration dialysis liquid；
1.3 by resin column (4) upper after ultrafiltration dialysis liquid acid adjustment；The blade diameter length ratio of resin column (4) is 1.6, and loading pH value is 3, loading
Amount is 12mgGSH/ml resin, and loading flow velocity is 0.8bv/h；
1.4 rinse macroporous resin column by the purified water of 1-3bv with the speed of 1.2bv/h；
1.5 ethanol speed eluting desorption macroporous resin column with 1.2bv/h using 50%-95%, collect 1,2,3-indantrione monohydrate coloured moiety
Eluent；
The 1.6 eluent 35 DEG C decompressions that will collect, vacuum≤-0.09MPa, concentrate, being concentrated into GSH content is 20%；
1.7 toward adding the acetone of 1.2 times amount in concentrated solution, under nitrogen protection, 22 DEG C of stirring and crystallizing 18h；
1.8 crystallizes are complete, and blowing is centrifuged, washing with alcohol, 35 DEG C of decompressions, vacuum≤-0.09MPa, are dried 7.5h, obtain GSH thick
Product 540g；
2) GSH crude product refining, comprises the steps:
2.1 GSH crude products add the water dissolution of 6 times amount, add the activated carbon decolorizing of 1.8%；
2.2 filter, and add the acetone of 6 times amount toward filtrate in, under nitrogen is protected, 18 DEG C of stirring and crystallizing 16h；
2.3 crystallizes are complete, and blowing is centrifuged, 38 DEG C, decompression, and vacuum≤-0.09MPa is dried 6.5h, obtains GSH fine work 380g.
Claims (6)
1. the extraction process system of a glutathion, it is characterised in that: from upstream to the equipment of arranged downstream, including reactor
(1), the first batch can (2), the first centrifuge (3), filter plant (4), the second batch can (5), resin column (6), the 3rd batch can (7),
4th batch can (8), bleacher (9), crystallize tank (10), the second centrifuge (11), the 5th batch can (12), also include organic solvent tank
(13), this organic solvent tank (13) lays respectively at described tree and refers to post (6), the 4th batch can (8), the upstream of crystallize tank (10), and logical
Piping connects.
The extraction process system of glutathion the most according to claim 1, it is characterised in that: described organic solvent tank (13)
For the one in methanol tank, Ethanol tank, isopropanol tank, acetone tank.
The extraction process system of glutathion the most according to claim 1, it is characterised in that: described filter plant (4)
For ultrafiltration apparatus, the filter sizes of this ultrafiltration apparatus is 8000-10000 dalton.
The extraction process system of glutathion the most according to claim 1, it is characterised in that: described bleacher (9) is
Activated carbon decolorizing tank.
The extraction process system of glutathion the most according to claim 1, it is characterised in that: described resin column (6) is
DA201-C type macroporous adsorptive resins.
6. the process of the extraction process system using glutathion as claimed in claim 1, it is characterised in that bag
Include following steps:
1) prepared by GSH crude product: comprise the steps:
The enzymatic clarification glutathion complete material of reaction is carried out blowing by 1.1, and feed liquid is centrifuged off insoluble matter, collects filtrate；
The filtrate obtained is carried out ultrafiltration by ultrafiltration apparatus by 1.2, collects ultrafiltration dialysis liquid；
1.3 by resin column (4) upper after ultrafiltration dialysis liquid acid adjustment；The blade diameter length ratio of resin column (4) is 0.05-0.2, and loading pH value is
2.0-3.5, applied sample amount is 8-20mgGSH/ml resin, and loading flow velocity is 0.5-1.5bv/h；
1.4 rinse macroporous resin column by the purified water of 1-3bv with the speed of 0.5-1.5bv/h；
1.5 ethanol speed eluting desorption macroporous resin column with 0.5-2.0bv/h using 50%-95%, collect 1,2,3-indantrione monohydrate colour developing
Elution fractions；
The 1.6 eluent 30-50 DEG C decompressions that will collect, vacuum≤-0.09MPa, concentrate, being concentrated into GSH content is 15%-
30%；
1.7 add the one in the methanol of 0.5-1.5 times amount, ethanol, isopropanol or acetone in concentrated solution, under nitrogen protection,
0-25 DEG C of stirring and crystallizing 10-24h；
1.8 crystallizes are complete, and blowing is centrifuged, washing with alcohol, 30-50 DEG C of decompression, vacuum≤-0.09MPa, are dried 6-8h,
GSH crude product；
2) GSH crude product refining, comprises the steps:
2.1 GSH crude products add the water dissolution of 4-12 times amount, add the activated carbon decolorizing of 1%-3%；
2.2 filter, and add the one in the methanol of 2-10 times amount, ethanol, isopropanol or acetone in filtrate, under nitrogen protection,
0-25 DEG C of stirring and crystallizing 10-24h；
2.3 crystallizes are complete, and blowing is centrifuged, 30-50 DEG C, decompression, and vacuum≤-0.09MPa is dried 6-8h, obtains GSH fine work.
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| CN201610277269.3A CN105906688A (en) | 2016-05-01 | 2016-05-01 | Technological system and technological method for extracting glutathione |
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| CN201610277269.3A CN105906688A (en) | 2016-05-01 | 2016-05-01 | Technological system and technological method for extracting glutathione |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106701564A (en) * | 2017-02-12 | 2017-05-24 | 江苏诚信药业有限公司 | Process system and method for preparing arbutin by use of enzyme method |
| CN115594731A (en) * | 2022-10-31 | 2023-01-13 | 南通紫琅生物医药科技有限公司（Cn） | Glutathione decoloring processing technology |
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| EP0071486A2 (en) * | 1981-07-30 | 1983-02-09 | Akira Kimura | Novel microorganisms of the genus Eschericia, hybrid DNA for use in their production and the use of the microorganisms in the preparation of glutathione |
| CN101429229A (en) * | 2008-12-14 | 2009-05-13 | 甘肃正生生物科技有限公司 | Method for producing high-purity glutathione |
| CN104560707A (en) * | 2015-02-06 | 2015-04-29 | 江苏诚信药业有限公司 | Technological method and system for enzymatically synthesizing L-ascorbic acid 2-glucoside |
-
2016
- 2016-05-01 CN CN201610277269.3A patent/CN105906688A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP0071486A2 (en) * | 1981-07-30 | 1983-02-09 | Akira Kimura | Novel microorganisms of the genus Eschericia, hybrid DNA for use in their production and the use of the microorganisms in the preparation of glutathione |
| CN101429229A (en) * | 2008-12-14 | 2009-05-13 | 甘肃正生生物科技有限公司 | Method for producing high-purity glutathione |
| CN104560707A (en) * | 2015-02-06 | 2015-04-29 | 江苏诚信药业有限公司 | Technological method and system for enzymatically synthesizing L-ascorbic acid 2-glucoside |
Non-Patent Citations (1)
| Title |
|---|
| 邱燕临 等: "铜离子金属螯合亲和层析分离纯化谷胱甘肽（GSH）的研究", 《中国化学会第四届有机化学学术会议论文集》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106701564A (en) * | 2017-02-12 | 2017-05-24 | 江苏诚信药业有限公司 | Process system and method for preparing arbutin by use of enzyme method |
| CN115594731A (en) * | 2022-10-31 | 2023-01-13 | 南通紫琅生物医药科技有限公司（Cn） | Glutathione decoloring processing technology |
| CN115594731B (en) * | 2022-10-31 | 2023-09-08 | 南通紫琅生物医药科技有限公司 | Glutathione decoloring processing technology |
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Application publication date: 20160831 |