CN101109017A - Method for purifying 5-inosinic acid zymotic fluid by crystallization - Google Patents
Method for purifying 5-inosinic acid zymotic fluid by crystallization Download PDFInfo
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- CN101109017A CN101109017A CNA2007101294873A CN200710129487A CN101109017A CN 101109017 A CN101109017 A CN 101109017A CN A2007101294873 A CNA2007101294873 A CN A2007101294873A CN 200710129487 A CN200710129487 A CN 200710129487A CN 101109017 A CN101109017 A CN 101109017A
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P19/00—Preparation of compounds containing saccharide radicals
- C12P19/26—Preparation of nitrogen-containing carbohydrates
- C12P19/28—N-glycosides
- C12P19/30—Nucleotides
- C12P19/32—Nucleotides having a condensed ring system containing a six-membered ring having two N-atoms in the same ring, e.g. purine nucleotides, nicotineamide-adenine dinucleotide
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- C07B—GENERAL METHODS OF ORGANIC CHEMISTRY; APPARATUS THEREFOR
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Abstract
The invention relates to a method for purifying the 5'-IMP2Na from a 5'-IMP fermenting liquor generated by the microbial fermentation. The invention improves the prior purification procedure, substitutes the prior procedure of an anion exchange resin vessel so as to reduce the yield of the waste water/waste liquid and the usage of the chemical medicine of the acid and alkali and the like in a large scale.
Description
Technical field
The present invention relates to a kind of 5 '-purifying method of inosine acid disodium (IMP2Na).Specifically, relate to a kind of utilize Crystallization Procedure from 5 '-purify 5 t-inosinic acid (IMP) fermented liquid '-method of inosine acid disodium salt.
Background technology
The purine derivative Nucleotide of IMP and so on is often used as the raw material of prophylactic treatment agent, growth stimulant, carcinostatic agent of metabolic disturbance etc. aspect medical, aspect food, is often used as the important substance of foodstuff additive such as condiment.Particularly, IMP is the flavor composition as food, is a kind of natural material that is present in the foods such as meat, fish, can be by flesh of fish extraction method, RNA enzyme decomposition method, microbe fermentation method, the combination of fermentation method and synthesis method, method productions such as RNA decomposition and synthetic combination.But,, all can contain pigment, carbohydrate in its goods no matter be to produce by which kind of method, amino acids, organic acid, compositions such as inorganic salts, therefore, for can obtain to can be used as 5 of foodstuff additive '-inosine acid disodium, just must purify, so that impurity is wherein removed it.
Up to the present, the purifying method known to us has the activated carbon treatment method, the ion-exchange membrane processing method, electroosmose process, the precipitator method, strongly basic anion exchange resin method, the storng-acid cation exchange resin method, the hybrid system of storng-acid cation exchange resin and weak base anion-exchange resin etc.
According to original technology, the general method of purification I MP is from microbial fermentation solution, the filtered liquid of removing the thalline in the fermented liquid with fermented liquid or by the membrane filtration operation is by exchange resin tower deionizing impurity, then, thus bleaching process by utilizing gac and Crystallization Procedure generate resultant articles.But this method has the more waste water/waste liquid of generation, shortcomings such as management and operation more complicated.For it is applied on the industry size, need be improved from economy and productive aspect.
Therefore, the present inventor is in order to overcome above-mentioned shortcoming, by carrying out that repeatedly the IMP cleaning section according to the exchange resin tower operation is carried out improved experiment, finally make the management of industrial aspect become simple, thereby and find to utilize IMP2Na in the less Crystallization Procedure purifying fermentation liquor of waste water/waste liquid generation, thereby finish the present invention.
The technical task that invention will realize
The object of the present invention is to provide a kind of 5 '-purifying method of inosine acid disodium, promptly produce the IMP that is comprised in the fermented liquid of microorganism for purification I MP, replace according to the employed ion exchange resin operation of original technology with Crystallization Procedure, so that the usage quantity of the pharmaceutical chemicals of the generation of waste water/waste liquid and acid in scavenging process, alkali and so on significantly reduces.
Summary of the invention
To achieve these goals, the invention provides and a kind ofly from microbial fermentation solution, purify 5 '-method of inosine acid disodium, aforesaid method comprises following several steps:
Cultivate 5 '-t-inosinic acid produces bacterial strain, then thalline is removed, thereby obtained to contain 5 '-step of the fermented liquid of t-inosinic acid;
In above-mentioned fermented liquid, add the wetting ability organic solvent, thereby make 5 '-step of inosine acid disodium crystallization;
Above-mentioned crystal is dissolved again, utilize gac to make the step of its decolouring then; And
Above-mentioned gac is removed, then with the step of the filtered liquid crystallization of gained.
For the present invention, so long as the bacterial strain that is used to ferment is a bacterial strain of producing IMP, then any bacterial strain all can use.Preferably, be that the coryneform bacteria (Corynebacterium) that frequently is used for the IMP fermentation belongs to bacterial strain.The not special restriction of the fermentation condition of microorganism, preferably, can utilize the substratum and the fermentation condition of following formation:
With 1L is standard, is comprising glucose 46g, fructose 30g, yeast extract 10g, KH
2PO
418g, K
2HPO
442g, urea 6g, MgSO
47H
2O 10g, vitamin H 30 μ g, VitB1-HCl 5mg, pH is in 6～8 substratum 18L, and culture temperature is 30-32 ℃, cultivates about 140 hours.
In according to one embodiment of present invention, at first to cultivate coryneform bacteria (Corynebacterium) and belong to bacterial strain, the fermented liquid that just can obtain approximately to comprise 5% to 10% IMP then is for use.
Cultivating 5 '-after t-inosinic acid produces bacterial strain, thalline is removed, thus obtain to contain 5 '-fermented liquid of t-inosinic acid.The step of removing thalline from microbial fermentation solution can be from filtering, centrifugation, and select in the operation such as thermal treatment and carry out.
In according to one embodiment of present invention, fermented liquid filters the back by the membrane filtration operation and obtains.By this filtration operation, fermented liquid just is separated into filtered liquid and bacterial sediment thing.Employed membrane filter is so long as can be with thalline isolating device from fermented liquid, and then any one filter plant all can use.The working conditions of membrane filter also can be by the relating operation personnel according to thalline isolating mode from fermented liquid being carried out the setting of condition simply.For example, can in advance fermented liquid be heated to about 40～50 ℃, the temperature at fermented liquid is approximately 40～50 ℃ then, and the pressure between the film carries out under the condition of (TMP) 1.2～1.5atm.The size of the hole of employed film (pore) also can be selected simply by the relating operation personnel.
For according to one embodiment of present invention, the filtered liquid that is obtained by the membrane filtration operation be carried out drying treatment, so that the content of its IMP reaches 15～30%.The process of this drying treatment is, the content of the moisture in the filtered liquid is reduced, thereby when the overall volume of filtered liquid is reduced, the operation that the content of IMP is increased relatively.Drying process is widely known in relevant industries.In the example of drying process, comprise drying under reduced pressure.
After concentration process is finished, add the wetting ability organic solvent in the fermented liquid after removing thalline, before carrying out Crystallization Procedure, the pH of the fermented liquid after concentrating is adjusted.Crystallization separate out be generating 5 '-scope of inosine acid disodium salt, that is, under the condition of pH 6～10, generate.Therefore, just the pH of fermented liquid is adjusted in this scope.Preferably, the pH that removes the fermented liquid behind the thalline is adjusted to 7.5～9.5.
The wetting ability organic solvent can use methyl alcohol, ethanol, propyl alcohol, Virahol, or their mixture.Preferably, use can make and obtain the methyl alcohol that the ideal crystal form is suitable for solid-liquid separation most.In addition, use though also employed organic solvent water can be diluted the back,, along with the increase of the ratio of diluting, the addition of solvent also just increases thereupon.Thereby on industrial circle, preferably, the concentration range of solvent is controlled at 80～100 volume %.
Injecting the process of adding organic solvent, temperature can be set in 50～80 ℃, preferably, be set at 65 ± 10 ℃.In addition, injecting the process of adding organic solvent, can implement the cooling operation equitemperature simultaneously and change.
After organic solvent injection interpolation is finished, though also can implement the solid-liquid separation operation immediately,,, can comprise cooling step again in order to improve its yield.
Under the liquid state when crystallization is separated out, the ratio (concentration) that organic solvent is shared though can be the scope of 40～80 volume %,, on industrial circle,, preferably, remain on more than the 50 volume % in order to ensure its yield.
The same by the crystallization that above-mentioned operation obtained with the purification inosine acid disodium method of original technology, difference according to crystalline quality, additional by bleaching process and the Crystallization Procedure of using gac more than 1 time or 2 times, the final inosine acid disodium goods that obtain, in this case, Crystallization Procedure both can be used the wetting ability organic solvent, also can utilize concentrated/crystallisation by cooling method.
Utilize the bleaching process of gac to be, the crystallization that obtains by above-mentioned crystallisation process is dissolved again, drop into gac to its solution then, and stir the regular hour, after the pigment composition is by charcoal absorption, again gac is separated.
After dropping into gac, the pigment composition is being carried out between adsorption cycle, though its temperature can be set in 30～80 ℃,, preferably under 50～70 ℃ condition, operate.
Make the operation of removing the filtered liquid crystallization that is obtained after the gac the same, both can use the wetting ability organic solvent, also can utilize the condensing crystal method with above-mentioned crystallisation procedure does.
The final crystallization of the IMP2Na that the method according to this invention obtained has following characteristic: relatively dry weight, IMP2Na content are 97.0～102.0%, and moisture is below 28.5%, pH (5% solution) 7.0～8.5.
Embodiment
Below, will be described in more details by embodiments of the invention.But, below the example just enumerated of these embodiment for the present invention is described in detail, it is to be confined to these embodiment that scope of the present invention has more than.
Embodiment 1: utilize the method for carrying out crystallization (1 time～3 times) by the wetting ability organic solvent
In the present embodiment, will contain the fermented liquid 6 of IMP, 000ml is heated to 40 ℃, then, at the pressure between the film (TMP) is under the condition of 0.5～3.0atm, and (Ceramic FilterPilot: pore size is 0.1 μ m, and area is 1.0m by membrane filter
2) filter, be separated into bacterial sediment thing and filtered liquid.Then, be 680mmHg with above-mentioned filtered liquid in vacuum tightness, vessel temp is to carry out drying under reduced pressure under 55 ℃ the condition, thereby acquisition IMP content is 25% concentrated solution 1,950ml adjusts to after 7.5 at the pH with concentrated solution, is injected in the crystallization precipitation tube again.Then, with 95 volume % methanol aqueous solutions 3,120ml injected 6 hours, and when beginning to inject methyl alcohol, the temperature of crystallization precipitation tube is 70 ℃, and when methyl alcohol injection interpolation was finished, the temperature of crystallization precipitation tube was 40 ℃.After methyl alcohol injects the interpolation end, once more above-mentioned solution is cooled to 30 ℃, then, with Crystallization Separation (the 1st time).
Is that 30% ratio is dissolved in the deionized water (DIW:deionized water) once more with the crystallization of separating according to IMP concentration, then, add gac, and be to stir 1 hour under 60 ℃ the condition keeping its temperature, then, gac is separated.
At the filtered liquid 2 that will remove gac, after 190ml was injected in the crystallization precipitation tube, keeping its temperature was 55 ℃, and then, with 95 volume % methanol aqueous solutions 1,752ml injected 3 hours.After methyl alcohol injection interpolation is finished, final solution is cooled to 25 ℃, then, crystal separation is come out (the 2nd time).
Is that 30% ratio is dissolved in the deionized water once more with the crystallization of separating according to IMP concentration, then, again to wherein adding gac, and is to stir 1 hour under 60 ℃ the condition keeping temperature, then, gac is separated again.
After the filtered liquid 866ml that will remove gac was injected in the crystallization precipitation tube, keeping its temperature was 60 ℃, then, 95 volume % methanol aqueous solution 866ml was injected 3 hours.After methyl alcohol injects the interpolation end, solution is cooled to 30 ℃ again, and Crystallization Separation is come out, then, carry out drying treatment (the 3rd time).
The final in the present embodiment IMP2Na crystallization that obtains, IMP content are 99.5%, and moisture is 22.7%, and pH is 7.6 (5% aqueous solution), and gross weight is 369.5g.
Embodiment 2: utilize the method for carrying out crystallization (1～2 time)+concentrated/crystallization (3 times) by the wetting ability organic solvent
In the present embodiment, will contain the fermented liquid 3 of IMP, 900ml is heated to 50 ℃, then, at the pressure between the film (TMP) is under the condition of 0.5～3.0atm, and (Ceramic FilterPilot: pore size is 0.1 μ m, and area is 1.0m by membrane filter
2) filter, and the bacterial sediment thing is separated with filtered liquid.Then, be 680mmHg with above-mentioned filtered liquid in vacuum tightness, vessel temp is to carry out drying under reduced pressure under 55 ℃ the condition, is 20% concentrated solution 2 thereby obtain IMP content, 430ml adjusts to after 8.0 at the pH with concentrated solution, is injected in the crystallization precipitation tube.When beginning to inject methyl alcohol, the temperature of crystallization precipitation tube is 65 ℃, and when methyl alcohol injection interpolation was finished, the temperature of crystallization precipitation tube was 30 ℃.After methyl alcohol injects the interpolation end, above-mentioned solution is cooled to 20 ℃, then, again crystal separation is come out (the 1st time).
Is that 30% ratio is dissolved in the deionized water once more with the crystallization of separating according to IMP concentration, then, again to wherein adding gac, and is to stir 1 hour under 60 ℃ the condition keeping temperature, then, gac is separated.
At the filtered liquid 2 that will remove gac, after 190ml was injected in the crystallization precipitation tube, keeping its temperature was 45 ℃, and then, with 95 volume % methanol aqueous solutions 1,970ml injected 3 hours.After methyl alcohol injects the interpolation end, solution is cooled to 30 ℃ again, Crystallization Separation is come out (the 2nd time).
Is that 30% ratio is dissolved in the deionized water once more with the crystal separated according to IMP concentration, then, again to wherein adding gac, and is to stir 1 hour under 60 ℃ the condition keeping temperature, then, gac is separated.
Is 680mmHg with the filtered liquid 866ml that removes gac in vacuum tightness, vessel temp is to carry out drying under reduced pressure under 55 ℃ the condition to handle, IMP concentration is being concentrated into after 68%, be injected into again in the crystallization precipitation tube, then, its temperature is cooled to 15 ℃, and Crystallization Separation is come out with 5 hours, then, carry out drying treatment (the 3rd time).
The final in the present embodiment IMP2Na crystallization that obtains, IMP content are 101.0%, and moisture is 20.4%, and pH is 7.9 (5% aqueous solution), and gross weight is 255.8g.
Embodiment 3: carry out the method for crystallization (1 time)+concentrated/crystallization (2～3 times) by utilizing the wetting ability organic solvent
In the present embodiment, will contain the fermented liquid 4 of IMP, 600ml is heated to 50 ℃, then, at the pressure between the film (TMP) is under the condition of 0.5～3.0atm, and (Ceramic FilterPilot: pore size is 0.1 μ m, and area is 1.0m by membrane filter
2) filter, and the bacterial sediment thing is separated with filtered liquid.Then, be 680mmHg with above-mentioned filtered liquid in vacuum tightness, vessel temp is to carry out drying under reduced pressure under 55 ℃ the condition, is 30% concentrated solution 1 thereby obtain IMP content, 010ml adjusts to after 8.5 at the pH with concentrated solution, is injected in the crystallization precipitation tube.Then, with 95 volume % methanol aqueous solutions 1,515ml injected 4 hours, and when beginning to inject methyl alcohol, the temperature of crystallization precipitation tube is 75 ℃, and when methyl alcohol injection interpolation was finished, the temperature of crystallization precipitation tube was 35 ℃.After methyl alcohol injects the interpolation end, more above-mentioned solution is cooled to 25 ℃, Crystallization Separation is come out (1 time).
Is that 30% ratio is dissolved in the deionized water once more with the crystallization of separating according to IMP concentration, then, adds gac, and after to keep temperature be to stir 1 hour under 60 ℃ the condition, gac is separated.
The filtered liquid 1 of gac will be removed, 270ml is 680mmHg in vacuum tightness, vessel temp is to carry out drying under reduced pressure under 55 ℃ the condition to handle, IMP concentration is being concentrated into after 68%, be injected in the crystallization precipitation tube, then, in 4 hours, its temperature is cooled to 15 ℃ after, crystal separation is come out (the 2nd time).
Is that 30% ratio is dissolved in the deionized water once more with the crystallization of separating according to IMP concentration, then, adds gac, and after to keep temperature be to stir 1 hour under 60 ℃ the condition, gac is separated.
Is 680mmHg with the filtered liquid 633ml that removes gac in vacuum tightness, vessel temp is to carry out drying under reduced pressure under 55 ℃ the condition to handle, IMP concentration is being concentrated into after 68%, be injected in the crystallization precipitation tube, then, its temperature is cooled to 12 ℃, and Crystallization Separation is come out with 5 hours, after, carry out drying treatment (3 times).
The final in the present embodiment IMP2Na crystallization that obtains, IMP content are 99.9%, and moisture is 16.8%, and pH is 7.8 (5% aqueous solution), and gross weight is 179.7g.
Beneficial effect
According to the present invention from microbial fermentation solution the method for purification I MP, do not need to carry out amberlite Fat tower operation, only just can produce by Crystallization Procedure can be as the IMP2Na of food additives use Goods owing to do not pass through the exchange resin tower operation, thereby can make waste liquid in cleaning procedure/useless The use amount of the chemicals of the generation of water and the acid of using as eluent/regenerative agent, alkali and so on significantly Reduce.
Claims (11)
- One kind from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, comprise following several steps:Cultivate 5 '-t-inosinic acid produces bacterial strain, then thalline is removed, thereby obtained to contain 5 '-step of the fermented liquid of t-inosinic acid;In above-mentioned fermented liquid, add the wetting ability organic solvent, thereby make 5 '-step of inosine acid disodium crystallization;Above-mentioned crystal is dissolved again, utilize gac to make the step of its decolouring then; AndAbove-mentioned gac is removed, then with the step of the filtered liquid crystallization of gained.
- 2. as claimed in claim 1ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that above-mentioned step of removing thalline can be from filtering, centrifugation, and select in the operation such as thermal treatment.
- 3. as claimed in claim 1ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that, the above-mentioned pH that removes the fermented liquid behind the thalline is adjusted to 6～10.
- 4. as claimed in claim 3ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that the pH of the fermented liquid behind the above-mentioned removal thalline is adjusted to 7.5～9.5.
- 5. as claimed in claim 1ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that above-mentioned wetting ability organic solvent can be from methyl alcohol, ethanol, propyl alcohol is selected more than one solvent in Virahol and their mixture.
- 6. as claimed in claim 1ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that above-mentioned wetting ability organic solvent is a methyl alcohol.
- 7. as claimed in claim 1ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that the interpolation of above-mentioned wetting ability organic solvent is to carry out under 50～80 ℃ condition.
- 8. as claimed in claim 1ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that, after adding above-mentioned organic solvent, also comprise the refrigerative step.
- 9. as claimed in claim 1ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that utilizing the above-mentioned gac step of decolouring is to carry out under 30～80 ℃ condition.
- 10. as claimed in claim 1ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that the step of utilizing above-mentioned gac to decolour need be implemented more than 2 times.
- 11. as claimed in claim 1ly from bacterial strain fermentation liquor, purify 5 '-method of inosine acid disodium, it is characterized in that the step to the filtered liquid crystallization that obtains after removing above-mentioned gac can be utilized organic solvent or utilize spissated method.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| KR1020060067305A KR100828706B1 (en) | 2006-07-19 | 2006-07-19 | A method for purifying 5'-Inosinic acid fermentation broth via crystallization process |
| KR1020060067305 | 2006-07-19 |
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| CN101109017A true CN101109017A (en) | 2008-01-23 |
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| CNA2007101294873A Pending CN101109017A (en) | 2006-07-19 | 2007-07-19 | Method for purifying 5-inosinic acid zymotic fluid by crystallization |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102199182A (en) * | 2011-04-10 | 2011-09-28 | 浙江钱江生物化学股份有限公司 | One-step extraction method for disodium 5'-inosinate |
| CN111286521A (en) * | 2020-03-02 | 2020-06-16 | 通辽梅花生物科技有限公司 | Preparation method of flavour development nucleotide disodium |
| CN111748592A (en) * | 2020-07-17 | 2020-10-09 | 通辽梅花生物科技有限公司 | Preparation method of high-purity flavor nucleotide disodium |
| CN114302888A (en) * | 2019-10-17 | 2022-04-08 | Cj第一制糖株式会社 | Method for separating disodium 5' -inosinate |
| RU2795523C1 (en) * | 2019-10-17 | 2023-05-04 | СиДжей ЧеилДжеданг Корпорейшн | Method for separating 5'-inosinate disodium |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101896240B1 (en) | 2018-06-20 | 2018-10-18 | 주식회사 아리바이오 | Decolorization method of Aureobasidium pullulans fermentation broth |
| KR102282384B1 (en) * | 2019-11-20 | 2021-07-27 | 씨제이제일제당 주식회사 | Purification method of nucleic acid |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NL6601640A (en) | 1965-02-11 | 1966-08-12 | ||
| US3634193A (en) | 1965-06-10 | 1972-01-11 | Takeda Chemical Industries Ltd | Method for the production of inosine and 5{40 -inosinic acid |
| JPH0669386B2 (en) | 1987-03-18 | 1994-09-07 | 協和醗酵工業株式会社 | Process for producing 5'-inosinic acid |
-
2006
- 2006-07-19 KR KR1020060067305A patent/KR100828706B1/en active IP Right Grant
-
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- 2007-07-19 CN CNA2007101294873A patent/CN101109017A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102199182A (en) * | 2011-04-10 | 2011-09-28 | 浙江钱江生物化学股份有限公司 | One-step extraction method for disodium 5'-inosinate |
| CN114302888A (en) * | 2019-10-17 | 2022-04-08 | Cj第一制糖株式会社 | Method for separating disodium 5' -inosinate |
| RU2795523C1 (en) * | 2019-10-17 | 2023-05-04 | СиДжей ЧеилДжеданг Корпорейшн | Method for separating 5'-inosinate disodium |
| CN114302888B (en) * | 2019-10-17 | 2024-08-06 | Cj第一制糖株式会社 | Separation method of disodium 5' -inosinate |
| CN111286521A (en) * | 2020-03-02 | 2020-06-16 | 通辽梅花生物科技有限公司 | Preparation method of flavour development nucleotide disodium |
| CN111748592A (en) * | 2020-07-17 | 2020-10-09 | 通辽梅花生物科技有限公司 | Preparation method of high-purity flavor nucleotide disodium |
| CN111748592B (en) * | 2020-07-17 | 2022-03-15 | 通辽梅花生物科技有限公司 | Preparation method of high-purity flavor nucleotide disodium |
Also Published As
| Publication number | Publication date |
|---|---|
| KR100828706B1 (en) | 2008-05-09 |
| KR20080007985A (en) | 2008-01-23 |
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Owner name: CJ CHEIL JEDANG CORP. Free format text: FORMER OWNER: CJ CO., LTD. Effective date: 20080829 |
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Effective date of registration: 20080829 Address after: Seoul, South Korea Applicant after: CJ Corp. Address before: Seoul, South Korea Applicant before: CJ Co., Ltd. |
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Application publication date: 20080123 |