Biomass conversion method and related device

Abstract

The present invention relates to a facility (1) for converting biomass (B) into products such as liquids (L1, L2), gases (G) and solid residues (RS), comprising a temperature regulation system, a circulation device (14) suitable for circulating a conversion mixture (MC), units for filtering the residues and for recovering the liquids, and a conversion tank (13) for the conversion of the biomass, operating at atmospheric pressure, wherein the pressure of the conversion mixture (MC) is locally increased. The present invention further describes a method for the automated conversion of biomass by means of this facility.

Description

Biomass conversion method and associated device Technical field

[0001] The present invention relates to an installation for the treatment and recovery of organic waste, as well as to a method for the production of marketable products based on such organic waste. In particular, the installation and the method are suitable for modular production of marketable products and relocated near organic waste collection points. State of the art

[0002] Many green waste recovery systems are being developed, in particular to produce fuels such as gas or coal. However, the processes used require the application of high pressures using complex and energy-intensive devices. Such facilities also prove to be inflexible in their use, both in the variety of waste processed and in the products extracted from it. Thus, they are sized to process large quantities of organic matter to remain profitable. They are difficult to adapt to market fluctuations.

[0003] Depending on the processes used, additives must often be used, including for example catalysts or other chemical reagents, which represent additional costs and risks for the environment.

[0004] Such facilities also require advanced skills that may not be readily available. As a result of these constraints, the facilities currently in operation can hardly be installed near the most remote sources of green waste.

[0005] There is therefore room for developing new processes and devices allowing greater flexibility in their geographical location and in the diversity of products processed. Brief summary of the invention

[0006] An aim of the present invention is to propose a device or installation, suitable for the conversion of variable quantities of organic matter. In particular, the device or installation according to the present description aims to remain profitable with small quantities of biomass, of the order of a few tens of kilograms up to a few tonnes per day.

[0007] Another aim of the present invention is to provide a device or installation making it possible to process a greater variety of plant material and / or to adjust the quantities and nature of the extracted products according to market needs.

[0008] Another aim of the invention is to propose a device or installation for converting green waste which can be easily relocated near the collection points for the plant materials to be converted.

[0009] Another object of the present invention is to provide a device or installation for converting organic waste making it possible to extract a variety of marketable products from this organic waste, without the need to add additives, catalysts or chemical reagents.

[0010] Another objective of the present invention is to provide a device or installation that is at least partially automated and / or can be controlled remotely.

[0011] Another aim of the present invention is to provide a flexible, inexpensive and relocatable method of converting biomass into marketable products.

[0012] According to the invention, these aims are achieved in particular by means of the installation and the method which are the subject of the independent claims and described in more detail in the claims which depend thereon.

[0013] This solution has the particular advantage over the prior art of treating organic materials close to their collection point and thus limiting their transport and possible degradation into undesirable products. The present solution also has the advantage of greater flexibility in the organic materials treated and in the production of marketable products, thus allowing a more adequate offer in relation to market fluctuations. Brief description of the figures

[0014] Examples of implementation of the invention are indicated in the description illustrated by the following figures: • Figure 1: schematic representation of the installation according to an embodiment of the present invention, • Figure 2: More detailed schematic representation of the installation according to an embodiment of the present invention, • Figure 3: Schematic representation of an example of a reactor used in the installation according to an embodiment of the present invention. Example(s) of embodiment of the invention

[0015] The present installation 1 is suitable for the conversion of biomass B into one or more products that can be recovered on the markets. Such products include, for example, liquids L1, L2, such as organic oils or water-soluble compounds, gases G such as methane or carbon dioxide, and solid materials RS such as vegetable charcoal or other residues from the drying or pyrolysis of biomass B. Liquids L1, L2 include, for example, pyroligneous acid, often referred to as wood vinegar. Pyroligneous acid is itself a mixture of multiple compounds or classes of compounds such as furans, pyrans, carboxaldehydes, sugars, alkyl and aryl esters, catechols, phenols, syringyl or guaiacyl derivatives, vanillin derivatives, various carboxylic acids and other chemical compounds.These products may result from the action of polymeric precursors initiating the cleavage of chemical bonds during the process described here. G gases are of variable composition, depending on the biomass treated and / or the conversion conditions. They mainly comprise carbon dioxide CO2, carbon monoxide CO and their mixture. G gases may also comprise other elements such as methane CH4, hydrogen H2 and / or traces of volatile organic compounds. The gases resulting from the conversion of biomass are commonly referred to as “syngas” or synthesis gas.

[0016] Alternatively or in addition, chemical transformations can take place under the conditions of this method to give rise to new products, which can also be used on the market.

[0017] Installation 1 allows the liquids L1, L2 to be separated from the gases G and the solid residues RS concomitantly, so as to recover these different categories of products in a single operation. The term concomitant must here be understood as designating steps carried out in parallel, during the same period. The liquids L1, L2, or the gases G or the solid residues RS may further undergo one or more further separation operations in order to recover single components or smaller fractions of mixtures. These subsequent operations of separation of products within the same class of products, for example liquids L1, L2, may also be carried out continuously during a single preceding step.

[0018] The various products obtained have a wide variety of applications. They can be used, for example, as pharmaceuticals, as agri-food products, or as raw materials for the production of other high-value-added products. The properties of such products include antioxidants, antimicrobials, anti-inflammatory properties, fertilizers, coagulants, and pesticides.

[0019] Biomass B refers to any plant material, whether natural or derived from agriculture. Preferably, the biomass used for the purposes of the present invention refers to plant materials that are inedible for humans, and advantageously inedible for livestock. Preferably, the biomass B used according to the present description refers to a second-generation biomass, resulting from activities of clearing, cleaning, and maintaining vegetated, urban, agricultural, or forested areas. Thus, biomass B is not collected or produced for the exclusive purposes of the process described here, but consists only of a by-product that would otherwise find no other application. The composition of biomass B may therefore vary depending on its geographical location, its natural or agricultural origin, the season, or multiple other parameters.Biomass B advantageously comprises lignocellulosic components, including lignin, cellulose, and hemicellulose. Preferably, biomass B is rich in organic molecules such as biopolymers, oils, resins, or tannins. Preferably, biomass B is low in moisture, ash or mineral compounds, and heteroatoms such as oxygen, nitrogen, sulfur, and phosphorus.

[0020] According to one embodiment, biomass B comprises or consists of straw, the moisture content of which is less than 15% and the ash content of which is less than 10%.

[0021] Installation 1 according to the present description makes it possible to adapt the process conditions in order to modulate the quantity and / or the quality of the different products contained in biomass B and thus to best respond to market needs, which can fluctuate rapidly.

[0022] The installation 1 according to the present description comprises a conversion unit 10 for converting the biomass into its products or product classes mentioned above. The conversion unit 10 comprises for this purpose a conversion tank 13 or any other container suitable for collecting a content to be treated or converted. The conversion tank 13 is preferably provided with at least one loading device 12 for the biomass B. The loading device 12 thus makes it possible to load the conversion tank mechanically as required. The loading device 12 may take the form of any suitable device such as a conveyor belt, an endless screw, a bucket system, or any equivalent. Preferably, the loading device 12 is suitable for transferring variable quantities of biomass B.In this case, if it is a conveyor belt or an endless screw or any other continuous loading device, the rotation or translation speed can be adapted to the demand so as to convey quantities of biomass B of between a few tens of kilograms and several tonnes per day. If it is a loading bucket, the size, number or frequency of the buckets can be adapted according to the needs. Alternatively, several independent loading devices 12 can be provided and activated on demand, to allow better adaptation of the quantities of biomass B treated.

[0023] According to one embodiment, the biomass B transferred to the conversion unit can be raw, i.e. without prior treatment. The most large elements may at most have been roughly cut to allow loading into the conversion tank 13.

[0024] According to another embodiment, the biomass B may have undergone one or more treatments before being loaded into the conversion unit 10. It may, for example, have undergone pre-drying in the open air or in a thermoregulated environment, have been sorted and / or have been cleaned. For example, the foliage may have been separated from the woody parts.

[0025] The loading device 12 preferably comprises a metering device 11, making it possible to control the flow rate of biomass B transferred into the conversion tank 13. According to one embodiment, the metering device 11 is integrated into the loading device 12. In the case where the loading device 12 is a conveyor belt, an endless screw or any other continuous loading device, the metering device 11 may take the form of a regulator making it possible to control the speed of rotation or translation of such devices so as to meter the quantities of biomass B transferred. Alternatively or in addition, a step-by-step advancement system may be provided. Alternatively, the metering device 11 may be an intermediate device making it possible to collect a predetermined quantity of biomass B from the loading device 12 before transferring it into the conversion tank 13.Any other suitable dosing device may be considered depending on the situation.

[0026] The conversion tank 13 is at atmospheric pressure, that is to say, it does not include any active pressurization system. Nevertheless, the conversion tank 13 is closed so as to remain airtight to the ambient air and in particular to oxygen. Safety valves, not shown, may be provided to prevent overpressure during the transformation of the biomass B without allowing air to enter the conversion tank 13.

[0027] When loading and / or upstream of loading, biomass B is conditioned in an anaerobic environment so as to limit or avoid any presence of gaseous oxygen. According to one embodiment, the loading of biomass B passes through an airlock under an inert atmosphere such as nitrogen. Alternatively, the environment is depressurized to remove the atmosphere. Alternatively, the gases G from the conversion process, or a fraction of these gases, in particular carbon dioxide CO2, are used to maintain the biomass under a non-oxygenated atmosphere before its conversion. Other known means, as well as their combination, can be implemented to maintain biomass B in such an anaerobic environment.

[0028] The conversion unit 10 further comprises at least one circulation device 14 for circulating the biomass B in a circulation loop BC. A circulation device 14 according to the present description designates any suitable means for circulating a fluid mixture in a circuit, such as a turbine, a rotor, a pump or any equivalent. An example of a circulation device 14 is described in more detail below.

[0029] A circulation loop BC designates a circuit comprising the circulation device 14, comprising at least one inlet 15 for accepting the biomass B and at least one outlet 16 for ejecting the biomass B. A circulation loop may further comprise one or more bypasses for redirecting the circulating fluid(s). An inlet 15 is arranged inside the conversion tank 13. An outlet 16 is also arranged inside the conversion tank 13. The remainder of the circuit constituting a circulation loop BC may be outside the conversion tank 13, or inside the conversion tank 13, or partially inside and partially outside the conversion tank 13. According to one embodiment, the circulation device 14 is external to the conversion tank and the remainder of the circuit comprising an inlet 15 and an outlet 16 is arranged in the conversion tank 13.According to such an arrangement, the temperature of the biomass B, in the form of a conversion mixture MC circulating in the circulation loop BC can be maintained close to or equal to the temperature of the conversion mixture MC present in the tank. conversion 13. The length of the circulation loop BC is variable. It is for example determined to allow sufficient acceleration of the conversion mixture MC before its ejection through outlet 16. Other parameters can be considered to determine the length of the circulation loop BC.

[0030] The circulation loop BC may for example comprise several turns included in the conversion tank 13.

[0031] Alternatively, the circulation loop BC can be housed in a double wall of the conversion tank 13 so as to benefit from its temperature without being immersed in the mixture present in the tank 13.

[0032] Other arrangements can be considered depending on needs.

[0033] According to one embodiment, the circulation loop BC comprises a single outlet 16 so that the conversion mixture is precisely ejected into the conversion tank 13 at a predetermined position. Alternatively, the circulation loop BC comprises several outlets 16 arranged in the conversion tank 13, so as to disperse the conversion mixture MC inside the conversion tank 13.

[0034] The outlet(s) 16 of the circulation loop BC may be designed so as to increase the pressure of the conversion mixture MC at this or these outlets, which then act as injectors. The ejection speed of the conversion mixture MC is thus increased and makes it possible to produce a mechanical force within the conversion mixture MC present in the conversion tank 13 resulting in homogenization of the conversion mixture within the conversion tank 13, both from the point of view of its composition and its temperature. In addition, the ejection speed of the conversion mixture through the outlet(s) 16 of the circulation loop BC increases the pressure locally within the conversion mixture 13. This This arrangement thus makes it possible to dispense with a complex and expensive system for overall pressurization. The ejection speed of the MC conversion mixture through the outlet(s) 16 can be modulated, for example, by means of the shape and / or diameter of the outlet(s) 16, or by means of the circulation device 14. According to one embodiment, the outlet(s) can be provided with valves of adjustable diameter or with a diaphragm making it possible to adapt the opening surface between limit values, such as between 0% and 100% of the available opening. The pressure locally obtained in the MC conversion mixture can then be easily adapted according to requirements. The pressure of the MC conversion mixture can, for example, be increased by a factor of the order of 3 to 10 or more. Locally, the pressure of the conversion mixture can thus be of the order of 5, 8, 10 or 12 bars.The provisions described above do not prohibit smaller increases in pressure, by a factor of between 1 and 4, or of the order of 1, 2 or 3. The factor is understood here as a multiplicative value of a reference pressure, which may be the local atmospheric pressure, or a pressure of 1 bar or 1 atmosphere.

[0035] A given circulation loop may contain more than one circulation device 14. According to one embodiment, several circulation devices 14, identical or different, may be arranged in series along the circulation loop BC. Alternatively, a circulation device 14 may contain several stages.

[0036] According to one embodiment, the installation 1 according to the present description comprises several circulation loops BC, each of which may have one or more dedicated circulation devices 14. Alternatively or in addition, a circulation device 14 may be common to several circulation loops BC.

[0037] A circulation loop BC according to the present description makes it possible to circulate a fluid such as a carrier fluid FV, described in more detail below. The carrier fluid FV can be circulated alone in a circulation loop BC, for example to bring it to a temperature of conversion TC or to preheat it to an intermediate temperature before initiating the conversion process, or to fill the conversion tank 13 to a predetermined level before or during the process, or to clean the circuit at the end of the process or for any other reason. A circulation loop BC is however particularly suitable for circulating the biomass B suspended in the carrier fluid FV, together forming a conversion mixture MC during the conversion process.

[0038] The installation according to the present description comprises a liquid recovery unit 20, adapted to collect the vapors from the conversion tank 13 during the conversion process, and to condense them into at least one liquid L1, or even two distinct liquids L1, L2 or more than two liquids. According to one embodiment, the installation 1 according to the present description comprises a gas collector 18 arranged downstream of the conversion unit 10 and adapted to collect the gases from the conversion tank 13. The gas collector 18 makes it possible to conduct the gases to at least a first condensation unit 21 comprising a first condenser 21a and a first collector 21b intended to store a first condensed liquid L1. The liquid recovery unit 20 advantageously comprises a second condensation unit 22, comprising a second condenser 22a and a second collector 22b adapted to collect a second liquid L2.The second condensation unit 22 may be arranged downstream of the first condensation unit 21 so as to condense the gases not yet condensed during their passage through the first condensation unit 21. The temperature of the second condensation unit may be lower than that of the first condensation unit 21 if the gases pass naturally without further heat treatment.

[0039] According to one embodiment, the gases are collected and condensed without heat treatment as soon as they leave the conversion tank 13. Alternatively, one or more of the condensation units 21, 22 can be thermostatically controlled so as to modulate their temperature and thus modify the nature of the collected liquids L1, L2.

[0040] According to one embodiment, the first and second condensing units 21, 22 can be arranged in parallel, supplied by different gas collectors 18 and maintained at different temperatures.

[0041] The liquid recovery unit 20 may comprise more than two condensation units as required. The condensed liquids L1, L2 may have variable compositions depending on the temperatures applied to the conversion process and / or the temperatures of the condensation units 21, 22, the nature of the biomass B, the circulation conditions of the biomass and other factors.

[0042] The uncondensed gases after passing through the condensing unit(s) can be collected and stored as marketable gas G. For example, methane, which will remain in a gaseous state under the process conditions, can be recovered. Depending on the nature of the recovered gas G, they can be used as fuel or for other industrial applications.

[0043] According to one embodiment, the liquid recovery unit 20 may comprise one or more burners 23 adapted to the combustion of non-condensed gases or a portion of these gases. Advantageously, the energy produced by the combustion of these gases may be exploited. For example, a portion of the energy thus produced or all of it may be used in the implementation of the method of the present description, in particular for heating or preheating the conversion mixture MC or the carrier liquid LV.

[0044] Activation of the circulation device 14, when the conversion temperature TC is reached, makes it possible to convert the biomass B according to a continuous process, during which the gases are collected and condensed into one or more liquid fractions in the liquid recovery unit 20. The loading of biomass B via the loading device 12 and the dosing device 11, if applicable, can also be carried out in continuous. The conversion mixture MC, containing the biomass B to be converted, thus circulates so as to continuously convert the biomass B into its liquid and gaseous products to be extracted. The residence time of the most volatile compounds in the conversion tank 13 can be determined using process parameters, such as the circulation speed of the conversion mixture. The less volatile products can remain in solid form and accumulate in the conversion mixture MC.

[0045] According to one embodiment, the residence time of the volatile compounds is less than 10, or 8, or 5, or 3 minutes. Preferably, the residence time of the least volatile products or solid residues is between a few minutes such as 15 minutes and one hour, or of the order of 1 hour, or % of an hour, or 30 minutes, or 20 minutes, or 15 minutes.

[0046] The installation 1 according to the present description further comprises a filtration unit 30, adapted to recover the solid residues resulting from the conversion process described here. The filtration unit 30 comprises at least one filtration device 31. Such a filtration device 31 makes it possible to separate the solid residues RS from the carrier liquid LV in which they are suspended. The solid residues RS are those which remain after evaporation of the most volatile substances under the conditions of the process. The solid residues RS can circulate in the circulation loop BC for a variable time. Alternatively, the solid residues RS are maintained in the conversion tank 13, for example by sedimentation, before being transferred to the filtration unit 30.

[0047] According to one embodiment, the circulation loop BC comprises at least one bypass 17, adapted to extract a portion of the conversion mixture MC to the filtration unit 30. The bypass circuit 17 can be put into operation by means of one or more bypass valves 170. Alternatively or in addition, the conversion tank 13 comprises a drain making it possible to collect the conversion mixture directly in the conversion tank 13 to transfer it to the filtration unit 30.

[0048] A filtration device 31 according to the present invention may comprise one or more porous filtration surfaces, the porosity of which may be adapted according to requirements. Filtration surfaces of different porosities may be arranged in parallel so as to adapt the nature of the solid residue(s) to be obtained. Alternatively, several surfaces of decreasing porosity may be arranged in series so as to best filter all of the solid residue(s). The carrier fluid FV may thus be recovered without contamination or with minimal contamination. The filtration of the solid residue(s) RS may be carried out at atmospheric pressure, by simple gravity. Alternatively, a pressurization system upstream and / or depressurization downstream of the filtration surface(s) may be envisaged.

[0049] According to one embodiment, the vector fluid FV or a portion of the vector fluid resulting from the filtration is returned to the circulation loop BC via a suitable pipe 32. The filtration advantageously takes place in parallel with the biomass conversion process in the conversion unit 10.

[0050] Alternatively, the FV carrier fluid from filtration can be stored separately for later use or for further processing such as rinsing or cleaning.

[0051] According to one embodiment, the filtration unit 30 comprises one or more solvent reservoirs 35, adapted to rinse the solid residue(s) RS during filtration. The solvent(s) make it possible in particular to rid the solid residue(s) RS of the remains of carrier fluid FV in which the biomass B was initially suspended. The carrier fluid FV potentially mixed with a solvent can be transferred to a separator 36 so as to be recovered clean in a carrier fluid reservoir 37 before being recirculated in the biomass conversion process. According to one embodiment, several successive steps can be implemented in the filtration. For example, a first step can consist of the recovery of the carrier fluid FV, which can be directly recirculated for the conversion process. A second step may include rinsing the captured solid residue RS using one or more solvents and recovering the fluids used to separate the remaining carrier fluids and the solvents.

[0052] The installation includes all the means necessary for the transit of materials such as one or more pumps 34, possible fans, turbines, valves and other accessories.

[0053] The installation 1 according to the present invention comprises a thermoregulation system, in particular a heating system making it possible to bring at least the vector fluid FV to a suitable temperature for the conversion process. Advantageously, the thermoregulation system makes it possible to maintain the conversion mixture MC at the suitable temperature throughout the conversion process, and throughout the circuit, in particular the circulation loop BC and the conversion tank 13. According to one embodiment, the thermoregulation system is associated with the conversion tank 13, so that the conversion fluid FV present in the conversion tank can be brought to a suitable temperature before the start of the conversion. When the biomass B is added to the conversion tank 13 to form the conversion mixture MC, the temperature of the conversion tank 13 is controlled by the thermoregulation system.

[0054] According to one embodiment, the circulation loop BC, or a part of the circulation loop BC is associated with the thermoregulation system, so as to bring and maintain the vector fluid FV at an adequate temperature during its circulation.

[0055] According to one embodiment, different portions of the installation can be thermoregulated to different temperatures. For example, the circulation loop BC can be brought to a temperature lower than that of the conversion tank 13 so that the conversion takes place essentially within the conversion tank 13.

[0056] According to one embodiment, the temperature of the installation can be modulated according to the conditions of the conversion process. In this case, it can be increased or decreased according to a pre-established program and / or according to data collected in real time. The thermoregulation system is particularly suitable for heating the FV carrier fluid and / or the conversion mixture to temperatures between 200°C and 400°C.

[0057] According to one embodiment, the conversion temperature is constant and of the order of 310°C.

[0058] The thermoregulation system may for example comprise one or more burners, or one or more electrical resistors, or their combination, arranged so as to directly heat the carrier fluid FV and / or the conversion mixture MC. Alternatively, the thermoregulation system may comprise an independent primary circuit, used to heat the carrier fluid FV and / or the conversion mixture. Some or all of the energy used by the thermoregulation system may come from the gases resulting from the conversion process and burned via the burner 23. Alternatively or in addition, the heating may be produced via an electrical source, or another mineral source such as fuel oil or a renewable energy source.

[0059] Figures 3a and 3b show a circulation device 14 according to an embodiment of the present invention. The circulation device 14 may comprise a drive assembly 140 comprising a rotor 141 and a stator 142. The rotation of the rotor via its drive shaft 143 makes it possible to suck in the fluids from the circuit and put them into circulation. For this purpose, the rotor comprises a drive head 144 nested in a part of the stator 142. The fluids of the circuit, including the vector fluid FV and the conversion mixture MC, are thus forced to pass between the drive head 144 and the stator 142. According to one embodiment, the drive head 144 and / or the stator 142 is provided with drive means such as blades, or suitable reliefs. to drive the fluids. For example, the drive head 144 may take the form of a cylinder, or a half-cylinder whose wall is notched with one or more notches forming rotor channels 145. Alternatively or in addition, the stator 142 may take the form of a cylinder arranged concentrically with the drive head, whose wall is notched with one or more notches forming stator channels 146. The number, shape and arrangement of the stator and rotor channels may be adapted as required. They may, for example, be oriented parallel to the drive axis 143.

[0060] In addition to the fluid entrainment effect, the circulation device 14 is adapted to condition the circulating biomass B into elements of a determined size, such as less than 10 cm or less than 5 cm or less than 1 cm depending on the requirements. The biomass B is thus ground during the conversion process, while it is suspended in the carrier fluid FV and circulated in the installation 1. According to one embodiment, the biomass B can be loaded into the conversion tank 13 without prior significant grinding, provided that it can pass into the circulation loop BC via its inlet 15. The circulation device 14 is adapted to size the elements of the circulating biomass B. For example, the stator 146 and / or rotor 145 channels can be sized accordingly. The largest elements of the biomass B are thus sheared during their entrainment.Alternatively or in addition, an adequate space d is provided between the drive head 144 and the stator 142.

[0061] According to one embodiment, several circulation devices 14 are arranged in series so as to break up the biomass into increasingly finer elements. According to another embodiment, a circulation device 14 according to the present invention comprises several stages, i.e. several rotors and several stators making it possible to increase the grinding efficiency.

[0062] The characteristics of the circulation device(s) 14, such as the distance d, the shape and dimensions of the rotor and stator channels, can be adapted so as to modulate the size of the biomass elements B as a function of parameters such as the nature of the biomass B, the nature and / or the proportion of the first liquid L1, where appropriate the nature and / or the proportion of the second liquid L2 to be obtained, the nature of the vector fluid FV and the temperature of the vector fluid FV.

[0063] The rotor(s) 141 may be driven by any suitable device, in this case electric motors which may be powered by the mains or via a generator, or autonomous thermal motors.

[0064] A suitable quantity of carrier fluid is circulated in the installation. The carrier fluid FV can be stored in a carrier fluid tank 37 and transferred to the conversion circuit(s), including the conversion tank 13 and the circulation loop(s) BC. The quantities of carrier fluid FV circulated can thus be easily adapted according to requirements.

[0065] According to one embodiment, several FV vector fluids are independently stored in reservoirs and usable as needed.

[0066] A carrier fluid FV according to the present description means any fluid that remains liquid, stable and non-volatile at the temperatures of the process implemented. Such carrier fluids advantageously comprise molecules of high molecular weight while remaining sufficiently fluid to be easily circulated under the conditions of the process. The molecules comprised or constituting such carrier fluids FV are typically between 250 and 5000 Da. Their viscosity is advantageously between 1 and 1000 cp at 0°C. Their boiling point is preferably greater than 350°C under 1 bar. The carrier fluids FV can remain in liquid form or take the form of a supercritical fluid under the process conditions. The molecules of the carrier fluids are preferably non-reactive, in particular non-oxidizable. The FV carrier fluids may be selected from a mineral oil comprising one or more aliphatic hydrocarbons, one or more aromatic hydrocarbons or their combination, a silicone oil, an ionic liquid, a molten salt, a vegetable oil, a chemically transformed vegetable oil, a synthetic oil, in particular when it emanates from renewable precursors, or their combination. According to one embodiment, the FV carrier fluid may comprise one or more compounds resulting from a biomass conversion process such as the process described herein.Alternatively or in addition, some or all of the organic compounds in the FV carrier fluid result from vegetable oils modified by sustainable transformation processes based, for example, on renewable raw materials or from waste recycling.

[0067] According to one embodiment, the FV vector fluids according to the present invention comprise or consist of a mixture of linear or branched alkanes having a molecular weight of between 250 and 500 g / mol, an initial boiling point greater than 350°C under 1 atmosphere and a viscosity less than 500 cp at 0°C.

[0068] Preferably, the carrier fluids are free of catalyst, additive and chemical reagents. Preferably, the method according to the present invention is carried out without the addition of such additives.

[0069] The installation 1 according to the present invention further comprises at least one sensor, preferably a set of sensors 210, 220, 130, 150, 300 for monitoring the process conditions in real time. Such sensors may be selected from a temperature sensor, a pressure sensor, a flow meter, a viscometer, or other sensors deemed necessary. For example, the conversion tank 13 may be provided with one or more pressure sensors and / or one or more temperature sensors. The liquid recovery tanks may be equipped with a pH sensor, or means for determining a bacterial development, or turbidity or transparency sensors. The gas flows can be analyzed online, for example, using infrared spectrometers or other online analysis means. The condensation units can alternatively or additionally be provided with temperature and / or pressure sensors and / or gas sensors. The circulation loop BC can also be provided with a viscometer, an internal circuit pressure sensor and / or a temperature sensor. The filtration unit 30 can alternatively or additionally comprise a pressure sensor at the filtration device 31 if pressures are required for filtration. Gauges can be provided in the various tanks, in particular in the carrier fluid tank(s) FV, so as to determine their quantity or the quantities used in the process.Pressure sensors can be used for weighing purposes, for example to determine the quantities of biomass or other products of the process. Position sensors of various components such as valves, including the pest control valve 170, flaps, or the rotor(s) can also be considered. The detection means described here make it possible in particular to determine in real time the presence and / or quality of the products involved in, and resulting from, the conversion process. The process parameters can then be adapted accordingly during the conversion of the biomass. This does not exclude the possibility of other characterization means being implemented, for example via sampling of the products and their delayed analysis in a laboratory, for example for quality control or research and development purposes.

[0070] The installation 1 according to the present invention comprises a control unit (not shown) making it possible to control at least one of the various components of the installation among the loading device(s) 12, the dosing device 11, the circulation device(s) 14, the filtration unit 30, the pump(s) 34, the bypass valve 17 and other useful components. The control unit can allow one or more agents to control the installation. Alternatively or in addition, the control unit can be adapted to receive real-time data from one or more sensors integrated into the installation 1 and to initiate one or more commands. of controls automatically in response to the values ​​received. The control unit according to the present description may take the form of a suitable industrial programmable controller, commonly referred to as PLC (Programmable Logic Controller) comprising the dedicated control programs and user interface.

[0071] Alternatively or in addition, the installation 1 is provided with communication means for remotely transmitting at least part of the information relating to the data measured by one or more sensors. The installation can be remotely controlled on the basis of the data received.

[0072] According to one embodiment, the installation further comprises an artificial intelligence and / or deep learning module making it possible to determine or adjust the parameters of the installation and / or the conversion process according to requirements.

[0073] The present description further covers a method for converting a biomass B into one or more of the products mentioned above. In this case, the method comprises a step E1 of introducing a quantity of a vector fluid FV into a conversion tank 13 of a conversion installation such as that described above. In particular, the conversion tank 13 is at atmospheric pressure and does not require any particular pressurization. The quantities of vector fluid FV can be introduced from a vector fluid reservoir 37 via a suitable pipe. The volume of vector fluid can be predetermined according to the needs and / or adjusted during the conversion process. The vector fluid can circulate through a circulation loop BC or be introduced directly into the conversion tank 13. According to one embodiment, the vector fluid FV is introduced at ambient temperature into the conversion tank 13.Alternatively, the vector fluid FV is brought to a predetermined temperature, corresponding to the conversion temperature TC necessary for the conversion of biomass B or to an intermediate preheating temperature.

[0074] The method according to the present invention comprises a step E2 of introducing biomass B into the conversion tank 13. The anaerobic conditions are maintained so as to avoid or limit the presence of oxygen in the conversion tank 13. The biomass B can be added to the empty tank, before the transfer of the vector fluid FV. Alternatively, the vector fluid FV is introduced into the conversion tank 13 before the biomass B is introduced therein. The biomass B once mixed with the vector fluid FV produces a conversion mixture MC. The quantity of biomass B introduced into the conversion tank 13 can be calibrated according to the needs, in particular at least of the dosing device 11. According to one embodiment, the loading of the biomass B into the conversion tank 13 is sequential. According to another embodiment, the loading of the biomass B into the conversion tank 13 is continuous.

[0075] The present method comprises a step E3 of bringing one or more of the conversion mixture MC and the carrier fluid FV to a predetermined temperature. According to one embodiment, the carrier fluid is brought to a conversion temperature TC or to an intermediate temperature before the biomass B is introduced into the conversion tank. According to another embodiment, the biomass B is added to the carrier fluid so as to produce a conversion mixture MC, which is brought to a predetermined temperature, which may be a conversion temperature TC or an intermediate temperature. According to one embodiment, a temperature profile as a function of the temp is applied so as to vary the temperature during the conversion process. Preferably, the conversion temperature TC is determined in a range between 200°C and 400°C.

[0076] The present method comprises a step E4 of circulating the conversion mixture MC for a predetermined duration. The circulation is carried out by means of one or more circulation devices 14 as described above. Preferably, the circulation is accompanied by the concomitant grinding of the biomass B into elements of calibrated size as described above. The circulation of the conversion mixture can be carried out at a controlled speed so that to control the residence times of the biomass in the conversion tank 13 and / or the local pressure obtained by the ejection of the conversion mixture MC. The conversion mixture MC is circulated in at least one circulation loop BC from one or more inlets 15 to one or more outlets 16. The conversion mixture MC can be circulated for a predetermined conversion time DC or evaluated in real time depending on the process conditions.

[0077] The present method comprises a step E5 of condensing at least one of the gases from the conversion tank so as to obtain one or more liquids, comprising at least a first liquid L1. The condensation of the gas(es) is carried out continuously while the conversion mixture circulates in the conversion loop and through the conversion tank 13. The condensation of the gases is carried out under the pressure conditions of the process, i.e. without pressurization or depressurization. According to one embodiment, a first liquid L1 and a second liquid L2 are obtained by fractional condensation of the gases from the conversion tank. The second liquid L2 may have an evaporation temperature lower than the first liquid L1.The proportions and / or quantities of the first L1 and second L2 liquids can be determined by adjusting one or more of the parameters among the conversion temperature TC, the conversion duration DC, the size of the elements of the biomass B, the nature of the carrier fluid FV, the flow rate of the conversion mixture MC and the nature of the biomass B. Other parameters can be considered as required.

[0078] The method according to the present description optionally comprises a step E6 of stopping the introduction of biomass into the conversion tank 13 after the conversion duration DC.

[0079] The present method comprises a step E7 of extracting part or all of the conversion mixture MC from the circulation loop to a filtration unit 30. In this way the solid residues suspended in the conversion mixture MC can be removed from the ongoing process. The extraction of the conversion mixture can be carried out by means of one or several bypass valves 17, advantageously controlled automatically and / or remotely, but which can alternatively or additionally be actuated manually. The quantities of conversion mixture thus withdrawn from the circulation loop can be determined on the basis of parameters such as the residence time of the conversion mixture MC in the circulation loop, the viscosity of the conversion mixture, a turbidity value where appropriate, the nature of the collected gases or condensed liquids, determined for example via their condensation temperature or any other parameter deemed relevant. Alternatively or additionally, the withdrawal of a portion of the conversion mixture can be carried out after a predetermined conversion time DC.

[0080] According to an alternative embodiment, the conversion mixture can be extracted directly from the conversion tank, for example from a lower part suitable for collecting any sedimented elements.

[0081] The extraction of the conversion mixture MC through the bypass valve(s) 17, or through the conversion tank, may require the interruption of the loading of biomass into the tank. Alternatively, the present method may be adapted to maintain the loading of biomass into the tank during the extraction of a portion of the conversion mixture, so that the entire process can be operated continuously.

[0082] The method comprises a step E8 of filtering the derived conversion mixture MC. The filtration of the conversion mixture, or certain steps of the filtration of the derived conversion mixture MC from the conversion circuit, such as the rinsing of the solid residues RS, can be carried out in parallel with the conversion process described above. The carrier fluid FV or a portion of the carrier fluid is reintroduced into the circulation loop, either directly or after a regeneration treatment. The step of filtering the conversion mixture MC results in obtaining at least one solid residue RS. The nature and / or composition of the residual residue can be determined as a function of the filtration conditions, including for example the number of filtration cycles, the porosity of the surfaces of filtration, the use or not of solvents and their nature, the use or not of pressurization or depressurization, etc.

[0083] According to one embodiment, the method implemented according to the present description makes it possible to collect 4 or more than 4 distinct liquids, at least one grade of coal, at least one grade of vegetable oil, at least one grade of pyrolignous acid, and a mixture of non-condensable gases, in particular carbon dioxide. The number of products recovered depends for example on the nature of the biomass treated.

[0084] According to one embodiment, 1 kg of biomass can be converted into at least 400 g of coal, 150 g of vegetable oil, 250 g of pyrroligneous aid, and 150 g of gas.

[0085] The process described herein is preferably carried out continuously or semi-continuously. In particular, one or more of the steps E1 to E5 described herein may be repeated during the filtration of the derived conversion mixture.

[0086] The method according to the present description can be implemented manually, by one or more operators located at the installation 1. Preferably, one or more of the steps mentioned above can be implemented in an automated or partially automated manner. According to one embodiment, one or more parameters among the pressure, the temperature, the viscosity, the flow rate, the mass, collected by means of sensors during the conversion process, are used to control the installation in real time, either manually, automatically, remotely, or according to a combination of these manual, remote and automated modes.According to one embodiment, one or more of the elements of the installation described here, in particular the loading device 12, the dosing device 11, the circulation device 14, the filtration unit 30, the pump 34, and the bypass valve 17 are controlled according to the values ​​transmitted by the sensors, in an at least partially automated and / or remote manner.

[0087] According to one embodiment, one or more of the values ​​collected by one or more of the sensors are stored in one or more databases. These values ​​can be consulted after the end of the conversion process, for control, maintenance or development operations. Advantageously, the collected values ​​can be processed according to specific algorithms, for example relating to artificial intelligence programs.

[0088] The various embodiments described here are not intended to be mutually exclusive. They may be combined or dissociated within the physical limits of the realization of the present installation and the present method. Reference numbers used in the figures 1 Biomass processing plant 10 Conversion unit 11 Dosing device 12 Loading device 13 Conversion tank 14 Circulation Device 18 Gas Collector 140 Drive Assembly 141 Rotor 142 Stator 143 Drive Shaft 144 Drive Head 145 Rotor Channels 146 Stator Channels 15, 16 Circulation loop 17 Bypass 170 Bypass valve 20 Liquid recovery unit 21 First condensing unit 21a First condenser 21b First collector 22 Second condensing unit 22a Second condenser 22b Second manifold 23 Burner 30 Filtration unit 31 Filtration device 32 Recovery line 34 Pump 35 Solvent tank 36 Solvent / carrier fluid separator 37 Carrier fluid reservoir B Biomass BC Traffic Loop G Gas FV Vector Fluid L1, L2 First and second liquid MC Conversion Mix RS Solid Residue 210, 220, 130, 150 Sensors 300

Claims

Claims 1. Installation (1) for converting biomass (B) into one or more products selected from one or more liquids (L1, L2), one or more gases (G) and a solid residue (RS), the installation comprising: - a conversion unit (10), comprising a loading device (12) for the biomass (B), a conversion tank (13) for the biomass, and at least one circulation device (14) adapted to circulate a conversion mixture (MC) in a circulation loop, - a liquid recovery unit (20), arranged downstream of the conversion unit (10), comprising at least one condensation unit (21, 22) adapted to condense the gases from the conversion tank (13) into at least one first liquid (L1), - a filtration unit (30), arranged downstream of the conversion unit (10), comprising at least one filtration device (31) suitable for the recovery of solid residues (RS), and - at least one thermoregulation system for the conversion mixture (MC), in which the conversion tank (13) remains at atmospheric pressure, the conversion mixture (MC) comprises biomass (B) mixed with a vector fluid (FV), the circulation loop comprising a supply (15) and an outlet (16) for circulating the conversion mixture (MC) through the conversion tank (13), so as to locally increase the pressure of the conversion mixture (MC) by a factor of 1 to 50, preferably 3 to 50.

2. Installation according to claim 1, said loading device (12) being adapted to maintain the biomass (B) in anaerobic conditions and to limit or avoid the introduction of oxygen into the conversion tank (CV).

3. Installation according to one of claims 1 and 2, in which said loading device (12) comprises or is associated with a metering device (11) for the biomass (B) introduced into the conversion tank (13), said metering device being adjustable so as to introduce a variable quantity of biomass (B) between 1 kg / hour and 10 tonnes / hour.

4. Installation according to one of claims 1 to 3, in which said at least one circulation device is further adapted to grind the biomass (B) into elements of size less than 10 cm or less than 1 cm.

5. Installation according to claim 4, said at least one circulation device being modular so as to adapt the size of the biomass elements according to one or more parameters among the nature of the biomass (B), the nature and / or the proportion of the first liquid (L1), where appropriate the nature and / or the proportion of the second liquid (L2) to be obtained, the nature of the vector fluid (FV) and the temperature of the vector fluid (FV).

6. Installation according to one of claims 1 to 5, said at least one circulation device comprising a drive assembly (140) comprising a rotor (141) provided with a drive shaft (143) and a drive head (144) comprising one or more rotor channels (145), and a stator (142) comprising one or more stator channels (146) and arranged concentrically to the drive head, said drive head (144) being spaced from said stator (142) by a distance d adapted to the size of the elements of the biomass to be obtained.

7. Installation according to one of claims 1 to 6, said circulation loop comprising at least one bypass (17), adapted to extract a portion of the conversion mixture (MC) towards the filtration unit (30).

8. Installation according to claim 7, said at least one bypass (17) being activatable by means of one or more bypass valves (170).

9. Installation according to one of claims 1 to 8, said filtration unit (30) comprising a recovery line (32) of the vector fluid (FV) resulting from the filtration.

10. Installation according to one of claims 1 to 8, in which said vector fluid (FV) comprises or consists of non-volatile molecules whose molecular weight is between 250 and 5000 Da and / or the boiling temperature is greater than 350°C under 1 bar, and / or the viscosity is between 1 and 1000 cp at 0°C.

11. Installation according to claim 10, said carrier fluid being selected from a mineral oil comprising one or more aliphatic hydrocarbons, one or more aromatic hydrocarbons or their combination, a silicone oil, an ionic liquid, a molten salt, a vegetable oil, a chemically modified vegetable oil, a synthetic oil resulting from renewable resources, or their combination.

12. Installation according to one of claims 10 and 11, in which the conversion mixture (MC) is free of catalyst, additives, and added chemical reagents.

13. Installation according to one of claims 1 to 12, in which the biomass (B) is a second-generation non-edible lignocellulosic biomass from municipal, agricultural or forestry activities.

14. Installation according to one of claims 1 to 13, said at least one thermoregulation system of the conversion mixture (MC) being adapted to maintain or vary the temperature of the conversion mixture at a temperature between 200°C and 400°C.

15. Installation according to one of claims 1 to 14, the liquid recovery unit (20) comprising one or more burners (23) adapted to the combustion of non-condensed gases and to the recovery of the corresponding energy.

16. Installation according to one of claims 1 to 15, further comprising at least one sensor (210, 220, 130, 150, 300) selected from a temperature sensor, a pressure sensor, a flow meter and a viscometer, and a control unit adapted to control one or more of the loading device (12), dosing device (11), circulation device (14), filtration unit (30), pump (34) and bypass valve (17), as a function of the data collected by said at least one sensor.

17. Installation according to one of claims 1 to 16, further comprising an artificial intelligence and / or deep learning module.

18. Method for converting a biomass (B) into one or more products selected from one or more liquids (L1, L2), one or more gases (G) and a solid residue (RS), by means of an installation according to one of claims 1 to 17, comprising the steps of: - (E 1 ) introducing a quantity of a vector fluid (FV) into a conversion tank (10) maintained at atmospheric pressure, - (E2) introducing biomass (B) into the conversion tank (10) under anaerobic conditions, so as to form a conversion mixture (MC) with said vector fluid (FV), - (E3) bringing the conversion mixture (CM) and / or the vector fluid (VF) to a conversion temperature (TC) between 200°C and 400°C, (E4) circulating for a conversion time (DC) the conversion mixture (MC) through the conversion tank (10) at by means of a circulation device (14) forming a circulation loop having a supply (15) and an outlet (16) so as to locally increase the pressure of the conversion mixture (MC) by a factor of 1 to 50, and - (E5) condensing the gases from the conversion tank (10) into at least a first liquid (L1), where the condensation of the gases takes place continuously and at atmospheric pressure during the circulation of the conversion mixture (MC) in the conversion loop.

19. The method of claim 18, further comprising the steps of: - (E6) stop the introduction of biomass into the conversion tank (10), - (E7) extracting a portion of the conversion mixture (MC) from the circulation loop to a filtration unit (30), by means of a bypass valve (17) after the conversion duration (DC), - (E8) filter the derived conversion mixture (MC) so as to reintroduce the vector fluid (FV) into the circulation loop and recover the solid residues (RS), and - repeat steps (E1) to (E5) during the filtration of the derived conversion mixture.

20. Conversion method according to one of claims 18 and 19, in which the circulation of the conversion mixture (MC) is accompanied by the grinding of the biomass (B) contained in the vector fluid (FV) into elements of size less than 10 cm or less than 1 cm.

21. Method according to one of claims 18 to 20, in which a first (L1) and a second (L2) liquid are obtained, the second liquid (L2) having an evaporation temperature lower than the first liquid (L1), and in which the proportions and / or the quantities of the first (L1) and second (L2) liquids are determined by adjusting one or more of the parameters among the conversion temperature (TC), the conversion duration (DC), the size of the elements of the biomass (B), the nature of the vector fluid (FV), the flow rate of the conversion mixture (MC) and the nature of the biomass (B).

22. Method according to claim 21, in which one or more parameters among the pressure, the temperature, the viscosity, the flow rate, the mass, collected by means of sensors are determined during conversion, and where one or more of the elements among the loading device (12), the dosing device (11), the circulation device (14), the filtration unit (30), the pump (34), and the bypass valve (17) are controlled according to said values, in an at least partially automated and / or remote manner.

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