• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The process for producing amino acids from volatile fatty acid (VFA) molecules, known as precursors, produced by anaerobic fermentation from fermentable biomass, comprises at least the following steps: a) extracting the acid molecules volatile fats (AGV), without interruption of the fermentation, by an extraction means chosen from means which are, at least, insoluble in the fermentation medium, b) collect, outside the fermentation reactor, the molecules of volatile fatty acids (VFA) once extracted, - c) synthesize, by halogenation, from a type of volatile fatty acid (VFA) chosen from the volatile fatty acids collected in step b) and defined according to the desired type of amino acid, a given α-halogenated acid; d) synthesizing from said α-halogenated acid a defined amino acid.
    公开号:FR3033166A1
    申请号:FR1551673
    申请日:2015-02-27
    公开日:2016-09-02
    发明作者:Regis Nouaille；Jeremy Pessiot；Marie Thieulin
    申请人:Afyren SAS；
    IPC主号:
    专利说明:

    [0001] The present invention relates to a process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass. Amino acids are the constituent compounds of peptides and therefore proteins. They are used, among other things, as animal feed additives (for example lysine, methionine or threonine), as flavor enhancers in human nutrition such as glutamate, serine or aspartic acid, as specific nutrients in the diet. medical field or in the cosmetic field. Glycine, alanine, norvaline and norleucine may also be mentioned as amino acids having applications in the field of pharmacopoeia, cosmetics and industrial chemistry. The production of amino acids is known by chemical synthesis or by conversion using enzymes. Such methods, although easily adaptable and allowing optimum control of the production parameters, are complex and expensive to implement.
    [0002] In order to minimize production costs, there are, for example, processes for obtaining amino acids microbially. Amino acids are primary metabolites produced by microorganisms in a fermentation process. If such methods make it possible to produce large amounts of amino acids directly assimilable by the body, the fact remains that this type of process is dedicated to a single type of amino acid. The invention aims more particularly at remedying these disadvantages by proposing a process for producing amino acids making it possible to produce various types of amino acids, in particular nonproteinogenic amino acids, in an easy manner and without the constraints related to the known production methods of the invention. 'state of the art.
    [0003] For this purpose, the subject of the invention is a process for producing amino acids from volatile fatty acid (VFA) molecules, referred to as precursors, produced by anaerobic fermentation from fermentable biomass, characterized in that it comprises at least the following steps: 5 - a) extracting the volatile fatty acid (VFA) molecules, without interruption of the fermentation, by an extraction means selected from means which are, at least, insoluble in the fermentation medium, - b) collect, outside the fermentation reactor, the volatile fatty acid (VFA) molecules once extracted, 10 - c) synthesize, by halogenation, from a type of volatile fatty acid (AGV) chosen from the volatile fatty acids collected in step b) and defined according to the type of amino acid desired, a given α-halogenated acid, - d) synthesize from this α-halogen acid a defined amino acid; . Thus, such a method makes it possible to couple a phase of continuous production of precursors by microorganisms with a synthesis phase carried out without fermentation, which allows easy control of the various parameters, while allowing greater variability in the type of precursor. amino acids produced. Such a method makes it possible to dispose, continuously, precursors, namely volatile fatty acids, while preserving the production capacity of the microorganisms present in the bioreactor. Indeed, the extraction and collection steps a) and b) not only make it possible to extract and continuously collect the volatile fatty acid molecules produced in the fermentation reactor, but also to preserve the microorganisms responsible for this production. . Indeed, the extraction, and de facto collection, is carried out under at least non-lethal conditions for all the microorganisms, that is to say in biocompatible extraction and collection conditions, that being the case. that the extraction preserves the activity of the microorganisms and that the collection is carried out outside the fermentation reactor.
    [0004] In this way, it is overcome problems related to the accumulation of metabolites in the fermentation reactor, for example acidification of the fermentation medium by accumulation of volatile fatty acids produced that are harmful to microorganisms. The amount and activity of the microorganisms is maintained at a high level, close to the initial level, throughout the fermentation cycle. By having a continuous and regular production of AGV, we have a source of varied precursors easily usable and quickly. In the process which is the subject of the invention, this use is made, starting from stage c), by chemical synthesis and therefore under easily controllable and modifiable conditions, this also offering a great variability in the type of molecules. synthesized. In fact, during step c), according to the VFA retained for carrying out the halogenation, a given type of α-halogen acid is obtained and therefore, subsequently, a given type of α-amino acid. Such a method makes it possible, during the anaerobic fermentation phase, to use fermentable biomass. By fermentable biomass, is meant here an organic substrate, preferably non-food, obtained from waste, by-products and co-products formed from organic materials, that is to say biomass, resulting from human activities, that they are domestic, industrial, agricultural, forestry, aquaculture, agro-industrial, resulting from breeding or other. By way of non-limiting example, mention may be made, as an organic substrate, of manure, the fermentable fraction of household refuse, slaughterhouse co-products, cellulosic or lignocellulosic residues originating from agro-industry, such as those derived from sugar cane (bagasse), sunflower or soy. By anaerobic fermentation is meant a fermentation carried out under anaerobic conditions by microorganisms, eukaryotic or prokaryotic, such as bacteria, fungi, algae or yeasts. According to advantageous but non-obligatory aspects of the invention, such a method may comprise one or more of the following characteristics: in step c), the halogenated compound used is bromine. In step c), the halogenated compound used is different from the dibrome. In step c), acetic anhydride is used in a molar percentage with respect to the volatile fatty acid close to 12%. In step c), an anhydride corresponding to the volatile fatty acid (VFA) to be halogenated is used. 5 - In step c), the temperature at which the bromination reaction is carried out is 20 ° C to 40 ° C below the boiling point of the volatile fatty acid. - In step d), the synthesis is carried out by reaction with ammonia in excess relative to the stoichiometry of the reaction. - In step d), the synthesis is carried out by reaction with an amine. In step d), the temperature is between 20 ° C and 50 ° C. In step d), at least one co-product defined as an iminodiacide and / or a nitrilotriacide is synthesized. There are several types of amino acids of interest for industrial, cosmetic, medical, food or other uses. By way of example, mention may be made of nonproteinogenic amino acids, such as homoalanine, norvaline, norleucine, which are sought for the synthesis of platform molecules for the pharmacopoeia. The term "amino acid" denotes acids having at least one primary, secondary or tertiary amine function.
    [0005] Furthermore, by virtue of the process of the invention, it is possible to synthesize several types of amino acids, such as but not exclusively those mentioned above, in a regular and controlled manner, from a bio-sourced substrate by combining a biological production with a chemical production. The invention will be better understood and other advantages thereof will appear more clearly on reading the description of several embodiments of the invention, given by way of non-limiting example. The various steps of the method are now described with reference to several embodiments, it being understood that the steps known per se are not detailed.
    [0006] First of all, the substrate used is advantageously untreated, ie it has not undergone any physicochemical or enzymatic pretreatment. This substrate is mainly constituted by fermentable biomass. As a nonlimiting complementary example, mention may be made of agricultural or plant wastes (straw, bagasse, corn kernels, herbs, wood, mastics) paper waste (cardboard, paper), agro-food waste, waste paper slaughterhouses, the fermentable fraction of household refuse, livestock manure (manure, manure, droppings), algae, aquaculture waste, forestry waste or fermentable co-products of the cosmetics industry. Some substrates contain organic molecules, such as organic acids, which will not, or only marginally, influence the fermentation process. On the other hand, these molecules can be found in the fermentation medium and participate, for example, in the production of the defined final organic molecules. As a reminder, and in a known manner, the substrate is introduced into a fermentation reactor, known per se and sized for the desired production, whether the latter is on a laboratory scale to carry out tests or on an industrial scale in the field. case of a production. In other words, the fermentation reactor or bioreactor has a volume ranging from a few liters to several hundred cubic meters, as needed.
    [0007] Microorganisms are advantageously initially introduced into the fermentation reactor, in an amount sufficient to start the fermentation. The microorganisms are advantageously inoculated in the form of a consortium. The term consortium means a mixture or mixture of microorganisms, eukaryotes and prokaryotes, whether they be bacteria, yeasts, fungi or algae. These different microorganisms come mainly from natural ecosystems, advantageously but not exclusively, anaerobic ecosystems such as, by way of non-limiting example, the anaerobic zone of aquatic environments such as the anoxic zone of certain lakes, soils, marshes , sewage sludge, ruminant rumen or termite gut. It should be borne in mind that the qualitative and quantitative distribution of the different types and species of microorganisms in the consortium is not known precisely and above all can vary in significant proportions. It turns out that this qualitative and quantitative diversity surprisingly provides robustness and adaptability of the microorganisms which make it possible to ensure an optimal use of the substrates, whatever the composition of the latter and this under variable fermentation conditions. Moreover, because the substrate is used as it is, that is to say, it is not sterilized or, more generally, it is not cleared of the microorganisms it contains prior to its introduction into the bioreactor, it turns out that the microorganisms endemic to the substrate are, de facto, incorporated into the consortium or at least associated with the latter in the bioreactor. Furthermore, the fermentation takes place under anaerobic conditions, more specifically when the redox potential is less than -300mV, advantageously between -550mV and -400mV and when the pH is less than 8, preferably between 4 and 7.
    [0008] The fermentation is, advantageously, limited to the production of so-called precursor fermentative metabolites, namely volatile fatty acids or AGV having from two to eight carbons, preferably from two to six. A reaction similar to the acidosis phenomenon encountered in ruminants is thus induced while having a production of methane close to zero. Methane is generally one of the final fermentative metabolites obtained during anaerobic fermentation by microorganisms from natural ecosystems. The fermentation leads initially to the formation of volatile fatty acids having mainly two to four carbons such as, for example, acetic acid, propionic acid and butyric acid. Less volatile fatty acids with a long chain, thus greater than four carbons, such as valeric and caproic, heptanoic or octanoic acids, are also obtained. By continuing the fermentation and / or increasing the amount of microorganisms in the bioreactor, if necessary with selected microorganisms, it is possible to promote the production of AGV long chain carbon, so greater than four carbons.
    [0009] In other words, the volatile fatty acids produced in quantity during the fermentation are essentially volatile fatty acids of two to six carbons. Fermentation is in all cases conducted to ensure the production of AGV in the liquid phase. Typically, the fermentation period is between 15 and 7 days, preferably between 2 and 4 days. The concentration of metabolites obtained in the fermentation medium at the end of this period is variable, but, for volatile fatty acids, is generally of the order of 10 to 20 g / L, depending on the volatile fatty acids, being understood that under certain conditions it may be greater than 35 g / l, for example close to 50 g / l. At the end of the fermentation step, the fermentation medium is at an acidic pH, which is generally between 4 and 6, because of the presence of the volatile fatty acids in the fermentation medium. When the production of AGV reaches a defined quantity, generally during the steady state phase of the fermentation, step a) of extraction of the molecules is initiated. Preferably, but not obligatory, this defined amount of AGV corresponds to a slowing down of the growth of the microorganisms, therefore in the vicinity of a threshold of inhibition of the microorganisms. The extraction means is selected from extraction means, liquid or solid, which are at least insoluble in the fermentation medium. When the extraction means is liquid, so when it is a solvent, preferably, the density of the solvent is lower than that of the fermentation medium. More specifically, the extraction is carried out with a solid or liquid extraction means, the implementation conditions of which make it possible to preserve the activity and / or the growth of the microorganisms under the fermentation conditions prevailing in the bioreactor. and which are defined to carry out the fermentation. The 25 AGV molecules are preferably extracted by molecular families and then advantageously separated individually by techniques known per se. When molecules such as volatile fatty acids are extracted from the fermentation medium, de facto the acidification of the fermentation medium is reduced by these 30 acids. Thus, the fermentation, and therefore the production of metabolites, continues under conditions similar to the initial conditions, the fermentation medium remaining slightly acidic. The extraction is advantageously carried out continuously or at least sequentially, for example with extraction every 12 hours. In other words, it is possible to continue the fermentation while extracting the metabolites produced, either as they are produced or on a regular basis. The liquid-liquid extraction with organic solvents as extraction means is the extraction mode, preferably but not exclusively, retained. In one embodiment, the extraction is not carried out in a separate member 10 of the fermentation reactor but directly in the latter. The solvent is, for example, introduced by a bubbler type device located in the lower part of the reactor. Alternatively, an extraction member is coupled with the reactor, a communication with the fermentation medium being arranged. At the end of the extraction, the collection step b) is implemented. In this step, the VFAs are collected from the organic phase by techniques known per se, such as distillation or evaporation. The collection is carried out either in a mixture of AGV or by type of AGV. It is conceivable that the choice of the AGV or the AGV mixture is determined by the type of final molecule (s) desired (s). For this, the collection conditions, typically the evaporation or distillation parameters, are adapted. Once this collection step has been performed, the following step c) is carried out. This is, advantageously but not exclusively, carried out following the collection step. Alternatively, it is carried out at another time and / or another place, the produced AGV being transported and / or stored, according to techniques known per se.
    [0010] This halogenation step consists in causing a halogen to act with an AGV in order to produce an α-halogen acid which is a type of highly reactive molecule and therefore of particular interest for producing other molecules. Such a reaction, known per se, is carried out by addition of bromine, this preferably, it being understood that it is possible to use the other halogens, namely chlorine, fluorine or iodine or halogenated molecules such as such as phosphorus trihalides, halogenated acids or acyl halides. The bromine was retained because a brominated α-haloacid is more reactive than the corresponding chlorinated α-haloacid, a carbon-brominated bond being easier to break than a carbon-chlorine bond. In addition, the bromine is easier to handle because of its liquid form. To carry out the synthesis of α-bromo acid, the route using an anhydride, here acetic anhydride, and pyridine was retained. It is conceivable that other synthetic routes, for example with polyphosphoric acid or phosphorus trihalides, are known per se. Tests with polyphosphoric acid were conducted but the results were inconclusive, among other things because of the high viscosity of this compound which makes handling difficult. Chlorination tests have also been conducted by the applicant for the synthesis of α-chlorinated acids, for example with trichloroisocyanuric acid. The results obtained are inferior in terms of efficiency and ease of use to those obtained with bromine. The synthetic route employing an anhydride corresponding to the volatile fatty acid that is to be halogenated is of interest and makes it possible to obtain an α-halogen acid, here an α-bromo acid of a given type. The use of acetic anhydride with other VFAs and / or a mixture of two to six carbons of AGV makes it possible to obtain a mixture of α-halogenated acids of two to six carbons. Tests using acetic acid (two-carbon AGV), propionic acid (three-carbon AGV), butyric acid (four-carbon AGV), caproic acid (six-fold AGV) carbons) and a mixture of two to six carbons of AGV were made by varying the amount of acetic anhydride as well as other parameters such as temperature. During the various tests, a protocol is respected. It is a preliminary phase of refluxing an initial mixture of AGV, acetic anhydride and pyridine. Then, during the actual bromination, the bromine is added slowly, for several hours, at a temperature below the boiling point of the mixture, once the bromine is added, the mixture is refluxed again. to be cooled. At the end of the reaction, advantageously, water is added to destroy the anhydride present. The α-bromo acid is then extracted by different methods, depending on the acid. It is for example, distillation, separation extraction. The initial temperature, to bring the mixture to reflux, is between 120 ° C, for AGV two carbons and 200 ° C, for AGV six carbons. The bromination temperature ranges from 80 ° C to 180 ° C, whereas VFAs have from two to six carbons. The time of the bromination reaction, thus de facto the time of addition of the dibroma, varies from about one hour for the six carbons AGV to about four hours for the two carbons AGVs. Two, three, four, six carbons volatile fatty acid bromination assays were performed as well as a test on a volatile fatty acid mixture: Acetic acid (C2): 0.53 mol Propionic acid (C3) 0.53 mol Butyric acid (C4): 0.53 mol Caproic acid (C6): 0.24 mol AGA mixture C2 to C6: 0.54 mol. The amount of bromine added is 0.21 mol or 0.11 mol so that the volatile fatty acid is in excess. Advantageously, the Applicant has found that a molar ratio of 2: 1 in favor of AGV is optimal. The amount of anhydride added is, for each acid, 0.06 mol for one test and 0.03 mol for another test. The AGV mixture comprises acetic (C2), propionic (C3), butyric (C4), valeric (C5) and caproic (C6) acids. The reflux temperatures during the preliminary phase vary according to the AGV: 120 ° C for acetic acid; 120 ° C and 140 ° C for testing with propionic acid; 150 ° C and 160 ° C for butyric acid; 200 ° C for caproic acid and 180 ° C for mixing.
    [0011] The bromination temperatures for the various tests with each acid are less than 10 ° C to 50 ° C, and preferably 200 to 40 ° C, at the reflux temperatures, thus boiling the volatile fatty acid. The yields and purities of the α-brominated acids obtained at the end of the various tests are given below in Table 1 in which the AGVs are, for simplicity, designated by the number of carbons. TABLE 1 Acids Amount Time Temperature Temperature Yield Anhydride purity reflux bromination (0/0) (0/0) (mol) (h) (° C) bromination (° C) 02 0.06 2.2 120 100 87 98 02 0.03 4 120 90 80 93 03 0.06 3 120 80 to 110 77 80 03 0.03 3 140 125 100 93 04 0.06 1.25 160 140 80 95 04 0.03 3 150 110 to 140 100 96 06 0.03 0.92 200 150 100 NC mixture 0.06 1.5 180 130 100 NC 10 Analysis and yield calculations were carried out by analytical techniques known per se, namely by NMR (Resonance Nuclear Magnetic) and HPLC (High Performance Liquid Chromatography). The yields are defined with respect to the amount of AGV consumed. The Applicant has found that the reaction rate, as shown by the discoloration of the reaction mixture after adding the dibrome, is faster when the amount of anhydride is greater, the purity being little affected. Nevertheless, it is appropriate that the temperature of the two stages, preliminary and bromination, be optimal.
    [0012] For this, the Applicant has noted that a bromination temperature below the boiling point of the volatile fatty acid is necessary, without being too far from this temperature. The various tests have made it possible to define a lower bromination temperature of about 10 ° C. to 50 ° C. at the boiling temperature of the volatile fatty acid and, advantageously, less than 20 ° C. identical, to obtain an optimal yield, typically between 60% and 100% with a reaction time of 1h to 4h. Regarding the role of acetic anhydride, in view of the results of the table, it appears that the molar percentage of anhydride relative to the AGV must be close to 12% for an optimal bromination reaction, it being understood that a percentage between 5% and 20% is acceptable. From the α-brominated acids obtained, or more precisely from a given α-bromo acid, the synthesis is then carried out during step d) of a given α-amino acid. For this we add ammonia, in gaseous form or in solution. Alternatively, the ammonia is replaced by a primary or secondary amine. Tests were carried out by the applicant by reaction of ammonia on α-bromoacids having from two to six carbons, namely on bromoacetic acid, α-bromopropionic acid, α-bromobutyric acid, α-bromovaleric acid, α-bromocapric acid. Such a reaction makes it possible to obtain α-amino acids having a carbon chain of two, three, four, five or six carbons, namely glycine, alanine, homoalanine, norvaline and norleucine. These α-amino acids are among the most used as constitutive of cosmetic products, food, whether in human or animal nutrition or as reaction intermediates in chemistry and pharmacopoeia. It is easy to see that the process which is the subject of the invention makes it possible to produce other types of amino acids. For the different tests, the protocol consisted in causing ammonia to react with the α-brominated acid at a temperature of between about 20 ° C. and 50 ° C. The reaction is conducted for a variable time, ranging from one half hour to seventy-two hours depending on the type of α-bromo acid and temperature. A long-brominated acid, that is to say having at least four carbons, requires a long reaction time, typically greater than 24 hours at room temperature but less than 12 hours at 50 ° C.
    [0013] The Applicant has found, surprisingly, that a high reaction temperature close to 50 ° C. makes it possible to reduce the reaction time. The Applicant has found that when the ammonia is put in excess, namely in a molar ratio of 1:10, the conversion to amino acid is optimized. Table 2 below shows the results obtained.
    [0014] The analysis and calculations of yields and conversion rates were performed by analytical techniques of NMR (Nuclear Magnetic Resonance) and HPLC (High Performance Liquid Chromatography). The conversion rates are calculated from the amount of amino acid produced in the reaction medium relative to the initial amount of α-brominated acid. The yields are defined in relation to the mass and qualitative analysis of the products, recovered after extraction and recrystallization from methanol. TABLE 2 Acids Ratio T (° C) Consumption Conversion Acid yield: NH3 to acid in AA (%) after α-brominated (%) - extraction time (h) (0/0) 02 1:10 (Ambient T) 99% - 5h 46 24 03 1: 5 (Ambient T) 95% - 5h 65 44 03 1:10 (Ambient T) 98% - 5h 66 52 03 1:10 50 99% - 1h 64 40 04 1: 5 (T ambient ) 96% - 24h 55 39 04 1:10 (Ambient T) 99% - 24h 76 54 04 1:10 50 99% - 2h 58 48 06 Excess NH3 (Ambient T) 99% - 72h / 43 3033166 14 We get and a production of amino acids from a bio-sourced source, this with production conditions easy to implement and control. In addition, since the amino acid conversion rates are lower than the levels of consumption of cl-brominated acid, it results from the synthesis of at least one co-product defined as iminodiacides and / or nitrilotriacids. By way of non-exhaustive example, for the synthesis of glycine, the coproducts are, inter alia, iminodiacetic acid and nitrilotriacetic acid and for the synthesis of alanine, the co-products are, inter alia α, α'-iminodipropionic acid and α, α ', α-nitrilotripropionic acid.
    权利要求:
    Claims (10)
    [0001]
    1. A process for producing amino acids from volatile fatty acid (VFA) molecules, called precursors, produced by anaerobic fermentation from fermentable biomass, characterized in that it comprises at least the following steps: a) extracting the volatile fatty acid (VFA) molecules, without interruption of the fermentation, by an extraction means chosen from means which are, at least, insoluble in the fermentation medium; b) collecting, in outside the fermentation reactor, the volatile fatty acid (VFA) molecules once extracted, 15 - c) synthesize, by halogenation, from a type of volatile fatty acid (VFA) selected from the volatile fatty acids collected in step b) and defined according to the desired type of amino acid, a given α-halogenated acid, - d) synthesize from this α-halogen acid a defined amino acid.
    [0002]
    2. Method according to claim 1, characterized in that, in step c), the halogenated compound used is bromine.
    [0003]
    3. A process according to claim 1, characterized in that, in step c), the halogenated compound used is different from the dibrome.
    [0004]
    4. A process according to claim 1 or 2, characterized in that in step c), acetic anhydride is used in a molar percentage relative to the volatile acid close to 12%.
    [0005]
    5. - Process according to claim 1 or 2, characterized in that in step c), an anhydride corresponding to the volatile fatty acid (AGV) to be halogenated.
    [0006]
    6. A process according to one of claims 2, 4, 5, characterized in that in step c), the temperature at which the bromination reaction is carried out is 20 ° C to 40 ° C below the temperature boiling volatile fatty acid. 3033166 2
    [0007]
    7. A process according to one of the preceding claims, characterized in that, in step d), the synthesis is carried out by reaction with ammonia in excess relative to the stoichiometry of the reaction.
    [0008]
    8. A process according to one of claims 1 to 6, characterized in that, in step d), the synthesis is carried out by reaction with an amine.
    [0009]
    9. A process according to claim 7 or 8, characterized in that, in step d), the temperature is between 20 ° C and 50 ° C.
    [0010]
    10. - Method according to one of the preceding claims, characterized in that during step d), is synthesized at least one co-product defined as an iminodiacide and / or a nitrilotriacide.
    类似技术:
    公开号 | 公开日 | 专利标题
    EP3262024B1|2019-04-03|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass
    CA2977438C|2021-03-02|Process for producing polyhydroxyalkanoates from precursors obtained by anaerobic fermentation from fermentable biomass
    CA2991003C|2021-03-09|Method for extracting carboxylic acids produced by anaerobic fermentation from fermentable biomass
    FR2463773A1|1981-02-27|COMPOUND HAVING ACARICIDAL AND ANTHELMINTIC ACTIVITIES OBTAINED BY CULTIVATION OF A MICROORGANISM OF THE GENUS STREPTOMYCES
    EP3172331A1|2017-05-31|Method for producing organic molecules from fermentable biomass
    Hêdji et al.2014|Valorisation de Azolla spp, Moringa oleifera, son de riz, et de co-produits de volaille et de poisson en alimentation animale: synthèse bibliographique
    EP0277482A1|1988-08-10|Method for rearing plancton and its use
    EP3171956B1|2020-04-29|Method for extracting molecules produced by anaerobic fermentation from fermentable biomass
    FR2652587A1|1991-04-05|Process for the synthesis of cis-3-hexen-1-ol from an unsaturated fatty acid
    FR2559646A1|1985-08-23|PROCESS FOR REDUCING THE LIGNIN RATE IN PLANTS AND NEW COMPOSITIONS FOR ITS IMPLEMENTATION
    FR2735125A1|1996-12-13|Prodn. of cis-3-hexen-1-ol from unsatd. fatty acids
    FR2768735A1|1999-03-26|Treatment of effluent containing a nitro substituted heterocycle or aromatic compound, to form the corresponding amino compound
    FR3101357A1|2021-04-02|PROCESS FOR PRODUCING 1,2,4-BUTANETRIOL FROM A PLANT
    CA3086382A1|2019-06-27|Stimulation of the nitrification of a soil with compounds comprising a plant extract
    BE861934A|1978-06-16|FERMENTATION PROCESS WITH MIXED THERMOPHILIC CULTURES
    同族专利:
    公开号 | 公开日
    FR3033166B1|2017-03-10|
    US20160251305A1|2016-09-01|
    PT3262024T|2019-07-12|
    SI3262024T1|2019-05-31|
    WO2016135397A1|2016-09-01|
    HRP20191172T1|2019-10-04|
    CN107207412B|2020-05-29|
    CN107207412A|2017-09-26|
    AU2016225311A1|2017-08-17|
    DK3262024T3|2019-05-27|
    US9701619B2|2017-07-11|
    LT3262024T|2019-05-10|
    TR201909274T4|2019-07-22|
    RU2680835C1|2019-02-28|
    PL3262024T3|2019-09-30|
    ES2731077T3|2019-11-13|
    HUE045211T2|2019-12-30|
    EP3262024B1|2019-04-03|
    CA2977441A1|2016-09-01|
    CA2977441C|2021-02-02|
    AU2016225311B2|2019-07-04|
    EP3262024A1|2018-01-03|
    BR112017016975A2|2018-04-03|
    BR112017016975B1|2021-07-06|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3642887A|1966-12-19|1972-02-15|Ethyl Corp|Preparation of amino-substituted carboxylic acids|
    US4377638A|1981-06-29|1983-03-22|University Patents, Inc.|Microbiological production of lower aliphatic carboxylic acids|
    EP0295550A1|1987-06-13|1988-12-21|BASF Aktiengesellschaft|Process for the preparation of D- or L-alanine with high enantiomeric purity|
    CN102030669B|2009-09-25|2014-07-23|李其奎|Production method for glycine|
    US4148811A|1977-07-12|1979-04-10|The Procter & Gamble Company|Halogenation process|
    DE2810975A1|1978-03-14|1979-09-27|Hoechst Ag|glycolic acid prodn. by hydrolysis of mono:chloro-acetic acid - in aq. soln. avoids pollution and contamination with salt|
    FR2536388B1|1982-11-22|1985-03-08|Rhone Poulenc Spec Chim|
    AT195145T|1991-12-23|2000-08-15|Genzyme Ltd|SYNTHESIS OF HOMOCHIRAL 2-HYDROXYSIC ACIDS|
    RU2080388C1|1994-09-05|1997-05-27|Институт микробиологии РАН|Method of microbiological synthesis of acetic acid|
    US7141400B2|2002-01-16|2006-11-28|University Of Hawaii|Production of biodegradable thermoplastic materials from organic wastes|
    WO2013022998A2|2011-08-09|2013-02-14|Cornell University|Production of carboxylates and methane from biomass waste|
    EP2749650B1|2012-12-27|2019-03-06|Veolia Water Solutions & Technologies Support|Method for producing polyhydroxyalkanoates by microorganisms|
    FR3004727B1|2013-04-19|2015-12-18|Bio Think|PROCESS FOR PRODUCING HYDROCARBONS|
    FR3033166B1|2015-02-27|2017-03-10|Afyren|PROCESS FOR THE PRODUCTION OF AMINO ACIDS FROM PRECURSORS OBTAINED BY ANAEROBIC FERMENTATION FROM FERMENTABLE BIOMASS|
    FR3033168B1|2015-02-27|2017-03-10|Afyren|PROCESS FOR THE PRODUCTION OF POLYHYDROXYALKANOATES FROM PRECURSORS OBTAINED BY ANAEROBIC FERMENTATION FROM FERMENTABLE BIOMASS|FR3033166B1|2015-02-27|2017-03-10|Afyren|PROCESS FOR THE PRODUCTION OF AMINO ACIDS FROM PRECURSORS OBTAINED BY ANAEROBIC FERMENTATION FROM FERMENTABLE BIOMASS|
    FR3033168B1|2015-02-27|2017-03-10|Afyren|PROCESS FOR THE PRODUCTION OF POLYHYDROXYALKANOATES FROM PRECURSORS OBTAINED BY ANAEROBIC FERMENTATION FROM FERMENTABLE BIOMASS|
    FR3074174B1|2017-11-30|2020-02-07|Afyren|PROCESS FOR THE VALORIZATION OF COPRODUCED POTASSIUM SALTS FROM FERMENTATION PROCESSES|
    FR3075222A1|2017-12-19|2019-06-21|Afyren|VINASSE AS A MEDIUM OF FERMENTATION|
    FR3087449A1|2018-10-19|2020-04-24|Afyren|PROCESS FOR THE PREPARATION OF ORGANIC MOLECULES BY ANAEROBIC FERMENTATION|
    CN110803989A|2019-11-26|2020-02-18|江西盛伟科技股份有限公司|Synthesis method of ethyl 3-hydroxycaproate|
    法律状态:
    2015-12-14| PLFP| Fee payment|Year of fee payment: 2 |
    2016-09-02| PLSC| Search report ready|Effective date: 20160902 |
    2017-02-09| PLFP| Fee payment|Year of fee payment: 3 |
    2017-11-21| PLFP| Fee payment|Year of fee payment: 4 |
    2019-01-21| PLFP| Fee payment|Year of fee payment: 5 |
    2020-11-06| ST| Notification of lapse|Effective date: 20201006 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1551673A|FR3033166B1|2015-02-27|2015-02-27|PROCESS FOR THE PRODUCTION OF AMINO ACIDS FROM PRECURSORS OBTAINED BY ANAEROBIC FERMENTATION FROM FERMENTABLE BIOMASS|FR1551673A| FR3033166B1|2015-02-27|2015-02-27|PROCESS FOR THE PRODUCTION OF AMINO ACIDS FROM PRECURSORS OBTAINED BY ANAEROBIC FERMENTATION FROM FERMENTABLE BIOMASS|
    PT16709991T| PT3262024T|2015-02-27|2016-02-17|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    RU2017128409A| RU2680835C1|2015-02-27|2016-02-17|Process for production of amino acids from precursors obtained by means of anaerobic fermentation from fermentable biomass|
    SI201630239T| SI3262024T1|2015-02-27|2016-02-17|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    TR2019/09274T| TR201909274T4|2015-02-27|2016-02-17|Process for the production of amino acids from precursors obtained by anaerobic fermentation from fermentable biomass.|
    LTEP16709991.0T| LT3262024T|2015-02-27|2016-02-17|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    AU2016225311A| AU2016225311B2|2015-02-27|2016-02-17|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    PL16709991T| PL3262024T3|2015-02-27|2016-02-17|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    EP16709991.0A| EP3262024B1|2015-02-27|2016-02-17|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    ES16709991T| ES2731077T3|2015-02-27|2016-02-17|Amino acid production process from precursors obtained by anaerobic fermentation of fermentable biomass|
    HUE16709991A| HUE045211T2|2015-02-27|2016-02-17|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    BR112017016975-4A| BR112017016975B1|2015-02-27|2016-02-17|PROCESS TO PRODUCE AMINO ACIDS FROM PRECURSORS OBTAINED BY ANAEROBIC FERMENTATION OF FERMENTABLE BIOMASS|
    DK16709991.0T| DK3262024T3|2015-02-27|2016-02-17|PROCEDURE FOR MANUFACTURE OF AMINO ACIDS FROM THE OUTPUTS OBTAINED AT THE ACCESSION OF FERMENTATION FROM THE FERMENTATION BIOMASE|
    PCT/FR2016/050364| WO2016135397A1|2015-02-27|2016-02-17|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    CN201680008682.8A| CN107207412B|2015-02-27|2016-02-17|Method for producing amino acids from precursors obtained by anaerobic fermentation of fermentable biomass|
    CA2977441A| CA2977441C|2015-02-27|2016-02-17|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    US15/053,854| US9701619B2|2015-02-27|2016-02-25|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    HRP20191172TT| HRP20191172T1|2015-02-27|2019-06-28|Process for producing amino acids from precursors obtained by anaerobic fermentation from fermentable biomass|
    [返回顶部]