EP2596110A2

EP2596110A2 - Method for producing sugars from lignocellulosic biomass pretreated with a mixture of hydrated inorganic salts and metal salts

Info

Publication number: EP2596110A2
Application number: EP11749870.9A
Authority: EP
Inventors: Christophe Vallee; Didier Morvan; Emmanuel Pellier; Hélène Olivier-Bourbigou
Original assignee: IFP Energies Nouvelles IFPEN
Current assignee: IFP Energies Nouvelles IFPEN
Priority date: 2010-07-23
Filing date: 2011-07-19
Publication date: 2013-05-29
Also published as: US20130210089A1; WO2012010750A2; FR2963008B1; WO2012010750A3; CA2801831A1; FR2963008A1; BR112013001757A2

Abstract

The present invention relates to a method for converting lignocellulosic biomass into sugars, comprising at least three steps. The first step is a step of cooking the lignocellulosic biomass in the presence of at least one hydrated inorganic salt as a mixture with at least one other metal salt. The second step is a step of separating at least one solid fraction having undergone the cooking step, and the third step is a step of enzymatic hydrolysis of said solid fraction so as to convert the polysaccharides into monosaccharides. The resulting sugars are then able to be fermented into alcohols.

Description

PROCESS FOR THE PRODUCTION OF SUGARS FROM LIGNOCELLULOSIC BIOMASS PRE-TREATED WITH A MIXTURE OF HYDRATED INORGANIC SALTS AND METAL SALTS

Field of the invention

The present invention is part of a process for producing so-called "second generation" alcohol from lignocellulosic biomass.

Prior art

Faced with the increase in pollution and global warming, many studies are currently being conducted to use and optimize renewable bio-resources, such as lignocellulosic biomass.

Lignocellulosic biomass is composed of three main polymers: cellulose (35 to 50%), hemicellulose (23 to 32%) which is a polysaccharide essentially consisting of pentoses and hexoses and lignin (15 to 25%) which is a polymer of complex structure and high molecular weight, from the copolymerization of phenylpropenoic alcohols. These different molecules are responsible for the intrinsic properties of the plant wall and are organized in a complex entanglement.

Cellulose, the majority of this biomass, is thus the most abundant polymer on Earth and the one with the greatest potential for forming materials and biofuels. However, the potential of cellulose and its derivatives has not, for the moment, been fully exploited, mainly because of the difficulty of extracting cellulose. Indeed, this step is made difficult by the very structure of the plants. The identified technological barriers related to the transformation of cellulose include its accessibility, its crystallinity, its degree of polymerization, the presence of hemicellulose and lignin. It is therefore essential to develop new pretreatment methods for lignocellulosic biomass for easier access to cellulose and to allow its transformation.

Biofuel production is an application requiring pretreatment of biomass. Indeed, the second generation of biofuel uses as load vegetable or agricultural waste, such as wood, wheat straw, or plantations with high growth potential such as miscanthus. This raw material is perceived as an alternative, sustainable solution with little or no impact on the environment and its low cost and high availability make it a solid candidate for biofuel production. The principle of the process of converting lignocellulosic biomass into biofuel uses a step of enzymatic hydrolysis of the cellulose contained in the plant material to produce glucose. This glucose is then fermented into ethanol, the biofuel.

However, the cellulose contained in the lignocellulosic biomass is particularly refractory to enzymatic hydrolysis, especially since the cellulose is not directly accessible to the enzymes. To overcome this refractory nature, a pretreatment step upstream of the enzymatic hydrolysis is necessary. There are many methods of treating materials rich in cellulose, chemical, enzymatic, microbiological to improve the subsequent stage of enzymatic hydrolysis.

These methods are for example: steam explosion, organosolv process, dilute or concentrated acid hydrolysis or AFEX ("Ammonia Fiber Explosion") process. These techniques can still be improved and suffer in particular from costs that are still too high, problems of corrosion, low yields and difficulties of extrapolation at the industrial level (F. Talebnia, D. Karakashev, I. Angelidaki Biores, Technol 2010, 101 , 4744-4753).

In recent years, a new type of pretreatment consisting of using ionic liquids has been studied. Ionic liquids are salts consisting solely of liquid ions at temperatures of less than or equal to 100 ° C and provide highly polar media. They are thus used as solvents or as reaction media for treating cellulose or lignocellulosic materials (WO 05/17252; WO 05/23873). But like other pretreatments, ionic liquids have significant cost issues related to the price of ionic liquids and their often difficult recyclability.

It appears necessary to limit the pretreatment costs, in particular by using readily available and inexpensive reagents. This is the context of the present invention.

Summary of the invention

The present invention relates to a process for converting lignocellulosic biomass to sugars comprising at least three steps. The first step is a step of cooking the lignocellulosic biomass in a medium comprising at least one inorganic salt hydrated mixture with at least one other metal salt. The second step is a step of separating at least one solid fraction having undergone the firing step and the third step is a step of enzymatic hydrolysis of said solid fraction to convert the polysaccharides to monosaccharides. The sugars thus obtained are then fermentable in alcohols.

Description of the Figures

Figure 1 shows the kinetics of the enzymatic hydrolysis of wheat straw according to the method of the present invention, implementing a step of baking the biomass in the presence of LiCI.H ₂ 0 (98%) / ZnCl _2. 2.5 H ₂ 0 (2%) at 140 ° C.

FIG. 2 represents the kinetics of the enzymatic hydrolysis of wheat straw according to the method of the present invention, implementing a step of cooking the biomass in the presence of LiCl ₂ H ₂ O (10%) / ZnCl ₂ . 2.5 H ₂ O (90%) at 80 ° C.

FIG. 3 represents the kinetics of the enzymatic hydrolysis of the wheat straw according to the process of the present invention, implementing a step of cooking the biomass in the presence of NaCl ₆ H ₂ O (10%) / ZnCl ₂ . 2.5 H ₂ O (90%) at 80 ° C.

FIG. 4 represents the kinetics of the enzymatic hydrolysis of the wheat straw according to the process of the present invention, implementing a step of cooking the biomass in the presence of NaCl ₆ H ₂ O (10%) / ZnCl ₂ . 2.5 H ₂ O (90%) recycled at 80 ° C. FIG. 5 represents the kinetics of the enzymatic hydrolysis of wheat straw according to the method of the present invention, implementing a step of cooking the biomass in the presence of LiCl ₂ H ₂ O (10%) / FeCl ₃ . 6 H ₂ O (90%) at 60 ° C.

FIG. 6 represents the kinetics of the enzymatic hydrolysis of the wheat straw according to the process of the present invention, implementing a step of cooking the biomass in the presence of LiCl ₂ H ₂ O (20%) / FeCl ₃ . 6 H ₂ O (80%) at 60 ° C.

Figure 7 shows the kinetics of enzymatic hydrolysis of a native wheat straw, having not undergone any pretreatment. Figure 8 shows the kinetics of the enzymatic hydrolysis of wheat straw when pretreated by steam explosion prior to enzymatic hydrolysis.

Detailed description of the invention

The process for converting lignocellulosic biomass into monosaccharides according to the present invention comprises at least:

a) a step of cooking the biomass in the presence or absence of an organic solvent, in a medium comprising at least one hydrated inorganic salt of formula (1):

ΜΧ _π .ηΉ ₂ 0

wherein X is an anion and M is a metal selected from groups 1 and 2 of the Periodic Table, n is an integer of 1 or 2 and n is between 0.5 and 6

in admixture with at least one other metal salt, hydrated or not, of general formula (2):

M'Y _m .m'H ₂ 0

wherein Y is an anion, identical to or different from X, and M 'a metal selected from Groups 3 to 13 of the Periodic Table, m is an integer from 1 to 6 and m' is from 0 to 6.

b) a step of separating a solid fraction having undergone the firing step;

c) a step of enzymatic hydrolysis of said solid fraction.

This process transforms lignocellulosic biomass into fermentable sugars with excellent yields. It also has the advantage of using inexpensive reagents, widely available and recyclable, thus obtaining a low pretreatment cost, especially compared to a process using ionic liquids. This technology is also simple to implement and makes it easy to envisage an extrapolation at the industrial level.

Thanks to the process according to the present invention, the transformation of the lignocellulosic biomass into fermentable sugars is carried out with an excellent yield. The firing step carried out according to the process of the present invention makes it possible to reduce the duration of enzymatic hydrolysis with respect to the processes described in the prior art. The method according to the present invention makes it possible to achieve high glucose yields with short cooking times, allowing a significant gain in terms of productivity of the products. equipment since it becomes possible to use smaller amounts of enzymes and / or to reduce the size of the enzymatic hydrolysis tanks.

The process according to the invention makes it possible to carry out the step of cooking the lignocellulosic biomass at moderate temperatures, in the absence of pressure, which constitutes a significant gain in terms of energy costs.

Preferably, the medium in which the firing step is carried out consists of one or more hydrated inorganic salts of formula (1) mixed with at least one other metal salt, hydrated or not, of formula (2).

This firing step is carried out in the presence or absence of an organic solvent. The lignocellulosic biomass, or lignocellulosic materials used in the process according to the invention is obtained from wood (hardwood and softwood), raw or treated, by agricultural products such as straw, plant fibers, cultures. forestry, residues of alcoholic, sugar and cereal plants, residues of the paper industry, or products of transformation of cellulosic or lignocellulosic materials. The lignocellulosic materials can also be biopolymers and are preferably rich in cellulose.

Preferentially the lignocellulosic biomass used is wood, wheat straw, wood pulp, rice straw or corn stalks.

According to the process of the present invention, the different types of lignocellulosic biomass can be used alone or in mixture.

In the firing step, the lignocellulosic biomass is present in an amount of between 0.5% and 40% by weight of the total mass of the lignocellulosic biomass / hydrated inorganic salt / metal salt mixture, preferably in an amount of between 3% and 25% weight.

Preferably, the anion X is a halide anion chosen from Cl, F, Br and I, a perchlorate anion (ClO ₄ ), a thiocyanate anion (SCN), a nitrate anion (NO ₃ ) or an acetate anion (CH ₃ ). ₃ COO).

The metal M is preferably selected from lithium, magnesium, calcium, potassium or sodium. Preferably, in the formula MX _n .n'H ₂ 0 (1) of the hydrated inorganic salt, n 'is between 1 and 6.

According to the present invention, the hydrated inorganic salt having the formula (1) can be prepared in situ by the combination of a salt composed of a cation of groups 1 and 2 of the periodic table and a carbonate anion, hydrogen carbonate or hydroxide with an acid. The acid can be used pure or in aqueous solution.

Preferably, in the metal salt of formula (2), the anion Y is chosen from anions halides, nitrates, carboxylates, halocarboxylates, acetylacetonates, alkoxides, phenolates, optionally substituted, sulphates, alkyl sulphates, phosphates, alkyl phosphates, fluorosulphonates, alkylsulphonates, for example methylsulphonate, perfluoroalkylsulphonates, for example trifluoromethylsulphonate, bis (perfluoroalkylsulphonyl) amides, for example bis (trifluoromethylsulphonyl) amide of formula N (CF ₃ SO ₂ ) ₂ ^- , arenesulphonates, optionally substituted with halogen or haloalkyl groups; .

More preferably, the anion Y is selected from fluoride anions, chloride, bromide, acetate, and triflate.

Preferably the metal M 'is selected from iron, cobalt, nickel, copper, zinc, aluminum, indium or lanthanum.

Preferably, the metal salt of general formula (2) is chosen from FeBr ₃ , FeCl ₃ , FeCl ₃ .6H ₂ O, FeF ₃ , Fe (NO ₃ ) ₃ , CoCl ₂ , CoCl ₂ .6H ₂ O, Ni (CH ₃ COO) ₂ .4H ₂ O, NiBr ₂ , NiCl ₂ NiCl ₂ .6H ₂ O, Zn (CH ₃ COO) ₂ .2H ₂ O, ZnBr ₂ , ZnCl ₂ , ZnCl ₂ .2,5H ₂ O, AIBr ₃ , AICI ₃ , AICI ₃ .6H ₂ OLaCl ₃ , LaCI ₃ .6H ₂ O.

The molar fraction of the hydrated inorganic salt of formula (1) in the mixture of at least one hydrated inorganic salt of formula (1) and of at least one metal salt of formula (2) may be between 0.05 and 1 .

The step of cooking the biomass may be carried out in a medium consisting of a mixture of different hydrated inorganic salts corresponding to formula (1) and / or different metal salts corresponding to formula (2). By way of examples of mixtures of hydrated inorganic salts and of metal salts which can be used for the firing step according to the present invention, mention may be made of the following molar compositions:

-LiCl .H ₂ O (98%) / ZnCl ₂ .2.5H ₂ O (2%),

LiCl ₂ H ₂ O (10%) / ZnCl ₂ .2.5H ₂ O (90%),

-NaCl ₆ H ₂ O (10%) / ZnCl ₂ .2.5H ₂ O (90%),

LiCl ₃ COO ₃ H ₂ O (10%) / ZnCl ₂ .2.5H ₂ O (90%),

LiCl ₂ H ₂ O (20%) / ZnCl ₂ .2.5H ₂ O (80%),

-NaCl ₆ H ₂ O (20%) / ZnCl ₂ .2.5H ₂ O (80%),

LiCl ₂ H ₂ O (10%) / FeCl ₃ H ₆ O (90%),

-NaCI.6H ₂ 0 (10%) / FeCl ₃ .6 H ₂ O (90%),

LiCl ₃ COO ₃ H ₂ O (10%) / FeCl ₃ .6H ₂ O (90%),

LiCl ₂ H ₂ O (20%) / FeCl ₃ .6H ₂ O (80%),

-NaCl ₆ H ₂ O (20%) / FeCl ₃ H ₆ O (80%).

According to the method of the present invention, several successive firing steps can be carried out in a medium consisting of at least one hydrated inorganic salt of formula (1) mixed with at least one metal salt of formula (2).

Preferably, the firing temperature is preferably between -20 ° C and 250 ° C, preferably between 20 and 160 ° C. Very preferably, the cooking temperature does not exceed 100 ° C.

The duration of the cooking is between 0.5 minutes and 168 hours, preferably between 5 minutes and 4 hours and even more preferably between 20 minutes and 2 hours.

The step of cooking the lignocellulosic biomass according to the present invention can be carried out in the presence of an organic solvent. The organic solvent may be chosen from alcohols such as methanol, ethanol, n-propanol, isopropanol, n-butanol, isobutanol or tert-butanol, diols and polyols such as ethanediol. , propanediol or glycerol, amino alcohols such as ethanolamine, diethanolamine or triethanolamine, ketones such as acetone or methyl ethyl ketone, carboxylic acids such as formic acid or acetic acid, esters such as ethyl acetate or isopropyl acetate, dimethylformamide, dimethylacetamide, dimethylsulfoxide, acetonitrile, aromatic solvents such as benzene, toluene, xylenes, alkanes. According to another embodiment, the step of cooking the lignocellulosic biomass according to the present invention can be carried out in the absence of an organic solvent.

The second step b) of the process according to the invention consists in separating a solid fraction, which has undergone the firing step a) described above. This separation is generally carried out by adding at least one anti-solvent which causes the precipitation of the solid fraction.

The separation of this precipitated solid fraction and a liquid fraction containing the hydrated inorganic salt, the metal salt and the anti-solvent can be carried out by the usual solid-liquid separation techniques. For example, the separation of the solid fraction having undergone the cooking step can be carried out by filtration or by centrifugation.

The solid fraction may optionally be subjected to additional treatments before the enzymatic hydrolysis step. These additional treatments may in particular be intended to eliminate traces of hydrated inorganic salts and / or metal salts in the solid fraction having undergone the cooking step. These additional treatments may be, for example, washes, carried out with the anti-solvent, with water or with any other flow of the process.

The liquid obtained after washing contains the fluid used for the additional treatment and traces of hydrated inorganic salts and / or metal salts. This liquid can advantageously be recycled for use during the separation step, thus allowing a better recovery rate of salts and better purity of the solid fraction while limiting the consumption of anti-solvent or other washing fluid.

The solid fraction may optionally be dried or pressed to increase the percentage of dry matter contained in the solid.

The anti-solvent used is a solvent or a mixture of solvents chosen from water, alcohols such as methanol, ethanol, n-propanol, isopropanol, n-butanol, isobutanol or tert-butanol, diols and polyols such as ethanediol, propanediol or glycerol, amino alcohols such as ethanolamine, diethanolamine or triethanolamine, ketones such as acetone or methyl ethyl ketone, carboxylic acids such as formic acid or acetic acid, esters such as ethyl acetate or isopropyl acetate, dimethylformamide, dimethylacetamide, dimethylsulfoxide, acetonitrile.

Preferably, the anti-solvent is selected from water, methanol or ethanol.

Very preferably, the anti-solvent is water. The hydrated inorganic salt and the metal salt contained in the liquid fraction can be separated from the anti-solvent and recycled, for example to be used during the baking step. This separation can be carried out by any method known to those skilled in the art, such as, for example, evaporation, precipitation, extraction, passage over ion exchange resin, electrodialysis, chromatographic methods, solidification. hydrated inorganic salt and metal salt by lowering the temperature or adding a third body, reverse osmosis.

The liquid fraction containing the hydrated inorganic salt, mixed with the metal salt, and the anti-solvent may also contain products derived from biomass. For example, the liquid fraction may contain hemicellulose (or products derived from hemicellulose) and lignin.

Biomass products contained in the liquid fraction can be separated before or after separation of the hydrated inorganic salt in admixture with metal salt - anti-solvent. The products derived from biomass may for example be extracted by addition of an immiscible solvent with the hydrated inorganic salt mixed with the metal salt or with the mixture of the inorganic salt hydrate mixed with the metal salt - anti-solvent. Products derived from biomass can also be precipitated by changing conditions (temperature, pH, etc.) or by adding a third body.

The hydrated inorganic salt mixed with the metal salt thus recovered can be purified by heating at high temperatures, above 400 ° C, to remove by combustion the organic products derived from biomass potentially still present. The third step c) of the process according to the invention is the enzymatic hydrolysis step of the solid fraction obtained in step b).

The solid fraction, also referred to below as pretreated substrate, is subjected to enzymatic hydrolysis to convert the polysaccharides to monosaccharides under the usual conditions normally applied in these conversion processes.

Typically, the pretreated substrate is placed in an aqueous medium to reach dry matter concentrations of between 0.5% and 40%, preferably between 1% and 20% by weight. The enzymatic hydrolysis is carried out under mild conditions, at a temperature of the order of 40 to 60 ° C, at a pH of between 4.5 and 5.5. Very preferably, the pH is between 4.8 and 5.2. If a pH adjustment is necessary, it is carried out prior to the enzymatic hydrolysis step, when the pretreated substrate is placed in an aqueous medium, in particular by adding a buffer solution.

Enzymatic hydrolysis is carried out by means of enzymes produced by a microorganism. Microorganisms, such as fungi belonging to the genera Trichoderma, Aspergillus, Penicillum or Schizophyllum, or anaerobic bacteria belonging for example to the genus Clostridium, produce these enzymes, notably containing cellulases and hemicellulases, suitable for the extensive hydrolysis of cellulose and hemicelluloses.

The duration of the hydrolysis step c) varies between 1 h and 150 h, preferably between 2 h and 72 h, preferably between 4 h and 24 h.

At the end of the enzymatic hydrolysis step, the glucose formed is soluble in water while the optionally unconverted cellulose, lignin or other products remain insoluble. The aqueous glucose solution is recovered by filtration.

The monosaccharide thus obtained is easily converted into alcohol by fermentation with yeasts such as, for example, Saccharomyces cerevisiae. The fermentation must obtained is then distilled to separate the vinasses and the alcohol produced.

According to one embodiment of the invention, the enzymatic hydrolysis step is carried out simultaneously with the fermentation.

EXAMPLES

The substrate used in these examples is a wheat straw. The compositional analysis carried out according to the NREL protocol TP-510-42618 indicates that the composition of the raw substrate is the following (in% of dry matter): 37% cellulose, 28% hemicellulose and 20% lignin. In the examples below, the compositions are given in mole fractions.

Examples 1 to 5 are in accordance with the invention. Example 6 is given by way of comparison, the enzymatic hydrolysis being carried out on a native wheat straw. Example 7 is a comparative example, the pretreatment carried out consisting of a steam explosion, currently known as one of the best technologies for fermentable sugars.

Example 1: Pretreatment of wheat straw by LiCI.H ₂ 0 (98%) / ZnCl ₂ .2.5 H ₂ 0 (2%) 1 0 ° C and enzymatic hydrolysis

38 g of LiCI.H ₂ O (98%) / ZnCl ₂ .2.5H ₂ O (2%) and 2 g of wheat straw (500-1000 μπι) are placed in a 170 ml flask and stirred mechanically. by pale at 140 ° C for 1 hour in a Tornado ^® shaker with a 6-position carousel (Radleys).

After this pretreatment (step a) of the process according to the invention), the heating is stopped and 80 ml of distilled water are rapidly added to the mixture: the pretreated straw precipitates. The suspension containing the salt mixture, water and biomass is placed in a centrifuge tube and stirred at 9500 rpm for 10 minutes. The supernatant containing the salt mixture is then separated from the solid. The operation is repeated three times by adding 80 ml of distilled water to the solid part still present in the centrifugation tube. 7.4 g of solid, with a dry matter content of 9%, are recovered.

The solid recovered after precipitation and washing is subjected to enzymatic hydrolysis. Half of the recovered solid is placed in a 100 ml Schott flask. 5 ml of acetate buffer, 10 ml of a 1 wt.% Solution of NaN ₃ in water are added and the mixture is then made up to 100 g with distilled water. This solution is then left overnight at 50 ° C for "activation" with stirring of 550 rpm in a STEM dry water bath. The known quantities of enzyme are then added to the solution:

-Cellulases XL508, 10FPU per gram of dry matter

- β-glucosidases NOVOZYM 188, 25 CBU per gram of dry matter

The solution is then stirred at 400 rpm at 50 ° C., still in dry-water baths, and samples are taken after 1 h, 4 h, and 7 h. These samples are placed in centrifuge tubes and rapidly placed for 10 minutes in an oil at a temperature of 103 ° C. to neutralize the enzymatic activity. Centrifuge tubes are stored in a refrigerator at 4 ° C while waiting for glucose measurement. They are then diluted by 5 with distilled water before being assayed using the Analox GL6 analyzer apparatus, called glucostat, which measures by enzymatic assay the glucose concentration in aqueous solutions.

The result of the enzymatic hydrolysis is shown in FIG. 1. It is expressed in glucose yield, defined as the ratio of the glucose concentration in the solution the theoretical maximum concentration according to the cellulose content of the substrate. This glucose yield therefore represents the percentage of the cellulose actually converted into glucose. Example 2 Pretreatment of wheat straw by LiCl ₂ H ₂ O (10%) / ZnCl ₂ .2.5H ₂ O (90%) at 80 ° C. and enzymatic hydrolysis

The protocol is identical to that of Example 1 except that 38 g of LiCl ₂ H ₂ O (10%) / ZnCl ₂ .2.5H ₂ O (90%) are used in place of 38 g of LiCI.H ₂ 0 (98%) / ZnCl ₂ .2.5 H ₂ 0 (2%) and that the pretreatment is carried out at 80 ° C. The result of the enzymatic hydrolysis is shown in FIG.

Example 3 Pretreatment of Wheat Straw by NaCl ₆ H ₂ O (10%) / ZnCl ₂ .2.5H ₂ O (90%) at 80 ° C. and Enzymatic Hydrolysis

The protocol is identical to that of Example 1 except that 38 g of NaCl ₆ H ₂ O (10%) / ZnCl ₂ .2.5H ₂ O (90%) are used in place of 38 g of LiCI.H ₂ 0 (98%) / ZnCl ₂ .2.5 H ₂ 0 (2%) and that the pretreatment is carried out at 80 ° C. The result of the enzymatic hydrolysis is shown in FIG.

Example 4: Pre-treatment of wheat straw by NaCI.6H ₂ O (10%) / ZnCl ₂ .2.5 H ₂ O (90%) recycled at 80 ° C and enzymatic hydrolysis

The centrifugation supernatants obtained during a pretreatment as described in Example 3 are combined and concentrated on a rotary evaporator (T max = 120 ° C. - P mim = 90 mbar) to yield 34.8 g of residue containing 32.2. g of ZnCl ₂ .2.3H ₂ O and 1.9 g of NaCl, 8H ₂ O. The water stoichiometry with respect to the salts is adjusted by adding 2 g of water.

The mixture of recycled salts thus obtained and 2 g of wheat straw (500-1000 μιη) are placed in a 170 ml flask and stirred mechanically at 60 ° C for 1 h in a Tornado ^® stirrer fitted with a turntable 6 positions (Radleys).

After this cooking (step a) of the process according to the invention), the heating is stopped and 80 ml of distilled water are rapidly added to the mixture: the pretreated straw precipitates. The suspension containing the inorganic salt, water and biomass is placed in a centrifuge tube and centrifuged at 9500 rpm for 10 minutes. The supernatant, containing the Inorganic salt is then separated from the solid. The operation is repeated twice by adding 80 ml of distilled water to the solid part still present in the centrifugation tube. 11.2 g of solid, with a solids content of 13%, are recovered. The solid recovered after precipitation and washing was subjected to enzymatic hydrolysis. Half of the recovered solid is placed in a 100 ml Schott flask. 5 ml of acetate buffer, 10 ml of a 1 wt.% Solution of NaN ₃ in water are added and the mixture is then made up to 100 g with distilled water. This solution is then left overnight at 50 ° C for "activation" with stirring of 550 rpm in a STEM dry water bath. The known quantities of enzyme are then added to the solution:

-Cellulases XL508, 10FPU per gram of dry matter

- β-glucosidases NOVOZYM 188, 25 CBU per gram of dry matter

The solution is then stirred at 400 rpm at 50 ° C., still in the dry-water baths, and samples are taken after 1 h, 4 h and 7 h. These samples are placed in centrifuge tubes and rapidly placed for 10 minutes in an oil at a temperature of 03 ° C. to neutralize the enzymatic activity. Centrifuge tubes are stored in a refrigerator at 4 ° C while waiting for glucose measurement. They are then diluted by 5 with distilled water before being assayed using the Analox GL6 analyzer apparatus, called glucostat, which measures by enzymatic assay the glucose concentration in aqueous solutions.

The result of the enzymatic hydrolysis is shown in FIG. 4. It is expressed in glucose yield, defined as the ratio of the glucose concentration in the solution to the theoretical maximum concentration according to the cellulose content of the native wheat straw. This glucose yield therefore represents the percentage of the cellulose contained in the native substrate actually converted into glucose after the pretreatment and enzymatic hydrolysis steps.

EXAMPLE 5 Pretreatment of Wheat Straw by LiCl.2H ₂ O (10%) / FeCl ₃ .6H ₂ O (90%) at 60 ° C. and Enzymatic Hydrolysis

The protocol is identical to that of Example 1 except that 38 g of LiCl ₂ H ₂ O (10%) / FeCl ₃ .6H ₂ O (90%) are used in place of 38 g of LiCl. H ₂ O (98%) / ZnCl ₂ .2.5H ₂ O (2%) and pretreatment is performed at 60 ° C. The result of the enzymatic hydrolysis is shown in FIG. Example 6 Pretreatment of Wheat Straw by LiCl ₂ H ₂ O (20%) / FeCl ₃ .6H ₂ O (80%) at 60 ° C. and Enzymatic Hydrolysis

The protocol is identical to that of Example 1 except that 38 g of LiCl ₆ H ₂ O (20%) / FeCl ₃ H ₂ O (80%) are used in place of 38 g of LiCl. H ₂ O (98%) / ZnCl ₂ .2.5H ₂ O (2%) and pretreatment is performed at 60 ° C. The result of the enzymatic hydrolysis is shown in FIG.

Example 7 (not in accordance with the invention): Enzymatic hydrolysis of native wheat straw (without pretreatment)

The protocol used for the enzymatic hydrolysis is identical to that described in the example

1. Wheat straw is used native, without any pretreatment.

The result of the enzymatic hydrolysis is shown in FIG.

Example 8 (not in accordance with the invention): Enzymatic hydrolysis of wheat straw resulting from pretreatment by steam explosion.

The protocol used for the enzymatic hydrolysis is identical to that described in Example 1. The wheat straw used was pretreated by steam explosion, pretreatment whose three steps are described below.

1. Impregnation of wheat straw with 0.1 N sulfuric acid for a minimum of 8 hours followed by draining and pressing (100 bar) of the straw to obtain a solid at about 30% dry matter .

2. Pretreatment at 210 ° C (18 bar) of the straw for 2.5 minutes then decompression.

3. Final treatment by pressing at 100 bar.

The result of the enzymatic hydrolysis is shown in FIG.

From the various representative diagrams of each of the examples, it appears that the process according to the present invention makes it possible to obtain glucose yields significantly higher than those obtained without pretreatment, or even after, after 1 hour of enzymatic hydrolysis. pretreatment type steam explosion, since in this case, the glucose yield at one hour is only about 20%. In the same manner, the glucose yields obtained after 7 hours of hydrolysis are improved compared with those of the reference technology (steam explosion), when the firing step is carried out according to the method described herein. invention.

Excellent yields (greater than 80% glucose yield) are obtained at moderate temperatures (of the order of 60 ° C).

Claims

A process for converting lignocellulosic biomass into monosaccharides comprising at least:

a) a step of cooking the biomass in the presence or absence of an organic solvent, in a medium comprising at least one hydrated inorganic salt of formula (1)

MX _n .n'H ₂ 0

wherein X is an anion and M is a metal selected from groups 1 and 2 of the Periodic Table, n is an integer of 1 and 2 and n 'is from 0.5 to 6 in admixture with at least one other metal salt , hydrated or not, of general formula (2):

M'Y _m .m'H ₂ 0

wherein Y is an anion, identical to or different from X, and M 'a metal selected from Groups 3 to 13 of the Periodic Table, m is an integer from 1 to 6 and m ¹ is from 0 to 6.

b) a step of separating a solid fraction having undergone step a);

c) a step of enzymatic hydrolysis of said solid fraction.

2. Method according to claim 1 wherein the medium in which the firing step is carried out consists of one or more hydrated inorganic salts of formula (1) mixed with at least one other metal salt, hydrated or not, of formula (2).

3. Method according to one of the preceding claims wherein the anion X is a halide anion selected from Cl, F, Br, I, a perchlorate anion, a thiocyanate anion, a nitrate anion or an acetate anion.

4. Method according to one of the preceding claims wherein the Y anion, identical or different from the anion X, is chosen from anions halides, nitrate, carboxyiates, halocarboxylates, acetylacetonate, alkoxides, phenolate, optionally substituted, sulfate, alkylsulfates, phosphates, alkylphosphates, fluorosulfonates, alkylsulfonates, perfluoroalkylsulfonates, bis (perfluoroalkylsulfonyl) amides, arenesulphonates, optionally substituted with halogen or haloalkyl groups.

5. Method according to the preceding claim wherein the Y anion is selected from fluoride anions, chloride, bromide, acetate and triflate.

6. Method according to one of claims 1 to 5 wherein the metal M is preferably selected from lithium, magnesium, calcium, potassium or sodium.

7. Method according to one of claims 1 to 6 wherein the metal M 'is selected from iron, cobalt, nickel, copper, zinc, aluminum, indium or lanthanum.

8. Method according to one of claims 1 to 7 wherein the firing step is carried out at a temperature between -20 and 250 ° C, preferably between 20 and 160 ° C.

9. Method according to one of claims 1 to 8 wherein the molar fraction of the inorganic salt hydrate of general formula (1) in the mixture of salts of formula (1) and

(2) is between 0.05 and 1.

10. Method according to one of claims 1 to 9 wherein the firing time is between 0.5 min and 168 h, preferably between 5 minutes and 4 hours.

11. Method according to one of the preceding claims wherein the lignocellulosic biomass is present in an amount of between 0.5% and 40% by weight of the total mass of the lignocellulosic biomass / hydrated inorganic salt / metal salt mixture, preferably in an amount of between 3% and 25% by weight.

12. Method according to one of the preceding claims wherein the step of cooking the biomass may be carried out in a medium consisting of a mixture of different hydrated inorganic salts corresponding to formula (1) and / or different metal salts. having the formula (2)

13. Method according to one of claims 1 to 12 wherein the step of cooking the lignocellulosic biomass is carried out in the presence of an organic solvent selected from alcohols such as methanol, ethanol, n-propanol, isopropanol, n-butanol, isobutanol or tert-butanol, diols and polyols such as ethanediol, propanediol or glycerol, amino alcohols such as ethanolamine, diethanolamine or triethanolamine, ketones such as acetone or methyl ethyl ketone, acids carboxylic acids such as formic acid or acetic acid, esters such as ethyl acetate or isopropyl acetate, dimethylformamide, dimethylacetamide, dimethylsulfoxide, acetonitrile, aromatic solvents such as benzene, toluene, xylenes, alkanes.

14. Method according to one of claims 1 to 13 wherein the step of separating the solid fraction is carried out by precipitation by addition of at least one anti-solvent selected from water, alcohols such as methanol, ethanol, n-propanol, isopropanol, n-butanol, isobutanol or tert-butanol, diols and polyols such as ethanediol, propanediol or glycerol, amino alcohols such as ethanolamine, diethanolamine or triethanolamine, ketones such as acetone or methyl ethyl ketone, carboxylic acids such as formic acid or acetic acid, esters such as ethyl acetate or acetate of isopropyl, dimethylformamide, dimethylacetamide, dimethylsulfoxide, acetonitrile.

15. Method according to one of claims 1 to 14 wherein the enzymatic hydrolysis is carried out at a temperature of the order of 40 to 60 ° C, at a pH between 4.5 and 5.5, for a period of time. varying from 1 to 150h.