JPH0789942B2 - Lactic acid purification method - Google Patents
Lactic acid purification methodInfo
- Publication number
- JPH0789942B2 JPH0789942B2 JP62248592A JP24859287A JPH0789942B2 JP H0789942 B2 JPH0789942 B2 JP H0789942B2 JP 62248592 A JP62248592 A JP 62248592A JP 24859287 A JP24859287 A JP 24859287A JP H0789942 B2 JPH0789942 B2 JP H0789942B2
- Authority
- JP
- Japan
- Prior art keywords
- lactic acid
- lactate
- exchange resin
- cation exchange
- vacuum distillation
- 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.)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
【発明の詳細な説明】 （イ）産業上の利用分野 この発明は乳酸の精製法に関する。さらに詳しくは乳酸
発酵液から高純度乳酸を連続的に精製する乳酸の精製法
に関する。TECHNICAL FIELD The present invention relates to a method for purifying lactic acid. More specifically, it relates to a method for purifying lactic acid in which high-purity lactic acid is continuously purified from a lactic acid fermentation broth.
（ロ）従来の技術 乳酸発酵は通常過剰の炭酸石灰の存在下で行われるた
め、ロウ中に乳酸石灰として生産される。この得られる
乳酸石灰を精製する方法としては通常ｉ）乳酸カルシウ
ム法、ii）エステル化法、iii）亜鉛塩化法、iv）減圧
蒸留法等が知られている。(B) Conventional technology Since lactic acid fermentation is usually performed in the presence of excess lime carbonate, it is produced as lactic acid lime in wax. As a method for purifying the obtained lime lactate, generally, i) calcium lactate method, ii) esterification method, iii) zinc chloride method, iv) vacuum distillation method and the like are known.
（ハ）発明が解決しようとする問題点 しかしながら上記方法において、乳酸カルシウム法
（ｉ）は石灰分除去、その他硫酸銀、鉄分、重金属イオ
ン等の除去等精製工程が煩雑であり、さらに発酵の中和
剤として用いる水酸化カルシウムは溶解度が低いため工
程中に沈殿が生じやすく連続的に行い難いこと、エステ
ル化法（ii）はエステル化に用いるイソプロピルエーテ
ルが有害であり、これの混入の虞れがあること、亜鉛塩
化法（iii）は亜鉛の損失がかなりあること、減圧減留
法（iv）は酸型でしか行えないこと等、いずれの方法も
工程的、経済的にロスが多く工業的精製法として満足で
きる方法ではなかった。(C) Problems to be Solved by the Invention In the above method, however, the calcium lactate method (i) has complicated purification steps such as removal of lime and removal of silver sulfate, iron, heavy metal ions, etc. Calcium hydroxide used as a solvating agent has a low solubility and is liable to precipitate during the process, making it difficult to carry out continuously. In the esterification method (ii), isopropyl ether used for esterification is harmful and may be mixed. The zinc chloride method (iii) has a considerable loss of zinc, and the depressurization distillation method (iv) can be performed only in the acid form. The method was not a satisfactory one.
この発明はかかる状況に鑑みなされたものであり、乳酸
発酵で得られる乳酸塩混合物から乳酸を低コストで高純
度にかつ連続して精製しうる方法を提供しようとするも
のである。The present invention has been made in view of such circumstances, and an object thereof is to provide a method capable of continuously purifying lactic acid from a lactate mixture obtained by lactic acid fermentation at a low cost with high purity.
（ニ）問題点を解決するための手段 かくしてこの発明によれば、 （ａ）アルカリ金属塩の形態の乳酸を含有する乳酸菌含
有培養液を濾過する工程、 （ｂ）上記工程（ａ）で得られる乳酸塩含有液をカチオ
ン交換樹脂カラムに導入してそこで乳酸塩を遊離乳酸に
変換する工程、 （ｃ）上記工程（ｂ）で得られる乳酸含有液を乳酸濃度
80％以上になるまで減圧濃縮する工程、 （ｄ）上記工程（ｃ）で得られる乳酸濃縮液を減圧蒸留
に付して乳酸留分を回収する工程 とからなる乳酸の精製法が提供される。(D) Means for Solving the Problems Thus, according to the present invention, (a) a step of filtering a lactic acid bacterium-containing culture solution containing lactic acid in the form of an alkali metal salt, (b) obtained in the step (a) above The lactate-containing solution obtained is introduced into a cation exchange resin column to convert the lactate into free lactic acid, (c) the lactic acid-containing solution obtained in the above step (b)
A method for purifying lactic acid is provided, which comprises a step of concentrating under reduced pressure to 80% or more, and a step of subjecting the concentrated lactic acid solution obtained in the step (c) to vacuum distillation to recover a lactic acid fraction. .
この発明の方法は、バイオリアクタ等により工業的に多
量に生産される乳酸菌・乳酸塩含有液からろ過された乳
酸塩含有液を、そのままカチオン交換樹脂カラムを通じ
ることにより連続して遊離乳酸にし、さらにこの遊離乳
酸を連続して濃縮・蒸留することにより高純度に精製で
きうる方法であることを特徴とする。The method of the present invention is a lactate-containing solution filtered from a lactic acid bacterium / lactate-containing solution that is industrially produced in large quantities by a bioreactor or the like, and is continuously converted into free lactic acid by directly passing through a cation exchange resin column, Furthermore, this free lactic acid is characterized by being a method that can be purified to high purity by continuously concentrating and distilling it.
この発明の方法において、乳酸塩・乳酸菌含有培養液か
ら乳酸菌を除去する方法としては、当該分野で公知のフ
ィルタろ過による方法を用いることができる。In the method of the present invention, as a method for removing lactic acid bacteria from the lactate / lactic acid bacteria-containing culture solution, a method by filter filtration known in the art can be used.
この発明の方法において、カチオン交換樹脂カラムに導
入される乳酸塩の形態としては、アルカリ金属塩または
アルカリ土類金属塩の形態で用いられるが、この場合こ
とにナトリウム塩の形態がカチオン交換樹脂カラムの再
生が容易に行える点で好ましい。In the method of the present invention, the lactate salt introduced into the cation exchange resin column is used in the form of an alkali metal salt or an alkaline earth metal salt. In this case, the sodium salt form is used in particular. Is preferable because it can be easily regenerated.
この発明の方法において、カチオン交換樹脂カラムに用
いられる樹脂としては、通常のカチオン交換樹脂が用い
られるが、例えばDIAIONSK 1B Ｈ型カチオン交換樹脂
（三菱化成工業製）等が挙げられる。In the method of the present invention, as the resin used for the cation exchange resin column, an ordinary cation exchange resin is used, and examples thereof include DIAIONSK 1B H type cation exchange resin (manufactured by Mitsubishi Kasei Co., Ltd.).
この発明の方法の実施において、上記カチオン交換樹脂
カラムを複数本用意し、これらを乳酸塩含有液供給流路
に切換接続可能に並設し、さらにこれらのカラムにカラ
ム再生・洗浄用液を供給する流路を切換接続可能に設け
て用いることが好ましい。詳しくは後述する実施例の記
載が参照される。In carrying out the method of the present invention, a plurality of the above cation exchange resin columns are prepared, and these are arranged side by side in a lactate-containing liquid supply flow path so as to be switchably connectable, and a column regeneration / washing liquid is further supplied to these columns. It is preferable that the flow passages are provided so that they can be switched and connected. For details, reference is made to the description of Examples below.
この発明において、上記カチオン交換樹脂カラムから得
られる乳酸含有液は、通常乳酸濃度が５〜７％で多量の
水分が含有されているため蒸留精製に先立って予め減圧
濃縮される。この場合乳酸濃度80％以上の濃度が好まし
く、以降の蒸留精製工程においてかかる時間の効率良い
短縮を考慮すれば、90％まで濃縮することがより好まし
い。In the present invention, the lactic acid-containing liquid obtained from the cation exchange resin column is usually concentrated under reduced pressure prior to distillation and purification because the lactic acid concentration is usually 5 to 7% and a large amount of water is contained. In this case, the concentration of lactic acid is preferably 80% or more, and it is more preferable that the concentration is 90% in consideration of efficient reduction of the time required in the subsequent distillation purification step.
この発明の方法において、上記濃縮工程で得られる乳酸
濃縮液は、減圧蒸留に付されて精製される。この減圧蒸
留の条件は通常の乳酸の精製法として用いられる減圧蒸
留の条件と同様に設定される。In the method of the present invention, the concentrated lactic acid solution obtained in the above-mentioned concentration step is subjected to vacuum distillation for purification. The conditions of this vacuum distillation are set in the same manner as the conditions of the vacuum distillation used as a usual lactic acid purification method.
以上のごとくこの発明の方法に従えば、食用から局方級
のいずれの等級の精製乳酸でも得ることができる。As described above, according to the method of the present invention, any grade of purified lactic acid from edible to pharmacopoeia can be obtained.
（ホ）作用 この発明によれば、アルカリ金属塩またはアルカリ土類
金属塩の形態の乳酸塩含有液は、直接カチオン交換樹脂
カラムを通過して遊離乳酸に変換され、この得られる遊
離乳酸含有液は順次濃縮され多量の水分が除去された
後、得られる乳酸濃縮液はさらに減圧蒸留に付されて精
製される。(E) Action According to the present invention, a lactate-containing liquid in the form of an alkali metal salt or an alkaline earth metal salt is directly passed through a cation exchange resin column to be converted into free lactic acid, and the resulting free lactic acid-containing liquid is obtained. After being sequentially concentrated to remove a large amount of water, the obtained lactic acid concentrated liquid is further subjected to vacuum distillation for purification.
以下実施例によりこの発明を詳細に説明するが、これに
よりこの発明は限定されるものではない。Hereinafter, the present invention will be described in detail with reference to Examples, but the present invention is not limited thereto.
（ヘ）実施例 第１図はこの発明の乳酸精製法を実施する装置の一例の
構成説明図である。図において該装置（１）は、図示し
ないバイオリアクタ部で生成される乳酸塩含有液をイオ
ン交換部（２）に移送する乳酸塩含有液供給流路（ａ）
と、上記イオン交換部（２）から流出される乳酸含有液
を減圧濃縮部（３）に移送する乳酸含有液供給流路
（ｂ）と、上記減圧濃縮部（３）で得られる乳酸濃縮液
を減圧蒸留部（４）に移送する乳酸濃縮液供給流路
（ｃ）とから主として構成されている。(F) Example FIG. 1 is a structural explanatory view of an example of an apparatus for carrying out the lactic acid purification method of the present invention. In the figure, the device (1) includes a lactate-containing solution supply channel (a) for transferring a lactate-containing solution produced in a bioreactor section (not shown) to an ion exchange section (2).
And a lactic acid-containing liquid supply channel (b) for transferring the lactic acid-containing liquid flowing out from the ion exchange unit (2) to the vacuum concentration unit (3), and the lactic acid concentrated liquid obtained in the vacuum concentration unit (3) Is mainly composed of a lactic acid concentrated liquid supply flow channel (c) for transferring the liquid to the vacuum distillation section (4).
上記図示しないバイオリアクタ部は、下記条件で運転さ
れている。The bioreactor unit (not shown) is operated under the following conditions.
培 地：グルコース10％， イーストエキス0.5％， ポリペプトン0.5％ 反応器条件：温度37〜39℃ 滞留時間４〜5h （48％NaOHで調整） 上記イオン交換部（２）には、２本のカチオン交換樹脂
カラム（21）（22）が並列に用いられ、これらの各上部
に接続される管路（d1）（d2）と前記乳酸塩含有液供給
路（ａ）とは三方電磁弁（V1）を介して分岐接続されて
いる。また一方上記２本のカチオン交換樹脂カラム（2
1）（22）のそれぞれの下部に接続される管路（e1）（e
2）と前記乳酸含有液供給流路（ｂ）とは三方電磁弁（V
2）を介して分岐接続されている。また、上記管路
（d1）（d2）それぞれには三方電磁弁（v3）（v4）をこ
の順を介して硫酸貯留槽（５）および洗浄水槽（６）に
接続される再生・洗浄用流路（f1）（f2）がそれぞれ管
路接続されている。また一方上記管路（e1）（e2）には
それぞれ三方電磁弁（v5）（v6）を介して廃液流路
（g1）（g2）が管路接続されている。また上記カチオン
交換樹脂カラムにはいずれもDIAION SK 1B H型カチオン
交換樹脂（三菱化成工業製）が用いられている。Culture place: Glucose 10%, Yeast extract 0.5%, Polypeptone 0.5% Reactor conditions: Temperature 37-39 ℃ Residence time 4-5h (adjusted with 48% NaOH) The above ion exchange part (2) has two cations. Exchange resin columns (21) and (22) are used in parallel, and the pipelines (d 1 ) (d 2 ) connected to the respective upper parts of these columns and the lactate-containing liquid supply channel (a) are three-way solenoid valves ( Branched via V 1 ). On the other hand, the above two cation exchange resin columns (2
1) Pipes connected to the lower part of (22) (e 1 ) (e
2 ) and the lactic acid-containing liquid supply flow path (b) are three-way solenoid valves (V
2 ) is branched and connected via. In addition, a regeneration system in which a three-way solenoid valve (v 3 ) (v 4 ) is connected to the sulfuric acid storage tank (5) and the washing water tank (6) in this order in each of the pipelines (d 1 ) (d 2 ) -The washing channels (f 1 ) and (f 2 ) are connected to each other. On the other hand, waste fluid channels (g 1 ) (g 2 ) are connected to the pipelines (e 1 ) (e 2 ) via three-way solenoid valves (v 5 ) (v 6 ) respectively. Further, DIAION SK 1B H type cation exchange resin (manufactured by Mitsubishi Kasei Co., Ltd.) is used in each of the above cation exchange resin columns.
減圧濃縮部（３）には図示しない濃縮器および得られる
乳酸濃縮液を貯留する図示しない乳酸濃縮液貯留槽とを
この順に備え、上記イオン交換部（２）から得られる乳
酸含有液を通常90％まで濃縮するよう設定されている。The vacuum concentration unit (3) is provided with a concentrator (not shown) and a lactic acid concentrate storage tank (not shown) that stores the obtained lactic acid concentrate, in that order, and the lactic acid-containing liquid obtained from the ion exchange unit (2) is usually used. It is set to concentrate to%.
減圧蒸留部（５）は図示しない２つの減圧蒸留器を備え
これらを順次経過して減圧蒸留されるよう構成されてい
る。The vacuum distillation section (5) is equipped with two vacuum distillation units (not shown) and is configured to sequentially undergo vacuum distillation.
また上記各流路（ａ）（ｂ）（ｃ）には図示しない送液
ポンプが設定されており、これらの駆動により、バイオ
リアクタ部から得られる乳酸塩含有液は順次イオン交換
部（２）→減圧濃縮部（３）→減圧蒸留部（４）を経て
精製されることとなる。Further, a liquid feed pump (not shown) is set in each of the flow paths (a), (b), and (c), and the lactate-containing liquid obtained from the bioreactor unit is sequentially driven by the drive of these pumps. -> It will be refine | purified through a vacuum concentration part (3)-> vacuum distillation part (4).
次に上記装置（１）の作動を説明する。Next, the operation of the device (1) will be described.
バイオリアクタ部での上記した運転条件下で得られる乳
酸塩（乳酸ナトリウム）含有液は、乳酸塩含有液供給流
路（ａ）→三方電磁弁（V1）→管路（d1）を通ってカチ
オン交換樹脂カラム（21）に導入される。該カラムを通
過する間に乳酸ナトリウムは中和され遊離乳酸とされ
る。このとき上記カラム出口からは５〜７％濃度の乳酸
含有液として流出され続いて管路（e1）→三方電磁弁
（V2）→乳酸含有液供給流路（ｂ）を経て、減圧濃縮部
（３）に移送される。ここで上記乳酸含有液は濃縮器に
より約90％濃度にまで濃縮される。このようにして得ら
れた高濃度乳酸濃縮液は乳酸濃縮液供給流路（ｃ）を移
送されて、減圧蒸留部（４）に導入される。ここでは乳
酸の重合を避けるため、例えば5mmHg程度の真空下で130
℃以下で留出させると高純度の乳酸を得ることができ
る。The lactate (sodium lactate) -containing liquid obtained under the above operating conditions in the bioreactor section passes through the lactate-containing liquid supply flow path (a) → three-way solenoid valve (V 1 ) → pipe line (d 1 ). And is introduced into the cation exchange resin column (21). Sodium lactate is neutralized into free lactic acid while passing through the column. At this time, the lactic acid-containing liquid having a concentration of 5 to 7% was discharged from the outlet of the column, and then was concentrated under reduced pressure via the conduit (e 1 ) → three-way solenoid valve (V 2 ) → the lactic acid-containing liquid supply flow path (b). Transferred to department (3). Here, the lactic acid-containing liquid is concentrated by a concentrator to a concentration of about 90%. The high-concentration lactic acid concentrate thus obtained is transferred through the lactic acid concentrate supply channel (c) and introduced into the vacuum distillation section (4). Here, in order to avoid the polymerization of lactic acid, for example, in a vacuum of about 5 mmHg, 130
High-purity lactic acid can be obtained by distilling at a temperature of not higher than ° C.
なお、このとき並行して一方のカチオン交換樹脂カラム
（22）の再生・洗浄を行なうことも可能である。すなわ
ち上記作動の間三方電磁弁（v4）（v3）を切換えて硫酸
貯留槽から硫酸を再生・洗浄用流路（f2）→管路（d2）
を経てカチオン交換樹脂カラム（22）に導入し、一方該
カラムから流出する硫酸ナトリウムを、管路（e2）→三
方電磁弁（v6）→廃液流路（g2）を経てドレインへ排出
することにより上記カラム（22）が再生・洗浄される。
この再生・洗浄の作動と上記乳酸精製の作動とは同時に
行うことができ、こうすることにより常にいずれかのカ
チオン交換樹脂カラムを精製に用いることができ、バイ
オリアクタ部で産生される乳酸塩含有液を連続して精製
することができる。またカラムの交換も容易にできる。At this time, it is possible to regenerate and wash one of the cation exchange resin columns (22) in parallel. That is, during the above operation, the three-way solenoid valve (v 4 ) (v 3 ) is switched to regenerate and wash sulfuric acid from the sulfuric acid storage tank (f 2 ) → pipeline (d 2 )
Introduced into the cation exchange resin column (22) through the column, while the sodium sulfate flowing out of the column is discharged to the drain via the conduit (e 2 ) → three-way solenoid valve (v 6 ) → waste liquid flow path (g 2 ). By doing so, the column (22) is regenerated and washed.
The operation of this regeneration / washing and the operation of the above-mentioned lactic acid purification can be performed at the same time, so that any of the cation exchange resin columns can always be used for purification, and the lactate-containing product produced in the bioreactor part can be contained. The liquid can be continuously purified. Also, the column can be easily replaced.
上記装置における減圧濃縮部（３）で得られた乳酸濃縮
液および減圧蒸留部（４）で得られた留出液それぞれに
ついて、液体クロマトグラフにより分析したところ、第
２図および第３図に示す結果を得た。なお、このとき使
用したカラムはshimpack 101 SCR 101H,検出器は示差屈
折率計RID2ASである。第２図と第３図とを比較すると、
第２図では原料のグルコース（イ）と生成物の乳酸
（ロ）との両方のクロマトグラムがあらわれており、こ
の段階ではまだ少量の原料の混在が認められるが、第３
図では生成物の乳酸（ロ）のクロマトグラムのみがあら
われているけであり、減圧蒸留部において得られる乳酸
は高純度（局方級程度）に生成されていることがわか
る。The lactic acid concentrate obtained in the vacuum concentration section (3) and the distillate obtained in the vacuum distillation section (4) of the above apparatus were analyzed by liquid chromatography, and the results are shown in FIGS. 2 and 3. I got the result. The column used at this time was shimpack 101 SCR 101H, and the detector was a differential refractometer RID2AS. Comparing FIG. 2 and FIG. 3,
In Fig. 2, a chromatogram of both glucose (a) as a raw material and lactic acid (b) as a product appears, and at this stage, a small amount of raw material is still present.
Only the chromatogram of the product lactic acid (b) appears in the figure, and it can be seen that the lactic acid obtained in the vacuum distillation section is produced in high purity (about the pharmacopoeia grade).
（ト）発明の効果 この発明によれば、バイオリアクタ等で得られる乳酸塩
含有液を直接かつ連続して精製できるので、多量に処理
できる。また低コストで高純度に乳酸を精製することが
できる。(G) Effect of the Invention According to the present invention, since the lactate-containing liquid obtained in a bioreactor or the like can be directly and continuously purified, a large amount can be treated. Further, lactic acid can be purified with high purity at low cost.
第１図はこの発明の方法を実施する装置の一例の構成説
明図、第２図は第１図の装置の減圧濃縮部で得られる乳
酸濃縮液の液体クロマトグラム図、第３図は第１図の装
置の減圧蒸留部で得られる留出液の液体クロマトグラム
図である。 （２）……イオン交換部、（３）……減圧濃縮部、 （４）……減圧蒸留部、（５）……硫酸貯留槽、 （６）……洗浄水槽、 （21）（22）……カチオン交換樹脂カラム、 （ａ）……乳酸塩含有液供給流路、 （ｂ）……乳酸含有液切換流路、 （ｃ）……乳酸濃縮液供給流路、 （d1）（d2）（e1）（e2）……管路、 （f1）（f2）……再生・洗浄用流路、 （g1）（g2）……廃液流路。FIG. 1 is an explanatory view of the constitution of an example of an apparatus for carrying out the method of the present invention, FIG. 2 is a liquid chromatogram of a lactic acid concentrate obtained in a vacuum concentration section of the apparatus of FIG. 1, and FIG. It is a liquid chromatogram figure of the distillate obtained by the vacuum distillation part of the apparatus of a figure. (2) …… Ion exchange section, (3) …… Vacuum concentration section, (4) …… Vacuum distillation section, (5) …… Sulfuric acid storage tank, (6) …… Wash water tank, (21) (22) ... cation exchange resin column, (a) ... lactate-containing liquid supply flow path, (b) ... lactic acid-containing liquid switching flow path, (c) ... lactic acid concentrated liquid supply flow path, (d 1 ) (d 2 ) (e 1 ) (e 2 ) ... Pipeline, (f 1 ) (f 2 ) ... Regeneration / cleaning flow channel, (g 1 ) (g 2 ) ... Waste liquid flow channel.
Claims (1)
する乳酸菌含有培養液を濾過する工程、 （ｂ）上記工程（ａ）で得られる乳酸塩含有液をカチオ
ン交換樹脂カラムに導入してそこで乳酸塩を遊離乳酸に
変換する工程、 （ｃ）上記工程（ｂ）で得られる乳酸含有液を乳酸濃度
80％以上になるまで減圧濃縮する工程、 （ｄ）上記工程（ｃ）で得られる乳酸濃縮液を減圧蒸留
に付して乳酸留分を回収する工程 とからなる乳酸の精製法。1. A step of: (a) filtering a lactic acid bacterium-containing culture solution containing lactic acid in the form of an alkali metal salt; (b) introducing the lactate-containing solution obtained in the step (a) into a cation exchange resin column. And then converting lactate into free lactic acid, (c) the lactic acid-containing liquid obtained in the above step (b)
A method for purifying lactic acid, which comprises a step of concentrating under reduced pressure to 80% or more, and a step of subjecting the concentrated lactic acid solution obtained in the step (c) to vacuum distillation to recover a lactic acid fraction.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62248592A JPH0789942B2 (en) | 1987-09-30 | 1987-09-30 | Lactic acid purification method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62248592A JPH0789942B2 (en) | 1987-09-30 | 1987-09-30 | Lactic acid purification method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0191788A JPH0191788A (en) | 1989-04-11 |
| JPH0789942B2 true JPH0789942B2 (en) | 1995-10-04 |
Family
ID=17180410
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62248592A Expired - Lifetime JPH0789942B2 (en) | 1987-09-30 | 1987-09-30 | Lactic acid purification method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0789942B2 (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| IT1247995B (en) * | 1991-06-06 | 1995-01-05 | Himont Inc | PROCESS FOR THE PRODUCTION OF AQUATIC LACTIC ACID SOLUTIONS PURIFIED FROM FERMENTATION BRODS. |
| AT398982B (en) * | 1993-02-18 | 1995-02-27 | Vogelbusch Gmbh | METHOD FOR SEPARATING AND PURIFYING LACTIC ACID |
| IL119389A (en) | 1996-10-09 | 2001-10-31 | Cargill Inc | Process for the recovery of lactic acid by liquid-liquid extraction using a cation exchanger |
| BE1011197A3 (en) † | 1997-06-06 | 1999-06-01 | Brussels Biotech En Abrege Bb | Process for purification lactic acid. |
| NL1013682C2 (en) * | 1999-11-26 | 2001-05-30 | Purac Biochem Bv | Method and device for purifying an aqueous solution of lactic acid. |
| US8772440B2 (en) * | 2010-02-08 | 2014-07-08 | Purac Biochem B.V. | Process for manufacturing lactic acid |
| JP2013537541A (en) * | 2010-08-19 | 2013-10-03 | コンパニア レフィナドラ ダ アマゾニア | Method to obtain high purity lactic acid from fermentation broth |
| CN111164215A (en) * | 2017-10-02 | 2020-05-15 | 代谢探索者公司 | Method for producing organic acid salts from fermentation broth |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60217897A (en) * | 1984-04-13 | 1985-10-31 | Taki Chem Co Ltd | Method for separating and purifying lactic acid |
-
1987
- 1987-09-30 JP JP62248592A patent/JPH0789942B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0191788A (en) | 1989-04-11 |
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