WO2017168207A1

WO2017168207A1 - Pre-treatment process for lignocellulosic biomass for producing carbohydrates and other byproducts

Info

Publication number: WO2017168207A1
Application number: PCT/IB2016/051794
Authority: WO
Inventors: Henrique Macedo Baudel; Eduardo DIEBOLD
Original assignee: Renner Herrmann Sa
Priority date: 2016-03-30
Filing date: 2016-03-30
Publication date: 2017-10-05

Abstract

A pre-treatment process for lignocellulosic biomass is described, used for producing carbohydrates and other subproducts in two steps, at least one nitrogenated additive, particularly carbamide, being used in at least one step, in a hydrothermal process that ensures maximum recovery of sugars from hemicelluloses and cellulose and minimum degradation of the sugars provided, producing carbohydrates that can be converted into biofuels and chemicals, such as ethanol, butanol and a multiplicity of products of industrial interest by chemical and biochemical pathways.

Description

PRE-TR PROCESS AT BIOMASS

LIGNOCELLULOSIS FOR CARBOHYDRATE PRODUCTION AND

OTHER FIELD OF THE INVENTION

[01] The present invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other byproducts. More specifically it comprises a lignocellulosic biomass pretreatment process by means of at least one reactor hydrothermal treatment step and impregnation of nitrogenous alkaline additive without recirculation or recovery of the additive.

BACKGROUND OF THE INVENTION

[02] Given the oil crisis and greenhouse gas climate change, one of the biggest challenges for the coming years is the production of energy from renewable sources, especially from agro-industrial or wood waste. , which are mainly composed of lignocellulosic biomass.

[03] Lignocellulosic biomass comprises on average 10-18% lignin, 12-20% hemicelluloses and 50% cellulose. The crystalline cellulose content and other components depend on the source vegetation and intrinsic characteristics of the plant [Balat, M .; Balat, H .; ÕZ, C; Progress in Energy and Combustion Science, 2008, 34, 551].

[04] The most urgent and important challenges arising from the use of lignocellulosic biomass for biofuel production are related to the need for synergy between the lignin complex disorganization processes, hemicelluloses and cellulose; and the later stages, where saccharification and enzymatic fermentation are performed [Martin, C; et. al. Quim New 2010, 33, 904].

[05] The use of lignocellulosic biomass for the production of liquid fuels requires pretreatments that seek to provide greater accessibility to cellulose and hemicelluloses that are in a branched structure with different degrees of crystallinity.

[06] Pretreatment methods can be classified into: physical, chemical, biological and physicochemical techniques. Thus, a pretreatment must: (i) efficiently separate lignocellulosic biomass components, obtaining high concentration of free saccharides at the end; (ii) disrupting the existing crosslink between lignin and hemicelluloses in the cellulosic fiber; (iii) cause the reduction of cellulose crystallinity by undoing the existing intermolecular hydrogen bonds, (iv) not intoxicating the system; (v) increase the surface area accessible to enzymes, facilitating saccharification, usually enzymatic; (vi) have low energy consumption and (vii) facilitate the recovery of extracted lignin, which may become other products, following the concept of biorefinery [Alviza, P .; Pejó, T. E. Black, M. G. Bioresour. Technol. 2010, 101, 4851].

[07] Lignocellulosic materials have two types of surface area, the outer one that is dependent on particle size and shape and the inner one dependent on the structural characteristics of cellulosic fiber [Taherzadeh, M. J .; Karimi, K.lnt. J. Mol. I know. 2008, 9, 1621] and [Wyman, CE. Handbook on bioethanol: production and utilization; Taylor & Francis: Washington DC, USA, 1996].

[08] Physical pre-treatment methods have been developed. In order to increase the available surface area, reduce the interference of the cellulose crystalline structure, multiplying the porous interstices and the efficiency of enzymatic hydrolysis [Wyman, CE. Handbook on bioethanol: production and utilization; Taylor & Francis: Washington DC, USA, 1996]. They are mainly based on the reduction of biomass particle size (increase of surface area) and increase of pore volume, which by kinetic factors, added to the destruction of the crystalline structure and decrease of the degree of cellulose polymerization, facilitate the saccharification steps. [Taherzadeh, MJ; Karimi, K.lnt. J. Mol. I know. 2008, 9, 1621].

[09] Physical methods performed by grinding and spraying have the advantage of not using solvents or chemical agents, reducing the risks and needs of effluent treatment; but are limited by high energy consumption and low lignin separation efficiency [Harun, R .; Danquah, M.K.Process Biochem. 201 1.46, 304.].

[010] The most widely used physicochemical treatment methods today are steam blast pretreatment, ultrasonic sonication, the use of ionic liquids (LI), and electromagnetic processes such as microwave irradiation. These methods have shown several advantages by using milder reaction conditions, less toxic reagents (water) and easily recovering sugars [Zhu, Z .; Zhu, M .; Wu, Z. Bioresource Technol. 2012, 1119, 199; Duarte, C.L; Ribeiro, M.A .; Oikawa, H .; Mori, M.N .; Neapolitan, C. M .; Galvao, C. A. Radiat. Phys.Chem. 2012, 81, 1008].

[011] Among the chemical methods of biomass pretreatment, alkaline pretreatment based on biomass solvation and saponification is described, causing swelling to increase surface area available for enzymatic hydrolysis. These methods require lower temperatures and pressures than those commonly used in other pretreatment processes [Harun, R .; et. al .; Appl. Energy 201 1.88, 3464]. However, it can lead to the formation of salts (originating from catalysts) irreversibly bound to cellulose, causing greater stability of the polysaccharide crystal structure [Mathew, AK; et. al.; Bioresource Technol. 201 1, 102, 6547] and [Hendriks, ATWM; Zeeman, G .; Bioresour. Technol. 2009, 100, 10].

[012] Currently the alkaline-oxidative conjugate processes have been widely used, where the decomposition efficiency of lignocellulosic biomass is maximized. However, due to the easy solubilization of hemicelluloses, it can oxidize in degradation products, such as saccharin acids, which are enzyme inhibitors [Assunção, F. C. R. In Green Chemistry in Brazil: 2010-2030; Carioca, J. O. B .; Almeida, M.F. L; Seidl, P. R. 2010].

Acid pretreatment is based on the use primarily of hydrochloric and sulfuric acid at concentrations ranging from 0.4 to 1% (v / v). The procedure is based on the heating of the acid (catalyst) causing cleavage of acetyl groups of hemicelluloses, which will also act as a hydrolytic agent, facilitating the removal of hemicelluloses. However, this technique is limited by the risk of cellulose fusion and depolymerization, followed by intense surface repolymerization and redistribution, making saccharification difficult [Canilha, L; et. al .; Analytica Magazine. 2010, 44, 80].

[014] Biological and physicochemical pretreatment methods are the most environmentally and energetically favorable. However, the biological technique is still limited due to the low conversion rate of cellulose to sugars by the enzymes laccases and peroxidases, which take up to 5 weeks of reaction, making it inapplicable industrially [Harun, R .; Danquah, MKProcess Biochem. 201 1.46, 304].

Thus, biomass pretreatment processes can only use saturated steam and water at high temperatures (self-hydrolysis), or use chemical agents such as organic and mineral acids, alkalis, bases and metal salts, which may act as promoters, catalysts or additives capable of altering the structure of cellulose present in the pretreated biomass or altering the rate of chemical reactions involved in the process.

[016] Generally, the pretreatment process generally requires more than one operational step, including additive impregnation and intermediate or final wash of the pretreated biomass, which may result in lower temporal productivity (mass produced / time of process) and higher water consumption per unit of pre-treated biomass produced, even in cases where there is a significant reuse and recirculation rate of the liquid streams produced in the pretreatment stage.

[017] Although an indispensable step for saccharification steps, increasing yields by at least 80%, lignocellulosic biomass pretreatment accounts for about 35% of total production costs [Balat, M .; Balat, H .; Oz, C; Progress in Energy and Combustion Science, 2008, 34, 551]. Detoxification of the reaction medium as well as solid waste (cellulose and lignin) from the pretreatment steps is still an indispensable predecessor for maintaining enzymatic efficiency in the saccharification and fermentation stages. Apart from the high costs, detoxification operations can also cause partial loss of monosaccharides obtained, effluent generation and high energy consumption [Asunción, FCR In Green Chemistry in Brazil: 2010-2030; Carioca, JOB; Almeida, MF L; Seidl, PR 2010].

US20080008783 describes a process for treating biomass for processing the most accessible structural carbohydrates and / or digestion using concentrated ammonium hydroxide, with or without the addition of anhydrous ammonia. The process preferably uses steam to remove the ammonia from the biomass.

US20070031953 describes an ethanol production process using biocatalysts capable of fermenting sugars derived from the treated biomass, said sugars obtained by pretreatment of the biomass under conditions of high solids and low ammonia concentration, followed by saccharification.

[020] US20070031918 describes a biomass pretreatment with a low ammonium hydroxide concentration at a high biomass concentration.

[021] US20070031919 describes target chemicals produced using biocatalysts which are capable of fermenting treated biomass sugars under high solids and low ammonia conditions, followed by saccharification.

US5037663 describes a process for increasing the reactivity of cellulose-containing materials, comprising the steps of disposing the biomass in a waste container. pressure with a volatile liquid having a vapor pressure greater than atmospheric pressure in a time sufficient to swell the pulp of the material. The pressure is then rapidly reduced to atmospheric pressure, thus causing the agent to change the morphological structure of the lignocellulosic material and partially deconstruct the cellulosic matrix (lignin-carbohydrate-LCC complex), resulting in greater accessibility to the latter. hydrolyzing agents such as cellulolytic enzymes.

US4880473 describes a process for producing fermentable sugars from wood or other cellulose-containing biomass, which comprises the steps of hydrolysis of the biomass with dilute sulfuric acid, solid phase separation which is subjected to rapid pyrolysis. at a temperature of 400 to 600 ° C, preferably in a fluidized bed reactor with a short residence time to obtain a crude pyrolysis product by condensation of pyrolytic vapors.

[024] US20100041 1 19 describes a method for converting cellulosic material into ethanol and other products, the cellulosic material undergoing continuous hydrothermal pretreatment without addition of chemicals, with the fiber fraction undergoing liquefaction and saccharification. enzymatic

However, differently, a lignocellulosic biomass pretreatment process by at least one reactor hydrothermal treatment step and impregnation of nitrogenous alkaline additive, such as carbamide, without the need for recirculation or recovery of the additive. Carbamide can be converted to ammonium carbonate and This, in turn, can be converted into a mixture of ammonia and carbon dioxide (C0 _2). Ammonia tends to promote selective deconstruction of the lignocellulosic fraction of biomass with minimal degradation of cellulose and sugars, while carbon dioxide acts as a catalyst in the deconstruction of biomass lignin-carbohydrate complex (LCC), with greater selectivity in hemicellulose conversion. Thus, carbamide acts as a bifunctional catalyst-promoter in the conversion of biomass, making it more accessible to chemical and enzymatic agents that will act on the cellulosic matrix. Such action results in reduced degradation of the produced sugars, as well as minimal production of inhibitor compounds (eg furfural, hydroxymethyl-furfural and organic / humic acids) from subsequent enzymatic hydrolysis and fermentation steps.

In addition, the use of carbamide makes it possible to produce ammonia "within the reactor itself", which eliminates the need to introduce ammonia or ammonium hydroxide through feed systems (pressurized or not), pumping, loading and transport. Last but not least, such a technique avoids the need to use high excess ammonia / ammonium hydroxide over stoichiometric values, representing lower operating costs and lower operational risks associated with process safety and industrial hygiene.

SUMMARY

[027] The invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other byproducts that provides a high fiber reactivity (accessibility) biomass to chemical and enzymatic hydrolytic agents, particularly enzymes, favoring enzymatic digestibility, obtaining adequate recovery of sugars from hemicellulosic (preferably pentoses) and cellulosic (preferably hexoses) fractions.

[028] The invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other by-products employing a nitrogenous additive, particularly carbamide, and hydrothermal treatment with varying liquid water contents, enabling maximum recovery of sugars. from hemicelluloses and cellulose, with minimal degradation of available sugars.

[029] The invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other byproducts in which the temperature of 140 to 240 ^S C is reached in the reactor and is rapidly depressurised, causing a structural change in biomass, making It is most accessible to hydrolytic agents such as enzymes and chemicals capable of fractionating cellulose and hemicelluloses into smaller sugars.

[030] The invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other by-products that can be converted into biofuels and chemicals such as ethanol, butanol and a myriad of industrially interesting products by chemical and biochemical routes. .

[031] The invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other byproducts that provides for selective removal of hemicelluloses and lignin with minimal cellulose degradation.

[032] The invention describes a process of pretreatment of Lignocellulosic biomass for the production of carbohydrates and other byproducts that do not require the use of severe process conditions such as temperature, process time and use of aggressive chemical compounds such as organic and inorganic acids.

[033] The invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other byproducts that provides reduced saccharide degradation.

[034] The invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other byproducts that provides enhanced sugar recovery.

[035] The invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other byproducts with reduced formation of sugar degradation products (such as furfural, HMF, organic acids) which tend to be inhibitors of action of enzymes and fermentative microorganisms.

[036] The invention describes a lignocellulosic biomass pretreatment process for the production of carbohydrates and other byproducts that provides high throughput of the ethanolic fermentation process.

BRIEF DESCRIPTION OF THE FIGURES

[037] Figure 1 presents the graphical representation of saccharide yield (kg ART / ton. Dry biomass) produced from eucalyptus biomass residues (root, stem and miscellaneous chips).

[038] Figure 2 presents the graphical representation of the ethanol yield (L ethanol / ton. Dry biomass) produced from eucalyptus biomass residues (root, stem and miscellaneous chips). [039] Figure 3 shows the typical chromatogram of a hydrolyzate (carbohydrate solution) produced from enzymatic hydrolysis of pretreated biomass (eucalyptus).

[040] Figure 4 shows the typical wine chromatogram (ethanolic solution) produced from the fermentation of carbohydrates produced by enzymatic hydrolysis of pretreated biomass (eucalyptus).

DETAILED DESCRIPTION OF THE INVENTION

The lignocellulosic biomass pretreatment process for the production of carbohydrates and other byproducts, object of the present invention, comprises an initial stage of preparation of lignocellulosic biomass which is subjected to fragmentation to obtain appropriate dimensions (width, width, thickness). height and length) and particle size classification to ensure the dimensional homogeneity of the biomass to be processed.

[042] Optionally, the lignocellulosic biomass is subjected to washing to remove foreign substances, contaminants and other components that may affect process efficiency, as well as to provide an adequate biomass moisture content for subsequent processing.

[043] In a first reaction step, the fragmented lignocellulosic biomass is loaded into a continuous or batch reactor for hydrothermal treatment, preferably maintaining a head-space in the range of 0-40%, preferably 20%, according to the lignocellulosic biomass to be processed.

[044] The biomass charge deposited in the reactor is injected with water, saturated steam or equilibrium vapor-water mixtures. thermodynamic, from 1 to 20 minutes, preferably 8 minutes, in order to promote the removal of atmospheric air stored inside the biomass, obtaining adequate homogenization of temperature and humidity.

[045] Biomass heating within the reactor is by direct contact with process steam (saturated steam at 18-26 kgf / cm ² , preferably at 20 kgf / cm ² ). Once the temperature reached 160 to 210 ^S C, the steam injection is stopped and the biomass remains under treatment cooking ^ ") from 30 seconds to 1800 seconds.

Depending on the lignocellulosic biomass to be processed, characterized essentially by specific mass and fiber morphology, the first reaction step is performed in at least one cycle. For example, eucalyptus fibers have a length ranging from 0.75 to 1.30 millimeters, showing an average close to 1 mm, being considered short fibers when compared to conifer fibers, called long fibers, which have a length three to five times higher. Thus, long fiber biomasses tend to demand optimum operating conditions distinct from those used with short fiber biomasses.

Optionally, in the first reaction step, lignocellulosic biomass is impregnated with catalysts, selected from mineral acids, metal salts, organic acids, organic and inorganic bases (alkalis), said catalysts added in at least one step in order to improve process efficiency and / or promote structural changes in the biomass lignocellulosic matrix resulting in higher fiber reactivity, accessibility and digestibility enzymatic

[048] After the reaction time has elapsed, the reactor undergoes rapid depressurization which, for the purposes of the present invention, implies a return of working pressure to or near ambient pressure within 5 seconds to cause a structural change in biomass, making it more accessible to hydrolytic agents such as enzymes and chemicals capable of fractionating cellulose and hemicelluloses into smaller sugars.

[049] The biomass deposited in the reactor is discharged into a blow-tanK, atmospheric cyclone or storage tank and subjected to a solid-liquid separation operation such as filtration or centrifugation.

[050] The liquid produced (prehydrolyzed), usually rich in sugars from biomass hemicelluloses, can be used in subsequent processing steps, or later recycled and reincorporated into the production process.

[051] Solid fraction, ie wet pretreated biomass, is impregnated with a nitrogenous compound to promote important structural changes in the lignocellulosic matrix of biomass, which enable greater accessibility of cellulose to hydrolytic agents used in the stages. subsequent

[052] The nitrogenous compound is selected from carbamide, ammonia, ammonium hydroxide, ammonium carbonate or amines.

[053] The biomass is then subjected to a liquid-solid extraction operation such as washing with water or dilute acid or alkaline solutions followed by solid-liquid separation such as filtration or centrifugation to remove the liquid. produced (prehydrolyzed), usually rich in sugars from the biomass hemicelluloses, which can be used in subsequent processing steps, or later recycled and reincorporated into the production process.

[054] The wet solid fraction proceeds to an enzymatic (enzymatic hydrolysis) or chemical saccharification step.

[055] The biomass impregnated with the nitrogenous compound may be subjected to a second reaction step including reactor vapor hydrothermal treatment at a temperature of 180 to 220 ^S C, 30 seconds to 1200 seconds and then subjected to an operation. solid-liquid extraction, such as washing with water or dilute acid or alkaline solutions, followed by solid-liquid separation, such as filtration or centrifugation, to remove the produced (prehydrolyzed) liquid, and the wet solid fraction follows for an enzymatic saccharification (enzymatic hydrolysis) or chemical step.

[056] Example 1. Carbohydrate production from eucalyptus waste

[057] Used 40-45% moisture biomass after prewashing with water at room temperature. Steam pre-treatments (STEX) were carried out in two steps, the first being conducted at 200-205 ^s C (internal pressure 17-18 kgf / cm ² ) for 8-12 minutes by injection of saturated steam at 20 kgf / cm ² . After the reaction time, the reactor was suddenly discharged to carry the biomass into a blow collecting tanK. The biomass was collected and filtered using a mesh of tissue. solid fraction (wet pretreated biomass) was impregnated with carbamide (particularly urea) dosed at 0.02 - 0.05g / g biomass for 2 hours. Then the carbamide-impregnated pretreated biomass was loaded into the steam pretreatment reactor and processed at 200-205 ^s C (internal pressure 17-18 kgf / cm ² ) for 8-12 minutes by injection of saturated steam at 20 kgf / cm ² . After the reaction time, the reactor was suddenly discharged to carry the biomass into a blow collecting tanK. The biomass was collected and filtered using a mesh fabric. The liquid fraction was separated from the fraction. solid (wet pretreated biomass) using vacuum filtration The pretreated biomass was subjected to enzymatic hydrolysis conducted in mechanically agitated batch reactors under single batch fed pH 4.8-5.2, temperature 48 to 52 ^O C, solid content 8 to 20% for 48 to 72 hours, using the commercial formulation (Cellic Ctec3, Novozymes). After the reaction time, the reactor was discharged, the biomass was collected and filtered using mesh fabric. the The liquid fraction (enzymatic hydrolyzate) was separated from the solid fraction (cellulignin), quantified and analyzed for sugar content.

[058] As shown in Table 1, a saccharide solution with a sugar concentration of approximately 60 g / L (measured in Brix degrees) was obtained, corresponding to a yield of over 320 kg sugars / tonne of dry biomass.

[059] Table 1: Production of sugars from eucalyptus residues.

Liquid Fraction Solid Fraction

PH Concentration Extraction

(g / l) (%)

Pretreatment Step 1 3.5 - 19.4 Step 2 8.8 - 5.0

Enzymatic Hydrolysis 4.9 60.0 12.8

[060] Figure 1 presents the results for saccharide yields (expressed in kg ART / ton. Dry biomass) obtained in 10 operational ethanol production runs from eucalyptus residues consisting of root, stem and various chips.

[061] Example 2. Production of cellulosic ethanol from eucalyptus residues

[062] Biomass with 40-45% humidity is used after prewashing with water at room temperature. Steam pre-treatments (STEX) were carried out in two steps, the first being conducted at 200-205 ^s C (internal pressure 17-18 kgf / cm ² ) for 8-12 minutes by injection of saturated steam at 20 kgf / cm ² . After the reaction time, the reactor was suddenly discharged to conduct the biomass into a blow collecting tanK. The biomass was then collected and filtered using a mesh of tissue. The liquid fraction was separated. while the solid fraction (wet pretreated biomass) was impregnated with carbamide (particularly urea) dosed at 0.02-0.05g / g biomass for 2 hours and then the carbamide impregnated pretreated biomass was steam pretreatment reactor and processed at 200-205 ^s C (internal pressure 17-18 kgf / cm ² ) for 8 to 12 minutes by injection of saturated steam at 20 kgf / cm ² . reaction time, the reactor was suddenly discharged to carry the biomass into a blow collecting tank. The biomass was collected and filtered using a mesh fabric. The liquid fraction was separated from the solid fraction ( pre-treated biomass) using from filtration to vacuum. The pretreated biomass was subjected to enzymatic hydrolysis conducted in mechanically agitated batch reactors under single and fed batch regimes, pH 4.8-5.2, temperature 48-52 ^s C, solids content 8-20%. for 48 to 72 hours using commercial formulation (Cellic Ctec3, Novozymes). After the reaction time, the reactor was discharged. Whole slurr, composed of solid and liquid fractions, was subjected to an ethanolic fermentation process using commercial yeast (Saccharomices cerevisaé) Mauri Y-904, batch fed, yeast load 0.01 g / g total, temperature 32-36 ^s C, pH 4.6-5.4 for 24-48 h The process was concluded after evidence of microbial inactivity The liquid (wine) fraction was separated from the solid (cellulignin) fraction. and ethanol content) As shown in Table 2, a hydroethanolic solution with an ethanol concentration of approximately 3.2% wt (measured in ^S GL), corresponding to a higher yield yield, was obtained. 213 liters of ethanol / tonne of dry biomass.

[063] Table 2: Ethanol production from eucalyptus residues.

Sugar Production Production of

Ethanol

Pretreatment Hydrolysis Fermentation

Step 1 Step 2 Enzyme

Liquid / medium pH 4.1 9.0 5.3 4.8

Extraction 6.3 10.8 13.7 -

Concentration 62.0

(g / l)

(% pp) - - - 3.20

Yield - - 425.0 - (kg / ton BS)

(L / ton BS) - - - 2.13

[064] Figure 2 presents the results concerning the ethanolic yields (expressed in liters ethanol / tonne dry biomass) obtained in 10 operational runs of ethanol production from eucalyptus residues consisting of root, stem and various chips.

Claims

CLAIMS:

1. LIGNOCELLULOSTIC BIOMASS PRE-TREATMENT PROCESS FOR CARBOHYDRATE PRODUCTION AND OTHER BY-PRODUCTS characterized by comprising the steps of:

a) fragmentation of lignocellulosic biomass;

(b) first reaction step including hydrothermal treatment of lignocellulosic biomass at a temperature between 160 to 210 ^S C when steam injection is interrupted, with the biomass remaining under treatment for 30 seconds to 1800 seconds;

c) reactor depressurization to or near ambient pressure within no more than 5 seconds;

d) solid-liquid separation of biomass;

e) impregnating the solid fraction with a nitrogenous compound selected from carbamide, ammonia, ammonium hydroxide, ammonium carbonate or amines;

f) liquid-solid extraction of biomass;

g) enzymatic or chemical hydrolysis of the wet solid fraction;

Pretreatment process of lignocellulosic biome for the production of carbohydrates and other byproducts according to claim 1, characterized in that the first reaction step is carried out in at least one cycle.

Pretreatment process of lignocellulosic biome for the production of carbohydrates and other byproducts according to claim 1; characterized in that the first reaction step includes the addition of selected catalysts from mineral acids, metal salts, organic acids, organic and inorganic bases (alkalis).

Pretreatment process of lignocellulosic biome for the production of carbohydrates and other byproducts according to claim 1, characterized in that the biomass impregnated with the nitrogenous compound is subjected to a second reaction step that includes hydrothermal steam treatment in reactor. 180 to 220 ^S C, 30 seconds to 1200 seconds, then undergoing a liquid-solid extraction operation, followed by solid-liquid separation, and the wet solid fraction being enzymatically or chemically hydrolyzed.