JPS63188632A - Purification of organic acid and apparatus therefor - Google Patents
Purification of organic acid and apparatus thereforInfo
- Publication number
- JPS63188632A JPS63188632A JP2117287A JP2117287A JPS63188632A JP S63188632 A JPS63188632 A JP S63188632A JP 2117287 A JP2117287 A JP 2117287A JP 2117287 A JP2117287 A JP 2117287A JP S63188632 A JPS63188632 A JP S63188632A
- Authority
- JP
- Japan
- Prior art keywords
- exchange resin
- organic acid
- acid
- anion exchange
- tank
- 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
- 150000007524 organic acids Chemical class 0.000 title claims abstract description 42
- 238000000746 purification Methods 0.000 title claims description 4
- 239000003957 anion exchange resin Substances 0.000 claims abstract description 31
- 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 claims abstract description 28
- 239000003729 cation exchange resin Substances 0.000 claims abstract description 24
- 238000000034 method Methods 0.000 claims abstract description 23
- 238000005342 ion exchange Methods 0.000 claims abstract description 12
- 239000002253 acid Substances 0.000 claims abstract description 11
- 238000006243 chemical reaction Methods 0.000 claims abstract description 8
- 150000003839 salts Chemical class 0.000 claims abstract description 7
- 238000011084 recovery Methods 0.000 claims abstract description 6
- 235000005985 organic acids Nutrition 0.000 claims description 12
- 238000004519 manufacturing process Methods 0.000 claims 2
- 239000003513 alkali Substances 0.000 claims 1
- 238000005349 anion exchange Methods 0.000 claims 1
- JVTAAEKCZFNVCJ-UHFFFAOYSA-N lactic acid Chemical compound CC(O)C(O)=O JVTAAEKCZFNVCJ-UHFFFAOYSA-N 0.000 abstract description 64
- 239000004310 lactic acid Substances 0.000 abstract description 32
- 235000014655 lactic acid Nutrition 0.000 abstract description 32
- 238000000855 fermentation Methods 0.000 abstract description 21
- 230000004151 fermentation Effects 0.000 abstract description 21
- 238000010828 elution Methods 0.000 abstract description 10
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 abstract description 9
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 abstract description 9
- 238000001179 sorption measurement Methods 0.000 abstract description 9
- 239000000126 substance Substances 0.000 abstract description 9
- 239000006227 byproduct Substances 0.000 abstract description 5
- 239000011541 reaction mixture Substances 0.000 abstract description 5
- 239000002904 solvent Substances 0.000 abstract description 4
- 239000003814 drug Substances 0.000 abstract description 3
- 150000002170 ethers Chemical class 0.000 abstract description 3
- 235000013305 food Nutrition 0.000 abstract description 3
- 239000012295 chemical reaction liquid Substances 0.000 abstract 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 14
- 239000007788 liquid Substances 0.000 description 13
- 230000008929 regeneration Effects 0.000 description 8
- 238000011069 regeneration method Methods 0.000 description 8
- 230000007423 decrease Effects 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 6
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 6
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 5
- 239000008103 glucose Substances 0.000 description 5
- 239000011347 resin Substances 0.000 description 5
- 229920005989 resin Polymers 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- 238000000605 extraction Methods 0.000 description 4
- 239000003456 ion exchange resin Substances 0.000 description 4
- 229920003303 ion-exchange polymer Polymers 0.000 description 4
- -1 isopropyl ether Chemical class 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000012670 alkaline solution Substances 0.000 description 2
- 238000005341 cation exchange Methods 0.000 description 2
- 230000032050 esterification Effects 0.000 description 2
- 238000005886 esterification reaction Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 235000011121 sodium hydroxide Nutrition 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- KVZLHPXEUGJPAH-DKWTVANSSA-N 2-hydroxypropanoic acid;(2s)-2-hydroxypropanoic acid Chemical compound CC(O)C(O)=O.C[C@H](O)C(O)=O KVZLHPXEUGJPAH-DKWTVANSSA-N 0.000 description 1
- ZAFNJMIOTHYJRJ-UHFFFAOYSA-N Diisopropyl ether Chemical compound CC(C)OC(C)C ZAFNJMIOTHYJRJ-UHFFFAOYSA-N 0.000 description 1
- JVTAAEKCZFNVCJ-UHFFFAOYSA-M Lactate Chemical compound CC(O)C([O-])=O JVTAAEKCZFNVCJ-UHFFFAOYSA-M 0.000 description 1
- 238000002835 absorbance Methods 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 239000000022 bacteriostatic agent Substances 0.000 description 1
- 239000000920 calcium hydroxide Substances 0.000 description 1
- 235000011116 calcium hydroxide Nutrition 0.000 description 1
- 150000001768 cations Chemical class 0.000 description 1
- 238000004587 chromatography analysis Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 238000004042 decolorization Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000005194 fractionation Methods 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 150000003893 lactate salts Chemical class 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 235000010755 mineral Nutrition 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
Abstract
Description
【発明の詳細な説明】
産業上の利用分野
本発明は、イオン交換樹脂を用いたクロマトグラフィ法
により、有機酸、特に発酵法によって得られた乳酸等を
効率よく分離、精製する方法およびその装置に関する。Detailed Description of the Invention Field of the Invention The present invention relates to a method and apparatus for efficiently separating and purifying organic acids, particularly lactic acid obtained by fermentation, by a chromatography method using an ion exchange resin. .
従来の技術
従来、乳酸、クエン酸、酢酸など、特に発酵法により得
られた有機酸を精製するには、発酵液に（ｉ）石灰乳を
加えて中和し硫酸等で分解する方法、（１１）エーテル
を加えて抽出、分離する方法、（ｉｉｉ ）アルコール
を加えエステル化して分離した後加水分解する方法など
が行われている。BACKGROUND OF THE INVENTION Conventionally, in order to purify organic acids such as lactic acid, citric acid, and acetic acid, especially those obtained by fermentation methods, there are two methods: (i) adding milk of lime to the fermentation liquid to neutralize it and decomposing it with sulfuric acid, etc. 11) A method of adding ether for extraction and separation, and (iii) a method of adding alcohol to esterify, separate, and then hydrolyze.
これら有機酸のうち、特に乳酸は医薬品（輸液）、醸造
（静菌剤）、食品（酸味）、化学工業の分野において広
く使用されているが、近年ｗＨｏ（１！ｊ界保健機横）
の提唱により食品、医薬などとして人体に摂取される乳
酸については化学合成乳酸から天然発酵乳酸（Ｌ−乳酸
）への転換が進められつつある。Among these organic acids, lactic acid in particular is widely used in the fields of pharmaceuticals (infusions), brewing (bacteriostatic agents), foods (acidity), and the chemical industry.
As a result of this proposal, conversion from chemically synthesized lactic acid to natural fermented lactic acid (L-lactic acid) is being promoted for lactic acid ingested by the human body as food, medicine, etc.
従来の発酵法による乳酸の精製法としては、前記エーテ
ル抽出法、エステル化法が主として用いられている。As a conventional method for purifying lactic acid by fermentation, the above-mentioned ether extraction method and esterification method are mainly used.
発明が解決しようとする問題点
しかしながら、エーテル抽出法により何機酸を分離精製
するには、人体に何方なイソプロピルエーテルなどのエ
ーテル類を溶媒として用いなければならない。また、エ
ステル化法ではエステルとアルコールとの分溜を行なう
際、分溜塔内で発酵乳酸液に含まれるグルコースの焦げ
着きが生じ、操業上好ましくないだけでなく、未反応の
グルコースを回収し再利用することができない。Problems to be Solved by the Invention However, in order to separate and purify organic acids using the ether extraction method, ethers such as isopropyl ether, which are common to the human body, must be used as a solvent. In addition, in the esterification method, when fractionating ester and alcohol, the glucose contained in the fermented lactic acid solution burns in the fractionation tower, which is not only undesirable for operation, but also requires recovery of unreacted glucose. cannot be reused.
問題点を解決するための手段
本発明者は、かかる問題点を解決すべく種々検討を重ね
た結果、これら有機酸を含む反応液をイオン交換樹脂で
処理することにより、効率よく有機酸の分離、精製が行
えることを見いだし本発明を完成するに至った。Means for Solving the Problems As a result of various studies aimed at solving these problems, the present inventors have found that they can efficiently separate organic acids by treating reaction solutions containing these organic acids with an ion exchange resin. They discovered that purification can be carried out and completed the present invention.
すなイつち、本発明は、有機酸の塩を含む反応液を（ａ
）カチオン交換樹脂で処理してイオン交換を行い有機酸
の塩を何機酸とする工程、（ｂ）該有機酸を含む反応液
をアニオン交換樹脂に吸着させて反応混合液に含まれる
未反応物質および副生物から分離する工程、（ｃ）該ア
ニオン交換樹脂を強酸で処理して、吸着された有機酸を
溶出する工程からなることを特徴とする有機酸の精製方
法、およびその装置を提供するものである。In other words, the present invention provides a reaction solution containing a salt of an organic acid (a
) A step of treating with a cation exchange resin to perform ion exchange and converting the salt of an organic acid into an organic acid; (b) adsorbing the reaction solution containing the organic acid onto an anion exchange resin to remove unreacted substances contained in the reaction mixture. Provided is a method for purifying an organic acid, which comprises the steps of: separating it from substances and by-products; and (c) treating the anion exchange resin with a strong acid to elute the adsorbed organic acid, and an apparatus therefor. It is something to do.
つぎに本発明の詳細な説明する。Next, the present invention will be explained in detail.
（ａ）イオン交換工程
中和された有機酸の塩を含む・反応混合液を活性炭など
により前処理した後、カチオン交換樹脂により処理し、
陽イオンをプロトンと交換して有機酸を得、吸着工程に
供給する。(a) Ion exchange process: The reaction mixture containing a neutralized organic acid salt is pretreated with activated carbon, etc., and then treated with a cation exchange resin.
Cations are exchanged for protons to obtain organic acids, which are fed to the adsorption step.
（ｂ）有機酸の吸着工程
イオン交換工程を経て有機酸を含む反応混合液をアニオ
ン交換樹脂で処理し有機酸を吸着、分離する。有機酸と
分離された反応混合液中に含まれる未反応物質および副
生物は、前工程に返送、回収する。(b) Organic acid adsorption step The reaction mixture containing organic acids after an ion exchange step is treated with an anion exchange resin to adsorb and separate the organic acids. Unreacted substances and byproducts contained in the reaction mixture separated from the organic acid are returned to the previous step and recovered.
（ｃ）有機酸の溶出工程
アニオン交換樹脂が有機酸の吸着により飽和し交換能が
低下すれば、たとえば硫酸、塩酸などの鉱酸により処理
してアニオン交換樹脂に吸着された乳酸を製品として溶
出する。(c) Organic acid elution process If the anion exchange resin becomes saturated due to the adsorption of organic acids and its exchange capacity decreases, the lactic acid adsorbed on the anion exchange resin can be eluted as a product by treatment with mineral acids such as sulfuric acid or hydrochloric acid. do.
これら（ａ）〜（ｃ）の工程で処理能力の低下したカチ
オン交換樹脂およびアニオン交換樹脂はつぎの方法で再
生する。The cation exchange resin and anion exchange resin whose processing capacity has decreased in these steps (a) to (c) are regenerated by the following method.
（１）カチオン交換樹脂の再生
イオン交換能の低下したカチオン交換樹脂は、硫酸、塩
酸等の強酸で処理してカチオン交換樹脂の再生を行なっ
た後、純水にて水洗する。(1) Regeneration of cation exchange resin A cation exchange resin with reduced ion exchange ability is treated with a strong acid such as sulfuric acid or hydrochloric acid to regenerate the cation exchange resin, and then washed with pure water.
（１１）アニオン交換樹脂の再生
有機酸溶出後のアニオン交換樹脂は、苛性ソーダなどの
アルカリ溶液により再生する。再生完了後、純水により
アニオン交換樹脂を洗浄し、交換サイクルに戻る。(11) Regeneration of anion exchange resin The anion exchange resin after organic acid elution is regenerated with an alkaline solution such as caustic soda. After the regeneration is completed, the anion exchange resin is washed with pure water and the exchange cycle returns.
本発明方法は乳酸のほか、クエン酸、酢酸などの有機酸
の分離、精製に摘要することができる。The method of the present invention can be applied to the separation and purification of organic acids such as citric acid and acetic acid in addition to lactic acid.
本発明方法にて用いられるイオン交換樹脂は公知のもの
がいずれら用い得るが、カチオン交換樹脂としては強酸
樹脂、例えばダイヤイオンＰＫ２０８．５ＫＩＢ（三菱
化成（昧）製）、アニオン交換樹脂としては強塩基樹脂
、例えばＰＡ３１２（三菱化成（株）製）などが好適に
用いられる。Any known ion exchange resin can be used as the ion exchange resin used in the method of the present invention, but the cation exchange resin is a strong acid resin, such as Diaion PK208.5KIB (manufactured by Mitsubishi Kasei), and the anion exchange resin is a strong acid resin. A basic resin such as PA312 (manufactured by Mitsubishi Kasei Corporation) is preferably used.
また、カチオン交換樹脂槽、およびアニオン交換樹脂槽
を複数とすることにより連続操作が可能となる。Continuous operation is also possible by providing a plurality of cation exchange resin tanks and anion exchange resin tanks.
夫胤■
つぎに、本発明を実施例により添付の図面を参照してさ
らに具体的に説明する。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Next, the present invention will be described in more detail by way of examples with reference to the accompanying drawings.
第１図は、本発明の方法を用いて、発酵法にて得られた
乳酸を発酵液から分離、精製する方法を示すフローチャ
ートである。FIG. 1 is a flowchart showing a method for separating and purifying lactic acid obtained by fermentation from a fermentation liquid using the method of the present invention.
（ａ）イオン交換工程
（ｉ）イオン交換サイクル
発酵工程にて得られた乳酸をアンモニアにより中和する
（図示せず）。ついで、この乳酸塩を含む発酵液（乳酸
として１％）を活性炭槽１に供給し、活性炭により脱色
する。脱色後、発酵液をバッファータンク２を経てカチ
オン交換樹脂槽３に導入する。該樹脂槽３にて、発酵液
中の乳酸塩はカチオン交換樹脂によりカチオン交換がお
こなわれ、そのアンモニウムイオンがプロトンに置換さ
れて乳酸となる。つぎにこの乳酸を含む発酵液はタンク
４を通って吸着工程に向かう。（イオン交換サイクル中
、バルブＡＩ、Ｂ２：開放、バルブＡ２、Ａ３、Ｂｌ：
閉止）
（ｉｉ ）カチオン交換樹脂の再生
カチオン交換中、カチオン交換樹脂の交換能の低下は、
ｐＨメーター７の指示値の上昇により検知される。ｐ
Ｉ−１メーターの指示値か上昇（ｐＨ１０）すると、バ
ルブＡ１を閉止して発酵工程から送液される発酵液をタ
ンク２に一時貯蔵する。(a) Ion exchange step (i) Ion exchange cycle The lactic acid obtained in the fermentation step is neutralized with ammonia (not shown). Next, the fermentation liquor containing this lactate (1% as lactic acid) is supplied to the activated carbon tank 1 and decolorized with activated carbon. After decolorization, the fermentation liquid is introduced into a cation exchange resin tank 3 via a buffer tank 2. In the resin tank 3, the lactate in the fermentation liquor undergoes cation exchange using a cation exchange resin, and the ammonium ions are replaced with protons to become lactic acid. Next, this fermentation liquid containing lactic acid passes through tank 4 and heads to the adsorption step. (During the ion exchange cycle, valves AI, B2: open, valves A2, A3, Bl:
(ii) Regeneration of cation exchange resin During cation exchange, the decrease in the exchange capacity of the cation exchange resin
This is detected by an increase in the indicated value of the pH meter 7. p
When the indicated value of the I-1 meter increases (pH 10), the valve A1 is closed and the fermented liquid sent from the fermentation process is temporarily stored in the tank 2.
つぎに、バルブＡ２およびバルブＢｌを開放、バルブＢ
２を閉止して、硫酸タンク８よりＩＮＨ，ＳＯ，をカチ
オン交換樹脂１に導入し、（ＮＨＪｔＳＯ４を排出して
カチオン交換樹脂の再生を行なう。ｐＨメーター７の指
示値が低下（ｐＨ４）すればバルブＡ２を閉止し、カチ
オン交換樹脂の再生を完了する。ついで、バルブＡ３を
開放し、純水にてカチオン交換樹脂を洗浄する。洗浄完
了後、バルブＡ３、Ｂ１を閉止、バルブＡＩおよびバル
ブＢ２を再び開放して前記イオン交換サイクルを復帰す
る。Next, open valve A2 and valve Bl, and open valve B1.
2 is closed, INH, SO, is introduced into the cation exchange resin 1 from the sulfuric acid tank 8, and the cation exchange resin is regenerated by discharging (NHJtSO4). Close valve A2 to complete regeneration of the cation exchange resin.Next, open valve A3 and wash the cation exchange resin with pure water.After washing is complete, close valves A3 and B1, and valve AI and valve B2. is opened again to resume the ion exchange cycle.
（ｂ）乳酸の吸着・溶出工程
（ｉ）乳酸の吸着工程
イオン交換工程を経た乳酸を含む発酵液は、つぎにアニ
オン交換樹脂槽５に導入される。該樹脂槽５にて発酵液
中の乳酸は、アニオン交換樹脂に吸着され、グルコース
等の未反応物質および副生物から分離される。未反応物
質および副生物は回収ライン６を通って、前工程（発酵
工程）に返送される。（吸着サイクル中、バルブＣＩ、
Ｄ２：開放、Ｃ２、Ｃ３、Ｃ４、Ｃ５、Ｄｌ、Ｂ３、Ｂ
４、Ｂ５：閉止）
（１１）乳酸の溶出工程
アニオン交換樹脂の交換能の低下は、ｐＨメーター９の
指示値の低下により検知される。第２図に示すごとく時
間経過に伴い発酵液の供給（積算量）が増加するとｐ
Ｈメーター９の指示値が低下し、アニオン交換樹脂槽５
内に吸着されないで流出する乳酸が増大する。ｐＨメー
ター９の指示値が低下（ｐＨ３）すると、バルブＣＩを
閉止し、カチオン交換樹脂槽３からの送液をタンク４に
一時貯蔵する。ついで、バルブＣ５、ＨよびバルブＤ３
、Ｂ４を開放、バルブＤ２を閉止して、アニオン交換樹
脂槽５内に残存するグルコースおよび未吸着の乳酸を純
水により洗浄し、洗浄液をタンク１０に貯蔵する。つぎ
にバルブＣ５、Ｂ４を閉止し、バルブＣ２、Ｂ５を開放
して前記硫酸タンク８よりＩＮＨ，Ｓｏ、をライン１１
を介してアニオン交換樹脂槽５に導入しアニオン交換樹
脂に吸着された乳酸を取出ライン１３より溶出する。溶
出完了はｐＨメーター９の指示値の低下により検知され
る。第３図に示すごとく、乳酸は溶出操作により１０％
以上にまで濃縮される。溶出が完了（ｐ）１０．８）す
るとバルブＣ２、バルブＤ５を閉止する。(b) Lactic acid adsorption/elution step (i) Lactic acid adsorption step The fermentation liquid containing lactic acid that has undergone the ion exchange step is then introduced into the anion exchange resin tank 5. In the resin tank 5, lactic acid in the fermentation liquid is adsorbed by an anion exchange resin and separated from unreacted substances such as glucose and by-products. Unreacted substances and byproducts are returned to the previous step (fermentation step) through the recovery line 6. (During the adsorption cycle, valve CI,
D2: Open, C2, C3, C4, C5, Dl, B3, B
4, B5: Closed) (11) Lactic acid elution step A decrease in the exchange ability of the anion exchange resin is detected by a decrease in the indicated value of the pH meter 9. As shown in Figure 2, as the supply (cumulative amount) of fermentation liquid increases over time, p
The indicated value of the H meter 9 decreases, and the anion exchange resin tank 5
The amount of lactic acid that flows out without being adsorbed inside increases. When the indicated value of the pH meter 9 decreases (pH 3), the valve CI is closed and the liquid sent from the cation exchange resin tank 3 is temporarily stored in the tank 4. Then, valves C5, H and valve D3
, B4 is opened and valve D2 is closed, glucose remaining in the anion exchange resin tank 5 and unadsorbed lactic acid are washed with pure water, and the washing liquid is stored in the tank 10. Next, valves C5 and B4 are closed, valves C2 and B5 are opened, and INH, So are supplied from the sulfuric acid tank 8 to the line 11.
The lactic acid is introduced into the anion exchange resin tank 5 through the anion exchange resin, and the lactic acid adsorbed on the anion exchange resin is eluted from the extraction line 13. Completion of elution is detected by a decrease in the indicated value of the pH meter 9. As shown in Figure 3, lactic acid was reduced to 10% by the elution procedure.
It is concentrated to more than that. When elution is completed (p) 10.8), valves C2 and D5 are closed.
（ｉｉｉ ）アニオン交換樹脂の再生
乳酸の溶出を完了したアニオン交換樹脂をアルカリ溶液
により再生ずる。バルブＣ３およびバルブＤ１を開放し
、苛性ソーダｆｆｆ１２よりＩＮＮ ａ ＯＨをアニオ
ン交換樹脂槽５に導入しバルブＤＩを介してＮａ２５Ｏ
＊を排出する。再生が完了するとｐ ）Ｉメーター９の
指示値が上昇する。再生完了（ＩｌｙＨ１２）後、バル
ブＣ３を閉止、バルブＣ５を開放して純水によりアニオ
ン交換樹脂を洗浄する。洗浄が完了しｐＨメーター９の
指示値か低下（ｐＨ７）すればバルブＣ５、ＤＩを閉止
、バルブＣＩを開放して、もとの交換サイクルに戻る。(iii) Regeneration of anion exchange resin The anion exchange resin from which elution of lactic acid has been completed is regenerated with an alkaline solution. Valve C3 and valve D1 are opened, INN a OH is introduced from caustic soda fff12 into anion exchange resin tank 5, and Na25O is introduced through valve DI.
Emit *. When the regeneration is completed, the indicated value of the I meter 9 increases. After completion of regeneration (IlyH12), valve C3 is closed, valve C5 is opened, and the anion exchange resin is washed with pure water. When the cleaning is completed and the indicated value of the pH meter 9 drops (pH 7), valves C5 and DI are closed, valve CI is opened, and the original exchange cycle is resumed.
タンクｌＯ内の乳酸は、Ｃ４を開放して槽５に返送し、
未吸着の乳酸を再び吸着させる。The lactic acid in tank 10 is returned to tank 5 by releasing C4,
Adsorb unadsorbed lactic acid again.
なお、ｐＨメーター７および９の代わりに他の検出器、
例えば吸光度計を用いてらよい。In addition, other detectors can be used instead of pH meters 7 and 9.
For example, an absorbance meter may be used.
発明の効果
本発明によれば、人体に有害なエーテル類などを溶媒と
して用いることなく、有機酸を含む反応液から効率よく
有機酸を分離、精製し得るとともに、安定した操業およ
び未反応物質の回収、有効な再使用が可能となるうEffects of the Invention According to the present invention, an organic acid can be efficiently separated and purified from a reaction solution containing an organic acid without using ethers or the like that are harmful to the human body as a solvent, and stable operation and removal of unreacted substances can be achieved. Recovery and effective reuse will be possible.
第１図は、本発明の方法を用いて発酵法にて得られた乳
酸を発酵液から分離、精製する方法を示ずフローチャー
ト、第２図は吸着時の発酵液流量に対するｐＨ値と乳酸
およびグルコース濃度を示すグラフ、第３図は溶出時の
発酵液流量に対するｐＨ値と乳酸および硫酸の濃度を示
すグラフである。
図中の主な符号はつぎのとおりである。
３；カチオン交換樹脂槽、５：アニオン交換樹脂槽、６
：回収ライン、８ 硫酸タンク、１３：取出ライン。
１収Figure 1 is a flowchart showing a method for separating and purifying lactic acid obtained by fermentation from fermentation liquid using the method of the present invention, and Figure 2 shows the pH value and lactic acid and the flow rate of fermentation liquid during adsorption. A graph showing the glucose concentration, and FIG. 3 is a graph showing the pH value and the concentration of lactic acid and sulfuric acid with respect to the flow rate of the fermentation liquid at the time of elution. The main symbols in the figure are as follows. 3; Cation exchange resin tank, 5: Anion exchange resin tank, 6
: Recovery line, 8 Sulfuric acid tank, 13: Takeout line. 1 income
Claims (2)
脂で処理してイオン交換を行い有機酸の塩を有機酸とす
る工程、（ｂ）該有機酸を含む反応液をアニオン交換樹
脂に吸着させて反応混合液に含まれる未反応物質および
副生物から分離する工程、（ｃ）該アニオン交換樹脂を
強酸で処理して、吸着された有機酸を溶出する工程から
なることを特徴とする有機酸の精製方法。(1) Process of (a) treating a reaction solution containing a salt of an organic acid with a cation exchange resin to perform ion exchange and converting the salt of an organic acid into an organic acid; (b) anion exchange of the reaction solution containing the organic acid. (c) treating the anion exchange resin with a strong acid to elute the adsorbed organic acid; A method for purifying organic acids.
該カチオン交換樹脂槽と連通するアニオン交換樹脂槽、
並びに該アニオン交換樹脂槽と連通する有機酸取出ライ
ンおよび前記有機酸生成工程への回収ラインからなり、
前記カチオン交換樹脂槽が強酸タンクと連通し、アニオ
ン交換樹脂槽が強酸タンクおよびアルカリタンクと連通
することを特徴とする有機酸の精製装置。(2) a cation exchange resin tank communicating with the organic acid production process;
an anion exchange resin tank communicating with the cation exchange resin tank;
and an organic acid take-off line communicating with the anion exchange resin tank and a recovery line to the organic acid production step,
An organic acid purification apparatus characterized in that the cation exchange resin tank communicates with a strong acid tank, and the anion exchange resin tank communicates with a strong acid tank and an alkali tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2117287A JPS63188632A (en) | 1987-01-30 | 1987-01-30 | Purification of organic acid and apparatus therefor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2117287A JPS63188632A (en) | 1987-01-30 | 1987-01-30 | Purification of organic acid and apparatus therefor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63188632A true JPS63188632A (en) | 1988-08-04 |
Family
ID=12047500
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2117287A Pending JPS63188632A (en) | 1987-01-30 | 1987-01-30 | Purification of organic acid and apparatus therefor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63188632A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01102033A (en) * | 1987-10-15 | 1989-04-19 | Sumitomo Chem Co Ltd | Removal of organic acid |
| EP0517242A2 (en) * | 1991-06-06 | 1992-12-09 | Montell North America Inc. | Process for the production of purified lactic acid aqueous solutions starting from fermentation broths |
| US6280985B1 (en) | 1999-10-18 | 2001-08-28 | Roquette Freres | Process for the separation and purification of lactic acid from a fermentation medium |
| JP2007124931A (en) * | 2005-11-02 | 2007-05-24 | Ccy:Kk | Method for purifying lactic acid |
| JP2008286952A (en) * | 2007-05-16 | 2008-11-27 | Denso Corp | Liquid crystal display device |
| JP2014015474A (en) * | 2007-09-17 | 2014-01-30 | Rohm & Haas Co | Process for converting hydroxy carboxylic acid, or salt thereof, to unsaturated carboxylic acid and/or esters thereof |
| WO2020050068A1 (en) * | 2018-09-06 | 2020-03-12 | 日機装株式会社 | Lactic acid absorber and method for removing lactic acid |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5576839A (en) * | 1978-12-04 | 1980-06-10 | Mitsubishi Chem Ind Ltd | Treatment of polycarboxylic acid solution containing mineral acid |
| JPS58164541A (en) * | 1982-03-25 | 1983-09-29 | Mitsubishi Chem Ind Ltd | Purification of polycarboxylic acid |
| JPS60199390A (en) * | 1984-02-03 | 1985-10-08 | ヨ−・ア−・ベンキザ−・ゲゼルシヤフト・ミツト・ベシユレンクテル・ハフツング | Obtaining of citric acid |
-
1987
- 1987-01-30 JP JP2117287A patent/JPS63188632A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5576839A (en) * | 1978-12-04 | 1980-06-10 | Mitsubishi Chem Ind Ltd | Treatment of polycarboxylic acid solution containing mineral acid |
| JPS58164541A (en) * | 1982-03-25 | 1983-09-29 | Mitsubishi Chem Ind Ltd | Purification of polycarboxylic acid |
| JPS60199390A (en) * | 1984-02-03 | 1985-10-08 | ヨ−・ア−・ベンキザ−・ゲゼルシヤフト・ミツト・ベシユレンクテル・ハフツング | Obtaining of citric acid |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01102033A (en) * | 1987-10-15 | 1989-04-19 | Sumitomo Chem Co Ltd | Removal of organic acid |
| EP0517242A2 (en) * | 1991-06-06 | 1992-12-09 | Montell North America Inc. | Process for the production of purified lactic acid aqueous solutions starting from fermentation broths |
| US6280985B1 (en) | 1999-10-18 | 2001-08-28 | Roquette Freres | Process for the separation and purification of lactic acid from a fermentation medium |
| JP2007124931A (en) * | 2005-11-02 | 2007-05-24 | Ccy:Kk | Method for purifying lactic acid |
| JP2008286952A (en) * | 2007-05-16 | 2008-11-27 | Denso Corp | Liquid crystal display device |
| JP2014015474A (en) * | 2007-09-17 | 2014-01-30 | Rohm & Haas Co | Process for converting hydroxy carboxylic acid, or salt thereof, to unsaturated carboxylic acid and/or esters thereof |
| WO2020050068A1 (en) * | 2018-09-06 | 2020-03-12 | 日機装株式会社 | Lactic acid absorber and method for removing lactic acid |
| JPWO2020050068A1 (en) * | 2018-09-06 | 2021-10-21 | 日機装株式会社 | Lactic acid adsorbent and lactic acid removal method |
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