JPH0366663A - Method for recovering methionine and alkali metal carbonate - Google Patents
Method for recovering methionine and alkali metal carbonateInfo
- Publication number
- JPH0366663A JPH0366663A JP1201558A JP20155889A JPH0366663A JP H0366663 A JPH0366663 A JP H0366663A JP 1201558 A JP1201558 A JP 1201558A JP 20155889 A JP20155889 A JP 20155889A JP H0366663 A JPH0366663 A JP H0366663A
- Authority
- JP
- Japan
- Prior art keywords
- alkali metal
- methionine
- metal carbonate
- aqueous solution
- impurities
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 229930182817 methionine Natural products 0.000 title claims abstract description 43
- FFEARJCKVFRZRR-BYPYZUCNSA-N L-methionine Chemical compound CSCC[C@H](N)C(O)=O FFEARJCKVFRZRR-BYPYZUCNSA-N 0.000 title claims abstract description 42
- 229910000288 alkali metal carbonate Inorganic materials 0.000 title claims abstract description 26
- 150000008041 alkali metal carbonates Chemical class 0.000 title claims abstract description 26
- 238000000034 method Methods 0.000 title claims description 17
- 229910052783 alkali metal Inorganic materials 0.000 claims abstract description 22
- 239000007864 aqueous solution Substances 0.000 claims abstract description 22
- 239000012535 impurity Substances 0.000 claims abstract description 22
- -1 alkali metal bicarbonate Chemical class 0.000 claims abstract description 21
- 238000000909 electrodialysis Methods 0.000 claims abstract description 17
- 239000012528 membrane Substances 0.000 claims abstract description 8
- 238000005341 cation exchange Methods 0.000 claims abstract description 7
- 239000003011 anion exchange membrane Substances 0.000 claims description 5
- 239000012266 salt solution Substances 0.000 claims description 3
- 239000000243 solution Substances 0.000 abstract description 12
- 239000003729 cation exchange resin Substances 0.000 abstract description 3
- 239000003957 anion exchange resin Substances 0.000 abstract 1
- 230000015572 biosynthetic process Effects 0.000 abstract 1
- 239000000126 substance Substances 0.000 abstract 1
- 238000011084 recovery Methods 0.000 description 12
- 239000000706 filtrate Substances 0.000 description 10
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 239000003513 alkali Substances 0.000 description 6
- 239000002253 acid Substances 0.000 description 5
- 239000006103 coloring component Substances 0.000 description 5
- 239000003014 ion exchange membrane Substances 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 4
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 4
- 229910052700 potassium Inorganic materials 0.000 description 4
- 239000011591 potassium Substances 0.000 description 4
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 238000010494 dissociation reaction Methods 0.000 description 3
- 230000005593 dissociations Effects 0.000 description 3
- 239000003792 electrolyte Substances 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 239000010936 titanium Substances 0.000 description 3
- 229910052719 titanium Inorganic materials 0.000 description 3
- UKAUYVFTDYCKQA-UHFFFAOYSA-N -2-Amino-4-hydroxybutanoic acid Natural products OC(=O)C(N)CCO UKAUYVFTDYCKQA-UHFFFAOYSA-N 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 2
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- UKAUYVFTDYCKQA-VKHMYHEASA-N L-homoserine Chemical compound OC(=O)[C@@H](N)CCO UKAUYVFTDYCKQA-VKHMYHEASA-N 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 229910000272 alkali metal oxide Inorganic materials 0.000 description 2
- 150000001340 alkali metals Chemical class 0.000 description 2
- 150000001447 alkali salts Chemical class 0.000 description 2
- 150000001413 amino acids Chemical class 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- WJRBRSLFGCUECM-UHFFFAOYSA-N hydantoin Chemical compound O=C1CNC(=O)N1 WJRBRSLFGCUECM-UHFFFAOYSA-N 0.000 description 2
- 229940091173 hydantoin Drugs 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- 230000003301 hydrolyzing effect Effects 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 230000003472 neutralizing effect Effects 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 229910052697 platinum Inorganic materials 0.000 description 2
- 229920006254 polymer film Polymers 0.000 description 2
- XAEFZNCEHLXOMS-UHFFFAOYSA-M potassium benzoate Chemical compound [K+].[O-]C(=O)C1=CC=CC=C1 XAEFZNCEHLXOMS-UHFFFAOYSA-M 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- SBKRXUMXMKBCLD-UHFFFAOYSA-N 5-(2-methylsulfanylethyl)imidazolidine-2,4-dione Chemical compound CSCCC1NC(=O)NC1=O SBKRXUMXMKBCLD-UHFFFAOYSA-N 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 238000002835 absorbance Methods 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- 229910001413 alkali metal ion Inorganic materials 0.000 description 1
- 150000001450 anions Chemical class 0.000 description 1
- 125000002843 carboxylic acid group Chemical group 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 238000004040 coloring Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 238000000502 dialysis Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 159000000011 group IA salts Chemical class 0.000 description 1
- 150000001469 hydantoins Chemical class 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 description 1
- 229910052939 potassium sulfate Inorganic materials 0.000 description 1
- 235000019252 potassium sulphite Nutrition 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 125000001453 quaternary ammonium group Chemical group 0.000 description 1
- 125000000542 sulfonic acid group Chemical group 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Abstract
Description
【発明の詳細な説明】 〈産業上の利用分野〉 本発明は、メチオニンの回収方法に関する。[Detailed description of the invention] <Industrial application field> The present invention relates to a method for recovering methionine.
さらに詳しくは電気透析による不純物の少ないメチオニ
ンおよびアルカリ金属炭酸塩の回収方法に関する。More specifically, the present invention relates to a method for recovering methionine and alkali metal carbonate with few impurities by electrodialysis.
〈従来の技術〉
メチオニンは５−（β−メチルメルカプトエチル）−ヒ
ダントインをアルカリの存在下に加水分解し、溶液を酸
で中和し、結晶を析出、分離させて得られる。この場合
アルカリとしてアルカリ金属炭酸塩とアルカリ金属水酸
化物の混合物、酸として二酸化炭素を〈特公昭４３．−
１９５３０号公報）、またアルカリとしてアルカリ金属
炭酸塩および／またはアルカリ金属重炭酸塩、酸として
二酸化炭素を（特公昭５４−９１７４号公報）使用して
行われる。<Prior Art> Methionine is obtained by hydrolyzing 5-(β-methylmercaptoethyl)-hydantoin in the presence of an alkali, neutralizing the solution with an acid, and precipitating and separating crystals. In this case, a mixture of alkali metal carbonate and alkali metal hydroxide is used as the alkali, and carbon dioxide is used as the acid. −
19530), and using an alkali metal carbonate and/or alkali metal bicarbonate as the alkali and carbon dioxide as the acid (Japanese Patent Publication No. 54-9174).
メチオニンを晶析分離後の濾液にはメチオニンの一部が
溶存し、これを回収するために濾液を濃縮し、さらに晶
析分離したり、濾液のリサイクル使用（特公昭５４−９
１７４号公報）が行われる。A part of methionine is dissolved in the filtrate after methionine is crystallized and separated, and in order to recover it, the filtrate is concentrated and further crystallized, or the filtrate is recycled (Japanese Patent Publication No. 54-9
No. 174) will be carried out.
またヒダントイン類の加水分解後、溶液からアミノ酸を
得る方法として、陽イオン交換樹脂と溶液を接触させて
イオン交換する方法、溶液を電気分解してアミノ酸と苛
性アルカリにする方法、電気透析によって分離する方法
（特開昭６２−３０７４２号公報）が知られている。After hydrolysis of hydantoins, amino acids can be obtained from the solution by ion exchange by contacting the solution with a cation exchange resin, by electrolyzing the solution to produce amino acids and caustic alkali, and by electrodialysis. A method (Japanese Unexamined Patent Publication No. 62-30742) is known.
〈発明が解決しようとする課題〉
しかしながら、メチオニンを晶析、濾過分離後の濾液を
濃縮してさらに晶析分離する方法によってもメチオニン
の回収は１００％にならないし、濾液のリサイクル使用
を行う場合でもホモセリンのような不純物や着色成分等
の蓄積が生じるために、ある一定比率でもって濾液を廃
棄しなければならない。廃棄する濾液にアセトン等の有
機溶剤を添加してメチオニン等を晶析分離してさらに回
収することも可能であるが非常に複雑なプロセスとなる
。<Problems to be Solved by the Invention> However, even with the method of crystallizing methionine, concentrating the filtrate after filtration separation, and further crystallizing and separating it, the recovery of methionine is not 100%, and when the filtrate is recycled and used. However, due to the accumulation of impurities such as homoserine and coloring components, a certain proportion of the filtrate must be discarded. Although it is possible to add an organic solvent such as acetone to the filtrate to be discarded and crystallize and separate methionine and the like for further recovery, this is a very complicated process.
陽イオン交換樹脂を用いる方法は多量の酸、アルカリを
必要とするとともに、バッチシステムでの操作を行わな
ければならないので工業上問題点が多い。The method using a cation exchange resin requires a large amount of acid or alkali, and requires operation in a batch system, which poses many industrial problems.
電解法は電気透析法に比べ高電圧を必要とし、装置が大
規模となり、かつ電力を多く使用する等大きな欠点があ
る。The electrolytic method requires a higher voltage than the electrodialysis method, requires a larger scale apparatus, and has major drawbacks such as requiring a large amount of electricity.
電気透析法も電解法と同様にスケールメリットを期待で
きず、加水分解液を全て透析にかけるとコストがかかり
過ぎる欠点がある。そして従来の電気透析法はメチオニ
ンと無機塩との分離を目的とするもので、この方法を晶
析分離濾液に適用してもホモセリンのような不純物や着
色成分とメチオニンを分離することはできない。Like the electrolytic method, the electrodialysis method cannot be expected to achieve economies of scale, and has the drawback that it is too costly to subject all the hydrolyzed solution to dialysis. Conventional electrodialysis methods are aimed at separating methionine and inorganic salts, and even if this method is applied to the crystallization separation filtrate, it is not possible to separate methionine from impurities such as homoserine or coloring components.
かかる事情に鑑み、メチオニン、アルカリ金属炭酸塩お
よび／またはアルカリ金属重炭酸塩および不純物を含む
水溶液から不純物の含まないメチオニン、アルカリ金属
炭酸塩および／またはアルカリ金属重炭酸塩を回収する
方法について鋭意検討した結果、本発明を完成するに至
った。In view of these circumstances, we are conducting intensive studies on methods for recovering methionine, alkali metal carbonates, and/or alkali metal bicarbonates, and impurity-free methionine, alkali metal carbonates, and/or alkali metal bicarbonates from aqueous solutions containing impurities. As a result, the present invention was completed.
〈課題を解決するための手段〉
すなわち、本発明は陽イオン交換膜と陰イオン交換膜が
交互に組み込まれて構成される電気透析槽の並列する室
の一室おきに、不純物、アルカリ金属炭酸塩および／ま
たはアルカリ金属重炭酸塩を含むメチオニンのアルカリ
塩水溶液とアルカリ金属炭酸塩および／またはアルカリ
金属重炭酸塩水溶液を流して、電気透析することを特徴
とするメチオニンおよびアルカリ金属炭酸塩および／ま
たはアルカリ金属重炭酸塩の回収方法である。<Means for Solving the Problems> In other words, the present invention is capable of removing impurities, alkali metal carbonate, Methionine and alkali metal carbonate and/or electrodialyzed by flowing an aqueous solution of alkali salt of methionine containing salt and/or alkali metal bicarbonate and an aqueous solution of alkali metal carbonate and/or alkali metal bicarbonate. Alternatively, it is a method for recovering alkali metal bicarbonate.
本発明の不純物、アルカリ金属炭酸塩および／またはア
ルカリ金属重炭酸塩を含むメチオニンのアルカリ塩水溶
液の例として、５−（β−メチルメルカブトエチル）−
ヒダントインをアルカリの存在下に加水分解し、溶液を
酸で中和してメチオニンを晶析分離した後の濾液、およ
びこの濾液を濃縮した水溶液が挙げられる。As an example of an aqueous solution of an alkali salt of methionine containing an impurity, an alkali metal carbonate and/or an alkali metal bicarbonate, 5-(β-methylmercabutethyl)-
Examples include a filtrate obtained by hydrolyzing hydantoin in the presence of an alkali, neutralizing the solution with an acid, and crystallizing and separating methionine, and an aqueous solution obtained by concentrating this filtrate.
本発明を図面にもとに説明する。第１図は本発明の一例
を示す図である。The present invention will be explained based on the drawings. FIG. 1 is a diagram showing an example of the present invention.
電気透析槽１の両端には陽極２および陰極３が設けられ
、その間は陽イオン交換膜４および陰イオン交換膜５で
交互に仕切られ、並列する複数の室が構成されている。An anode 2 and a cathode 3 are provided at both ends of the electrodialysis cell 1, and the space between them is alternately partitioned by cation exchange membranes 4 and anion exchange membranes 5 to form a plurality of parallel chambers.
陽極２および陰極３のある室は陽極室６および陰極室７
であり、これらの間は中間室８および中間室９が交互に
配置されている。The chambers containing the anode 2 and cathode 3 are anode chamber 6 and cathode chamber 7.
Between these, intermediate chambers 8 and 9 are arranged alternately.
陽極２としては白金、白金メツキチタン等が、陰極３と
しては鉄、ニッケル、ニッケルメッキ鉄、白金、白金メ
ツキチタン等が用いられる。As the anode 2, platinum, platinum-plated titanium, etc. are used, and as the cathode 3, iron, nickel, nickel-plated iron, platinum, platinum-plated titanium, etc. are used.
陽イオン交換膜４としてはその構造中にそれぞれスルフ
ォン酸基、カルボン酸基等を、陰イオン交換膜５として
はその構造中に四級アンモニウム基等を有する高分子フ
ィルムが用いられ、いずれも市販されている。As the cation exchange membrane 4, a polymer film having a sulfonic acid group, a carboxylic acid group, etc. in its structure is used, and as the anion exchange membrane 5, a polymer film having a quaternary ammonium group, etc. in its structure is used, and both are commercially available. has been done.
陽極室６および陰極室７にはに２ＣＯ３、Ｋ２ＳＯ３、
Ｎ ａ ｚ ＣＯ３、ＮａｚＳＯ，等の電解質水溶液１
２を供給し、中間室８にはＫｉｃＯｓ、Ｎ ａ ２ Ｃ
Ｏ２、ＫＨＣＯ，、ＮａＨＣＯｉ等のアルカリ金属炭酸
塩またはアルカリ金属重炭酸塩水溶液１１を供給する。The anode chamber 6 and the cathode chamber 7 contain 2CO3, K2SO3,
Electrolyte aqueous solution 1 such as Naz CO3, NazSO, etc.
2 is supplied, and the intermediate chamber 8 is supplied with KicOs, Na 2 C
An aqueous alkali metal carbonate or alkali metal bicarbonate solution 11 such as O2, KHCO, NaHCOi, etc. is supplied.
中間室９には本発明の対象とする不純物、アルカリ金属
炭酸塩および／またはアルカリ金属重炭酸塩を含むメチ
オニンのアルカリ塩水溶液を供給する。この水溶液のｐ
Ｈはメチオニンの等電点より充分に高くしておく。An aqueous alkaline salt solution of methionine containing an impurity targeted by the present invention, an alkali metal carbonate and/or an alkali metal bicarbonate, is supplied to the intermediate chamber 9 . p of this aqueous solution
H is set sufficiently higher than the isoelectric point of methionine.
陽極室６、陰極室７、中間室８および中間室９に供給す
る水溶液は通常、循環して通液される。The aqueous solution supplied to the anode chamber 6, cathode chamber 7, intermediate chamber 8, and intermediate chamber 9 is normally circulated.
次に陽極２と陰極３の間に電圧をかけると、中間室９の
アルカリ金属イオンは陽イオン交換膜４を透過して中間
室８に移行し、メチオニン、炭酸イオン、重炭酸イオン
は陰イオン交換膜５を透過して中間室８へ移行する。し
たがってメチオニン、アルカリ金属炭酸塩および／また
はアルカリ金属重炭酸塩は中間室８より回収される。Next, when a voltage is applied between the anode 2 and the cathode 3, the alkali metal ions in the intermediate chamber 9 pass through the cation exchange membrane 4 and move to the intermediate chamber 8, and methionine, carbonate ions, and bicarbonate ions are converted into anions. It passes through the exchange membrane 5 and moves to the intermediate chamber 8. Methionine, alkali metal carbonate and/or alkali metal bicarbonate are therefore recovered from intermediate chamber 8.
中間室９の水溶液中に含まれる着色成分の如き不純物は
、その解離度がメチオニンに比べて低いためにイオン交
換膜を透過し難い。したがってメチオニン等は着色成分
の如き不純物の含有量の少い水溶液の形で回収出来る。Impurities such as colored components contained in the aqueous solution in the intermediate chamber 9 have a lower degree of dissociation than methionine, and therefore are difficult to permeate through the ion exchange membrane. Therefore, methionine and the like can be recovered in the form of an aqueous solution with a low content of impurities such as coloring components.
イオン交換膜を透過せずに残った不純物は最終廃液とし
て系外へ排出される。Impurities that remain without passing through the ion exchange membrane are discharged out of the system as final waste liquid.
中間室９に供給する水溶液のｐＨは８〜１１が適当であ
る。ｐＨ８未満では等電点がｐＨ６付近にあるメチオニ
ンの解離度が低いため、イオン交換膜を透過し難く、し
たがってメチオニンは充分回収されない。ｐＨ＝１１を
越えると着色成分の如き不純物の解離度も高くなり、回
収液中に不純物の量が増大する。メチオニン等の回収率
または不純物の許容量を勘案してｐＨは設定される。The pH of the aqueous solution supplied to the intermediate chamber 9 is suitably 8 to 11. If the pH is less than 8, the degree of dissociation of methionine whose isoelectric point is around pH 6 is low, so it is difficult to permeate through the ion exchange membrane, and therefore methionine is not sufficiently recovered. When pH exceeds 11, the degree of dissociation of impurities such as coloring components also increases, and the amount of impurities in the recovered liquid increases. The pH is set in consideration of the recovery rate of methionine and the like or the allowable amount of impurities.
中間室９に供給する水溶液のアルカリ金属炭酸塩および
／またはアルカリ金属重炭酸塩の濃度はアルカリ金属濃
度として３〜２０ｗｔ％が適当である。３ｗｔ％未満で
は処理能力が低くなり、２０ｗｔ％を越えると結晶の析
出等の問題が生じるので好ましくない。The concentration of the alkali metal carbonate and/or alkali metal bicarbonate in the aqueous solution supplied to the intermediate chamber 9 is suitably 3 to 20 wt% in terms of alkali metal concentration. If it is less than 3 wt%, the processing capacity will be low, and if it exceeds 20 wt%, problems such as crystal precipitation will occur, which is not preferable.
一方、中間室８に供給されるに、ＣＯ２、ＮａｚＣＯ４
、Ｎ ａ ＨＣＯｓ等のアルカリ金属炭酸塩またはアル
カリ金属重炭酸塩水溶液の濃度は２〜ｌＱｗｔ％の範囲
が用いられる。２ｗｔ％未満では電導度が低く、ｌ ９
ｗｔ％を越すと電流効率の低下を招き好ましくない。On the other hand, CO2, NazCO4 are supplied to the intermediate chamber 8.
The concentration of the aqueous alkali metal carbonate or alkali metal bicarbonate solution, such as NaHCOs, is in the range of 2 to 1Qwt%. If it is less than 2 wt%, the conductivity is low, l 9
If it exceeds wt%, the current efficiency will decrease, which is not preferable.
また陽極室６および陰極室７に供給されるに２ＣＯ３、
Ｋ２ＳＯ４、Ｎ ａ ２ ＣＯ２、Ｎ ａ ２ ＳＯ２
等の電解質水溶液の濃度は、中間室８への供給液の場合
と同じ理由で２〜ｌ ９ｗｔ％が適当である。In addition, 2CO3 is supplied to the anode chamber 6 and the cathode chamber 7,
K2SO4, Na2CO2, Na2SO2
The appropriate concentration of the electrolyte aqueous solution is 2 to 9 wt % for the same reason as the case of the solution supplied to the intermediate chamber 8.
中間室８より回収される不純物を含まないメチオニン、
アルカリ金属炭酸塩および／またはアルカリ金屑重炭酸
塩の溶液はヒダントインの加水分解工程に循環使用され
る。impurity-free methionine recovered from the intermediate chamber 8;
The alkali metal carbonate and/or alkali metal scrap bicarbonate solution is recycled to the hydantoin hydrolysis step.
〈発明の効果〉
本発明の方法により、不純物、アルカリ金属炭酸塩およ
び／またはアルカリ金属重炭酸塩を含むメチオニンのア
ルカリ塩水溶液から容易に不純物を含まないメチオニン
等を回収することができる。<Effects of the Invention> According to the method of the present invention, methionine and the like free of impurities can be easily recovered from an aqueous aqueous salt of methionine containing impurities, alkali metal carbonates, and/or alkali metal bicarbonates.
〈実施例〉
以下、本発明を実施例により更に具体的に説明するが、
本発明はこれら実施例に限定されない。<Examples> Hereinafter, the present invention will be explained in more detail with reference to Examples.
The invention is not limited to these examples.
実施例１
第１図に示すような中間室９を４室および中間室８を４
室備えた電気透析槽を用いた。Example 1 Four intermediate chambers 9 and four intermediate chambers 8 as shown in FIG.
An electrodialysis tank equipped with a chamber was used.
陽極２、陰極３として大きさが６．８ ｃｒｌの白金メ
ツキチタンを用いた。Platinum-plated titanium with a size of 6.8 crl was used as the anode 2 and the cathode 3.
陽イオン交換膜として強酸性イオン交換膜で、あるネオ
セプタＣＭ−１、陰イオン交換膜として強塩基性イオン
交換膜であるネオセプタＡＭ−１（いずれも徳山曹達■
製で大きさは６．８ｃｒｌ）を使用した。Neocepta CM-1 is a strongly acidic ion exchange membrane as a cation exchange membrane, and Neocepta AM-1 is a strongly basic ion exchange membrane as an anion exchange membrane (both manufactured by Tokuyama Soda).
A size 6.8 crl) was used.
中間室９にはｐ Ｈ８，５、カリウム濃度３ｗｔ％、メ
チオニン濃度３．５ ｗ ｔ％、重炭酸イオン濃度Ｉ
９ｗｔ％のメチオニンのカリウム塩水溶液１００ｍｇを
、陽極室６、陰極室７および中間室８それぞれに３ｗｔ
％に２Ｃ○コ水溶液を各１００−を循環させた。The intermediate chamber 9 has a pH of 8.5, a potassium concentration of 3 wt%, a methionine concentration of 3.5 wt%, and a bicarbonate ion concentration of I.
100 mg of a 9 wt% potassium salt aqueous solution of methionine was added to each of the anode chamber 6, cathode chamber 7, and intermediate chamber 8 in an amount of 3 wt.
% of each 100% of the 2C◯ aqueous solution was circulated.
次いで初期の電流密度を５Ａ／ｄｍ２に設定して直流電
流を流し、その後電圧がほぼ７，５Ｖになるように電流
密度を調整し、電流密度が１Ａ／ｄｍ”迄下った時点で
電気透析を終了させた。Next, the initial current density was set to 5 A/dm2 and a direct current was applied, and then the current density was adjusted so that the voltage was approximately 7.5 V, and when the current density dropped to 1 A/dm, electrodialysis was performed. Finished it.
４゜ 電気透析中、液の温度は４０℃に保った。4゜ During electrodialysis, the temperature of the solution was maintained at 40°C.
電気透析終了後分析を行った結果、カリウムの回収率は
９８％、メチオニンの回収率は５５％、重炭酸イオンの
回収率は９６％であった。As a result of analysis after the electrodialysis, the recovery rate of potassium was 98%, the recovery rate of methionine was 55%, and the recovery rate of bicarbonate ion was 96%.
これに対して不純物である着色成分の回収率は５％、す
なわち除去率は９５％であった。On the other hand, the recovery rate of the colored component, which is an impurity, was 5%, that is, the removal rate was 95%.
着色は黄褐色であり、着色成分の回収率は波長４３４
ｎｍにおける吸光度を測定して求めた。The coloring is yellowish brown, and the recovery rate of the colored component is at wavelength 434.
It was determined by measuring the absorbance at nm.
実施例２
ｐ Ｈ１０，４、カリウム濃度１８ｗｔ％、メチオニン
濃度３ｗｔ％、重炭酸イオン濃度２２ｗｔ％であるメチ
オニンのカリウム塩水溶液を用いた他は、実施例１と同
様に電気透析を行った。Example 2 Electrodialysis was carried out in the same manner as in Example 1, except that an aqueous potassium salt solution of methionine having a pH of 10.4, a potassium concentration of 18 wt%, a methionine concentration of 3 wt%, and a bicarbonate ion concentration of 22 wt% was used.
電気透析終了後分析を行った結果、カリウムの回収率は
９９％、メチオニンの回収率は８８％、重炭酸イオンの
回収率は９７％であった。As a result of analysis after completion of electrodialysis, the recovery rate of potassium was 99%, the recovery rate of methionine was 88%, and the recovery rate of bicarbonate ion was 97%.
これに対して不純物である着色成分の回収率は１１％、
すなわち除去率が８９％であった。In contrast, the recovery rate of coloring components, which are impurities, was 11%.
That is, the removal rate was 89%.
第１図は本発明に係わる電気透析を行う装置の一例を示
す図である。
１・・・電気透析槽、２・・・陽極、３・・・陰極４・
・・陽イオン交換膜、５・・・陰イオン交換膜６・・・
陽極室、７・・・陰極室、８．９・・・中間室１０・・
・メチオニンのアルカリ塩水溶液貯槽１１・・・アルカ
リ金属炭酸塩または金属重炭酸塩水溶液貯槽
１２・・・電解質水溶液貯槽
＼＼
＼
＼
＼
＼
＼
＼
＼
＼
＼FIG. 1 is a diagram showing an example of an apparatus for performing electrodialysis according to the present invention. 1... Electrodialysis tank, 2... Anode, 3... Cathode 4.
...Cation exchange membrane, 5...Anion exchange membrane 6...
Anode chamber, 7... Cathode chamber, 8.9... Intermediate chamber 10...
・Methionine alkaline salt aqueous solution storage tank 11... Alkali metal carbonate or metal bicarbonate aqueous solution storage tank 12... Electrolyte aqueous solution storage tank \\ \ \ \ \ \ \ \ \ \ \ \ \
Claims (1)
れて構成される電気透析槽の並列する室の一室おきに、
ｐＨが８〜１１である不純物、アルカリ金属炭酸塩およ
び／またはアルカリ金属重炭酸塩を含むメチオニンのア
ルカリ塩水溶液とアルカリ金属炭酸塩および／またはア
ルカリ金属重炭酸塩水溶液を流して、電気透析すること
を特徴とするメチオニンおよびアルカリ金属炭酸塩およ
び／またはアルカリ金属重炭酸塩の回収方法。1. In every other parallel chamber of the electrodialysis tank, which is composed of alternating cation exchange membranes and anion exchange membranes,
Electrodialysis by flowing an aqueous methionine aqueous salt solution containing impurities, alkali metal carbonate and/or alkali metal bicarbonate and an alkali metal carbonate and/or alkali metal bicarbonate aqueous solution having a pH of 8 to 11. A method for recovering methionine and alkali metal carbonate and/or alkali metal bicarbonate, characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1201558A JPH0366663A (en) | 1989-08-02 | 1989-08-02 | Method for recovering methionine and alkali metal carbonate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1201558A JPH0366663A (en) | 1989-08-02 | 1989-08-02 | Method for recovering methionine and alkali metal carbonate |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0366663A true JPH0366663A (en) | 1991-03-22 |
Family
ID=16443045
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1201558A Pending JPH0366663A (en) | 1989-08-02 | 1989-08-02 | Method for recovering methionine and alkali metal carbonate |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0366663A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5464717A (en) * | 1993-06-04 | 1995-11-07 | Fuji Xerox Co., Ltd. | Electrophotographic photoreceptor with subbing layer and charge generating layer |
| US5789127A (en) * | 1995-02-14 | 1998-08-04 | Fuji Xerox Co., Ltd. | Electrophotographic photoreceptor |
| CN103922980A (en) * | 2014-04-22 | 2014-07-16 | 中国科学技术大学 | Method for separating methionine from mixed solution of methionine salt and carbonate by using bipolar membrane electrodialysis |
| JP2020520897A (en) * | 2017-05-24 | 2020-07-16 | エボニック オペレーションズ ゲーエムベーハー | Method for producing methionine |
-
1989
- 1989-08-02 JP JP1201558A patent/JPH0366663A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5464717A (en) * | 1993-06-04 | 1995-11-07 | Fuji Xerox Co., Ltd. | Electrophotographic photoreceptor with subbing layer and charge generating layer |
| US5789127A (en) * | 1995-02-14 | 1998-08-04 | Fuji Xerox Co., Ltd. | Electrophotographic photoreceptor |
| CN103922980A (en) * | 2014-04-22 | 2014-07-16 | 中国科学技术大学 | Method for separating methionine from mixed solution of methionine salt and carbonate by using bipolar membrane electrodialysis |
| CN103922980B (en) * | 2014-04-22 | 2016-08-24 | 中国科学技术大学 | A kind of method utilizing bipolar membrane electrodialysis to isolate methionine from the mixed solution of methionine salt and carbonate |
| JP2020520897A (en) * | 2017-05-24 | 2020-07-16 | エボニック オペレーションズ ゲーエムベーハー | Method for producing methionine |
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