• 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:
    New procedure of depolymerization of lignin. The invention describes a new process for the depolymerization of lignin comprising the steps of: providing a black liquor from the treatment of the delignification of biomass; concentrate said black liquor; submit the concentrated black liquor to hydrothermal treatment; adding an acid to the reaction mixture obtained in the previous step; separation of the precipitate from the liquid phase resulting in the previous step, and extraction from the liquid phase recovered from the aromatic depolymerization products of lignin such as phenol, cresols, catechol and its derivatives (3-methylcatechol, 4-methylcatechol and 4-ethylcatechol). (Machine-translation by Google Translate, not legally binding)
    公开号:ES2539651A1
    申请号:ES201331705
    申请日:2013-11-22
    公开日:2015-07-02
    发明作者:Xabier ERDOCIA IRIARTE；Mª De Los Ángeles CORCUERA MAESO；Jalel LABIDI BOUCHRIKA
    申请人:Euskal Herriko Unibertsitatea；
    IPC主号:
    专利说明:

    DESCRIPTION

    New procedure for depolymerization of lignin.

    Field of the invention 5
    The present invention relates to a new lignin depolymerization process that starts from a black liquor that contains it from biomass delignification.

    Background of the invention
    The methods of degradation of lignin in the state of the art are diverse and although they employ a wide range of methods and operating conditions, all have similar disadvantages. There are numerous processes that allow lignin degradation but all have some problems that limit their use on an industrial scale. Among other things, due to inadequate adaptation to industrial needs and / or incompatibility with increasingly stringent environmental requirements.
    Among these procedures for depolymerization of lignin, the following can be mentioned, for example: the procedure described in US 5,807,952 based on pyrolysis; a solvothermal procedure described in US 5,959,167; processes using transition metal-based catalysts (US 2,220,624), a process in the presence of molten salts of a general formula M (OH) hydroxide, not a mixture of alkaline or alkaline earth hydroxides (US 20130066116) or a hydrothermal process in which the lignin is subjected in a basic medium to pressure and temperature. twenty
    All these current lignin depolymerization processes, which allow their revaluation and the obtaining of phenolic products of high added value, however, have disadvantages, of which one is common to all; they start from the precipitated solid lignin. The solid lignin is obtained from biomass in general, which is subjected to a paste stage, from which a black liquor (or black liquor) is obtained as a byproduct, to which is added an acid that causes lignin to precipitate. . The lignin precipitate is isolated, and the resulting precipitated solid lignin is subjected to a depolymerization process.
    For the precipitation of lignin it is necessary to carry out a series of process steps that extend the overall biomass treatment process to obtain aromatic compounds. In addition, the precipitation of lignin includes the use of additional elements, such as filters and reagents that obviously make the procedure as a whole more expensive and complicate it. 30
    In view of the above, there is still a need to provide a simpler, more efficient and economical process that is scalable at the industrial level, which provides aromatic compounds with high yields, overcoming at least part of the disadvantages of prior art procedures. current.
     35
    Description of the Figures
    Figure 1: Schematic representation of an embodiment of the process for obtaining a black liquor with depolymerized lignin (9) from biomass (1) (for example: almond shell)
    Figure 2: Schematic representation of the treatment of depolymerized lignin (9) to obtain the phenolic products (18). 40
    Figure 3: represents the chromatogram obtained by gas chromatography-mass spectrometry (GC / MS) analysis of oil obtained in Example 1 with NaOH.
    Figure 4: represents the chromatogram obtained by gas chromatography-mass spectrometry (GC / MS) analysis of oil obtained in Example 1 with KOH.
     Four. Five
    Description of the invention
    In a first aspect the invention relates to a process for depolymerization of lignin comprising the following steps:
    (i) Provide a black liquor from the treatment of biomass delignification;
    (ii) Concentrate said black liquor; fifty
    (iii) Subject the concentrated black liquor to hydrothermal treatment;
    (iv) Add an acid to the reaction mixture obtained in the previous step;
    (v) Separation of the precipitate from the liquid phase resulting in the previous stage; Y
    (vi) Extraction from the liquid phase recovered from the depolymerization products of lignin.
     55
    The type of biomass that can be subjected to this process, hereinafter the process of the invention, is lignocellulosic biomass containing, among other polymers, lignin.
    Lignin is a phenolic macromolecule whose structure is not yet perfectly elucidated. It is present among the cell walls of numerous plants, specifically wood, to which they confer rigidity. The biomass usable in the present invention can be derived from wood, green waste in general, or straw for example. In a particular embodiment it comes from the nutshell, such as the almond shell.

    Lignin is available in black liquors that result as by-products of biomass delignification treatments, for example, that which takes place during the production of paper to obtain cellulose (paper pulp) that generates these by-products also called black liquors or from the production of 65 second generation bioethanol.
    Biomass delignification is a process known in the state of the art that consists in performing an alkaline treatment of the biomass, preferably using sodium hydroxide or potassium hydroxide in a typical concentration of 15% by weight based on the weight of solution used in delignification (see Figure 1, where (1) represents the biomass, (2) the delignification stage). In the example of the present invention, for example, a solid to liquid ratio of 1:10 by weight is used, and it is carried out in an autoclave at 5 121 ° C.

    The product that is produced from the delignification is generally filtered first with a metal mesh, and a cloth filter then to separate any solid residue from the liquid phase where the lignin (black liquor) is dissolved (see Figure 1, (3) where this filtering stage is schematically represented, (5) the delignified paste, and (4) the resulting black liquor).

    In step (ii) the black liquor (4) is concentrated by any conventional technique (Figure 1, (6)). In a particular embodiment it is done by evaporation either at atmospheric pressure or by applying vacuum and temperature, for example using a rotary evaporator with a water bath. Typically the concentration is made at 15 60 ° C and vacuum of 0.02MPa.

    The concentration of the black liquor (4) is carried out until the initial volume of the liquor is reduced (see (7) in Figure 1, which represents the concentrated liquor). The volume reduction can be variable. Preferably it should be carried out, preventing lignin from precipitating. In a preferred embodiment the concentration of the black liquor is carried out until the initial volume is reduced by half. In this sense, the inventors have observed that in this way a very good depolymerization performance is obtained and, on the other, excessive energy expenditure is avoided in further concentrating the black liquor, which entails only a small additional improvement in performance.
     25
    The hydrothermal treatment to which the black liquor is subjected is a conventional treatment well known to a person skilled in the art. During it the depolymerization of lignin takes place. This step (iii) is represented in Figure 1, by means of the element (8) after which (9) is obtained: a reaction mixture. This treatment is generally carried out in the presence of a base, at a temperature between 250-500 ° C, and high pressure, generally between 5-30 MPa. In a preferred embodiment according to the present invention, the hydrothermal treatment is carried out at 300 ° C, 9 MPa and under continuous stirring. During this treatment the lignin is depolymerized, and a reaction mixture containing the depolymerized lignin is obtained from which it is possible to separate the products obtained. Depolymerization times are usually between 30 minutes and 2 hours depending for example on the depolymerization conditions. 35

    For the separation of the obtained products found in the reaction mixture (Figure 1, (9), and Figure 2 (9)) resulting from step (iii) an acid such as hydrochloric acid, sulfuric acid or a mixture of both to the reaction mixture (Figure 2, (10)). It is added in an amount that allows to raise a pH value of 1. At this pH value the inventors have observed that the total precipitation of all the residue that is formed in the depolymerization reaction is achieved. The pH can be adjusted to a value greater than 1 but in that case the subsequent liquid-liquid extraction is difficult, since it has been observed that a precipitate appears.

    Next, the step of separating the precipitate from the liquid phase is carried out, for example by filtration, although any other conventional separation means can be used. In a particular embodiment, filtration is done using a filter with a pore diameter of 7-12 µm. In Figure 2, (11) represents the acidified reaction mixture, (3) the filtering stage, (12) the precipitate and (13) the liquid phase.

    The liquid phase (13) separated in the previous stage is subjected to an extraction stage of the depolymerization products (14). The extraction gives rise to an aqueous phase (16) and an organic phase (15). The extraction is preferably done with ethyl acetate, since it is most suitable for dissolving the monomers formed, although other organic solvents such as diethyl ether, vinyl acetate or n-butyl acetate can also be used.

    The process of the invention further comprises recovering the depolymerization products. 55

    Recovery is done by the steps of: (a) evaporating the solvent from the organic liquid phase resulting from the extraction; (b) resuspend the organic oil resulting from step (a) in an organic solvent; and (c) subject the resulting suspension to chromatography separation.
     60
    Evaporation (schematized in (17), Figure 2) is carried out, for example, in a rotary evaporator at a typical temperature of 50 ° C and under vacuum (for example at 0.02 MPa) until the complete elimination of the solvent used in the liquid-liquid extraction . The resulting isolated oil (without solvent) (18) is weighed to know the yield and resuspended (dissolved) in the same solvent used in the extraction, preferably in ethyl acetate, [but of high efficiency Liquid Chromatography grade (HPLC)]. The suspension is then subjected to chromatography, for example gas chromatography, to separate the present compounds.

    These compounds are generally aromatic and are essentially of the phenol family. Among the compounds that can be obtained, in the form of a mixture, are phenol, cresols, catechol and their derivatives (3-methylcatechol, 4-methylcatechol and 4-ethylcatechol).
     5
    Figure 1 schematically represents the steps of the process of the invention (i) to (iii). In (1) the biomass that in (2) is subjected to alkaline delignification treatment described above. The resulting product is filtered in (3) giving rise to delignified paste (5), and a black liquor (4). The black liquor is concentrated according to step (ii) of the process of the invention in (6), and then the concentrated liquor (7) is subjected to depolymerization (step (iii) of the process of the invention), represented in (8 ), to give the reaction mixture represented in (9).

    Figure 2 represents the continuation of the process where the reaction mixture (9) is acidified according to step (iv) of the process of the invention in (10), to yield an acidified mixture (11) that is subjected to a filtering stage (3), to give rise to a solid precipitate (12) and a liquid phase (13) separated according to step 15 (v) of the process of the invention. The liquid-liquid extraction, step (vi) of the process of the invention, is represented as (14) gives rise to an aqueous phase (16) and an organic phase (15). From this phase, for example, by evaporation of the solvent in (17) an oil is obtained with the depolymerization products (18).

    The process of the invention is more economical, and more interesting from the environmental point of view 20 as mentioned above. It allows the output of an industrial by-product, black bleach, and its revaluation by obtaining a mixture of organic compounds with high added value that can be used in numerous industries and applications.

    Examples 25

    Example 1

    50 grams of almond husk were crushed in a Retsch 2000 hammer mill to produce 4–6 mm chips free of small stones, dust and dirt. 30
    The 50 grams of ground almond husk were then placed in a 1 liter vessel made of borosilicate glass 3.3 according to DIN EN ISO 4796-1 together with 500 grams of a 15% KOH solution by weight. The autoclave delignification process was performed for 90 min, at a temperature of 121 ° C and a pressure of 0.2 MPa.
    After the delignification process the reaction mixture was filtered first with a metal mesh (size 35 of the 2 mm hole) and then with a cloth filter to separate the solid residue from the black liquor where the lignin was dissolved. After that, the black liquor was concentrated to reduce its volume in half, using a rotary evaporator, at 60 ° C in a vacuum atmosphere (0.02 MPa). Once the liquor was concentrated, the depolymerization process was performed.
    The depolymerization process was carried out as follows. 30 grams of the concentrated liquor were introduced into a 40-pressure steel reactor. The conditions were: 300 ° C, 80 min, 9 MPa and continuous stirring. Once the process of depolymerization of the lignin contained in the black liquor was carried out, the products were separated.

    To this end, the reaction mixture obtained after the depolymerization process with HCl was acidified to reach a pH 1. Upon making this acid addition, a precipitate (residue) was produced which was filtered off with a filter paper of a diameter of pore of 7-12 µm. To the liquid phase, where the lignin depolymerization products were found, a liquid-liquid extraction with ethyl acetate was performed. This extraction process was carried out until when adding ethyl acetate no change in color was observed in the solvent, that is, no more products were extracted from the aqueous phase. After said extraction process, the 50 phenolic products derived from lignin were in the organic phase. This organic phase was subjected to an evaporation process to remove the solvent and isolate the depolymerization products of lignin. Evaporation was carried out in a rotary evaporator at 50 ° C and in a vacuum atmosphere (0.02 MPa).

    Once all the solvent (ethyl acetate) was removed, evaporation was completed and 0.337 grams of an oil containing the lignin depolymerization compounds were obtained.

    The concrete results for the case described and for the same case using 15% NaOH by weight instead of KOH are shown below.
    The calculations of the oil obtained have been made with respect to three parameters: lignin contained in the black liquor, 60 organic matter contained in the black liquor and with respect to the entire black liquor.



     65

    Table 1. Oil yield with lignin depolymerization products (% by weight).

     Oil / lignin Oil / organic matter Oil / black liquor
     NaOH  54,5052 12,6458 0.8612
     Koh  71.0224 20.3289 1.1222

    Products generated after direct depolymerization of lignin have been identified by gas chromatography / mass spectroscopy (GC / MS). The most representative compounds that have also been quantified are shown in the following table:

    Table 2. Weight percentage with respect to the oil of the monomer units of phenolic compounds obtained
     10
     Compound (%)  NaOH KOH
     Phenol  0.31 0.64
     Cresols  0.38 0.40
     Guaiacol  0.03 0.19
     Catechol  1.51 0.99
     4-methylcatecol  0.20 0.23
     Syringol     0.27
     4-hydroxybenzaldehyde     0.05
     Vanillin     0.20
     Acetovanillone     0.07
     4-hydroxy-3-methoxy-phenylacetone     0.02
     4-ethylcatecol  0.23

    The chromatogram obtained by GC / MS from the analysis of the oil produced after depolymerization of lignin with NaOH is shown in Figure 3 and in Figure 4 with KOH.

     fifteen
    The invention is not limited to the specific embodiments that have been described but also covers, for example, the variants that can be made by the average person skilled in the art within what follows from the claims.
    权利要求:
    Claims (10)
    [1]

    1.- Procedure for depolymerization of lignin comprising the following steps:
    (i) Provide a black liquor from the treatment of biomass delignification; 5
    (ii) Concentrate said black liquor;
    (iii) Subject the concentrated black liquor to hydrothermal treatment;
    (iv) Add an acid to the reaction mixture obtained in the previous step;
    (v) Separation of the precipitate from the liquid phase resulting in the previous stage; Y
    (vi) Extraction from the recovered liquid phase of the depolymerization products of lignin. 10

    [2]
    2. The method according to claim 1 wherein the concentration of the black liquor is carried out until the initial volume of the liquor is reduced by half.

    [3]
    3. The method according to claim 1 or 2, wherein the concentration is made at 60 ° C and a vacuum of 0.02MPa. fifteen

    [4]
    4. Method according to any one of claims 1 to 3, wherein the hydrothermal treatment is carried out at 300 ° C, 9 MPa and under continuous stirring.

    [5]
    5. Process according to any one of claims 1 to 4, wherein the acid added in step 20 (iv) is hydrochloric acid, sulfuric acid or a mixture.

    [6]
    6. The method according to claim 5 wherein the amount of acid added is that necessary to adjust the pH to 1.
     25
    [7]
    7. Method according to any one of claims 1 to 6, wherein the separation of the precipitate from the liquid phase is done by filtration.

    [8]
    8. Process according to any one of claims 1 to 7, wherein the extraction of depolymerization products is done with ethyl acetate.

    [9]
    9. Method according to any one of claims 1 to 8, further comprising recovering the depolymerization products.

    [10]
    10. Method according to claim 9, wherein the recovery comprises carrying out the following steps: (a) evaporating from the solvent of the organic liquid phase resulting from the extraction; (b) resuspend the organic oil resulting from step (a) in an organic solvent; and (c) subject the suspension to separation by chromatography.
     40
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    引用文献:
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    US2220624A|1939-07-15|1940-11-05|Henry A Wallace|Process for the hydrogenation of lignin and waste pulp liquors and the products thereof|
    WO1996009350A1|1994-09-19|1996-03-28|Midwest Research Institute|Process for producing phenolic compounds from lignins|
    US5959167A|1997-08-25|1999-09-28|The University Of Utah Research Foundation|Process for conversion of lignin to reformulated hydrocarbon gasoline|
    FR2957599B1|2010-03-18|2014-01-10|Commissariat Energie Atomique|PROCESS FOR THE DEPOLYMERIZATION OF LIGNOCELLULOSIC BIOMASS|
    US8940129B2|2010-12-30|2015-01-27|Uop Llc|Process for reducing one or more insoluble solids in a black liquor|EP3502118A1|2017-12-22|2019-06-26|Universidad De Valladolid|Ultra-fast lignin depolymerization process|
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