A process for producing BTX through catalytic pyrolysis from biomass without recycling the oxygenated compounds.

Abstract

A process is described for producing BTX and alcohols from biomass, comprising at least a) catalytic pyrolysis of said biomass in a fluidized-bed reactor producing a gaseous pyrolysis effluent; b) separating said gaseous pyrolysis effluent into at least one BTX fraction and a gaseous effluent comprising at least carbon monoxide and carbon dioxide, c) recycling at least part of said gaseous effluent comprising at least carbon monoxide and carbon dioxide into the reactor of said step a), d) purging said gaseous effluent recycled according to step c) to produce a purge effluent, e) sending at least part of said purge effluent from step d) into a fermentation step producing a liquid fermentation stream comprising at least one stream comprising at least one oxygenated compound chosen from alcohols containing 2 to 6 carbon atoms, diols containing 2 to 4 carbon atoms, acid alcohols containing 2 to 4 carbon atoms, carboxylic acids containing 2 to 6 carbon atoms, aldehydes containing 2 to 12 carbon atoms, ketones containing 3 to 12 carbon atoms and esters containing 2 to 12 carbon atoms, alone or as a mixture.

Description

BTX PRODUCTION PROCESS BY CATALYTIC PYROLYSIS FROM BIOMASS WITHOUT RECYCLING OXYGENATED COMPOUNDS technical field Chemical intermediates are normally produced from fossil resources such as oil, natural gas, or coal in multi-stage processes. To replace or supplement the production of chemical intermediates from fossil resources, it is necessary to develop processes that process non-fossil feedstocks, namely biomass. The present invention relates to a process for producing chemical intermediates and / or fuel base materials, and in particular BTX and alcohols, from biomass. Previous art US patent 8277643 describes a process for producing aromatics, biofuel, and olefins by catalytic pyrolysis of biomass in the presence of a zeolite catalyst such as ZSM-5. The process is carried out at a temperature at least above 300°C, at a pressure between 1 and 4 atm, and at a vvh between 0.01 and 10 h "1 The process is also characterized by a residence time of biomass in the reactor of between 2 seconds and 5 minutes. Patent application WO2009 / 1 1 1026 describes in more detail the type of catalyst that can be used in the catalytic pyrolysis step, and in particular zeolite catalysts that can be doped with iron, gallium, or zinc. Patent application WO201 1 / 031320 describes a process for producing aromatics, biofuel, and olefins by catalytic pyrolysis of biomass in the presence of a zeolite catalyst, in which the pyrolysis products are separated to obtain a fraction containing olefins, which is then recycled back into the pyrolysis reactor. The applicant has thus discovered that implementing a process for producing a BTX cut by catalytic pyrolysis of lignocellulosic biomass in the presence of a specific oxygenated compound stream results in improved BTX yields compared to prior art processes. Summary and significance of the invention The invention relates to a process for producing BTX and alcohols from biomass comprising at least the following steps: a) the catalytic pyrolysis of said biomass in a fluidized bed reactor producing a gaseous pyrolysis effluent; b) the separation of said pyrolysis gaseous effluent into at least a BTX fraction and a gaseous effluent comprising at least carbon monoxide and carbon dioxide, (c) recycles at least a portion of said gaseous effluent comprising at least carbon monoxide and carbon dioxide in the reactor of said step (a), (d) purging said recycled gaseous effluent according to step (c) to produce a purge effluent, (e) sending at least a part of said purge effluent from step (d) into a fermentation step producing a fermentative liquid stream comprising at least one stream comprising at least one oxygenated compound selected from alcohols having 2 to 6 carbon atoms, diols having 2 to 4 carbon atoms, acid alcohols having 2 to 4 carbon atoms, carboxylic acids having 2 to 6 carbon atoms, aldehydes having 2 to 12 carbon atoms, ketones having 3 to 12 carbon atoms and esters having 2 to 12 carbon atoms, alone or in mixture. Throughout the rest of the text, BTX cut refers to a fraction comprising a mixture of Benzene, Toluene and Xylenes (ortho, meta, para). An advantage of the present invention is to provide an integrated process for the production of BTX with a high yield by catalytic pyrolysis of biomass, followed by a fermentation step of conversion of part of the gaseous pyrolysis effluent comprising CO and CO2, said process also enabling the production of a stream of oxygenated compounds and in particular alcohol and preferably ethanol. Another advantage of this embodiment of the present invention lies in the valorization of the purging of said recycled gaseous fraction comprising CO and CO2 produced by catalytic pyrolysis in a fermentation step to produce at less an oxygenated compound as claimed and preferably ethanol, thus making it possible to significantly improve the profitability of the process according to the invention. Another advantage of this embodiment of the present invention lies in the optimization of the valorization of carbon from biomass, in particular in chemical intermediates such as BTX, but also as a base for biofuel. Another advantage of the present invention is that it provides an optimized process for producing a BTX cut, in that the gaseous effluent comprising CO and CO2 produced by catalytic pyrolysis and used as a feed for the fermentation step is drawn from the catalytic pyrolysis step at a temperature and pressure compatible with its direct use in a fermentation step, without an intermediate compression step. The gaseous effluent comprising CO and CO2 produced by catalytic pyrolysis also has a composition compatible with its use in a fermentation step. Detailed description of the invention According to the invention, the process for producing BTX and alcohols from biomass consists of a step a) catalytic pyrolysis of said biomass in a fluidized bed reactor producing a pyrolysis gaseous effluent. Stage a) of catalytic pyrolysis Examples of fluidized bed reactors can be found in Howard, RJ (1989). "Principles of Fluidized Bed Technology and Applications." New York, Adam Higler of NY; Tavoulareas, S. (1991) Combustion Technology. ** Annual Reviews Inc ** 16, 25-27. and Trambouze, P., and Euzen, J. (2004). "Chemical reactors: From design to operation." (R. Bonormo, Trans.). Paris: Editions Technip. The fluidized bed reactor used in the process according to the invention preferably operates in turbulent regime, that is to say in a range of surface gas velocity between 0.5 and 0.8 m / s. By surface gas velocity is meant the volumetric flow rate of gas referred to the surface of the reactor. This turbulent bed implementation is preferred over the "riser" technology commonly used for FCC because the yields of coke and partially converted biomass (usually called "char" in FCC technology) are significant, and consequently, the coke concentration on the catalyst is high. Thanks to the proposed implementation, the heat balance of the catalytic pyrolysis step is decoupled by adjusting the residence time of the catalyst in the reactor via the flow rate of the latter to the regenerator, thus limiting the percentage of coke on the catalyst and therefore limiting the temperature of the regenerator to an operable range. According to the invention, the feed used in the present invention is biomass. Preferably, the feedstock is lignocellulosic biomass or one or more lignocellulosic biomass constituents chosen from the group formed by cellulose, hemicellulose and / or lignin. Lignocellulosic biomass can consist of wood, agricultural waste, or plant waste. Other, non-limiting examples of lignocellulosic biomass include agricultural residues (straw, corn stalks, etc.), forestry residues (products of first thinning), forestry products, dedicated crops (short-rotation coppice), residues from the agri-food industry, household organic waste, waste from wood processing facilities, used construction timber, and paper, whether recycled or not. Lignocellulosic biomass can also come from by-products of the paper industry such as Kraft lignin, or black liquors from the manufacture of paper pulp. Lignocellulosic biomass can advantageously undergo at least one pretreatment step before being introduced into the process according to the invention. Preferably, the biomass is ground and dried until the desired particle size is obtained. A feedstock with a particle diameter between 0.3 and 0.5 mm can advantageously be obtained. Typically, the particle size of the lignocellulosic biomass to be pyrolyzed ranges from a particle size sufficient to pass through a 1 mm sieve to a particle size sufficient to pass through a 30 mm sieve. Preferably, the biomass to be pyrolyzed is advantageously loaded into a drive compartment or pneumatic conveyor so as to be drawn into the fluidized bed by a drive fluid. Preferably, the drive fluid used is nitrogen gas. However, it is also envisaged that other non-oxidizing drive fluids may be used. Preferably, the pyrolysis gas produced during the process can be recycled and used as a drive fluid. Said pyrolysis gas consists mainly of a non-condensable gaseous effluent, comprising at least Carbon monoxide (CO) and carbon dioxide (CO2), and advantageously including light olefins comprising 2 to 4 carbon atoms, produced in step a). In this way, the cost of carrying out pyrolysis can be considerably reduced. The biomass can be loaded into a feed hopper or other device that delivers the biomass to the drive compartment in an appropriate quantity. In this way, a constant amount of biomass is delivered to the drive compartment. The drive fluid advantageously transports biomass from the drive compartment into the fluidized bed via a feed tube. Typically, the feed tube is cooled to maintain the biomass temperature at the required level before it enters the fluidized bed. The feed tube can be cooled by jacketing the tube, typically with an air-cooled or liquid-cooled jacket. However, it is also possible for the feed tube to remain uncooled. According to the invention, step a) of catalytic pyrolysis operates in the presence of a catalyst. Preferably, said step a) operates in the presence of a zeolite catalyst comprising, and preferably consisting of, at least one zeolite selected from ZSM-5, ferrierite, beta zeolite, Y zeolite, mordenite, ZSM-23, ZSM-57, EU-1, ZSM-1, and preferably the catalyst is a catalyst comprising only ZSM-5. The zeolite used in the catalyst implemented in step a) of catalytic pyrolysis can advantageously be doped, preferably with a metal selected from iron, gallium, zinc, and lanthanum. Depending on the catalyst used and the desired reaction products, the temperature implemented in step a) of catalytic pyrolysis can be adjusted. In some embodiments, the catalytic pyrolysis step is carried out at a temperature between 400 and 1000 < C, preferably between 400 and 650 <C, preferably between 450 and 600 < C and preferably between 450 and 590 Ό. In particular, it is the catalyst from the regeneration stage that ensures these reactor temperature ranges. Step a) of pyrolysis is also advantageously implemented at an absolute pressure between 0.1 and 0.5 MPa and at a vvh between 0.01 and 10 h "1 preferably between 0.01 and 5 hours "1 , preferably between 0.1 and 3 hours ~1 and preferably between 0.1 and 3 hours ~1 . Under these conditions, the biomass first undergoes rapid pyrolysis in the reactor upon contact with the hot catalyst from the regenerator, which acts as a heat transfer medium in this stage. The gases resulting from this pyrolysis then react with the catalyst, which now acts as a catalyst, catalyzing the reactions that produce the desired chemical intermediates. According to the invention, the products obtained at the end of step a) of catalytic pyrolysis are advantageously recovered in the form of a pyrolysis gaseous effluent comprising at least a part of the BTX cut. Step b) of separation According to the invention, the process includes a step b) of separating said pyrolysis gaseous effluent into at least a BTX fraction and a gaseous effluent comprising at least carbon monoxide (CO) and carbon dioxide (CO2). Advantageously, in addition to the BTX liquid fraction and the non-condensable gaseous effluent, comprising at least carbon monoxide (CO) and carbon dioxide (CO2), separation step b) also allows the separation of a liquid cut comprising mainly compounds with a number of carbon atoms greater than 9, i.e. at least 50% by weight of C9+ compounds and water. The said non-condensable gaseous effluent, comprising at least carbon monoxide (CO) and carbon dioxide (CO2), also advantageously comprises light olefins comprising 2 to 4 carbon atoms. The coked catalyst and the unconverted biomass usually referred to as "char" are advantageously withdrawn from the reactor and preferably sent to a stripper in order to eliminate potentially adsorbed hydrocarbons and thus avoid their combustion in the regenerator by contacting a gas chosen from among water vapor, an inert gas such as nitrogen and at least part of the non-condensable gaseous cut rich in CO and CO2 resulting from the fractionation of the gaseous effluent from the catalytic pyrolysis step. The said coke catalyst and char, possibly stripped, are advantageously sent into a regenerator where coke and char are burned by the addition of air or oxygen. The regenerated catalyst is advantageously recycled into the reactor of the catalytic pyrolysis stage in order to undergo another cycle. The catalytic pyrolysis step of the process according to the invention allows the production of at least 10% by weight and preferably at least 15% by weight of aromatics relative to the total mass of reaction products obtained, with a selectivity of at least 65% and preferably at least 70% in BTX. The process according to the invention comprising at least one catalytic pyrolysis step of a biomass feedstock therefore produces a gaseous effluent comprising at least a liquid fraction BTX and a gaseous effluent comprising at least carbon monoxide and carbon dioxide. The process also makes it possible to obtain, in addition to the BTX cut, a heavier liquid fraction, predominantly aromatic, called "C9+ cut", which can advantageously be used in a process external to the process according to the invention. Step c) of recycling According to the invention, the process includes a step c) of recycling at least a part of said gaseous effluent comprising at least carbon monoxide and carbon dioxide in the reactor of said step a). Preferably, the recycling of at least a portion of said gaseous effluent, comprising at least carbon monoxide and carbon dioxide, in the reactor of the catalytic pyrolysis stage is carried out via a compressor. This gaseous stream then serves as the feedstock entrainment fluid in said reactor. In this case, purging of said recycled gaseous effluent is inevitable. Step d) of purging According to the invention, the process includes a step d) of purging said recycled gaseous effluent according to step c) to produce a purge effluent. Preferably, said purging of said recycled gaseous effluent is carried out either upstream or downstream of said compressor placed on the recycle loop. Fermentation stage e) According to the invention, the process includes a step of sending at least a portion of said purge effluent from step d) into a fermentation step e) producing a fermentative liquid stream comprising at least one stream comprising at least one oxygenated compound selected from alcohols having 2 to 6 carbon atoms, diols having 2 to 4 carbon atoms, acid alcohols having 2 to 4 carbon atoms, carboxylic acids having 2 to 6 carbon atoms, aldehydes having 2 to 12 carbon atoms, ketones having 3 to 12 carbon atoms and esters having 2 to 12 carbon atoms, alone or in mixture. Said purge effluent of said gaseous fraction of recycle generally comprises a carbon monoxide (CO) content advantageously between 40 and 60% by mass and a carbon dioxide (CO2) content advantageously between 20 and 40% by mass. Furthermore, the said purge effluent also generally includes hydrogen, light C1-C4 gases, olefins and may also contain a low level of aromatic impurities such as, for example, benzene and toluene. The aromatic impurity content can advantageously be reduced by adjusting the operating conditions of the catalytic pyrolysis step as well as the recycled rate returned to the reactor. The gaseous effluent comprising CO and CO2 produced by catalytic pyrolysis has a composition compatible with its use in a fermentation step. Furthermore, the portion of said purge effluent from step d) comprising carbon monoxide (CO) and carbon dioxide (CO2) used as feed for fermentation step e) is withdrawn from catalytic pyrolysis step a) at a temperature and pressure compatible with its direct use in a fermentation step. The process according to the invention may require compressing or decompressing said purge to allow for improved operation of the fermentation step. In a preferred embodiment, the process according to the invention does not include a step of compressing or heating said purge effluent from step d) comprising carbon monoxide (CO) and carbon dioxide (CO2) to bring it to operating conditions compatible with a fermentation step. The portion of said purge effluent from step d) comprising carbon monoxide (CO) and carbon dioxide (CO2) used as feed for fermentation step e) is generally drawn off at a temperature between 20 and 60°C and at a pressure between 0.1 and 0.5 MPa. The fermentation step e) is advantageously implemented in the presence of at least one microorganism also called an acetogenic strain. Throughout the rest of the text, the terms "fermentation", "fermentation stage", or "fermentation reaction" refer to the conversion of H2, CO and / or CO2 gases and encompass both the growth phase of the fermenting microorganism and the production phase of molecules of interest, such as alcohols, acids, acid alcohols and / or carboxylic acids by this microorganism. Indeed, the ability of certain microorganisms to grow on gaseous substrates such as carbon monoxide (CO), carbon dioxide (CO2) and / or hydrogen (H2) as the sole source of carbon was discovered as early as 1903. A large number of anaerobic organisms, more particularly so-called "acetogenic" organisms, possess this ability to metabolize CO and / or the CO2 / H2 couple to produce various end molecules of interest such as acetate, butyrate, ethanol and / or n-butanol. The microorganisms capable of carrying out this fermentation process are mainly from the genus Clostridium, but other microorganisms, such as those from the genera Acetobacteria, Butyribacterium, Desulfobactrium, Moorella, Oxobacter or Eubacteria, can also be used to carry out this fermentation process. Microorganisms are therefore chosen to direct the production of desired products during the fermentation stage. Fermentation products can include, for example, alcohols and acids For example, various patents describe strains capable of producing the aforementioned products of interest from synthesis gas. Among the acetogenic strains of the genus Clostridium, one can cite patent US5173429 describing a strain of Clostridium ijungdahlii (ATCC 49587) producing ethanol and acetate. Other strains of the same species are described in documents WO 2000 / 68407, EP1 17309, patents US5173429, US5593886 and US6368819, W01998 / 00558 and WO2002 / 08438. Some Clostridium strains, such as Clostridium autoethanogemim, are also described. (DSM 10061 and DSM 19630) described in documents WO2007 / 1 17157 and WO2009 / 151342, Clostridium ragsdalei (P1 1 , ATCC BAA-622) described in patent US7704723 or Clostridium carboxidivorans (ATCC PTA-7827) described in patent application US2007 / 0276447, are also capable of producing molecules of interest from gases (H2, CO and / or CO2) by fermentation Le ou lesdits microorganisms ou souches acetogenes utilisés dans l'étape fermentaire du procédé selon l'invention sont de préférence choisies parmi les microorganismes suivants : Acetogenium kivui, Acetoanaerobium noterae, Acetobacterium woodii, Alkalibaculum bacchi CP1 1 (ATCC BAA-1772), Blautia producta, Butyribacterium methylotrophicum, Caldanaerobacter subterraneous, Caldanaerobacter pacificus subterranean, hydrogeno / ormans Carboxydothermus, Clostridium aceticum, Clostridium acetobutylicum, Clostridium acetobutylicum P262 (DSM 19630 from DSMZ Germany), Clostridium autoethanogenum (DSM 19630 from DSMZ Germany), Clostridium autoethanogenum (DSM 10061 from DSMZ Germany), Clostridium autoethanogenum (DSM 23693 from DSMZ Germany), Clostridium autoethanogenum (DSM 24138 from DSMZ Germany), Clostridium carboxydivorans P7 (ATCC PTA-7827), Clostridium coskatii (ATCC PTA- 10522), Clostridium drakei, Clostridium Ijungdahlii PETC (ATCC 49587), Clostridium ERI2 Ijungdahlii (ATCC 55380),Clostridium Ijungdahlii C-01 (ATCC 55988), Clostridium Ijungdahlii O- 52 (ATCC 55889), Clostridium magnum, Clostridium pasteurianum (DSM 525 from DSMZ Germany), Clostridium ragsdali P1 1 (ATCC BAA-622), Clostridium scatologenes, Clostridium thermoaceticum, Clostridium ultunense, Desulfotomaculum kuznetsovii, Eubacterium limosum, sulfurreducens Geobacter, Methanosarcina acetivorans, Methanosarcina Barken, Morrella thermoacetica, Morrella thermoautotrophica, Oxobacter pfennigii, Peptostreptococcus productus, Ruminococcus productus, Thermoanaerobacter kivui, and mixtures thereof., Furthermore, it should be understood that other microorganisms capable of assimilating H2, CO2 (also called carboxydotrophs), and / or CO2 as a carbon source can also be used in step e) of the present invention. All the microorganisms mentioned above are anaerobic, meaning they cannot grow in the presence of oxygen. However, aerobic microorganisms can also be used, such as microorganisms belonging to the species Escherichia coli. For example, a publication has demonstrated the possibility of creating a genetically modified strain to express the genes encoding the enzymes responsible for assimilating H2. CO (genes of the Wood-Ljungdahl metabolic pathway to produce molecules of interest, such as isopropanol, from an important metabolic intermediate: acetyl CoA (Trawick, JD; Burk, MJ; Burgard, AP Microorganisms and Methods for Conversion of Syngas and Other Carbon Sources to Useful Products. Patent WO2010 / 071697). Burk, M.; Schilling, CH.; Burgard, A.; Trawick, JD Methods and Organisms for Utilizing Synthesis Gas or Other Gaseous Carbon Sources and Methanol. Patent WO2009 / 094485). Other genetically modified microorganisms have been described to produce isopropanol, such as the microorganism C.Ijungdhalii (US2012 / 0252083; Lanzatech) In preferred embodiments, microorganisms are selected from Clostridium autoethanogenum, Clostridium Ijungdahlii, Clostridium aceticum, Morella thermoacetica, Acetobacterium woodi and Alkalibaculum bacchi for the production of ethanol and / or acetate, Clostridium autoethanogenum, Clostridium Ijungdahlii and C. ragdalei for the production of 2,3 Butanediol and Clostridium carboxidivorans, Clostridium drakei, Clostridium scatologenes or Butyribacterium methylotrophicum for the production of butyrate and butanol. Cultures comprising a mixture of two or more microorganisms can also be used. The fermentation step e) can advantageously be carried out aerobically or anaerobically, and preferably anaerobically. The fermentation step e) is advantageously implemented in one or more reactors or "bioreactors". The term "bioreactor" includes a fermentation device consisting of one or more tanks or tube reactors, including devices such as CSTR or Continuous Stirred Tank Reactor according to Anglo-Saxon terminology, ICR or Immobilized Cell Reactor according to Anglo-Saxon terminology, TBR or Trickle Bed Reactor, Gas Lift type fermenter, bubble columns, or membrane reactor such as the HFMBR or Hollow Fibre membrane Bio-Reactor system according to Anglo-Saxon terminology, a static mixer, or any other suitable device for gas-liquid contact. The portion of the purge effluent from step d) containing carbon monoxide (CO) and carbon dioxide (CO2) used as feedstock for fermentation step e) is introduced into the fermentation reactor(s) as a gaseous substrate. Each fermentation reactor contains a culture medium. Preferably, the required concentration of gaseous substrate from the purge (CO, CO2, H2) in the culture medium of said fermentation reactor(s) is at least 2.5 mmol / L of CO and / or CO2. 2. The portion of said purge effluent from step d) used as feed for the fermentation step e) is brought into the fermentation reactor(s) in the form of a gaseous substrate advantageously containing a substantial amount of CO, preferably between 2 and 100% by weight of CO, preferably between 20% and 100% by weight of CO, most preferably between 30% and 95% by weight of CO, most preferably between 35% and 80% by weight of CO, and even more preferably between 40% and 60% by weight of CO. Preferably, the portion of said purge effluent from step d) used as feed for fermentation step d) in the form of gaseous substrate advantageously has a mass ratio of H2 / CO between 0 and 1.2 and preferably between 0.5 and 1.2 and most preferably between 0.5 and 1.1 or H2 / CO2 between 0 and 1.7 and preferably between 1 and 1.7 and most preferably between 1.2 and 1.6. According to a preferred embodiment, the fermentation step e) includes a propagation chain for an acetogenic strain to provide a sufficient quantity of cells to inoculate one or more primary reactors, said propagation chain comprising: i) inoculation of the acetogenic strain into a first propagation reactor providing a minimum density of viable cells for a second propagation reactor having a larger volume, and ii) growth of said acetogenic strain in the second reactor to provide a cell density suitable for inoculating a third propagation reactor, the largest in volume. If necessary, the propagation chain may include a larger number of propagation reactors. The fermentation stage also includes a production stage in which the fermentation process is optimal, i.e., in which the molecules of interest are produced in large quantities. The stream comprising at least one oxygenated compound as claimed is therefore produced in said production stage. Preferably, the propagation step can be implemented in one or more microorganism propagation reactors, with all of these reactors connected to allow the transfer of the microbial culture. One or more "production" reactors in which the fermentation process takes place are also implemented. Acetogenic microorganisms or strains are generally cultured until an optimal cell density is reached for inoculating production reactors. This inoculum level can vary from 0.5% to 75%, allowing for larger production reactors than propagation reactors. Thus, the propagation reactor can be used to seed several other, larger production reactors. In the case where the fermentation stage includes a propagation stage and a production stage, the gaseous effluent comprising carbon monoxide (CO) and carbon dioxide (CO2) can advantageously be introduced into the fermentation stage at the reactors of the production stage. At least one additional carbon substrate can advantageously be used in combination with the gaseous substrates from separation step b) to grow the microorganisms in the propagation step. This carbon substrate can advantageously be selected from among n monosaccharides such as glucose, fructose, or xylose; polysaccharides such as starch, sucrose, lactose, or cellulose; metabolic intermediates such as pyruvate; or any other carbon substrate known to those skilled in the art to be assimilated by the microorganisms used in the process. This carbon substrate can also be a mixture of two or more of these carbon substrates. Control of the operating conditions is also necessary to optimize the implementation of the fermentation step.For example, Lowe et al. (Microbiological Review, 1993, 57: 451-509) and Henstra et al. (Current Opinion in Biotechnology, 2007, 18: 200-206) summarize the optimal operating conditions, in terms of temperature and pH, for growing microorganisms used in the fermentation process. pH is one of the most important factors for the fermentative activity of the microorganisms used in the process. Preferably, fermentation step d) is carried out at a pH between 3 and 9, preferably between 4 and 8, and even more preferably between 5 and 7.5. Temperature is also an important parameter for improving fermentation, as it influences both microbial activity and the solubility of the gases used as a substrate. The choice of temperature depends on the microorganism used; some strains are capable of growing under moderate temperature conditions (mesophilic strains), while others require high temperatures (thermophilic microorganisms). Preferably, fermentation step e) is carried out at a growth temperature between 20 and 80°C. Preferably, fermentation step c) is carried out at a growth temperature between 20 and 40°C for mesophilic strains, and preferably between 25 and 35°C and between 40 and 80°C for thermophilic strains, and preferably between 50 and 60°C. The oxidation-reduction potential (also known as the "redox potential") is also an important parameter to control in the fermentation process. The redox potential is preferably less than -450 mV and ideally between -150 and -250 mV. The said fermentation step c) is also advantageously implemented at a pressure between 0.1 and 0.4 MPa. The nutrient medium or culture medium of the fermentation stage may advantageously contain at least one reducing agent in order to improve the performance of the fermentation process by controlling the redox potential of the fermentation stage. The nutrient medium may also include minerals, vitamins, metallic cofactors, or metals specific to the metalloenzymes involved in the gas conversion pathways to products of interest. Suitable anaerobic nutrient media for ethanol fermentation using CO₂ and / or CO₂ as the sole carbon source(s) are known to those skilled in the art. For example, suitable media are described in US patents 5173429 and 5593886 and WO02 / 08438, WO2007 / 115157 and WO2008 / 115080, or in the publication by JR Phillips et al. (Bioresource Technology 190 (2015) 114-121). The composition of the nutrient medium must allow for efficient conversion of the gaseous substrate into the molecule of interest. This conversion is advantageously at a minimum of 5% and can go up to 99%, preferably from 10 to 90%, and preferably from 40 to 70%. The nutrient medium may contain at least one or more nitrogen sources, one or more phosphorus sources, and one or more potassium sources. The medium A nutrient medium may include one or any combination of these three compounds, and importantly, the medium must include all three. The nitrogen source may be chosen from ammonium chloride, ammonium phosphate, ammonium sulfate, ammonium nitrate, and mixtures thereof. The phosphorus source may be chosen from phosphoric acid, ammonium phosphate, potassium phosphate, and mixtures thereof. The potassium source may be chosen from potassium chloride, potassium phosphate, potassium nitrate, potassium sulfate, and mixtures thereof. The nutrient medium may also include one or more metals such as iron, tungsten, nickel, cobalt, magnesium, sulfur, and thiamine. The medium may include any one of these components, or any combination thereof, and, importantly, all of these components. The iron source may be chosen from ferrous chloride, ferrous sulfate, and mixtures thereof. The tungsten source may be chosen from sodium tungstate, calcium tungstate, potassium tungstate, and mixtures thereof. The nickel source may include a nickel source chosen from the group consisting of nickel chloride, nickel sulfate, nickel nitrate, and mixtures thereof. The cobalt source may be chosen from cobalt chloride, cobalt fluoride, cobalt bromide, cobalt iodide, and mixtures thereof.The magnesium source can be chosen from magnesium chloride, magnesium sulfate, magnesium phosphate, and mixtures thereof. The sulfur source can include cysteine, sodium sulfide, and mixtures thereof. The fermentation step e) can also advantageously be implemented as described in patent applications WO2007 / 1 17157, WO2008 / 1 15080, US6340581, US6136577, US 5593886, US5807722 and US5821 1 1 1. As mentioned previously, the optimal operating conditions for carrying out this fermentation step depend in part on the microorganism(s) used. The most important parameters to control include pressure, temperature, gas and liquid flow rates, pH of the medium, redox potential, stirring speed, and inoculum level. It is also necessary to ensure that the gaseous substrate concentrations in the liquid phase are not limiting. Examples of suitable operating conditions are described in patents WO02 / 08438, WO07 / 1 17157, and WO08 / 1 15080. The ratio between Iα2 and the gaseous substrates CO and CO2 can also be important for controlling the nature of the Alcohols produced by fermentative microorganisms. For example, patent application W012 / 131627 describes how, depending on the hydrogen content, it is possible to produce either ethanol alone or ethanol and 2,3-butanediol if the H2 percentage is less than 20% (by volume). The typical composition of the blowdown gas feeding the production reactors would advantageously allow for the production of 2,3-butanediol and ethanol by Clostridium autoethanogenum. Preferably, fermentation should be carried out at a pressure higher than ambient pressure. A pressure higher than ambient pressure substantially increases the gas transfer rate in the liquid phase, allowing it to be assimilated by the microorganism as a carbon source. This operation notably reduces the retention time (defined as the volume of liquid in the bioreactor divided by the inlet gas flow rate) in the bioreactor and thus improves the productivity (defined as the number of grams of molecules of interest produced per liter per day of production) of the fermentation process. Examples of productivity improvements are described in patent WO02 / 08438. According to the invention, said fermentation step e) produces a fermentative liquid stream comprising at least one stream comprising at least one oxygenated compound selected from alcohols having 2 to 6 carbon atoms, diols having 2 to 4 carbon atoms, acid alcohols having 2 to 4 carbon atoms, carboxylic acids having 2 to 6 carbon atoms, aldehydes having 2 to 12 carbon atoms and preferably 2 to 6 carbon atoms, ketones having 3 to 12 carbon atoms and preferably 3 to 6 carbon atoms and esters having 2 to 12 carbon atoms and preferably 2 to 6 carbon atoms, alone or in mixture. Preferably, alcohols with 2 to 6 carbon atoms are chosen from ethanol, n-propanol, isopropanol, butanol, isobutanol, and hexanol; diols with 2 to 4 carbon atoms are chosen from 2,3-butylene glycol (butane-2,3-diol); acid alcohols with 2 to 4 carbon atoms are preferably lactic acid; carboxylic acids with 2 to 6 carbon atoms are chosen from acetic acid, propionic acid, butyric acid, pyruvic acid, levulinic acid, and hexanoic acid; and aldehydes with 2 to 12 carbon atoms are chosen from ethanal, propanal, butanal, pentanal, 3-methylbutanal, hexanal, furfural, and glyoxal. alone or in mixtures, ketones having 3 to 12 carbon atoms and preferably 3 to 6 carbon atoms are chosen from acetone, butanone, cyclohexanone, acetophenone and acetylacetone, alone or in mixture and esters having 2 to 12 carbon atoms and preferably 2 to 6 carbon atoms are selected from methyl formate, methyl acetate, methyl propanoate, methyl butanoate, methyl pentanoate, ethyl acetate, propyl acetate, isopropyl acetate, butyl acetate, isobutyl acetate, and butyl butyrate, alone or in mixture. Preferably, the fermentative liquid stream comprises at least one stream comprising at least one oxygenated compound selected from ethanol, n-propanol, isopropanol, butanol, isobutanol, hexanol, acetic acid, butyric acid, hexanoic acid, lactic acid, acetone, butanone and 2,3-butylene glycol (butane-2,3-diol), alone or in mixture. The said fermentative liquid stream produced by the fermentative step e) also advantageously contains nutrient medium, molecules of interest (alcohols, acid alcohols, acids), i.e. a stream of oxygenated compounds as described above and bacterial cells. Hydrogen may advantageously be introduced or not in said fermentation step c) in the case where the composition of the feed supplying said step does not contain a sufficient quantity of hydrogen. The use of a gaseous substrate low in H2 leads to significant acid production. Indeed, as mentioned previously, the addition of hydrogen improves the conversion of CO present in the fermentation medium into alcohols (according to the balanced equations of Bertsch and Muller Biotechnol Biofuels (2015) 8:210: 6 CO→ 1 ethanol + 4 CO2 then 6 H2 + 2 CO2 → 1 ethanol + 0.3 ATP) and promotes CO2 conversion.The supplementary hydrogen can advantageously come from any process that allows the production of hydrogen, such as, for example, a steam reforming process or a catalytic reforming process, water electrolysis, alkane dehydrogenation, and its hydrogen purity is most often between 75 and 99.9% by volume. Optional separation step f). The said fermentative liquid stream produced by the fermentative step e) is advantageously separated in a step f) so as to obtain said stream of oxygenated compounds. The process according to the invention optionally includes a step f) of separating said fermentative stream obtained at the end of step e) into at least said stream comprising at least one oxygenated compound, an aqueous fraction, and an unreacted gaseous effluent. Preferably, the separated aqueous fraction consists mainly of water. Preferably, the unreacted gaseous effluent comprising non-condensable gases and preferably carbon monoxide and carbon dioxide which have not reacted during the fermentation step e). This separation step is advantageously implemented by separation methods known to a person skilled in the art. In a preferred embodiment, the separation step f) can advantageously be carried out with steam according to techniques known to those skilled in the art. In particular, said separation is advantageously carried out using water vapor from step a) of catalytic pyrolysis. Water vapor can advantageously be generated by the combustion of coke and char in the regenerator and recovered via a hot catalyst cooler or "cat-cooler" according to Anglo-Saxon terminology. In this embodiment, the energy required for separation is therefore supplied by the catalytic pyrolysis step, which strengthens the synergy between the two process steps. The stream of oxygenated compounds produced by the fermentation step and separated from the fermentative liquid stream in separation step f) can also advantageously be separated into different streams comprising the molecules of interest. For example, the various alcohols produced contained in the aforementioned stream of oxygenated compounds can be recovered by processes such as distillation or fractional evaporation. Examples of such processes include those described in WO2007 / 1 17157, WO2008 / 1 15080, US6340581, US6136577, US5593886, US5807722 and US5821 1 1 1. The distillation of alcohol from the fermentative liquid stream from step e) can advantageously be carried out after passing through a beer column, allowing for the production of concentrated alcohols and the possible recycling of acids and other molecules that can be re-assimilated by the microorganism(s) used in the fermentation step. The alcohol stream can then be processed via various distillation columns, allowing for the selective or non-selective separation of the different alcohols present. To this end, it is possible to use alcohol dehydration techniques, including molecular sieves, which are well known to those skilled in the art. The fermentation step e) therefore allows the obtaining of a stream of oxygenated compounds as described above, said stream, advantageously separated from the strain, comprising between 0.1 and 99.9% water and between 99.9 and 0.1% alcohols, diols and / or carboxylic acids and preferably between 30 and 98% water and between 2 and 70% alcohols, diols and / or carboxylic acids. According to a highly preferred embodiment of the invention, no stream from the fermentation step e) is recycled into said catalytic pyrolysis step a) and preferably said stream of oxygenated compounds is not recycled into the catalytic pyrolysis step a). Optional recycling step g) The process optionally includes a step g) of recycling in step a) of catalytic pyrolysis of at least a part of said unreacted gaseous effluent from step e) of fermentation and optionally separated in step f) of optional separation. The unreacted gaseous effluent from step f) of optional separation of the fermentation stream advantageously comprising carbon monoxide and carbon dioxide. The composition of said unreacted gaseous effluent is identical to the composition of the portion of said purge effluent from step d) used as feedstock for fermentation step e). Preferably, the unreacted gaseous effluent from step f) comprises a carbon monoxide content of between 2 and 100% by weight of CO, preferably a content of between 20% and 100% by weight of CO, most preferably between 30% and 95% by weight of CO, more preferably between 35% and 80% by weight of CO, and even more preferably between 40% and 60% by weight of CO, the percentages being expressed as a mass percentage relative to the total mass of the effluent. Preferably, the unreacted gaseous effluent from step f) advantageously has an H2 / CO mass ratio between 0 and 1.2 and preferably between 0.5 and 1.2 and most preferably between 0.5 and 1.1 or H2 / CO2 between 0 and 1.7 and preferably between 1 and 1.7 and most preferably between 1.2 and 1.6. The unreacted gaseous effluent from step f) of optional separation of the fermentation stream also advantageously comprises hydrogen, light O1-C4 gases, olefins and may also contain a low level of aromatic impurities such as for example in benzene and toluene. The sum of the content of elements composing said effluent is equal to 100%. Preferably, the unreacted gaseous effluent from the fermentation step, and possibly separated in step f), is recycled, preferably via a compressor, to the catalytic pyrolysis step a). This gaseous stream then serves as the feedstock entrainment fluid in the reactor. Furthermore, the unreacted non-condensable gaseous effluent from the fermentation stage and recycled in the catalytic pyrolysis stage has a higher hydrocarbon partial pressure compared to the prior art, which allows for improved BTX production in the catalytic pyrolysis stage. Description of the figures: Figure 1 illustrates the process according to the invention in the preferred embodiment in which the stream of oxygenated compounds produced in the fermentation step is not recycled in the catalytic pyrolysis step. In Figure 1, biomass is introduced via line 1 into a catalytic pyrolysis reactor operating in a fluidized bed A. The gaseous effluent from catalytic pyrolysis is then sent via line 2 to a fractionation section B in order to recover a non-condensable gaseous effluent, comprising at least carbon monoxide (CO) and carbon dioxide (CO2) via line 6, a liquid cut called BTX via line 3, a heavy liquid cut comprising mainly compounds with a number of carbon atoms greater than 9, via line 4 and water via line 5. Combustion fumes are also drawn from the pyrolysis reactor via pipe 9. At least part of said gaseous effluent comprising carbon monoxide (CO), and carbon dioxide (CO2) is recycled via a compressor C, into the reactor of the catalytic pyrolysis stage via line 8. A purge of said recycled gaseous effluent is carried out via line 7 upstream of compressor C. The purge of said recycled gaseous effluent is then sent via line 7 to a fermentation stage D, producing a fermentative liquid stream comprising at least one stream including at least one oxygenated compound withdrawn via line 10. The fermentation stage D also includes the separation of the resulting fermentative liquid stream into a stream comprising at least one oxygenated compound withdrawn via pipe 10, water withdrawn via pipe 12 and a non-condensable gaseous stream comprising unreacted CO and CO2, withdrawn via pipe 11. The invention is illustrated by the following examples which are in no way limiting. Example 1: Comparative: catalytic pyrolysis without introduction of a flow of oxygenated compounds. Example 1 presents the case of a catalytic pyrolysis of a pine variety with a capacity of 2500 tonnes per day. A portion of the non-condensable gaseous effluent, containing at least CO and CO2, is recycled into the catalytic pyrolysis reactor and separated from the pyrolysis gaseous effluent. Biomass is introduced into the catalytic pyrolysis reactor at a rate of 104 tonnes per hour. The recycled biomass-to-biomass mass ratio is 1.5 to achieve the desired hydrodynamic conditions. In this example, the catalyst used is a commercial ZSM5 with a crystal content of 40%. The reactor is operated at a temperature of 580°C, under a pressure of 0.2 MPa abs and under a catalytic VVH of 0.3 h-1. Under these conditions the BTX yield is 15% by weight relative to the dry load excluding ash. Example 2: according to the invention Example 2 corresponds to the case of catalytic pyrolysis carried out under the same operating conditions as those of Example 1, but in which the purge of the non-condensable gaseous effluent, comprising at least CO and CO2, is sent to a fermentation unit. This purge constitutes the feed for the fermentation stage and corresponds to a gaseous substrate flow of 33 tonnes per hour with the composition shown in Table 1. Table 1: Composition of the purge constituting the charge of the fermentation unit. The fermentation step is carried out using a strain of Clostridium lungdahlii specifically allowing the conversion of CO₂ to ethanol under the following operating conditions: The percentage of CO contained in the gaseous substrate arriving in the fermentation process is 50% by weight and the growth medium of the microorganism is PETC medium (American Type Culture Collection (ATCC) medium 1754). The fermentation stage is fed by the gaseous substrate flow described above and is conducted at atmospheric pressure, with agitation at 300 rpm, at a temperature of 39°C, at a pH regulated between 5.5 and 6.0, and at a redox potential of -250 mV. It includes an initial phase of microorganism production through a propagation chain resulting in a sufficient quantity of microorganisms to inoculate the production reactors. The production process results in the generation of a fermentative liquid stream separate from the strain extracted from the reactor. This fermentative liquid comprises 94% water by weight, 5% ethanol by weight, and 1% residual acetic acid by weight. The alcohols, primarily ethanol, contained in this stream are recovered by distillation, yielding an azeotropic fraction containing 95% alcohols. Thus, a total production of 8.5 tons of ethanol per hour is generated, corresponding to a yield of approximately 8% by weight relative to the dry biomass excluding ash. According to this embodiment of the invention, a high value-added product is generated in addition to the BTX fraction, from the CO₂ ultimately intended for combustion, which significantly improves the overall profitability of the system. Example 3: according to the invention Example 3 corresponds to the case of a catalytic pyrolysis carried out under the same operating conditions as those of example 1 but for which the purge of the non-condensable gaseous effluent comprising at least CO and CO2 is sent to a specific fermentation unit allowing the conversion of CO into ethanol and 2,3 butanediol. The purge in question corresponds to a gaseous substrate flow of 33 tonnes per hour with the same composition as in Example 3 and shown in Table 1. Compared to example 3, the fermentation step is carried out using a Clostridium autoethanogeum DSMZ 10061 strain specifically allowing the conversion of CO to ethanol and 2,3-butanediol under the following operating conditions: The percentage of CO₂ in the gaseous substrate entering the fermentation process is 50%, and the percentage of hydrogen is 0.5%. The growth medium is defined as follows: Growth and alcohol production medium: Per liter of medium Solution 1 (MgCl2.6H20 10 g / L, CaCl2.2H20 15 g / L): 8.33 mL Solution 2 (NaCL 12 g / L, KCl 15 g / L): 8.33 mL CH3COONH43.00 g Resazurine solution (1 g / L): 1.00 mL Metals solution 1:1 mL Metals solution 2: 1 mL Sodium tungstate solution (2.94 g / L): 0.1 mL Vitamin solution: 10.00 mL Composition of metal and vitamin solutions Metals solution 1 (Per liter) FeSO4.7H2O: 0.10 g ZnSO4.7H2O: 0.20 g NiCl2.6H20: 0.02 g HCI (38%): 30 mL Metals solution 2 (Per liter) MnSO4. H2O: 0.5 g CoCl2.6H20: 0.5 g Na2SeO3: 0.02 g HCI (38%): 5 ml Vitamin solution (per liter) Biotin: 20 mg Folic acid: 20 mg Pyridoxine: 10 mg Thiamine: 50 mg Riboflavin: 50 mg Vitamin B3: 50 mg Pantothenic acid: 50 mg Vitamin B12: 50 mg Para-aminobenzoate: 50 mg Lipoic acid: 50 mg The fermentation stage is fed by the gaseous substrate flow described above and is conducted at atmospheric pressure, at a temperature of 37 < C, a pH regulated at 5.3 by NH4OH, a redox potential maintained at -250 mV and a sulfur supply provided by additions of Na2S. It includes a first phase of microorganism production through a propagation chain resulting in a sufficient quantity of microorganisms to inoculate the production reactors. The production process results in the generation of a fermentative liquid stream separate from the culture extracted from the reactor. This fermentative liquid comprises 95% by weight water, 4.2% by weight ethanol, and 0.8% by weight 2,3-butanediol. These alcohols are then recovered by distillation, yielding an azeotropic cut containing 95% alcohols. Thus, a total production of 6.9 tonnes of ethanol and 1.4 tonnes of 2,3 butanediol per hour is generated, which corresponds to a yield of approximately 6.6% and 1.3% by weight relative to the dry biomass excluding ash, respectively, for Γ ethanol and 2,3 butanediol. As with Example 2, producing additional value-added products from CO intended for combustion significantly improves the overall profitability of the system. According to this alternative embodiment of the invention, alcohol production can vary depending on the fermentation process implementation, allowing for greater flexibility and a closer approximation of the economic optimum.

Claims

------03 / 05 / 2017------(OCR) Page 1 of 3 Claims 1. A process for the production of BTX and alcohol from biomass, which includes at least the following steps: a) Catalytic pyrolysis of such biomass in a fluidized-bed reactor producing gaseous pyrolysis effluent; b) Separation of such gaseous pyrolysis effluent into at least one fraction of BTX and a gaseous effluent consisting of at least carbon monoxide and carbon dioxide; c) Recycling of at least one fraction of such gaseous effluent consisting of With at least carbon monoxide and carbon dioxide introduced into the reactor in step a), d) the gaseous eluent is recycled in step c) to produce eluent, e) at least a portion of the eluent from step d) is sent into the fermentation step, which produces a liquid fermentation stream consisting of at least one stream containing at least one oxygenated compound selected from alcohols with 2 to 6 carbon atoms, diols with 2 to 4 carbon atoms, acid alcohols with 2 to 4 carbon atoms.

2. The process according to claim 1, in which the catalytic pyrolysis step a) occurs with the presence of a zeolite catalyst comprising at least one selected zeolite from ZSM-5, ferriride, beta zeolite, y zeolite, mordenide, ZSM-23, ZSM-57, EU-1 and ZSM-11, whether doped with a selected metal from iron, gallium, zinc and lanthanum or 3. Any process under claim 1 or 2, in which the catalytic pyrolysis step a) is carried out at a temperature between 400 and 1000°C, at an absolute pressure between 0.1 and 0.5 MPa and at a WHSV between 0.01 and 10 hours-1 page 2 of number 3.

4. Any process under claim 1 to 3, in which the fermentation step e) is carried out with at least one microorganism selected from the following microorganisms: Acetogenium kivui, Aceto anerobium noterae, Acetobacterium woodii, Alkaliba culumbacchi CP11 (ATCCBAA-1772), Blautia producta,Butyribacteriummethylotrophicum, Caldanaerobactersubterraneous, Caldanaerobacterpaci / icussubterraneous, hydrogeno / ormansCarboxydothermus, Clostridiumaceticum, Clostridiumacetobutylicum, ClostridiumacetobutylicumP262(DSM19630 from DSMZGermany), Clostridiumautoethanogenum(DSM19630 from DSMZGermany), Clostridiumautoethanogenum(DSM10061 from DSMZGermany), Clostridiumautoethanogenum(DSM23693 from DSMZGermany), Clostridiumautoethanogenum(DSM24138 from DSMZGermany), ClostridiumcarboxidivoransP7(ATCCPTA-7827), Clostridiumcoskat ii(ATCCPTA-10522),Clostridium drakei,ClostridiumljungdahliiPETC(ATCC49587),ClostridiumERI2ljungdahlii(ATCC55380),ClostridiumljungdahliiC-Ol(ATCC55988),Clostridiumljungdahlii0-52(ATCC55889),Clostridium magnus,Clostridium pasteurianum(DSM525 from DSMZGerman y),Clostridium ragsdaliPlI(ATCCBAA-622),Clostridiumscatologenes,Clostridiumthermoaceticum,ClostridiumνItunense,Desul / otomaculumkuznetsovii,Eubacteriumlimosum,sul / urreducensGeobacter,Methanosarcinaacetivorans,MethanosarcinaBarken,Morrellathermoacetica,Morrella thermoautotrophica, Oxobacter p / ennigii, Peptostreptococcus productus, Ruminococcus productus, Thermoanaerobacter kivui, and mixtures of them.

5. Process according to claim 4, in which microorganisms were selected from Clostridium autoethanogenum, Clostridium ljungdahlii, Clostridium aceticum, Morrella thermoacetica, Acetobacterium woodii and Alkaliba culumbacchi for the production of ethanol and / or acetate, Clostridium autoethanogenum, Clostridium ljungdahlii and C. ragdalei for the production of 2,3-butanediol and Clostridium carboxidivorans, Clostridium dra. kei, Clostridium scatologenes, or Butyribacterium methylotrophicum for the production of butyrate and butanol; cultures consisting of a mixture of two or more microorganisms may also be used.

6. Any of the processes of claims 1 to 5, in which the fermentation step e) is carried out at a growth temperature between 20 and 80°C, at an absolute pressure between 0.1 and 0.4 MPa and at a pH between 3 and 9. Page 3 of 3 of 7. Any of the processes of claims 1 to 6, in which alcohols with 2 to 6 carbon atoms are selected from ethanol, n-propanol,Isopropanol, butanol, isobutanol, and hexanol; diols with 2 to 4 carbon atoms are selected from 2,3-butylene glycol (2,3-butanediol); acid alcohols with 2 to 4 carbon atoms, preferably lactic acid; carboxylic acids with 2 to 6 carbon atoms are selected from acetic acid, butyric acid, and hexanoic acid; aldehydes with 2 to 12 carbon atoms are selected from ethanal, propanal, butanal, pentanal, 3-methylbutanal, hexanal, furfural, and glyoxal, alone or in mixtures; detones with 3 to 12 carbon atoms are selected from acetone, butanone, and cyclohexanone.

8. The process according to claim 7, in which a current containing at least one oxygenated compound is included, is including ethanol, n-propanol, isopropanol, butyl acetate, and esters with 2 to 12 carbon atoms, and preferably 2 to 6 carbon atoms, are selected from methyl formate, methyl acetate, methyl propionate, methyl butanoate, methyl pentanoate, ethyl acetate, propyl acetate, isopropyl acetate, butyl acetate, isobutyl acetate, and butyl butyrate, alone or in mixtures.Isobutanol, hexanol, acetic acid, butyric acid, hexanoic acid, lactic acid, acetone, butanone and 2,3-butylene glycol (2,3-butanediol), alone or as a mixture.

9. Any process under claims 1 to 8, in which hydrogen supplement may be selectively introduced into the fermentation step e) as described above.

10. Any process under claims 1 to 9, in which step f) the separation of the fermentation stream obtained after step e) into at least such stream which contains at least the compounds that were 11. A process under claim 10, in which the separation step f) is performed using steam generated from the catalytic pyrolysis step a).

12. A process under claim 10 or 11, in which the oxygenated compound stream, separated according to summary step e), is not recycled back into the catalytic pyrolysis step a). ------------ Page 1 of 3 pages of claims 1. Process for the production of BTX and alcohols from biomass.This process involves at least the following steps: a) catalytic pyrolysis of the biomass in a fluidized-bed reactor, which produces a gaseous pyrolysis effluent; b) separation of the gaseous pyrolysis effluent into at least one BTX fraction and a gaseous effluent containing at least carbon monoxide and carbon dioxide; c) recycling at least the gaseous effluent containing at least carbon monoxide and carbon dioxide into the reactor of step a); d) elution of the gaseous effluent recycled in step c) to produce an eluent; e) transferring at least the eluent from step d) into a fermentation stage, which produces a liquid fermentation stream containing at least one stream of at least one oxygenated compound selected from alcohols with 2 to 6 carbon atoms, diols with 2 to 4 carbon atoms, acid alcohols with 2 to 4 carbon atoms, carboxylic acids with 2 to 6 carbon atoms, and aldehydes with 2 to 12 carbon atoms.

1. Ketones containing 3 to 12 carbon atoms and esters containing 2 to 12 carbon atoms, alone or as a mixture.

2. A process under claim 1, in which the catalytic pyrolysis step a) occurs with a zeolite catalyst comprising at least one zeolite of a choice from ZSM-5, ferririte, beta zeolite, zeolide Y, mordenite, ZSM-23, ZSM-57, EU-1 and ZSM-11, whether or not doped with a metal of a choice from iron, gallium, zinc and lanthanum.

3. A process under claim 1 or 2, in which the catalytic pyrolysis step a) is performed at temperatures between 400 and 1000 °C, at absolute pressures between 0.1 and 0.5 MPa and at WHSV between 0.01 and 10 hours-1. Page 2 of 3, page 4. Which of the processes under claims 1 through 3, in which the fermentation step e) is carried out with at least one of the following microorganisms: Acetogenium kivui, Acetoanaerobium noterae, Acetobacterium woodii, Alkalibaculumbacchi CPI1 (ATCCBAA-1772), Blautia producta, Butyribacterium methylotrophicum, Caldanaerobacter subterraneous,Caldanaerobacterpaci / icussubterraneous,hydrogeno / ormansCarboxydothermus,Clostridiumaceticum,Clostridiumacetobutylicum,ClostridiumacetobutylicumP262(DSM19630จากDSMZGermany),Clostridiumautoethanogenum(DSM19630จากDSMZGermany),Clostridiumautoethanogenum(DSM10061จากDSMZGermany),Clostridiumautoethanogenum(DSM23693จากDSMZGermany),Clostridiumautoethanogenum(DSM24138จากDSMZGermany),ClostridiumcarboxidivoransP7(ATCCPTA-7827),Clostridiumcoskatii(ATCCPTA-10522),Clostridiumdrakei,ClostridiumljungdahliiPETC(ATCC49587),ClostridiumERI2ljungdahlii(ATCC55380),ClostridiumljungdahliiC-01(ATCC55988),Clostridiumljungdahlii0-52(ATCC55889),Clostridiummagnum,Clostridiumpasteurianum(DSM525จากDSMZGermany),ClostridiumragsdaliPI1(ATCCBAA-622),Clostridiumscatologenes,Clostridiumthermoaceticum,Clostridiumultunense,Desul / otomaculumkuznetsovii,Eubacteriumlimosum,sul / urreducensGeobacter,Methanosarcinaacetivorans,MethanosarcinaBarken,Morrellathermoacetica,Morrellathermoautotrophica,Oxobacterp / ennigii,Peptostreptococcus productus, Ruminococcus productus, Thermoanaerobacter kivui, and their mixtures.

5. The process according to claim 4, in which microorganisms are identified from Clostridium autoethanogenum, Clostridium ljungdahlii, Clostridium aceticum, Morrelathermoacetica, Acetobacterium woodii and Alkaliba culumbacchi for the production of ethanol and / or acetate, Clostridium autoethanogenum, Clostridium ljungdahlii and C. ragdalei for the production of 2,3-butanediol and Clostridium carboxidivorans, Clostridium drakei, Clostridium 6. Which of the processes in claims 1 through 5, in which the fermentation step e) is carried out at a growth temperature between 20 and 80 °C, at an absolute pressure between 0.1 and 0.4 MPa and at a pH between 3 and 9? 7. Which of the processes in claims 1 through 6, in which alcohols with 2 to 6 carbon atoms are selected from ethanol, t-propanol, isopropanol, butanol, isobutanol and hexanol?Diols with 2 to 4 carbon atoms are selected from 2,3-butylene glycol (2,3-butanediol); acid alcohols with 2 to 4 carbon atoms, preferably lactic acid; carboxylic acids with 2 to 6 carbon atoms are selected from acetic acid, butyric acid, and hexanoic acid; aldehydes with 2 to 12 carbon atoms are selected from ethanol, propanal, butanal, pentanal, 3-methylbutanal, hexanal, furfural, and glioxal, alone or in mixtures; ketones with 3 to 12 carbon atoms... Carbon atoms are selected from acetone, butanone, cyclohexanone, acetopenone, and acetylacetone, alone or in mixtures, and esters containing 2 to 12 carbon atoms, and preferably 2 to 6 carbon atoms, are selected from methylforate, methyl acetate, methylpropionate, methylbutanoate, methylpentanoate, ethyl acetate, propyl acetate, isopropyl acetate, butyl acetate, isobutyl acetate, and butylbutyrate, alone or in mixtures.

8. The process according to claim 7, in which the current contains at least one oxygenated compound, includes ethanol, t-propanol, isopropanol, butanol, isobutanol, hexanol, acetic acid, neutricular acid,9. Any process under claims 1 to 8, in which hydrogen supplementation may be selectively introduced into the fermentation step e); 10. Any process under claims 1 to 9, in which step 1) separates the fermentation stream obtained after step e into at least one stream containing at least one oxygenated compound, an aqueous portion, and an unreacted gaseous outflow; 11. Any process under claim 10, in which such separation step is accomplished using steam generated from the catalytic pyrolysis step a); 12. Any process under claim 10 or 11, in which the oxygenated compound stream separated in accordance with step e) is not recycled into the catalytic pyrolysis step a);