EP1235636A1 - Procede d'epuration de solutions contenant des acides amines par electrodialyse - Google Patents

Procede d'epuration de solutions contenant des acides amines par electrodialyse

Info

Publication number
EP1235636A1
EP1235636A1 EP00977477A EP00977477A EP1235636A1 EP 1235636 A1 EP1235636 A1 EP 1235636A1 EP 00977477 A EP00977477 A EP 00977477A EP 00977477 A EP00977477 A EP 00977477A EP 1235636 A1 EP1235636 A1 EP 1235636A1
Authority
EP
European Patent Office
Prior art keywords
amino acid
electrodialysis
circuit
lysine
containing solution
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.)
Withdrawn
Application number
EP00977477A
Other languages
German (de)
English (en)
Inventor
Andreas Fischer
Christoph Martin
Jürgen Müller
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of EP1235636A1 publication Critical patent/EP1235636A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P13/00—Preparation of nitrogen-containing organic compounds
    • C12P13/04—Alpha- or beta- amino acids
    • C12P13/08—Lysine; Diaminopimelic acid; Threonine; Valine
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/42—Electrodialysis; Electro-osmosis ; Electro-ultrafiltration; Membrane capacitive deionization
    • B01D61/44—Ion-selective electrodialysis
    • B01D61/445—Ion-selective electrodialysis with bipolar membranes; Water splitting
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P13/00—Preparation of nitrogen-containing organic compounds
    • C12P13/04—Alpha- or beta- amino acids

Definitions

  • the present invention relates to a method for purifying amino acid-containing solutions by electrodialysis, an amino acid-containing solution obtained from a fermentation being used.
  • Amino acids can be fermented from a carbon source, e.g. Molasses and raw sugar are made.
  • the solutions generally obtained in the fermentation contain, in addition to approximately 10% by weight of amino acid, large amounts of impurities, such as e.g. B. also cell mass.
  • the amino acid in its ionic form displaces the corresponding ions of the cation or Anion exchange column and is thus retained by this.
  • the cell mass can be filtered off before or after the ion exchange treatment.
  • the mother liquor obtained after the run still contains about 0.1% by weight of amino acid and a load of about 1 ton of salt, for example ammonium sulfate per ton of amino acid. This solution can be disposed of by dumping, which is also of particular ecological concern due to the high salt load of the solution to be dumped.
  • the mother liquor which essentially contains ammonium sulfate and cell mass, can be worked up by numerous evaporation and filtration stages, the ammonium sulfate being able to be recovered.
  • the mother liquor obtained must continue to be disposed of. In addition, this procedure is very labor intensive and has a high energy consumption.
  • the amino acid retained on the ion exchange resin is eluted, for example, with ammonia water.
  • the eluate is stripped of ammonia, whereby large amounts of ammonia water have to be evaporated.
  • the eluted amino acid is then treated with acid, e.g. B. hydrochloric acid, crystallized and dried.
  • acid e.g. B. hydrochloric acid
  • the amino acid thus obtained with a purity> 98.5% is referred to as a "feed-grade" amino acid.
  • the feed-grade Goods are subjected to a further cleaning procedure, for example an activated carbon treatment and / or repeated crystallization.
  • Electrodialysis is a very elegant cleaning or separation process with the u. a. Mixtures of amino acids can be separated. Such a method is described, for example, in J. Chem. Technol. Biotechnol. 71 (1998), pp. 267ff by Sandeaux et al. described. According to this scientific publication, acidic hydrolysis of animal or human residues, such as. B. feathers or hair obtained protein hydrolyzates first neutralized and decolorized with activated carbon and then subjected to a multi-stage electrodialysis, whereby different fractions of the individual amino acids are obtained.
  • the object of the present invention was to develop an improved method for purifying amino acid To provide fermentation discharges. This has been achieved with the application of electrodialysis to this problem.
  • the present invention relates to a method for purifying amino acid-containing solutions by electrodialysis (d), an amino acid-containing solution obtained from a fermentation for the production of at least one amino acid being used.
  • the present invention also relates to the use of electrodialysis for the purification of amino acid-containing solutions obtained from the fermentation up to an amino acid content of> 98.5% (% by weight).
  • the method according to the invention relates to the purification of amino acid-containing solutions which are obtained from the fermentation.
  • amino acid-containing solutions obtainable by the various fermentation processes can be used.
  • further stages such as treatment with an ion exchanger and / or crystallization, can be carried out, in which case only the resulting mother liquor is treated by means of electrodialysis.
  • the present invention thus also relates to a process which comprises the following additional steps (a) to (c):
  • FIG. 1 describes an embodiment of the present invention in which bipolar membranes are used in a 3-circuit electrodialysis
  • Figure 2 also describes another embodiment of the present invention using 3-circuit electrodialysis
  • FIG. 3 describes an embodiment of the present invention
  • amino acids with positively charged (basic) side groups, e.g. Lysine, arginine, histidine;
  • Amino acids with negatively charged (acidic) side groups such as aspartic acid or glutamic acid
  • amino acids with uncharged, polar or non-polar side groups such as alanine, valine, leucine, isoleucine, proline, Phenylalanine, tryptophan, methionine, glycine, serine, threonine, cysteine, tyrosine, asparagine and glutamine.
  • either the 3-circuit electrodialysis with bipolar membranes is used to purify the amino acid-containing solutions, it being possible to obtain amino acid as the free base or acid or a conventional two-circuit electrodialysis in which the amino acid as a salt, preferably as an amino acid hydrochloride, e.g. B. in the form of lysine hydrochloride.
  • FIG. 3 shows a schematic diagram of this electrodialysis arrangement.
  • an apparatus which has a positive (anode (+)) and a negative (cathode (-)) large-area electrode.
  • the space between these electrodes is divided by a large number of alternately arranged cation (C) and anion (A) exchange membranes into a large number of narrow chambers separated by the membranes, which are also referred to as diluate circuit (II) and concentrate circuit (IV) , divided up.
  • Chambers which have an anion exchange membrane on the cathode side and a cation exchange membrane on the anode side represent the so-called concentrate chambers or concentrate circles, while chambers which have the anion exchange membrane and on the cathode side have the cation exchange membrane, which form diluate chambers or the diluate circuit.
  • the diluate circles are filled with the amino acid-containing solution (2) to be purified, the concentrate circles, on the other hand, with an aqueous electrolyte (4), and the chambers in which the electrodes are located and, if necessary, those directly adjacent to them Adjacent chambers are charged with an electrode rinsing solution, usually a sodium sulfate solution.
  • an electrode rinsing solution usually a sodium sulfate solution.
  • the desired amino acid (5) is obtained as a salt in high purity, e.g. high purity lysine hydrochloride.
  • the diluate circuit which contains the solution to be cleaned (2), e.g. a solution of lysine hydrochloride, a lysine-free mother liquor (3) is obtained.
  • any membranes that are usually used in the context of electrodialysis processes can be used to carry out the process according to the invention.
  • commercially available ion exchange membranes are preferably used. These membranes preferably consist of organic polymers that have ion-active side chains.
  • Cation exchange membranes contain sulfo or carboxyl groups in the Polymer matrix, anion exchange membranes have tertiary or quaternary amino groups as substituents of the polymeric base material.
  • Copolymers of styrene and divinylbenzene are particularly suitable as polymeric base material for the ion exchange membranes.
  • Ion exchange membranes with a capacity of 0.8 to 5, preferably 1.2 to 3.2 milliequivalents per g (meq / g) are preferably used.
  • anion exchange membranes that can be used are: Tokuyama AMI, AM2, AM3, AMX, AMH, AFN, Asahi Glass AMV.
  • Tokuyama CM1, CM2, CMX, CMH and Asahi Glass CMV are examples of cation exchange membranes.
  • Bipolar membranes are laminates made from anion and cation exchange membranes. Compared to monopolar anion or cation exchange membranes, they are characterized by the fact that they catalyze efficient water splitting in the electrical field of electrodialysis and thus serve to simultaneously provide H + and OH ' equivalents.
  • a 3-circuit (chamber) arrangement (3-circuit bipolar electrodialysis) consisting of diluate (II), acid (III) and base (I) circuits is used.
  • the three-circle arrangement is achieved by an alternating sequence of the respective ion exchange membrane (cf. FIG. 1).
  • the electrodialysis is preferably carried out at approximately 10 to approximately 80 ° C., in particular between approximately 20 and approximately 60 ° C.
  • the current density in conventional 2-circuit electrodialysis varies between about 1 and about 1000 A / m, preferably between about 100 and about 800 A / m.
  • the current density varies between approximately 1 and approximately 1,500 A / m, preferably between approximately 200 and approximately 1,000 A / m.
  • Electrodialysis is carried out in the process according to the invention up to a final conductivity of the diluate of approximately 2 mS / cm, in particular approximately 1 mS / cm and below, for example approximately 0.8 or 0.5 mS / cm.
  • all amino acids can be separated in this way if the addition of acid exceeds the isoelectric point in the direction of low pH values and thus imprints a positive excess charge on the amino acid, or if the base is added to the isoelectric point of the amino acid in the direction of higher pH values exceeds and in this way imprints a negative total charge on the amino acid.
  • the amino acid enters the base circle through the cation exchange membrane in the direction of the cathode and accumulates there as the free base. In the latter case, the amino acid migrates in anionic form through the anion exchange membrane towards the anode and into the acid circuit, where it accumulates as free acid.
  • the corresponding salt of the amino acid is always obtained in the concentrate chamber.
  • a solution containing lysine in cationic form H lysine +
  • a solution containing lysine in cationic form H lysine +
  • e.g. B. contains as lysine * HCl
  • Lysine base is released from the protonated lysine then located in the base circle by the hydroxide ions formed on the bipolar membrane.
  • the anions, e.g. B. chloride or sulfate ions are transferred through an anion exchange membrane into the so-called acid circuit chamber and form the corresponding acid with the protons released there on the bipolar membrane.
  • uncharged particles such as e.g. B. cell mass
  • the electrodes are rinsed with an electrolyte solution in a separate circuit.
  • FIG. 1 illustrates this principle of the method. It should be noted that the arrangement shown there represents only one unit of the electrodialysis device used. Such units can be used according to the invention for electrodialysis devices with 1 to 1000 units.
  • AC denotes a bipolar membrane, C a cation exchange membrane and A an anion exchange membrane.
  • the dotted line indicates that the unit shown can be present several times in the electrodialysis apparatus, with "n" indicating the number of repetitions.
  • the acid circuit used is generally the acid corresponding to the resulting lysine-containing solution, for example salt - or sulfuric acid (3) is introduced into the acid circuit (III), the dilution being chosen as high as possible, only sufficient ionic conductivity of the solution having to be ensured at the beginning of electrodialysis.
  • concentrations of 0.5% by weight For use in the base circuit (I), a dilute solution of free lysine (1) is preferably used, which can originate, for example, from a batch that has already been cleaned, and both the solutions introduced into the acid and base circuit can be used in the course of electrodialysis
  • the acid circuit (III) it is possible to fill the acid circuit (III) with 0.5% H 2 SO, the concentration of H 2 SO during electrodialysis can rise to about 10%.
  • the base circle (I) in a concentration of z. B. 0.5% lysine used as a free base solution in general up Concentrated to a concentration of lysine as free base of 10 to 30% (1 ').
  • the acid formed in the acid circuit chamber can in turn serve to produce the lysine salt of the acid from the lysine monohydrate released in the electrodialysis or to acidify the fermentation output for use in electrodialysis.
  • Such an acidified fermentation discharge e.g. B. Lysine * H 2 SO, (2) is introduced using the above-mentioned 3-circuit electrodialysis via the diluate circuit (II), a lysine-free fermentation mother liquor (4) being obtained in the diluate circuit (II).
  • cationic lysine migrates through a cation exchange membrane into the base circuit (I) during electrodialysis, while the counterions reach the acid circuit (III) via an anion exchange membrane.
  • the bipolar membrane which is also present, supplies the acid circuit with H + ions and the base circuit with OH ⁇ ions.
  • the base circuit discharge merely has to be evaporated, the method of spray drying being preferred here.
  • the corresponding salts such as amino acid hydrochloride or sulfate
  • the solution containing amino acid hydrate must be crosslinked with the corresponding acids or alkalis.
  • the lysine thus obtained has a purity of> 98.5% according to the feed grade specification and can, for. B. further purified by simple activated carbon treatment or recrystallization, so that food or pharmaceutical grade lysine is accessible.
  • I ⁇ SO (2 ') ie an acidified fermentation output.
  • This can then be introduced in the next batch as diluate (2 ") into the diluate circuit (II) and cleaned as described above, the other reference numerals in FIG. 2 corresponding to those in FIG. 1.
  • This variant has the advantage that only in the first batch of diluate use, ie the fermentation discharge has to be acidified once and further addition of acid can be dispensed with in the further course of electrodialysis.
  • the present invention also relates to a method as defined above, which comprises:
  • lysine base is obtained, which can either be obtained and sold directly in the form of solid lysine monohydrate by drying, or can first be mixed with hydrochloric acid and then dried, then lysine hydrochloride is obtained.
  • lysine in cationic form e.g. B. lysine hydrochloride to be obtained as a valuable product
  • a so-called conventional electrodialysis without bipolar membranes can also be used. This procedure is shown schematically in FIG. 3.
  • Conventional electrodialysis consists of an alternating arrangement of cation exchange membranes (C) and anion exchange membranes (A).
  • the lysine-containing solution, the lysine in the form of a salt, e.g. B. lysine hydrochloride contains (2) are introduced into the so-called diluate chamber (II).
  • lysine in cationic form passes through the cation exchange membrane (C) into the concentrate circuit (IV).
  • the corresponding counterions, e.g. B. chloride ions migrate from the diluate circuit (II) over the anion exchange membrane (A) into the concentrate circuit.
  • the present invention relates to an integrated process for the production of a free amino acid comprising:
  • the electrodialysis was carried out at a maximum current density of 80 mA / cm 2 with an applied cell voltage of 35 V and a temperature of 50 ° C. After using a current of 25 Ah, a base circle discharge containing 32% by weight of lysine base with a residual chloride content of less than 0.2% by weight was obtained with a lysine yield of 96% of the amount used.
  • Example 2 (Separation of Lysine Hydrochloride from Contaminated Solutions Using Conventional Electrodialysis)
  • the electrodialysis was carried out at a maximum current density of 80 mA / cm 2 with an applied cell voltage of 20 V and a temperature of 50 ° C. After 8 hours of electrodialysis, a base circle discharge containing 29% by weight of lysine hydrochloride was obtained with a yield of> 98%.
  • the iodine color number of a lysine hydrochloride solution adjusted to 10% by weight from the concentrate discharge from the electrodialysis was 1.1. There was also a clear purification of the lysine hydrochloride.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Health & Medical Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Zoology (AREA)
  • Urology & Nephrology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Biochemistry (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Microbiology (AREA)
  • Biotechnology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)

Abstract

L'invention concerne un procédé d'épuration d'une solution contenant des acides aminés par électrodialyse, caractérisé en ce qu'il fait intervenir une solution contenant des acides aminés provenant de la fermentation destinée à la fabrication d'au moins un acide aminé.
EP00977477A 1999-11-03 2000-11-03 Procede d'epuration de solutions contenant des acides amines par electrodialyse Withdrawn EP1235636A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE19952961 1999-11-03
DE19952961A DE19952961A1 (de) 1999-11-03 1999-11-03 Verfahren zur Aufreinigung von aminosäurehaltigen Lösungen durch Elektrodialyse
PCT/EP2000/010852 WO2001032298A1 (fr) 1999-11-03 2000-11-03 Procede d'epuration de solutions contenant des acides amines par electrodialyse

Publications (1)

Publication Number Publication Date
EP1235636A1 true EP1235636A1 (fr) 2002-09-04

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EP00977477A Withdrawn EP1235636A1 (fr) 1999-11-03 2000-11-03 Procede d'epuration de solutions contenant des acides amines par electrodialyse

Country Status (10)

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US (1) US6551803B1 (fr)
EP (1) EP1235636A1 (fr)
JP (1) JP2003512853A (fr)
KR (1) KR20020059673A (fr)
CN (1) CN1387458A (fr)
AU (1) AU1517901A (fr)
BR (1) BR0015202A (fr)
DE (1) DE19952961A1 (fr)
RU (1) RU2002114827A (fr)
WO (1) WO2001032298A1 (fr)

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CN102757354A (zh) * 2012-07-26 2012-10-31 无锡晶海氨基酸有限公司 一种利用膜分离与电渗析组合技术从发酵液中提取分离l-亮氨酸的方法
CN103232353A (zh) * 2013-04-12 2013-08-07 北京轻发生物技术中心 一种从发酵液中高效分离提取l-缬氨酸的方法
CN103933861B (zh) * 2013-08-02 2017-04-26 浙江赛特膜技术有限公司 一种双极膜电渗析制备蛋氨酸和氢氧化钠的方法
EP3090039A1 (fr) * 2014-01-02 2016-11-09 Carlsberg Breweries A/S Boissons à saveur stable
CN103922980B (zh) * 2014-04-22 2016-08-24 中国科学技术大学 一种利用双极膜电渗析从蛋氨酸盐与碳酸盐的混合溶液中分离出蛋氨酸的方法
CN105348122B (zh) * 2015-10-30 2017-11-10 安徽丰原发酵技术工程研究有限公司 一种l‑丙氨酸末道母液的纯化方法
EP3801843A4 (fr) * 2018-06-06 2022-02-23 Monsanto Technology LLC Électrodialyse de sels d'acides aminés à membrane bipolaire à trois compartiments
CN111995748B (zh) * 2019-05-27 2022-05-24 浙江工业大学 一种基于电渗析技术的ε-聚赖氨酸的纯化方法
CN113087647B (zh) * 2019-12-23 2022-12-06 武汉远大弘元股份有限公司 一种半胱氨酸的制备方法
CN114014771B (zh) * 2021-06-30 2023-12-12 安徽华恒生物科技股份有限公司 一种超高纯度的氨基酸及其制备方法和其应用
CN114133354B (zh) * 2021-12-10 2023-08-29 河北一品生物医药有限公司 一种l-组氨酸的工业化制备方法
CN116254555B (zh) * 2023-02-08 2025-11-14 安徽中医药大学 一种离子置换膜反应器制备l-门冬氨酸钾的方法

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Publication number Publication date
RU2002114827A (ru) 2004-04-10
US6551803B1 (en) 2003-04-22
WO2001032298A1 (fr) 2001-05-10
CN1387458A (zh) 2002-12-25
BR0015202A (pt) 2002-07-23
DE19952961A1 (de) 2001-05-10
AU1517901A (en) 2001-05-14
KR20020059673A (ko) 2002-07-13
JP2003512853A (ja) 2003-04-08

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