EP2788310A1 - Procédé de purification d'acides carboxyliques issus de bouillons de fermentation - Google Patents

Procédé de purification d'acides carboxyliques issus de bouillons de fermentation

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Publication number
EP2788310A1
EP2788310A1 EP12794869.3A EP12794869A EP2788310A1 EP 2788310 A1 EP2788310 A1 EP 2788310A1 EP 12794869 A EP12794869 A EP 12794869A EP 2788310 A1 EP2788310 A1 EP 2788310A1
Authority
EP
European Patent Office
Prior art keywords
acid
separation
biomass
fermentation
lactic acid
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Withdrawn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
EP12794869.3A
Other languages
German (de)
English (en)
Inventor
Joachim Schulze
Wolfgang Tietz
Isabel WAENGLER
Klaus KÜHLEIN
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.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
ThyssenKrupp Industrial Solutions AG
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 ThyssenKrupp Industrial Solutions AG filed Critical ThyssenKrupp Industrial Solutions AG
Publication of EP2788310A1 publication Critical patent/EP2788310A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives
    • C07C51/47—Separation; Purification; Stabilisation; Use of additives by solid-liquid treatment; by chemisorption
    • 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
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/08—Apparatus therefor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/42—Separation; Purification; Stabilisation; Use of additives

Definitions

  • the invention relates to a process for the purification of carboxylic acids from fermentation broths, and to a device for carrying out the method according to the invention.
  • the isolation of carboxylic acids, which can not be separated or only with difficulty by distillation, is very complicated.
  • succinic acid for example.
  • the qualities of the succinic acid produced can be differentiated by the subdivision into a technical grade with a succinic acid content of at least 97% by mass and a succinic acid (polymer grade or 1,4 butanediol grade) especially suitable for use for the polymerization with a content of at least 99% , 5 Mao / o.
  • Extractive processes using extraction agents such as tributylamines, trialkylamines, olefins, various alcohols and aromatic
  • Membrane processes such as, for example, reverse osmosis and other filtration processes, wherein also couplings of these processes and supplementation by further prior art corresponding steps are discussed.
  • Such methods are described inter alia in the patents DE 69821951 T2; DE 69015233 T2; DE 69015019 T2; DE 69006555 T2; DE 69015019; DE 60028958T2; DE 10 2004 026152 A1.
  • lactic acid can be isolated, for example, from a fermentation broth acidified with sulfuric acid, which in addition to free lactic acid still contains ammonium and sulfate ions, can be isolated by means of chromatographic methods.
  • DE 69815369 T2 describes, inter alia, the separation of lactic acid from aqueous mixtures by adsorption on a solid adsorbent, preferably a solid adsorbent is used here, which adsorbs lactic acid versus lactate.
  • weak anion exchangers for lactic acid isolation come into question.
  • DE 10 2009 019 248 A1 further describes chromatographic Methods for purifying organic acids, in particular lactic acid, by performing Simulated Moving Bed Chromatography.
  • WO 2006/124633 A1 describes a process for the production of ammonium lactate by fermentation.
  • the ammonium salt of lactic acid formed from the fermentation solution e.g. can be separated by extraction.
  • the ammonium salt can be easily split in a subsequent step with weak acids or carbon dioxide. This gives you the free lactic acid, which can then be purified by distillation, for example.
  • WO99 / 19290 describes a lactic acid fermentation with subsequent filtration and extraction, wherein the extraction may be an adsorption.
  • the type of interaction with the solid phase of adsorption is not disclosed.
  • a similar process is disclosed in WO93 / 06226, in which case the solid phase of the adsorption is provided with tertiary amino groups and thereby the production rate of free acid is increased.
  • EP0135728 also teaches the isolation of enzymatically produced carboxylic acids via adsorbers which are provided with tertiary amino groups. The fermentation takes place via cells immobilized on columns.
  • DE19939630C2 discloses a process for the fine purification of aqueous solutions containing fermentatively produced organic acids, such as, for example, citric acid, lactic acid, succinic acid or tartaric acid.
  • the solution coming from the fermentation is first filtered and then the resulting solution is passed through an anion exchanger and a subsequent Adsorberharzbett.
  • the adsorbent resin bed used for the fine cleaning is initially loaded with OH " ions and binds the product acid, and there is no mention of further purification of the filtered solution downstream of the filtration to remove impurities contained, such as cell debris, carbohydrates, nutrients, amino acids and sugars.
  • the solid adsorbent may here be a poly-4-vinylpyridine resin or a tertiary polystyrene-bivinylbenzene-amine resin. Again, an intermediate step to remove other contaminants is not taught.
  • the object of the invention is to provide a process for the separation and purification of carboxylic acids from fermentation broths which has a high product purity of> 80% by mass and avoids known disadvantages of other processes.
  • the object is achieved by the use of a process for the separation and purification of carboxylic acids from fermentation broths, the process comprising the following steps,
  • the advantage of this method is that is greatly reduced by the arranged before the adsorption fine cleaning, the content of impurities in the fermentation broth from step a), which is then sent through the solid phase of adsorption, whereby the production rate of carboxylic acid on can be increased and the equipment cost is reduced, creating a cheaper method, as disclosed for example in EP0135728, created.
  • EP0135728 proposes to strongly adsorb the carboxylic acids and to carry out a circulation process in highly contaminated fermentation solutions, which is very expensive.
  • Another advantage of the inventive method is that is not neutralized during the fermentation and the separation and purification with the free acid and not with its salt, as is often the case in the prior art.
  • the process is simplified in that no acidification step is necessary and thus no further substances added during the fermentation must be separated off, which are normally used in the prior art for neutralization.
  • microorganisms for the fermentation itself, a variety of microorganisms can be used, including bacteria, yeasts and fungi.
  • the fermentation broth may also contain various recycle streams from the overall process.
  • the fermentation broth containing the carboxylic acid, biomass and constituents of the substrate is continuously fed to precoat filtration and / or microfiltration and / or ultrafiltration.
  • the resulting separated biomass is optionally returned to the fermenter.
  • temperature and pH correspond to the values of the fermentation, since it was found that by inactivating the biomass by increasing the temperature and lowering the pH by adding acid autolysis of the biomass is accelerated and more lysis products be discharged into the fermentation broth.
  • the time between completion of the fermentation and separation of the biomass should be kept as short as possible and should not be more than 2 hours, preferably less than 1-2 hours.
  • the biomass concentration in the filtrate should not exceed 1 g / l. This process management positively influences the end product quality.
  • step b In order to produce the production of carboxylic acids in a high-purity quality, a fine cleaning is performed due to still existing residues of dyes and impurities in step b), which is preferably configured as nanofiltration.
  • membranes of a separation size of 100 to 400 Da are used. It was shown that nanofiltration with a cut-off of 200 Da gives good quality results.
  • the process is conducted so that the retentate of the nanofiltration is not more than 10% of the total throughput.
  • the permeate is fed to the further process step c).
  • a reverse osmosis is carried out between the process steps b) and c). This step will serve as an exemplary further way of concentrating before
  • tertiary amino groups are preferably used, which are pryridine, which are preferably selected from the group comprising polyvinylpyridine and poly-2 or poly-4-vinylpyridine.
  • the one or more solid phase used for adsorption in process step c) is a polymer which is crosslinked with divinylbenzene.
  • the one or more solid phase used for adsorption in process step c) is formed from one or more different polymer materials.
  • Further suitable polymers having tertiary amino groups which selectively adsorb carboxylic acids and permit their desorption with polar solvents are described, for example, in DE 1274128 and DE 3043766.
  • the adsorbed carboxylic acids are desorbed in process step c) preferably by treatment with a polar solvent from the group of aliphatic alcohols, aliphatic ketones and aliphatic carboxylic acid esters.
  • Desorption is particularly preferably carried out by means of methyl acetate or ethyl acetate, acetone or methyl ethyl ketone and in particular with lower alcohols such as ethanol and particularly advantageously with methanol.
  • the desorption with water which is advantageously heated to a temperature of 20 ° C to 60 ° C, is possible.
  • the solvent is optionally then separated via a distillation of the carboxylic acid and / or the product is crystallized out.
  • further purification steps such as activated carbon filtration and / or anion and / or cation exchange can be provided.
  • the carboxylic acid to be separated off and to be purified is preferably selected from the group comprising hydroxycarboxylic acids and dicarboxylic acids.
  • the hydroxycarboxylic acid is selected from the group comprising
  • Malic acid glycolic acid, isocitric acid, mandelic acid, lactic acid, tartronic acid, tartaric acid, citric acid, ⁇ -hydroxybutyric acid, mevalonic acid and salicylic acid, and is preferably lactic acid.
  • the dicarboxylic acid is selected from the group comprising oxalic acid, maleic acid, succinic acid, glutaric acid, Adipic acid, pimelic acid, suberic acid, fumaric acid and itaconic acid, and is preferably succinic acid.
  • the present invention claims an apparatus for carrying out the method set forth in claim 1.
  • Embodiment 1 is a diagrammatic representation of Embodiment 1:
  • a fermentation broth containing exemplarily lactic acid, biomass and constituent parts of the substrate was continuously separated from the biomass by precoat filtration and microfiltration.
  • the resulting broth contained 2% lactic acid.
  • the lactic acid-containing permeate containing 2% is used in an adsorption-desorption experiment.
  • An adsorbent resin which carries poly-4-vinylpyridine as active component and is crosslinked with divinylbenzene and polymerized into a spherical structure is used here.
  • the lactic acid is to be seen here as an exemplary representative of a carboxylic acid. With the aid of the adsorber resin, the lactic acid is bound to the resin from the lactic acid solution. In a subsequent desorption step, the lactic acid is recovered. For desorption, 40 ° C. warm water was used here. The results can be found in the following Tab. 1.
  • Tab. 1 Adsorption and desorption of lactic acid to an amino group-bearing adsorbent resin, wherein the desorption was carried out with water, having a temperature of 40 ° C:
  • Table 1 shows a 6-fold adsorption-desorption cycle. 10 g of an adsorbent resin were used. It could be shown that a desorption of almost 100% is possible.
  • the loading capacity is 0.54 g of lactic acid per 10 g of polymer when 40 ° C warm water is used for desorption. % Desorption is calculated to be 95% over the last 5 cycles.
  • the first charge / discharge cycle shows a higher adsorption of 1.13 g of lactic acid and a reduced desorption. This can be explained by the fact that the resin must first be charged with a basic load.
  • the impurities still contained interfere with a subsequent processing of the lactic acid, e.g. to polylactic acid.
  • a subsequent processing of the lactic acid e.g. to polylactic acid.
  • even more adsorption desorption cycles are necessary to achieve a desired product quality, since the other impurities partially adsorb to the column material.
  • a larger number of adsorption columns would be necessary.
  • Embodiment 2 is a diagrammatic representation of Embodiment 1:
  • a process chain including nanofiltration as a fine cleaning is shown.
  • a fermentation broth containing carboxylic acids such as lactic acid was produced by fermentation of microorganisms. At this time, the pH became between 6.0 and 7.3 held constant, without neutralization agent, such as NaOH, were added. This was achieved by continuously withdrawing fermentation broth and purifying it. For this purpose, it is necessary for an average productivity of lactic acid during the fermentation of 4 g / l / h and the specified pH range, the subsequent microfiltration of the process step a) and the nanofiltration of the process step b) be interpreted such that the volume of the permeate from the nanofiltration corresponds to 2 times the working volume of the fermenter.
  • the fermentation broth exemplified by lactic acid, biomass and constituents of the substrate, was continuously separated from the biomass by precoat filtration and microfiltration.
  • the resulting broth contained 2% lactic acid. It was ensured that the temperature and the pH correspond to the values in the fermentation carried out.
  • the subsequent fine cleaning was carried out as nanofiltration. A membrane with a separation size of 200 Da was used. Care was taken that nanofiltration was carried out at a temperature equal to that of the fermentation, with a temperature difference of ⁇ 5 ° C being tolerated. It was worked here in a temperature range of 48 ° C to 52 ° C. Also, the pH of the fermentation, which ranges from 6 to 7.3, has been maintained.
  • the retentate stream, at The nanofiltration obtained and containing the impurities can be returned to the fermentation again.
  • the lactic acid-containing permeate containing 2% was used in an adsorption-desorption experiment.
  • An adsorbent resin which carries poly-4-vinylpyridine as the active component and is crosslinked with divinylbenzene and polymerized into a spherical structure was used.
  • the lactic acid is to be seen here as an exemplary representative of a carboxylic acid.
  • the adsorber resin With the aid of the adsorber resin, the lactic acid is bound to the resin from the lactic acid solution.
  • the lactic acid is recovered. For desorption, 40 ° C. warm water was used here. The results can be found in the following Tab. 1.
  • Tab. 2 Adsorption and desorption of lactic acid to an amino group-bearing adsorbent resin, wherein the desorption was carried out with water, having a temperature of 40 ° C:
  • Table 1 shows a 6-fold adsorption-desorption cycle. 10 g of an adsorbent resin were used. It could be shown that a desorption of almost 100% is possible. In summary it can be said that the loading capacity is 0.59 g of lactic acid per 10 g of polymer when 40 ° C warm water is used for desorption. The desorption in% is calculated over the last 5 cycles at 97%. The first charge / discharge cycle shows a higher adsorption of 1, 26 g lactic acid and a reduced desorption. This can be explained by the fact that the resin must first be charged with a basic load.
  • Embodiment 3 is
  • Embodiment 3 differs from Embodiment 2 in the choice of the desorbent.
  • Embodiment 3 methanol was used as an example of an aliphatic alcohol. The results can be found in the following Tab. 3.
  • Table 3 shows a 6-fold adsorption-desorption cycle.
  • the loading capacity of the adsorber resin is 0.78 g of lactic acid per 10 g of polymer when methanol is used for desorption.
  • The% desorption is calculated to be at least 100% over the last 5 cycles.
  • the first loading / unloading cycle shows a higher adsorption of 1, 14 g of lactic acid and a reduced desorption. This can also be explained by the fact that the resin must first be charged with a basic load.
  • Impurities that permanently damage the resin Possible components are including sugars, dyes and peptides.
  • Embodiment 4 is a diagrammatic representation of Embodiment 4:
  • Embodiment 4 differs from Embodiment 2 by an additional method step.
  • a reverse osmosis (UO) was additionally applied to the NF. The results can be found in FIG. 1.
  • Fig. 1 loading capacity after preconcentration of lactic acid
  • Fig. 1 the amount of lactic acid adsorbed in g on 10 g of polymer is plotted against the concentration of lactic acid solution in g / L used to charge the column. From this graph it can be seen that the loading capacity increases with the lactic acid concentration. A concentration by a factor of 4.5 leads to an increase in loading to 2.5 times. Further concentration by other known from the prior art measures or a
  • the additional process step requires much less resin for adsorption. Furthermore, the concentration of lactic acid after desorption is higher and thus the cost of further concentration lower.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Nanotechnology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Preparation Of Compounds By Using Micro-Organisms (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Procédé de séparation et de purification d'acides carboxyliques à partir de bouillons de fermentation, ledit procédé comprenant les étapes suivantes : a) séparation de la biomasse et des matières solides éventuellement présentes du bouillon de fermentation, b) purification du bouillon de fermentation obtenu à l'étape a) par nanofiltration, c) séparation de l'acide carboxylique par adsorption sur une ou plusieurs phase(s) solide(s) comportant des groupes amino tertiaires.
EP12794869.3A 2011-12-09 2012-11-15 Procédé de purification d'acides carboxyliques issus de bouillons de fermentation Withdrawn EP2788310A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102011120632A DE102011120632A1 (de) 2011-12-09 2011-12-09 Verfahren zur Aufreinigung von Carbonsäuren aus Fermentationsbrühen
PCT/EP2012/004741 WO2013083229A1 (fr) 2011-12-09 2012-11-15 Procédé de purification d'acides carboxyliques issus de bouillons de fermentation

Publications (1)

Publication Number Publication Date
EP2788310A1 true EP2788310A1 (fr) 2014-10-15

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EP12794869.3A Withdrawn EP2788310A1 (fr) 2011-12-09 2012-11-15 Procédé de purification d'acides carboxyliques issus de bouillons de fermentation

Country Status (5)

Country Link
US (1) US9272976B2 (fr)
EP (1) EP2788310A1 (fr)
BR (1) BR112014013798A2 (fr)
DE (1) DE102011120632A1 (fr)
WO (1) WO2013083229A1 (fr)

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Publication number Priority date Publication date Assignee Title
DE102016001070A1 (de) 2015-02-06 2016-08-11 Rwth Aachen Verfahren zur Trennung organischer Dicarbonsäuren durch Adsorption hydrophober poröser Materialien
EP3268099A1 (fr) * 2015-03-12 2018-01-17 Novasep Process SAS Procédé de purification d'un acide organique comprenant une étape de traitement par électrodialyse
EP3290101A1 (fr) * 2016-09-05 2018-03-07 Nanoscience for life GmbH & Co. KG Procede de fabrication de membranes separatrices a selection de matiere et son utilisation
KR20220052965A (ko) 2019-08-28 2022-04-28 다니스코 유에스 인크. 메발로노락톤을 포함하는 스킨 케어 조성물
EP3822356A1 (fr) * 2019-11-18 2021-05-19 Corvay Bioproducts GmbH Procédé de production d'un acide dicarboxylique
CN111138273A (zh) * 2019-12-24 2020-05-12 上海凯赛生物技术股份有限公司 一种长链二元酸的精制工艺及系统
US12017182B2 (en) 2019-12-24 2024-06-25 Cathay Biotech Inc. Method and system for refining long chain dicarboxylic acid
CN113880710B (zh) * 2021-10-22 2023-10-20 万华化学集团股份有限公司 一种乳酸的纯化方法
US20230248677A1 (en) * 2022-02-08 2023-08-10 Visolis Technologies, Inc. Novel highly sustainable compositions for modulation of gene expression in human skin, and methods of production thereof

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US9272976B2 (en) 2016-03-01
BR112014013798A8 (pt) 2017-06-13
WO2013083229A1 (fr) 2013-06-13
US20140371486A1 (en) 2014-12-18
DE102011120632A1 (de) 2013-06-13
BR112014013798A2 (pt) 2017-06-13

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