JPS60256392A - Treatment of fermentation mixture - Google Patents
Treatment of fermentation mixtureInfo
- Publication number
- JPS60256392A JPS60256392A JP11243084A JP11243084A JPS60256392A JP S60256392 A JPS60256392 A JP S60256392A JP 11243084 A JP11243084 A JP 11243084A JP 11243084 A JP11243084 A JP 11243084A JP S60256392 A JPS60256392 A JP S60256392A
- Authority
- JP
- Japan
- Prior art keywords
- treatment
- resin
- exchange resin
- ion exchange
- fermentation liquid
- 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
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- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
Description
【発明の詳細な説明】
産業上の利用分野
本発明は発酵液の処理法に関し、特にアミノ酸をイオン
交換樹脂を用いて処理する方法の改良に関する。DETAILED DESCRIPTION OF THE INVENTION Field of the Invention The present invention relates to a method for treating fermentation broth, and more particularly to an improvement in a method for treating amino acids using an ion exchange resin.
従来の技術
イオン交換樹脂はアミノ酸等の発酵液の精製に広範に利
用されている。例えばリジン等のアミノ酸発酵液の精製
に際しては、発酵液を酸性にした後イオン交換樹脂処理
してアミノ酸を吸着させ、吸着したアミノ酸を溶出し、
溶出液を濃縮し、晶析するアミノ酸を分離する。BACKGROUND OF THE INVENTION Ion exchange resins are widely used to purify fermentation liquors such as amino acids. For example, when purifying an amino acid fermentation liquid such as lysine, the fermentation liquid is made acidic, treated with an ion exchange resin to adsorb the amino acids, and the adsorbed amino acids are eluted.
Concentrate the eluate and separate the amino acids that crystallize.
アミノ酸の回収率を上げるために、晶出母液は再度イオ
ン交換樹脂塔へ循環される。In order to increase the recovery rate of amino acids, the crystallization mother liquor is recycled to the ion exchange resin column again.
発明が解決しようとする問題点
イオン交換樹脂の吸着能力は発酵液の処理量に比例して
低下し、生産性の低下、廃液量の増加につながる。吸着
能力の低下の原因について検討の結果、原因の1つは発
酵液中に存在する分子量500以下の物質が樹脂のミク
ロポア内部で高分子化するためであり、この影響は樹脂
に流す発酵液の温度が高い程大きいことが見い出され、
従って樹脂に流す発酵液の温度を下げることにより大巾
に改善されることが見い出された。Problems to be Solved by the Invention The adsorption capacity of ion exchange resins decreases in proportion to the amount of fermentation liquid processed, leading to a decrease in productivity and an increase in the amount of waste liquid. As a result of examining the causes of the decrease in adsorption capacity, we found that one of the causes is that substances with a molecular weight of 500 or less that exist in the fermentation liquid become polymerized inside the micropores of the resin, and this effect is due to the fact that the fermentation liquid flowing into the resin It was found that the higher the temperature, the larger the
Therefore, it has been found that lowering the temperature of the fermentation liquid poured into the resin can significantly improve the condition.
さらに、樹脂処理後の晶析母液中にもこの種の悪影響を
支える物質が存在し、この物質は酸性例で樹脂に吸着さ
れ易いことがわかった。Furthermore, it was found that there is a substance that supports this type of adverse effect in the crystallization mother liquor after resin treatment, and that this substance is easily adsorbed by the resin in acidic cases.
本発明が解決しようとする手段
本発明によれば発酵液を酸性にした後、温度を10〜3
2℃に下げてからイオン交換樹脂処理(第1R処理とい
う)することにより樹脂の単位時間当りの処理能力の低
下を減することができる。Means to be Solved by the Present Invention According to the present invention, after making the fermentation liquor acidic, the temperature is adjusted to 10 to 3
By treating the temperature with an ion exchange resin (referred to as 1R treatment) after lowering the temperature to 2° C., it is possible to reduce the decrease in the processing capacity of the resin per unit time.
又、後の晶析工程における晶析母液等目的物を含有する
液を第1R工程へ循環することによって目的物の回収率
を上げることができるが、好ましくは別に設けた第2イ
オン交換樹脂処理(以下第2R処理という)することに
よって目的物の回収率を上げることができる。In addition, the recovery rate of the target product can be increased by circulating the liquid containing the target product such as the crystallization mother liquor in the subsequent crystallization step to the 1R process, but it is preferable to use a second ion exchange resin treatment provided separately. (hereinafter referred to as 2nd R treatment), it is possible to increase the recovery rate of the target object.
該晶出母液中に目的物と競合するイオンの存在は一般に
少なく、従って第2R処理は弱酸性で行うことができる
ので処理能力が維持され、第1R処理工程の処理能力も
低下が小さく極めて長時間当初の処理能力を保持できる
ので経済的に有利である。The presence of ions that compete with the target product in the crystallization mother liquor is generally small, so the 2nd R treatment can be carried out under weak acidity, so the treatment capacity is maintained, and the treatment capacity of the 1st R treatment step is also minimally degraded and can last for an extremely long time. It is economically advantageous because the initial processing capacity can be maintained.
本発明の方法は発酵液を酸性にしてイオン交換樹脂処理
する工程を含む発酵液の精製に適用でき、アミノ酸、特
にリジン、アルギニン、オルニチン等の塩基性アミノ酸
、核酸、抗生物質等の発酵液に適用できる。The method of the present invention can be applied to the purification of fermentation liquid, which includes the step of acidifying the fermentation liquid and treating it with an ion exchange resin, and can be applied to the purification of fermentation liquid, including amino acids, particularly basic amino acids such as lysine, arginine, ornithine, nucleic acids, antibiotics, etc. Applicable.
アミノ酸発酵液を処理する場合を例として、処η 理方
法の詳細を以下に説明す。The details of the treatment method will be explained below, taking as an example the case of treating an amino acid fermentation liquid.
用いられるイオン交換樹脂としては、強酸性ゲル型イオ
ン交換樹脂、例えば5KIB(商品名、三菱化成製品)
、アンバーライト■R−120B(商品名、Rohm
& Haas社製品)、強酸性ポーラス型樹脂、例えば
PKi16(商品名、三菱化成製品)等が例示される。The ion exchange resin used is a strongly acidic gel type ion exchange resin, such as 5KIB (trade name, manufactured by Mitsubishi Kasei).
, Amberlight ■R-120B (product name, Rohm
& Haas Inc.), strongly acidic porous resins such as PKi16 (trade name, Mitsubishi Kasei products), and the like.
発酵液は鉱酸例えば塩酸、硫酸等で酸性好ましくはp
H1,5〜2.0に調整した後第1R処理工程で処理さ
れる。酸性にするとき発酵液の温度が上がるので冷却し
て10〜32℃にする。レジン処理能力維持のために低
い方が好ましいが、エネルギーを多量に消費することに
なるので経済的バランスを考慮して温度を決めればよい
。樹脂処理は一般には樹脂を充した塔に発酵液を通し次
いで水洗する。溶出はアンモニア水等で行われ、目的物
を含有する溶出液を加熱することによってアンモニアを
除去し、濃縮して目的物を晶析させ、分離する。The fermentation liquid is acidified with a mineral acid such as hydrochloric acid or sulfuric acid, preferably p
After adjusting to H1.5 to 2.0, it is processed in the first R treatment step. The temperature of the fermented liquid rises when acidifying it, so cool it to 10-32°C. A lower temperature is preferable in order to maintain resin processing ability, but since a large amount of energy is consumed, the temperature should be determined by considering economic balance. Resin treatment generally involves passing the fermented liquor through a column filled with resin, followed by washing with water. Elution is performed with aqueous ammonia or the like, and the eluate containing the target product is heated to remove ammonia, concentrated, and the target product is crystallized and separated.
該母液を第1R処理工程前に供給して発酵液と共に処理
することにより、晶析母液中に含まれている目的物を回
収することができる。この母液中にも樹脂の処理能力を
低下させる物質が含まれており、酸性側においてその物
質の樹脂への吸着が強いので好ましくは別に第2イオン
交換樹脂塔を設けて処理する。By supplying the mother liquor before the first R treatment step and treating it together with the fermentation liquor, the target substance contained in the crystallization mother liquor can be recovered. This mother liquor also contains substances that reduce the processing ability of the resin, and since these substances are strongly adsorbed to the resin on the acidic side, it is preferable to separately provide a second ion exchange resin column for treatment.
第2R処理工程を設けて晶析母液中の目的物を回収する
に際しては、晶析母液のpHを弱酸性、好ましくは6〜
7にアンモニア等で調整後、第2R処理工程で処理する
。用いられる樹脂は第1R処理工程で用いられる樹脂が
例示され、アンモニア水等を溶出剤として溶出すればよ
い。When the second R treatment step is provided to recover the target substance in the crystallization mother liquor, the pH of the crystallization mother liquor is set to a weakly acidic state, preferably 6 to 6.
After adjusting with ammonia or the like in step 7, it is treated in the second R treatment step. The resin used is exemplified by the resin used in the first R treatment step, and may be eluted using aqueous ammonia or the like as an eluent.
発酵液の種類によって、用いる樹脂、処理条件、その他
を変更することにより最良の方法を見つけることは当業
者にとって極めて容易になしうろことである。It would be extremely easy for those skilled in the art to find the best method by changing the resin used, processing conditions, etc., depending on the type of fermentation liquid.
以下に本発明の態様を実施例によって説明する。Aspects of the present invention will be explained below using examples.
実施例
リジン発酵液100dを硫酸でpH2に調整(液温的5
5℃)した後、液温を25℃に冷却する。100屁の5
KIBを詰めた塔に1001cI!/Hの速さで供給す
る。200妊の水で水洗した後2N−NH,DH水溶液
100kiを約70kJl/Hで供給してリジンを溶出
する(第1R処理理工程)。Example 100 d of lysine fermentation liquid was adjusted to pH 2 with sulfuric acid (liquid temperature 5
5°C), then cool the liquid temperature to 25°C. 5 of 100 farts
1001 cI in a tower filled with KIB! Supply at a speed of /H. After washing with 200 kg of water, 100 kg of a 2N-NH, DH aqueous solution was supplied at a rate of about 70 kJl/H to elute lysine (1st R treatment step).
80妊の溶出液を減圧濃縮してアンモニアを除去し、塩
酸でp H5,5としてリジンを塩酸塩とした後減圧濃
縮し、約6,0OOklのリジン塩酸塩を晶析させる。The eluate of 80 ml was concentrated under reduced pressure to remove ammonia, and the pH was adjusted to pH 5.5 with hydrochloric acid to convert lysine into hydrochloride, followed by concentration under reduced pressure to crystallize about 6.0 OOkl of lysine hydrochloride.
IOVの母液の中7妊を5KIBのレジン塔へ循環し、
3屁の母液のpHをアンモニアで6.5に調整し、上記
樹脂塔と別に設けた15/ci2の5KIBを詰めた塔
1ご送り、上記水洗、溶出。The 7 ml of IOV mother liquor is circulated to the 5 KIB resin tower,
The pH of the three farts of mother liquor was adjusted to 6.5 with ammonia, and sent to column 1 packed with 15/ci2 5KIB, which was provided separately from the resin column, and washed and eluted with water.
濃縮する。以下この工程を繰り返す(本発明方法)。Concentrate. This process is repeated thereafter (method of the present invention).
比較のために発酵液の冷却を行うことなく、又晶析母液
を全量発酵液へ戻す以外は上記と同様に行う(対照法)
。For comparison, the same procedure as above was carried out except that the fermentation liquid was not cooled and the entire crystallization mother liquor was returned to the fermentation liquid (control method).
.
結果を第1表に示す。The results are shown in Table 1.
第 1 表
N;第1R処理工程の樹脂の使用回数
SSC:塩の分解容量(Salt Splitting
Capacity>(eq/j!−R)
A:リジン吸着能(g/β−R〉
効 果
本発明によれば、当初の吸着能力は500回の処理後も
かなり高く維持されている。Table 1 N: Number of times the resin is used in the 1R treatment step SSC: Salt splitting capacity
Capacity>(eq/j!-R) A: Lysine adsorption capacity (g/β-R> Effect) According to the present invention, the initial adsorption capacity is maintained quite high even after 500 treatments.
特許出願人(1,02)協和醗酵工業株式会社手続補正
書
昭和60年8月30日
特許庁長官殿 参
1、事件の表示
昭和59年特許願第112430号
2、発明の名称
発酵液の処理法
3、補正をする者
事件との関係 特許出願人
郵便番号 100
住 所 東京都千代田区大手町−丁目6番1号名称 (
102)協和醗酵工業株式会社明細書の特許請求の範囲
の欄及び発明の詳細な説明の欄
明 細 書
1、発明の名称
発酵液の処理法
2、特許請求の範囲
(1)発酵液をイオン交換樹脂で処理するに際し、該発
酵液のpHを酸性にし、且つ温度を10〜32℃にした
後、イオン交換樹脂処理(第1R処理という)すること
を特徴とする発酵液の処理法。Patent Applicant (1,02) Kyowa Hakko Kogyo Co., Ltd. Procedural Amendment August 30, 1985 Dear Commissioner of the Japan Patent Office Part 1. Indication of the case 1982 Patent Application No. 112430 2. Name of the invention Processing of fermented liquid Law 3, Relationship with the amendment person case Patent applicant postal code 100 Address 6-1 Otemachi-chome, Chiyoda-ku, Tokyo Name (
102) Kyowa Hakko Kogyo Co., Ltd. Claims column and Detailed description of the invention column of the specification Description 1, Name of the invention Method for treating fermented liquor 2, Claims (1) Fermented liquor is ionized A method for treating a fermented liquor, which is characterized in that when treating with an exchange resin, the pH of the fermented liquor is made acidic and the temperature is set at 10 to 32°C, and then treated with an ion exchange resin (referred to as 1R treatment).
(2)イオン交換樹脂処理後の目的物の晶出工程におけ
る晶出母液を濃縮工程に循環する特許請求の範囲第1項
記載の方法。(2) The method according to claim 1, wherein the crystallization mother liquor in the crystallization step of the target product after treatment with the ion exchange resin is recycled to the concentration step.
(3)第1R処理後の晶出工程における晶出母液の」を
別途設けた第2イオン交換樹脂塔で処理する特許請求の
範囲第1ス旦)項記載の方法。(3) The method according to claim 1, wherein the crystallization mother liquor in the crystallization step after the 1R treatment is treated in a separately provided second ion exchange resin tower.
(4)該発酵液がアミノ酸発酵液である特許請求の範囲
第1,2又は3項記載の方法。(4) The method according to claim 1, 2 or 3, wherein the fermentation liquid is an amino acid fermentation liquid.
3、発明の詳細な説明
産業上の利用分野
本発明は発酵液の処理法に関し、特しアミノ酸をイオン
交換樹脂を用いて処理する方法の改良に関する。3. DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention relates to a method for treating fermentation broth, and more particularly to an improvement in a method for treating amino acids using an ion exchange resin.
従来の技術
イオン交換樹脂はアミノ酸等の発酵液の精製に広範に利
用されている。例えばリジン等のアミノ酸発酵液の精製
に際しては、発酵液を酸性にした後イオン交換樹脂処理
してアミノ酸を吸着させ、吸着したアミノ酸を溶出し、
溶出液を濃縮し、晶析するアミノ酸を分離する。BACKGROUND OF THE INVENTION Ion exchange resins are widely used to purify fermentation liquors such as amino acids. For example, when purifying an amino acid fermentation liquid such as lysine, the fermentation liquid is made acidic, treated with an ion exchange resin to adsorb the amino acids, and the adsorbed amino acids are eluted.
Concentrate the eluate and separate the amino acids that crystallize.
アミノ酸の回収率を上げるために、晶出母液は濃縮工程
あるいはイオン交換樹脂塔へ循環される。In order to increase the recovery of amino acids, the crystallization mother liquor is recycled to a concentration step or to an ion exchange resin column.
発明が解決しようとする問題点
イオン交換樹脂の吸着能力は発酵液の処理量に比例して
低下し、生産性の低下、廃液量の増加につながる。吸着
能力の低下の原因について検討の結果、原因の1つは発
酵液中に存在する分子量500以下の物質が樹脂のミク
ロポア内部で高分子化するた狛であり、この影響は樹脂
に流す発酵液の温度が高い程大きいことが見い出され、
従って樹脂に流す発酵液の温度を下げることにより大巾
に改善されることが見い出された。Problems to be Solved by the Invention The adsorption capacity of ion exchange resins decreases in proportion to the amount of fermentation liquid processed, leading to a decrease in productivity and an increase in the amount of waste liquid. As a result of examining the causes of the decrease in adsorption capacity, we found that one of the causes is that substances with a molecular weight of 500 or less present in the fermentation liquid become polymerized inside the micropores of the resin, and this effect is due to the fact that the fermentation liquid flowing into the resin It was found that the higher the temperature, the larger the
Therefore, it has been found that lowering the temperature of the fermentation liquid poured into the resin can significantly improve the condition.
さらに、樹脂処理後の晶析母液中にもこの種の ・悪影
響を支える物質が存在し、この物質は酸性例で樹脂に吸
着され易いことがわかった。Furthermore, it was found that substances that support this type of adverse effect also exist in the crystallization mother liquor after resin treatment, and that these substances are easily adsorbed by the resin in acidic cases.
問題点を解決するための手段
本発明によれば発酵液を酸性にした後、温度を10〜3
2℃に下げてからイオン交換樹脂処理(第1R処理とい
う)することにより樹脂の単位時間当りの処理能力の低
下を減することができる。Means for Solving the Problems According to the present invention, after making the fermentation liquor acidic, the temperature is lowered to 10-3.
By treating the temperature with an ion exchange resin (referred to as 1R treatment) after lowering the temperature to 2° C., it is possible to reduce the decrease in the processing capacity of the resin per unit time.
又、後の晶析工程における晶析母液等目的物を合釘する
液を濃縮工程あるいは第1R工程へ循環することによっ
て目的物の回収率を上げることかできるが、好ましくは
別に設けた第2イオン交換樹旧処理(以下第2R処理と
いう)することによっC目的物の回収率を上げ且つ第1
R工程のレジンD処理能力を長時間維持できる。In addition, it is possible to increase the recovery rate of the target product by circulating the liquid for doweling the target product, such as the crystallization mother liquor in the subsequent crystallization step, to the concentration step or the 1R step, but it is preferable to use a separately provided second By performing ion exchange tree old treatment (hereinafter referred to as 2nd R treatment), the recovery rate of the C target substance is increased and the 1st
The resin D processing ability of the R process can be maintained for a long time.
該晶出母液中に目的物と競合するイオンの存在は一般に
少なく、従って第2R処理は弱酸性で行うことができる
ので処理能力が維持され、第1R匹理工程の処理能力も
低下が小さく極めて長時間当初の処理能力を保持できる
ので経済的に有利でちる。The presence of ions that compete with the target product in the crystallization mother liquor is generally small, so the 2nd R treatment can be carried out in a weakly acidic environment, so the treatment capacity is maintained, and the treatment capacity of the 1st R physical process is also minimally degraded. It is economically advantageous because the original processing capacity can be maintained for a long time.
本発明の方法は発酵液を酸性にしてイオン交換針脂処理
する工程を含む発酵液の精製に適用でき、アミノ酸、特
にリジン、アルギニン、オルニチン専の塩基性アミノ酸
、核酸、抗生物質等の発酵液ご適用できる。The method of the present invention can be applied to the purification of fermentation liquid, which includes the step of acidifying the fermentation liquid and subjecting it to ion-exchange needle fat treatment. Applicable.
アミノ酸発酵液を処理する場合を例として、処里方法の
詳細を以下に説明す。The details of the processing method will be described below, taking the case of processing an amino acid fermentation liquid as an example.
用いられるイオン交換樹脂としては、強酸性ゲル型イオ
ン交換樹脂、例えば5KIB(商品名、三菱化成製品)
、アンバーライトIR−120B(商品名、Rohm
& Haas社製品)、強酸性ポーラス型樹脂、例えば
PK−216(商品名、三菱化成製品)等が例示される
。The ion exchange resin used is a strongly acidic gel type ion exchange resin, such as 5KIB (trade name, manufactured by Mitsubishi Kasei).
, Amberlight IR-120B (product name, Rohm
& Haas Inc.), strongly acidic porous resins such as PK-216 (trade name, Mitsubishi Kasei products), and the like.
発酵液は鉱酸例えば塩酸、硫酸等で酸性好ましくはp
H1,5〜2.0に調整した後第1R処理工程で処理さ
れる。酸性にするとき発酵液の温度が上がるので冷却し
て10〜32℃にする。レジン処理能力維持のために低
い方が好ましいが、エネルギーを多量に消費することに
なるので経済的バランスを考慮して温度を決めればよい
。樹脂処理は一般には樹脂を充した塔に発酵液を通し次
いで水洗する。溶出はアンモニア水等で行われ、目的物
を含有する溶出液を加熱することによってアンモニアを
除去し、濃縮して目的物を晶析させ、分離する。The fermentation liquid is acidified with a mineral acid such as hydrochloric acid or sulfuric acid, preferably p
After adjusting to H1.5 to 2.0, it is processed in the first R treatment step. The temperature of the fermented liquid rises when acidifying it, so cool it to 10-32°C. A lower temperature is preferable in order to maintain resin processing ability, but since a large amount of energy is consumed, the temperature should be determined by considering economic balance. Resin treatment generally involves passing the fermented liquor through a column filled with resin, followed by washing with water. Elution is performed with aqueous ammonia or the like, and the eluate containing the target product is heated to remove ammonia, concentrated, and the target product is crystallized and separated.
該母液を濃縮工程あるいは第1R処理工程前に供給して
発酵液と共に処理することにより、晶析母液中に含まれ
ている目的物を回収することかで11 きる。この母液
中にも樹脂の処理能力を低下させる物質が含まれており
、酸性側においてその物質の樹脂への吸着が強いので好
ましくは別に第2イオン交換樹脂塔を設けて処理する。The target substance contained in the crystallization mother liquor can be recovered by supplying the mother liquor before the concentration step or the first R treatment step and treating it together with the fermentation liquor. This mother liquor also contains substances that reduce the processing ability of the resin, and since these substances are strongly adsorbed to the resin on the acidic side, it is preferable to separately provide a second ion exchange resin column for treatment.
第2R処理工程を設けて晶析母液中の目的物を回収する
に際しては、晶析母液のpHを弱酸性、好ましくは6〜
7にアンモニア等で調整後、第2R処理工程で処理する
。用いられる樹脂は第1R処理工程で用いられる樹脂が
例示され、アンモニア水等を溶出剤として溶出すればよ
い。When the second R treatment step is provided to recover the target substance in the crystallization mother liquor, the pH of the crystallization mother liquor is set to a weakly acidic state, preferably 6 to 6.
After adjusting with ammonia or the like in step 7, it is treated in the second R treatment step. The resin used is exemplified by the resin used in the first R treatment step, and may be eluted using aqueous ammonia or the like as an eluent.
発酵液の種類によって、用いる樹脂、処理条件、その他
を変更することにより最良の方法を見つけることは当業
者にとって極めて容易になしうろことである。It would be extremely easy for those skilled in the art to find the best method by changing the resin used, processing conditions, etc., depending on the type of fermentation liquid.
以下に本発明の態様を実施例によって説明する。Aspects of the present invention will be explained below using examples.
実施例
リジン発酵液1001cffを硫酸でpH2に調整(液
温的55℃)した後、液温を25℃に冷却する。ioo
kgの5KIBを詰めた塔に100屁/Hの速さで供給
する。200Wの水で水洗した後2 N−NH,OH水
溶液1001cfflを約70屁/Hで供給してリジン
を溶出する(第1R処理理工程)。Example After adjusting the pH of 1001 cff of lysine fermentation liquid to 2 with sulfuric acid (liquid temperature: 55°C), the liquid temperature was cooled to 25°C. ioo
A tower packed with 5 KIB is fed at a rate of 100 farts/H. After washing with 200W water, 1001 cffl of 2N-NH,OH aqueous solution was supplied at about 70 farts/H to elute lysine (1st R treatment step).
80Vの溶出液を減圧濃縮してアンモニアを除去し、塩
酸でp H5,5としてリシンを塩酸塩とした後減圧濃
縮し、約6,000kgのリジン塩酸塩を晶 1析させ
る。10kflの母液の中7屁を前記濃縮工程へ循環し
、3kiの母液のpHをアンモニアで6.5に調整し、
上記樹脂塔と別に設けた15klの5KIBを詰めた塔
に送り、上記水洗、溶出、濃縮する。以下この工程を繰
り返す(本発明方法)。The 80V eluate is concentrated under reduced pressure to remove ammonia, and the pH is adjusted to 5.5 with hydrochloric acid to convert lysine into hydrochloride, which is then concentrated under reduced pressure to precipitate about 6,000 kg of lysine hydrochloride. 7 farts in 10kfl of mother liquor were recycled to the concentration step, and the pH of 3ki of mother liquor was adjusted to 6.5 with ammonia,
The resin is sent to a tower packed with 15 kl of 5KIB, which is provided separately from the resin tower, and subjected to the water washing, elution, and concentration. This process is repeated thereafter (method of the present invention).
比較のために発酵液の冷却を行うことなく、又晶析母液
を全量発酵液へ戻す以外は上記と同様に行う(対照法)
。For comparison, the same procedure as above was carried out except that the fermentation liquid was not cooled and the entire crystallization mother liquor was returned to the fermentation liquid (control method).
.
結果を第1表に示す。The results are shown in Table 1.
第 1 表
N:第1R処理工程の樹脂の使用回数
SSC:塩の分解容量(Salt Splitting
Capacity)(eq/jl!−R)
A;リジン吸着能(g/β−R)
効 果
本発明によれば、当初の吸着能力は500回の処理後も
かなり高く維持されている。1st Table N: Number of times the resin is used in the 1R treatment process SSC: Salt splitting capacity
Lysine Adsorption Capacity (eq/jl!-R) A; Lysine Adsorption Capacity (g/β-R) Effect According to the present invention, the initial adsorption capacity is maintained quite high even after 500 treatments.
Claims (4)
酵液のpHを酸性にし、且つ温度を10〜32℃にした
後、イオン交換樹脂処理(第1R処理という)すること
を特徴とする発酵液の処理法。(1) When treating the fermented liquor with an ion exchange resin, the pH of the fermented liquor is made acidic and the temperature is set to 10 to 32°C, and then the ion exchange resin treatment (referred to as 1R treatment) is carried out. Processing method for fermentation liquid.
る晶出母液をイオン交換樹脂処理前の発酵液に加える特
許請求の範囲第1項記載の方法。(2) The method according to claim 1, in which the crystallization mother liquor in the step of crystallizing the target product after the ion exchange resin treatment is added to the fermentation liquid before the ion exchange resin treatment.
設けた第2イオン交換樹脂塔で処理する特許請求の範囲
第1項記載の方法。(3) The method according to claim 1, wherein the crystallization mother liquor in the crystallization step after the first R treatment is treated in a second ion exchange resin column provided separately.
第1,2又は3項記載の方法。(4) The method according to claim 1, 2 or 3, wherein the fermentation liquid is an amino acid fermentation liquid.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP11243084A JPS60256392A (en) | 1984-06-01 | 1984-06-01 | Treatment of fermentation mixture |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP11243084A JPS60256392A (en) | 1984-06-01 | 1984-06-01 | Treatment of fermentation mixture |
Publications (1)
Publication Number | Publication Date |
---|---|
JPS60256392A true JPS60256392A (en) | 1985-12-18 |
Family
ID=14586440
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP11243084A Pending JPS60256392A (en) | 1984-06-01 | 1984-06-01 | Treatment of fermentation mixture |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS60256392A (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR100578426B1 (en) * | 1999-02-10 | 2006-05-11 | 씨제이 주식회사 | A process for producing L-lysine by a continuous crystallization |
WO2014020866A1 (en) * | 2012-08-03 | 2014-02-06 | 味の素株式会社 | Method for producing basic amino acid or basic amino acid salt |
-
1984
- 1984-06-01 JP JP11243084A patent/JPS60256392A/en active Pending
Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
KR100578426B1 (en) * | 1999-02-10 | 2006-05-11 | 씨제이 주식회사 | A process for producing L-lysine by a continuous crystallization |
WO2014020866A1 (en) * | 2012-08-03 | 2014-02-06 | 味の素株式会社 | Method for producing basic amino acid or basic amino acid salt |
US9216946B2 (en) | 2012-08-03 | 2015-12-22 | Ajinomoto Co., Inc. | Method of producing basic amino acid or basic amino acid salt |
JP5835489B2 (en) * | 2012-08-03 | 2015-12-24 | 味の素株式会社 | Method for producing basic amino acid or basic amino acid salt |
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