EP2171019A2

EP2171019A2 - Module, system and method for processing horizontal fixed bed biomass

Info

Publication number: EP2171019A2
Application number: EP08805812A
Authority: EP
Inventors: Isaac Behar
Original assignee: Individual
Current assignee: Individual
Priority date: 2007-06-01
Filing date: 2008-05-20
Publication date: 2010-04-07
Also published as: WO2008149026A3; FR2916760B1; FR2916760A1; WO2008149026A2

Abstract

The invention relates to a module for processing a solid and powder and/or liquid biomass using a processing gas flow on a substantially horizontal fixed bed, said module having an inlet for the biomass to be processed on said fixed bed and an opening for discharging the biomass after processing, characterised in that said processing module includes a plurality of so-called processing zones, and further includes: at least one means for injecting a processing gas flow into said module, said injection means being common to said processing zones; and, for each of said processing zones, means for extracting the charged processing gas flow obtained after processing with a substantially constant charge extraction loss over all said processing zones. The invention also relates to a system and a method for the pyrolysis and gasification of the solid, powder and liquid biomass using at least two modules of the invention in mutual communication.

Description

"Module, system and method for horizontal fixed bed biomass treatment"

The present invention relates to a horizontal fixed bed biomass treatment module. It also relates to a system for pyrolysis and gasification of horizontal fixed bed biomass using at least two modules according to the invention. Finally, the invention relates to a method implemented in the system according to the invention.

The field of the invention is the field of treatment of biomass on a substantially horizontal fixed bed. The invention is more particularly applicable to the pyrolysis and gasification of the mass biomass in a horizontal fixed bed system.

In this description:

- "Gasification" means an autothermal thermochemical conversion intended to convert a solid or liquid fuel into a gaseous fuel;

- "synthesis gas" or "synthetic gas" means the gases generated by "gasification". Thus, the charged gaseous gas stream comprises synthesis gases; - "autothermic" means that the energy contained in the gaseous fuel comes from solid or liquid fuel and that it is not necessary, once the gasification reaction has begun, to use any source of energy outside that available in the original solid or liquid fuel; - "Exothermic reaction" means a reaction that releases energy and "endothermic reaction" means a reaction that absorbs energy.

- "cracking" means the operation of breaking a complex organic molecule into smaller elements, which results in the formation of lighter hydrocarbons from heavier hydrocarbons.

- "gasifier" means an assembly that allows "gasification" and that includes a "reactor" allowing the transforming a solid or liquid fuel into a gaseous fuel.

- "reactor" means an enclosure that allows thermochemical transformations. - "biomass" means any carbon product directly or indirectly derived from photosynthesis and in particular but not limited to plants, animals, various organic waste, including household waste, sewage sludge, etc .; - "pulverulent biomass" means a biomass in the form of powder or particles small enough to be displaced by an average air flow or a reduced vacuum. By way of non-limiting example, let us mention sawdust, flours, and, more generally, very low density biomasses and in particular the light fractions of the selective sorting of household refuse;

- "liquid biomass" means a biomass that is in a more or less liquid form. By way of non-limiting example, mention may be made of sewage sludge which, because of the high water content, is in a liquid form.

- "valves" means any device that makes it possible to vary the flow of a pipe and therefore the pressure loss resulting from it, whether the control is manual, electric or pneumatic

- "Coal" means a carbon product, comparable to vegetable coke obtained by pyrolysis;

- "mass biomass" means a relatively dense biomass that will remain in place in an air circuit or in a depressed zone; by way of non-limiting example, mention wood logs, or maxi chips, or products densified from pulverulent biomass;

- "pci" means lower calorific value of synthesis gas;

- "pcs" means the gross calorific value of a gas - "combustion" means a process that consists of converting biomass into heat with the formation of non-combustible oxidized gases;

- "oxidizer" means air, air enriched with oxygen or oxygen; it is also possible to include in the term "oxidant" the water vapor which has an oxidizing character.

The document FR 2 440 398 describes a system for gasification of biomass on a fixed bed with a horizontal grid fed continuously at one end with biomass, the grid fixed bed allowing the circulation of the treatment gas stream transversely with respect to the direction of flow of the biomass through two openings situated respectively upstream of an area, or module, of drying-pyrolysis of the biomass and upstream of an area, or module, of gasification of the biomass, these openings being connected to two separate vacuums. The first upstream vacuum cleaner is connected to the opening located in the upstream drying-pyrolysis module and reinjects the hot gas treatment gas stream at the slope of the biomass to be treated in the immediate vicinity of an oxidizer pipe, thus allowing a forced circulation of hot gas through the biomass. The opening located upstream of the gasification zone is connected to an aspirator which recovers the charged gaseous gas flow, that is to say the gaseous flow used for the treatment of the biomass loaded with the components that have formed during the treatment of the biomass or reaction of the treatment gas stream with at least one component of the biomass. For example, during pyrolysis, the pyrolysis gas stream is charged with numerous gaseous compounds in virtually unpredictable proportions such as:

• CO (carbon monoxide); flammable gas (its combustion gives carbon dioxide.

• H2 (hydrogen); flammable gas (its combustion gives water). • CO2 (carbon dioxide); only non-flammable gas, because saturated with oxygen, resulting from pyrolysis;

• CH4 (methane); flammable gas, very present in natural gas; • CnHm (light hydrocarbons), flammable gases (butane, propane etc.) present only in trace amounts among the gases extracted from the gasifier,

• CyHw (heavy hydrocarbons driven by pyrolysis gases (pyroligneous liquor, tar).

At the same time, the carbon content of biomass is steadily increasing. The system described in document FR 2 440 398 has a disadvantage which is the difficulty of effectively passing all the biomass through the gaseous treatment stream. To remedy this drawback, the document FR 2 487 847 proposes a system in which a series of separate reactors are juxtaposed, from upstream to downstream, each reactor comprising an aspirator in the lower part of each reactor, injecting the flow gaseous recovered in the sky of each separate reactor, the oxidant being separately injected into each sky of each separate reactor. The provisions of this document will lead to a system whose drying, pyrolysis and gasification reactions will be very difficult to control. Indeed, the speed of advance of the biomass is unique for all juxtaposed reactors while the amount of water vapor and the amount of pyrolysis gas will decrease from the upstream system downstream of the system and will require also adjust the amount of oxidant in each juxtaposed reactor, which will also result in different temperatures in the sky of each of the juxtaposed reactors with also a significant risk of insufficient temperature in the sky juxtaposed reactors located in the downstream zone displacement of the biomass for efficient cracking of pyrolysis gases including tars, leading to a high tar content, or by increasing the risk of having to inject a quantity of oxidant greater than or equal to the stoichiometric amount in juxtaposed reactors downstream relative to the direction of movement of the biomass, leading then to the formation of an imp CO2, non-combustible gas. In addition to the complexity of controlling operations, the system described in this document is complex to implement and expensive. An object of the invention is to provide a module, system and method for treating biomass with a better circulation of the treatment gas stream through the biomass to be treated, while remaining less complex and less expensive than the systems of the invention. 'state of the art. The invention thus proposes a module for treating the biomass with a gaseous treatment stream on a substantially horizontal fixed bed, this module having an inlet opening for the biomass to be treated on the fixed bed and an opening for evacuating the biomass after treatment, characterized in that the treatment module comprises several zones, called treatment zones, this module further comprising:

at least one means for injecting a treatment gas stream into the module, the injection means being common to the treatment zones, and

for each of the treatment zones, means for extracting the charged process gas stream obtained after treatment with a substantially constant extraction pressure drop for all of the treatment zones.

The module according to the invention comprises homogeneous treatment zones each comprising means for extracting the charged treatment gas stream. The process gas stream is extracted with a substantially constant pressure drop across all sections, thus allowing the process gas stream to effectively traverse all the biomass uniformly and substantially independently of differences in biomass thickness throughout the process. fixed bed. Furthermore, the module according to the invention comprises means for injecting the treatment gas stream common to all the treatment zones thus making it possible to overcome the differences in the composition of the charged treatment gas stream extracted at the level of each of the zones. processing and the complexity of controlling the different operations that can take place in the module. In fact, the different parts of the treatment gas stream extracted at each of the treatment zones are then combined and recycled together to be reinjected into the sky of the treatment module by injection means common to all the treatment zones. Advantageously, the extraction means of the treatment gas stream loaded with a treatment zone comprise:

at least one extraction opening arranged under the horizontal fixed bed, this horizontal fixed bed being composed for example of a grid permeable to the gaseous treatment flow loaded, and

at least one suction means of said treatment gas stream loaded through said opening.

According to one embodiment, the suction means of the charged treatment gas flow may be common to all the treatment zones and the size of each of the extraction openings of each of the treatment zones is substantially proportional to the thickness of the treatment zone. the biomass present at the level of the treatment zone so that the extraction pressure drop is substantially constant for all the treatment zones. According to another embodiment, the suction means of the charged treatment gas stream may be common to all the treatment zones and the size of each of the extraction openings of each of the treatment zones being substantially constant, at least one suction control member is disposed at each of the extraction openings so that the pressure drop is substantially constant at all the treatment areas. Such a regulating member may, for example, comprise a valve disposed at the level of the extraction opening and arranged to regulate the suction of charged treatment gas flow. Thus, the regulation of each valve of each opening of each treatment zone as a function of the biomass thickness present at each of the treatment zones makes it possible to extract the treatment gas stream with a constant pressure drop. and resulting in an effective crossing of all the biomass by the gaseous treatment stream. The module may advantageously comprise means for measuring the thickness of the biomass present on the horizontal bed at each treatment and control zone of each of the valves as a function of the measured biomass thickness. According to yet another embodiment, the size of all the extraction openings of all the treatment zones may be substantially constant. Each of the extraction openings of each of the treatment zones may comprise a suction means adjusted so that the extraction pressure drop is substantially constant at all the treatment zones. An aspirator may be placed at each of the extraction openings of each of the treatment zones, the suction of each being adjusted according to the biomass thickness present on the fixed bed at each of the treatment areas.

Furthermore, the module according to the invention may comprise a device for advancing the biomass on said horizontal fixed bed, from the inlet opening to the discharge opening.

According to another aspect of the invention, there is provided a substantially horizontal fixed bed biomass treatment system, said system comprising:

an inlet opening for said biomass to be treated on said horizontal fixed bed;

a single reactor for treating biomass, comprising a first and a second biomass treatment module, as described above, communicating with one another:

the first pyrolysis module, pyrolyzing the biomass admitted by the inlet opening with a pyrolysis gas stream and comprising first means for extracting the charged pyrolysis gas stream, and

the second gasification module, which gasifies said biomass from the pyrolysis module by a gaseous gasification stream and comprises second extraction means for the charged gasification gas stream; and

an opening for evacuating residues from the gasification of the biomass.

The term "charged pyrolysis gas stream" means the treatment gas stream used for the pyrolysis of the biomass charged with the components. gaseous and solid gases that formed during the pyrolysis of biomass in the pyrolysis module.

The term "charged gaseous gas stream" means the gaseous treatment stream used for the gasification of the biomass charged with the gaseous components that have formed during the gasification of the biomass in the gasification module and possibly solid particles entrained by the flow of gas. gasification.

The system according to the invention may further comprise a pyrolysis gas feed circuit charged into the reactor sky, where the charged pyrolysis gas stream is partially oxidized in the presence of oxidant to obtain the gaseous treatment stream. biomass. The oxidant may be injected into the reactor skies by injection means. These injection means may for example comprise adjustable injection nozzles for varying the amount of oxidant injected into the sky of the reactor.

Furthermore, the charged pyrolysis gas feed circuit may comprise a device for entrainment, by venturi effect, of the pulverulent biomass in the sky of the reactor, said pulverulent biomass being in a reservoir or a module from which it is extracted. by the depression created by a venturi device, with, if necessary, a partial suspension of the pulverulent biomass, mechanically, or otherwise.

In another embodiment, the pulverulent biomass can be fluidized at room temperature or at high temperature before being extracted by venturi effect. Advantageously, the pulverulent biomass injected into the sky of the reactor is then pyrolyzed and gasified. Thus, the system according to the invention makes it possible to carry out the pyrolysis and gasification of pulverulent biomass, together with the pyrolysis and gasification of the mass biomass. The pyrolysed powder biomass can then react with the mass biomass present on the horizontal fixed bed, thus making it possible to purify the gaseous components that appear during the pyrolysis and the gasification of the pulverulent biomass.

The system according to the invention may advantageously comprise means making it possible to maintain the pulverulent biomass in the form a fluidized bed. These means may comprise mechanical means. The biomass can also be maintained in a fluidized bed by injecting a gas stream into the powder biomass reservoir.

In a particular embodiment, the gas flow injected into the pulverulent biomass reservoir may be a part of the charged pyrolysis gas. In this case the pulverulent biomass is partly pyrolyzed and gasified in the tank in which it is located.

In another particular embodiment, it is possible to treat liquid biomass simultaneously with the mass biomass by adding a drying module of the liquid biomass upstream, the system according to the invention further comprising a module comprising means atomization of the liquid biomass in the form of fine droplets treated with a hot gas stream allowing almost instantaneous evaporation of the liquid without the biomass not reaching 250 ⁰ C to avoid causing a pyrolysis operation, by the conjunction of the heat input by the hot gas, and the endothermic reaction of the evaporation of the liquid, thus allowing the elimination of the liquid, which may be water, the pyrolysis of the dry powdered biomass, obtained by drying liquid biomass, being in the sky of the reactor. Advantageously, the system according to the invention may comprise at least one heat exchanger designed to recover, at least in part, the thermal energy of charged gaseous gas flow and / or charged pyrolysis gas flow. At least a portion of this thermal energy can be used to heat a drying gas stream used to dry solid biomass, or pulverulent biomass, or liquid biomass in drying modules arranged upstream of the reactor, before the introduction of the biomass in the treatment reactor.

Furthermore, the system according to the invention may comprise means for separating at least one gaseous component, called synthesis gas, present in the charged gaseous gas stream extracted from the gasification module.

In a particular embodiment of the system according to the invention the pyrolysis module and the gasification module are superimposed. The pyrolysis module is disposed above the gasification module. In the gasification module the biomass has a direction of circulation opposite to the direction of circulation of the biomass in the pyrolysis module. In this particular embodiment, the system further comprises at least one passage opening allowing the gaseous treatment flow to pass from the pyrolysis module in the gasification module.

According to yet another aspect of the invention there is provided a method for treating biomass on a substantially horizontal fixed bed with a treatment gas stream. This process comprises the following steps: pyrolysis of the biomass in a module, called pyrolysis, by the gaseous treatment stream;

- Gasification of the biomass in a module, said gasification, by the gaseous treatment stream, the pyrolysis and gasification modules being in communication with each other and arranged in a single reactor, each of the modules comprising several zones, called treatment, the method further comprising

an injection of the treatment gas stream into the sky of the modules, the injection being common to the treatment zones of each of the modules; an extraction of the charged pyrolysis gas stream, this extraction being carried out with a substantially constant loss of charge for each of the treatment zones of the pyrolysis module, and

an extraction of the charged gaseous gas stream, this extraction being carried out with a substantially constant loss of charge for each of the gasification module's treatment zones.

The method according to the invention further comprises an introduction of the biomass on the horizontal fixed bed and an extraction of the residues of the biomass after gasification. Advantageously, the process according to the invention further comprises an injection of the charged pyrolysis gas stream into the reactor, where said charged pyrolysis gas stream is oxidized in a controlled manner in the presence of oxidant to obtain the treatment gas stream. The oxidizer can be air enriched with oxygen or oxygen, or water vapor and injected directly into the sky of the reactor.

Advantageously, the process according to the invention comprises an injection of pulverulent biomass into the reactor skies, this pulverulent biomass being entrained by the charged pyrolysis gas stream, by venturi effect. The biomass injected into the sky of the reactor is then pyrolyzed and gasified in the sky of the reactor. The mass biomass on the horizontal fixed bed makes it possible to purify the pyrolysis and gasification gases of the pulverulent biomass. The pulverulent biomass can be in the form of a fluidized bed in a tank connected to the feed circuit of the charged pyrolysis gas stream.

The liquid biomass can be previously transformed into pulverulent biomass by atomization of the liquid biomass in the form of fine droplets in a drying module, the liquid biomass droplets being treated with a hot gas stream allowing rapid evaporation of the liquid. The pulverized biomass obtained is then injected into the sky of the reactor to be pyrolyzed and / or gasified.

The method according to the invention may further comprise at least one heat exchange for recovering, at least in part, the thermal energy of the charged gaseous gas stream. At least a portion of this thermal energy can then be used for the drying of the mass biomass during a drying step prior to pyrolysis and / or the drying of the liquid biomass and its conversion into pulverulent biomass.

Finally, the process according to the invention may comprise a step of separating at least one gaseous component from the charged gaseous gas stream.

Other advantages and characteristics will appear on examining the detailed description of a non-limiting embodiment, and the attached drawings in which:

FIG. 1 is a schematic representation of a first embodiment of the module according to the invention; FIG. 2 is a schematic representation of a second embodiment of the module according to the invention; Figure 3 is a schematic representation of a third embodiment of the module according to the invention; FIG. 4 is a diagrammatic representation of a system for treating mass, powder and liquid biomass according to the invention;

FIG. 5 is a representation of a first embodiment of a reactor implemented in the system according to the invention;

FIG. 6 is a schematic representation of a second embodiment of a system according to the invention;

- Figure 7 is a schematic representation of the system of Figure 6 in a sectional top view; FIG. 8 is a schematic representation of the principle of entrainment of the pulverulent biomass by the charged pyrolysis gas stream; FIG. 9 is a schematic representation of a very fast pyrolysis / gasification module of the powdered biomass fluidized by the charged pyrolysis gas and driven by depression by the charged pyrolysis gas stream; and FIG. 10 is a schematic representation of a liquid biomass drying module for obtaining pulverulent biomass. Figures 1 to 3 are three schematic representations of three embodiments of a mass biomass processing module 10. The modules 10 shown in FIGS. 1 to 3 comprise a substantially horizontal fixed bed L receiving the biomass B to be treated by an inlet opening 11. The residues after treatment of the biomass B are discharged out of the module 10 via an opening of evacuation 12. Each module 10 comprises an injection means 13 of the treatment gaseous flow in the sky of the module 10. The module 10 has several treatment zones 14 of the biomass B which has a decreasing thickness of the admission opening 11 to the evacuation opening. 12. Each of the zones of treatment 13 has an opening 15 for extracting the charged treatment gas stream which opens onto a single pipe common to all the extraction openings 15 of all the treatment zones 13.

The injection means 13 of the treatment gas flow are common to all the treatment zones 14 thus making it possible to overcome compositional differences in the treated treatment gas stream extracted at each of the treatment zones 14 and the complexity. control of the various operations that can take place in the module. The different parts of the treatment gas stream extracted at each of the treatment zones 14 are then combined and recycled together to, for example, be reinjected into the sky of the treatment module 10 by the common injection means 13 to all the treatment areas 14.

According to the first embodiment, shown in FIG. 1, each treatment zone 14 comprises an extraction opening 15. The size of each of the extraction openings 15 of each of the treatment zones 14 is substantially constant. The module 10 comprises suction means 17 of the charged treatment gas stream common to all the treatment zones 14. At each extraction opening 15 is disposed a valve 16 whose opening is proportional to the thickness of the the biomass present at the corresponding treatment zone 14, so that the pressure drop is constant for all the evacuation openings 15 of the module 10. Thus, the opening of the valves 16 decreases from the admission opening 11 to the discharge opening 12 in proportion to the thickness of the biomass present on the bed L.

According to a second embodiment, represented in FIG. 2, the module comprises suction means 17 for the charged treatment gas stream common to all the treatment zones 14. However, in this second embodiment, the size of each of the extraction openings 15 is proportional to the thickness of the biomass present at the corresponding treatment zone 14 so that the extraction pressure drop is substantially constant for all the treatment zones 14. the treatment zone 14 located near the inlet opening 11, the size of the opening extraction 15 is large because the thickness of the biomass in this area is large while at the level of the treatment zone 14 located near the discharge opening 12, the size of the opening of Extraction 15 is small because the thickness of the biomass at this zone is small. Thus, the size of the extraction openings 15 decreases from the inlet opening 11 to the discharge opening 12 because the thickness of the biomass decreases from the inlet opening to the discharge opening.

According to the third embodiment, represented in FIG. 3, the module 10 comprises extraction apertures 15 whose size is substantially constant for all the treatment zones 14. Each opening 15 of each treatment zone 14 comprises a means of suction 18, the suction of which is adjusted proportionally to the thickness of the biomass present on the bed L at this treatment zone 14, so that the pressure drop of extraction is substantially constant for all the treatment zones 14 the treatment module

10.

Whatever the embodiment, the module 10 further comprises means 19 for advancing the biomass of the inlet opening 11 to the discharge opening 12. These means 19 have a movement back and forth symbolized by the double arrow at a predetermined and adjustable frequency to push the biomass towards the discharge opening.

The gaseous treatment flow is injected into the sky of the module 10 on the side of the discharge opening 12 towards the side of the inlet opening 11.

A module for treating biomass according to the invention, on a fixed horizontal bed, has the following advantages:

uniform treatment of biomass irrespective of the height of the biomass present on the fixed bed in the different zones; treatment of the biomass by a gaseous flow of substantially the same composition whatever the treatment zone. We will now describe a system according to the invention implementing two treatment modules according to the invention in the particular case of a pyrolysis and a gasification of the biomass. In order to be able to appreciate the advantages of the invention in the particular case of the gasification of biomass, it is essential to understand the exothermic and endothermic reactions that occur simultaneously and / or successively in the gasification when the temperature of the wood increases progressively. wood being considered as a non-limiting example of biomass.

It is legitimate to contrast the combustion processes that consist of transforming biomass into heat with the formation of non-combustible oxidized gases, and the gasification processes that consist in transforming the energy contained in a solid or a liquid into a combustible gas. and therefore not entirely oxidized.

Gasification is a complex process that involves an incomplete oxidation of the biomass and therefore the supply of an insufficient quantity of oxygen with respect to the stoichiometric quantity necessary to transform all the available carbon in the biomass into carbon dioxide (CO2). , and hydrogen in water (H2O).

Gasification is a thermochemical process for converting a solid or liquid fuel into a gaseous fuel. It is therefore an incomplete combustion because it must lead to combustible gases. It takes place in four stages. a) Drying

It is a question of evaporating the humidity. This decreases the calorific value of wood. b) Pyrolysis This is the first of the steps that takes place inside the reactor. This is also generally the time-limiting step of many gasification processes.

During pyrolysis, the wood decomposes by heat and gives a "vegetable coke" that can be called charcoal or "coal". It is very rich in carbon and also contains hydrogen. It is free of oxygen, which escaped as CO, H2O (water) and CO2.

At the same time as this "tank" is formed, water, in the form of water vapor, and several gases appear in almost unpredictable proportions: • CO (carbon monoxide); flammable gas (its combustion gives carbon dioxide.

• H2 (hydrogen); flammable gas (its combustion gives water).

• CO2 (carbon dioxide); only non-flammable gas, because saturated with oxygen, resulting from pyrolysis;

• CH4 (methane); flammable gas, very present in natural gas;

• CnHm (light hydrocarbons), flammable gases (butane, propane, etc.) present only in trace amounts among gases drawn from the gasogen • CyHw (heavy hydrocarbons) entrained by the pyrolysis gases

All these gases come from wood, whose carbon content is constantly growing.

Pyrolysis is endothermic and therefore consumes energy, at least as long as the temperature is below 250 ⁰ C; above 400 ⁰ C, pyrolysis looks more and more like a combustion and it releases more heat than it consumes; between 250 ⁰ C and 400 ⁰ C equilibrium occurs between the endothermic reactions and exothermic reactions.

During the pyrolysis, heavy hydrocarbons are also formed in the form of pyroligneous liquids or tars. c) Oxidation - combustion

In the presence of oxygen (air), it reacts with the carbon from 400 ⁰ C and triggers a combustion reaction. The heat required for pyrolysis comes from the combustion of the carbon contained in the biomass, which is produced intermediately by pyrolysis. This assumes that initially, when starting the gasifier, an external energy supply is made that will no longer be necessary, once the complex gasification reactions initiated. The oxidation step can also be used for the "cracking" destruction of the complex molecules that form the tars.

Oxidation of carbon into CO2 releases a large amount of energy; the incomplete oxidation of carbon to CO also releases energy, but in a lesser quantity, d) Reduction

In chemistry, we call reduction any reaction that leads to compounds that are poorer in oxygen. This is the last step of the process gasification complex which results in the formation of combustible gases. This operation is endothermic.

To summarize, gasification, from a purely scientific point of view, is described, in its ultimate phase as a heterogeneous reaction, that is to say a surface reaction between the carbon (C) contained in the solid and a reactant gas that may be water vapor

(H2O) or carbon dioxide (CO2) according to the reactions (1) and

(2) below.

(1) C + H2O ^< "→ ^> CO + H2 (2) C + CO2 <" → 2 CO

These two reactions occur at the reactive surface of the particle, a surface that varies between the outer surface of the particle and the total surface of the pores of the particle depending on the diffusion properties in the solid core and chemical kinetics. They are slow, compared to total or partial oxidation by oxygen during combustion: reaction (3) and (4) which provide the necessary energy.

(3) C + O2 - * CO2

(4) C + 1 / 2O2 - * CO

The rate of conversion of solid carbon into gas and the composition of these are determined by: a. The equilibrium constants of the various reactions implemented b. The speeds of these reactions. vs. The composition of the oxidant mixture On the industrial level, the objective of the gasification process used in the system according to the invention is to promote the reactions (1) and

(2) which will produce a mixture of combustible gases, but to do this, it is necessary beforehand or simultaneously generate the elements necessary for these two reactions, namely: the highly reactive carbon, the reactants (CO2 and H2O) as well as a significant amount of energy produced by oxidation of a carbon fraction included in the biomass to be gasified. These three components (energy, CO2, H2O) of the gasification process, which globally corresponds to incomplete combustion, are produced by:

Pyrolysis reactions which allow the very rapid production of gaseous hydrocarbon compounds, as soon as the fuel is heated in the reactor, even in the absence of oxygen,

• oxidation reactions, homogeneous (gas phase) and heterogeneous (solid phase) more or less complete and which occur in the presence of oxygen as is conventionally the case in combustion. FIG. 4 is a schematic representation of a mass, powdered and / or liquid biomass treatment system. The system 20 comprises a module 21/22 for drying the mass biomass by a drying gas stream GS. A module 25 for transforming liquid biomass BL into pulverulent biomass BP. The dried mass biomass, or being dried, is supplied by feed means 22 into the reactor 23 where it is pyrolyzed and gasified. This reactor will be detailed below.

The charged pyrolysis gas stream GPC is then purified by purification means 24 to remove the residues present in this gas. After purification, the charged pyrolysis gas stream is injected into the sky of the reactor 23 to be oxidized in a controlled manner in the presence of an oxidant C which may in particular be air, and generate the pyrolysis and gasification gas streams biomass B. The pulverulent biomass, contained in a reservoir 26, is driven by the venturi effect created by the GPC loaded pyrolysis gas stream circulating in the feed circuit. Thus, the pulverulent biomass entrained by the GPC-charged pyrolysis gas stream is injected at the same time as the GPC-loaded pyrolysis gas stream in the reactor 23, where the gasification of the pulverulent biomass takes place. The mass biomass present on the horizontal fixed bed can thus react with the pyrolysed powder biomass and thus make it possible to purify the gaseous components that appear during the pyrolysis and the gasification of the pulverulent biomass. Thus, the reactor makes it possible to perform the combined gasification of the mass biomass present in the reactor and the pulverulent biomass entrained by the GPC-loaded pyrolysis gas stream.

The liquid biomass BL is first converted into pulverulent biomass BP in the module 25 by dispersion of the liquid biomass BL in the form of fine droplets treated with a hot gas stream allowing rapid evaporation of the liquid.

The gaseous gasification gas stream GGC extracted from the gasification module is purified by purification means 27 to remove residues, then enters a heat exchanger 28 to exchange at least a portion of its thermal energy with a drying gas stream GS , used for drying the mass biomass in drying module 21/22 and also for converting liquid biomass BL into pulverulent biomass BP in module 25. The drying gas stream GS can for example be air or any other gas stream generally used for drying the biomass. The charged GGC gasification gas stream having exchanged a portion of its thermal energy with the drying gas stream GS then enters a separation module 29 effecting the separation of the synthesis gases GS1, GS2, GS3 present in the charged gasification gas stream. . The synthesis gases GS1, GS2, GS3 are, for example, hydrogen, CO, and CO2, respectively.

The purification means 24 and 27 are cleaning means of the cyclone type, sleeves or others.

To initiate the pyrolysis of the biomass, it is necessary to provide energy in the form of combustible gas G. The reactor 23 must have a sky connected to an external source of gas. The fuel gas G will be burned in the reactor skylight and the air contained in the reactor will heat up progressively and pass transversely through the biomass to be treated through the extraction openings located in the lower part of the modules 231 and 232. As the pyrolysis progresses, it will develop, maintained by the combustion of the supplied gas, until the biomass has reached a temperature sufficient for the pyrolysis to be self-sustaining. It is then possible to close the pipeline supplying the external gas G and maintaining the pyrolysis and the gasification only by the energy produced by the oxidation of the pyrolysis gases.

The oxidation zone must therefore comprise at least one burner for burning the pyrolysis initiation gas with the addition of oxidant (in particular air or oxygen or oxygen enriched air) and a second burner for burning the pyrolysis gases. less than using a single burner capable of burning the filler gas and the pyrolysis gases present in the charged pyrolysis gas stream, closing the gas supply pipe when the pyrolysis gas supply is sufficient to maintain the reaction and opening it automatically in the case where the pyrolysis gas combustion flame goes out for some reason, or by providing a pilot for this purpose fed by a supply gas.

To avoid cooling the pyrolysis gas circuit, it is possible to pass the oxidizer in the reactor sky to heat it, just before being injected into the burner.

FIG. 5 shows a first embodiment of a reactor 23 implemented in the system according to the invention.

In the embodiment shown in FIG. 5, the reactor 23 comprises two modules 231 and 232, according to the invention, which are arranged one behind the other. The two modules 231 and 232 communicate with each other so that the biomass B in the reactor passes from the module 231 to the module 232. There is no wall between the modules 231 and 232.

The module 231 is the pyrolysis module and performs the pyrolysis of the biomass introduced into the reactor through an amission opening 233. This inlet opening 233 is also the inlet opening of the biomass B in the pyrolysis module. 231. The pyrolysis module 231 has a plurality of treatment zones, each of the treatment zones comprising an opening for extracting the pyrolysis gases (or the charged pyrolysis gas stream). The size of these extraction openings is proportional to the thickness of biomass present in the corresponding treatment zones. The pyrolysis module 231 comprises a vacuum cleaner common to all the extraction openings and making it possible to extract the GPC-loaded pyrolysis gas stream. The module 232 is the gasification module and carries out the gasification of the biomass from the pyrolysis module 231. The gasification residues are evacuated from the gasification module by an evacuation opening 235. These residues are accommodated in a receptacle 236 which discharges residues out of the reactor. The gasification module 232 has a plurality of treatment zones, each of the treatment zones comprising an opening for extracting the gasification gases (or the charged gasification gas stream). The size of these extraction openings is proportional to the thickness of biomass present in the corresponding treatment zones. The gasification module 232 comprises a vacuum cleaner common to all the extraction openings and making it possible to extract the gaseous gasification gas flow GGC.

In the first embodiment, the means 234 making it possible to advance the biomass are common to the pyrolysis modules 231 and the gasification modules 232, as well as the fixed bed L.

FIG. 6 is a representation of a second embodiment of the reactor 23 implemented in the system according to the invention. In the embodiment shown in FIG. 6, the reactor 23 comprises two modules 231 and 232, according to the invention, which are arranged one above the other. The two modules 231 and 232 communicate with each other via two openings: the passage opening 237 allowing the passage of the pyrolysed biomass pyrolysis module 231 to the gasification module 232, and the passage opening 238 allowing the treatment gas flow. to switch from the pyrolysis module 231 in the gasification module 232. In the embodiment shown in Figure 6, the biomass is pyrolyzed in the module 231 on the bed Ll. It is pushed along the bed L1 by means 2341. At the end of the bed L1, the biomass passes by gravitation in the gasification module 232 through the passage opening 237. The biomass is then gasified in the module 232 of gasification. The treatment gas stream injected into the sky of the pyrolysis module 231 passes into the gasification module 232 via at least one passage opening 238. The biomass is pushed all along the bed L2, in the gasification module 232, by means of Means 2342. The residues fall by gravity into the receptacle 236 and are evacuated. Figure 7 gives a schematic representation in a top view of the system shown in Figure 6, in section along the axis AA. As can be seen, the passage openings 238 connecting the skies of the pyrolysis module and the sky of the gasification module in no way prevent the longitudinal passage of the biomass on the fixed bed Ll of the pyrolysis module.

231 before falling by gravity on the fixed bed L2 of the gasification module

232 through the passage opening 237.

Whatever the embodiment, the means for advancing the biomass along the fixed bed (s) are push-type means driven back and forth. Other systems allowing the advancement of biomass can be substituted for the pusher moving back and forth, for example, without limitation, scrapers or conveyor belts, further, the advancement of the residues, such as that ashes recovered in the receptacle 236 is made by a worm or any equivalent device.

For safety reasons, it is necessary for the reactor to operate constantly in depression. To do this, the relative suction speed of the vacuum cleaner of each of the pyrolysis and gasification modules is adjusted according to the volume of gas corresponding to the volume of injected gas (oxidant) + the volume of gas generated by the biomass.

Unrepresented devices for measuring the temperature and control as a function of the temperatures recorded will be arranged in different zones of the reactor assembly and biomass feed. By way of nonlimiting example, the temperature measuring devices will be placed in the reactor sky, along the pyrolysis gate L1 and the gasification gate L2. These measurements can be used to control, in particular and in a nonlimiting manner, the circulation velocity of the treatment gas flow, the quantity of oxidant injected per unit time, the speed of displacement of the biomass in the pyrolysis module, the speed of injection of powder biomass, the speed of advancement of the biomass in the gasification module, the objective being to control these various parameters in order to obtain the maximum power of the reactor. Outside the reactor, devices for measuring the temperature of the biomass in the feed and drying device will make it possible to regulate the rate of circulation of the air conveying the recovered thermal energy, in particular so as to maintain the temperature of the biomass below 250 ⁰ C to avoid triggering a pyrolysis operation.

Sampling and chemical analysis devices will be, by way of non-limiting examples, located at the level of the charged pyrolysis gas flow circuit and the gaseous gasification stream comprising the synthesis gases and will be used to control the other described parameters.

The embodiment shown in Figure 6 is the preferred mode. In this preferred embodiment, the three biomass circulation stages corresponding to pyrolysis, gasification and ash extraction are represented, each stage occupying the entire length of the reactor and changing direction at each stage; it is the variant that should lead to maximum power with space and relatively constant cost.

The system according to the invention allows a significant gain in power, at a relatively constant cost and size. The recycling of pyrolysis gases in a single sky eliminates the major drawback of the system described in document FR 2,487,847. Finally, the use of the pyrolysis gas reinjection circuit in the reactor sky to allow rapid pyrolysis of the pulverulent biomass together with the pyrolysis of the mass biomass circulating horizontally makes it possible to further increase the power of the reactor at a substantially constant cost and bulk.

The same is true of the possibility of transforming liquid biomass into pulverulent biomass, which is then transformed at the same time as mass biomass.

FIG. 8 is a representation of the first driving principle of the pulverulent biomass BP by the GPC loaded pyrolysis gas stream. The pulverulent biomass reservoir BP has a supply opening 261 made of pulverulent biomass BP and an opening 262 connected to the GPC-charged pyrolysis gas flow circuit in which the charged pyrolysis gas stream GPC circulates at a high speed. This circuit has a throat 264 located upstream and near the opening 262 of the reservoir 26 of pulverulent biomass BP. The passage of the GPC loaded pyrolysis gas stream by this constriction creates a venturi effect driving the pulverulent biomass BP in the charged pyrolysis gas flow circuit and thus making it possible to extract the pulverulent biomass BP from the reservoir 26. In the case where the Venturi effect is not sufficient to drive the pulverulent biomass, the reservoir 26 may comprise mechanical means 263 for suspending and keeping in suspension the pulverulent biomass BP in the reservoir 26. In this embodiment, the pyrolysis and the Gasification of pulverulent biomass is done in the sky of the reactor 23.

FIG. 9 is a second principle for driving the pulverulent biomass BP by the GPC loaded pyrolysis gas stream. The pulverulent biomass reservoir BP has a supply opening 261 made of pulverulent biomass BP and an opening 262 connected to the GPC-charged pyrolysis gas flow circuit in which the charged pyrolysis gas stream GPC circulates at a high speed. This circuit has a throat 264 located upstream and near the opening 262 of the reservoir 26 of pulverulent biomass BP. The passage of the pyrolysis gas stream GPC loaded by this constriction creates a venturi effect driving the pulverulent biomass BP into the charged pyrolysis gas flow circuit. The reservoir 26 furthermore has an opening 265. In this embodiment, this opening 265 is connected to the GPC-charged pyrolysis gas flow circuit and a portion of the charged pyrolysis gas flow GPC passes through this opening and enters the reservoir 26. The velocity of the charged pyrolysis gas stream GPC contributes to the creation and maintenance of a fluidized bed of pulverulent biomass. In addition, the GPC-charged pyrolysis gas stream entering the reservoir being hot, the pyrolysis and the gasification of the biomass is at least partly in the reservoir 26. The residues of the pyrolysis / gasification of the pulverulent biomass BP are entrained and injected into the sky of the reactor 23 by the GPC loaded pyrolysis gas stream.

FIG. 10 is a schematic representation of the drying module of liquid biomass BL for obtaining pulverulent biomass BP. In this example, the liquid biomass BL is in a tank 250. The liquid biomass BL at the bottom of this tank is sprayed into the top of the tank 250, by any method of atomizing a liquid, in the form of The reservoir 250 further comprises an inlet opening 252 of a hot drying gas stream GS which is projected towards the fine droplets of liquid biomass BL. The meeting of the fine droplets of liquid biomass BL and the drying gas stream GS produces the almost instantaneous evaporation of the liquid, by releasing a pulverulent biomass BP and water vapor H ₂ O. The pulverulent biomass mixture BP and steam H ₂ O water is then sent through an opening 254 to a cyclone 255 effecting the separation of pulverulent biomass BP and water vapor H ₂ O. The transformation of liquid biomass into pulverulent biomass can comprise several modules similar to tank 250, in parallel and the completion of the drying of the pulverulent biomass can be obtained by several modules similar to cyclone 255 operating in series allowing both to dry the pulverulent biomass and separate it from the water vapor thus generated.

The significant increase in power of the system according to the invention, compared to the state of the prior art, at a relatively constant cost and space requirement, is obtained by the implementation of:

A drying module external to the reactor by recovering the calories available in the gasification gases,

Means for extracting the pyrolysis and charged gasification gases that compensate for the variation in pressure drop as a function of the height of the biomass,

Means for injecting pulverulent biomass into the reactor skies by using the circulation circuit of the charged pyrolysis gas flow; a step-by-step biomass treatment; the biomass changing direction;

• a drying treatment of liquid biomass to transform it into pulverulent biomass by recovering the calories available in gasification gases The advantages of the system according to the invention as well as the method implemented in the system according to the invention also appear by analyzing the various parameters on which it is possible to act to optimize the reactions and increase the power of the gasifier, congestion and substantially constant cost compared to the reactors according to the state of the prior art.

Referring to the various preferred embodiments of the invention, it can be seen that: a) By recovering the calories from the gasification gas and using it to dry the biomass outside the single pyrolysis / gasification reactor,

• the pyrolysis zone is correspondingly increased by reducing the drying zone within the reactor, thereby accelerating the rate of passage of the biomass, • reducing the amount of water vapor that is always in excess in the biomass, whose evaporation is endothermic, which avoids having to compensate for the loss of energy by a greater consumption of the carbon contained in the biomass and makes it possible to increase the CGI of the synthesis gas, reducing the amount of water vapor in the charged gasification gas, the pci per volume of gas is automatically increased, the water vapor not being combustible. b) By implementing a compensating device for the variation of pressure loss as a function of the height of biomass, the reactive zone of the biomass is increased, c) By replacing the single grid (fixed bed) of drying, pyrolysis and gasification. whose total length corresponds to the length of the reactor by two superimposed grids (beds), as represented in FIG. 6, each covering the total length of the reactor it is practically possible to double the feed rate of the biomass, with a surplus low cost compared to a single grid. d) By having a separate grid for the gasification, under the pyrolysis grid, this makes it possible to reduce the width of the grid of gasification to increase the height of the reducing material and increase the reactions

C + H2O ++ CO + H2

C + CO2 +> 2 CO e) By having two systems for advancing biomass in the pyrolysis module on the one hand and in the gasification module on the other hand, it is possible to adjust the relative velocities for optimize the reactions f) By having a single location in the reactor sky for the supply of the oxidant, for the injection of the pyrolysis gases and for the injection of the pulverulent biomass, entrained in the reactor by a venturi effect the zone of oxidation is delimited in a single zone, which makes it possible to obtain an optimum average temperature for controlled oxidation and at the same time to obtain the addition of complementary energy by the pulverulent biomass, allowing an acceleration of the speed of circulation of the pyrolysis gas and consequently an acceleration of the pyrolysis. g) By adding a device allowing to treat the pulverulent biomass, the power produced by the only mass biomass is increased without any significant modification of the bulk and the cost of the reactor, h) By treating in the same reactor a pulverulent biomass and a mass biomass it allows to use the mass biomass to purify the pyrolysis gases of the pulverulent biomass, which would be found after gasification of the pulverulent biomass if one operated with a reactor dedicated to the only pulverulent biomass operating then in fluidized bed. i) By transforming the liquid biomass into pulverulent biomass and gasifying it at the same time as the mass biomass by recovering the calories from the gasification gas available to evaporate the previously atomized liquid into fine droplets, the power of the reactor is further increased and we are expanding the nature of gasifiable biomasses. In addition, the system that is the subject of the invention makes it possible to modulate the power of the reactor by reducing the power with respect to the maximum possible power for a given size and cost, which could be useful if the energy requirement periodically decreases for example. in Week-end.

The elements available to reduce the power of the installation are in a non-limiting way:

stopping the gasification of the pulverulent biomass in order to conserve only the mass biomass; reducing the suction means while simultaneously reducing the biomass supply and reducing the oxidant input.

Naturally, the invention is not limited to the examples and embodiments that we have just described.

Claims

1) Biomass treatment module (B) with a treatment gas stream on a substantially horizontal fixed bed (L), said module having an inlet opening (11) for the biomass (B) to be treated on said fixed bed ( L) and an outlet opening (12) for the biomass (B) after treatment, characterized in that said treatment module comprises a plurality of zones (14), said treatment zones, said module further comprising:

at least one injection means (13) for a treatment gas flow in said module, said injection means (13) being common to said treatment zones (14), and extraction means (15, 16, 17) of the treated treatment gas stream obtained after treatment, said extraction means producing, at each of said treatment zones (14), a regulation of the extraction of said loaded stream as a function of the biomass thickness at said zone, so that said extraction is carried out with a substantially constant pressure drop for all of said treatment zones (14).

2) Module according to claim 1, characterized in that the extraction means (15, 16, 17) of the treatment gas stream loaded with a treatment zone (14) comprise: at least one extraction opening ( 15) arranged under the fixed horizontal bed (L), and

at least one suction means (17) of said treatment gas stream loaded through said opening (15).

3) Module according to claim 2, characterized in that the suction means (17) of the treated treatment gas stream are common to the treatment zones (14) and the size of each of the extraction openings (15) of each treatment areas (14) is substantially proportional to the thickness of the biomass (B) present at level of said treatment zone (14) so that the extraction pressure drop is substantially constant for all the treatment zones (14).

4) Module according to claim 2, characterized in that the suction means (17) of the charged treatment gas stream are common to all the treatment zones (14) and the size of each of the extraction openings (15) each of the treatment zones (14) being substantially constant, and at least one suction regulating member (16) being disposed at each of said extraction openings (15) so that the pressure drop is substantially constant at all treatment areas (14).

5) Module according to claim 4, characterized in that the regulating member (16) is a valve disposed at the extraction opening (15) and arranged to regulate the suction of treated treatment gas stream.

6) Module according to claim 2, characterized in that the size of the extraction openings (15) is substantially constant, each of the extraction openings (15) of each of the treatment zones (14) comprising a suction means (16) adjusted so that the extraction pressure drop is substantially constant at all the treatment zones (14).

7) Module according to any one of the preceding claims, characterized in that the substantially horizontal fixed bed (L) is permeable to the treated treatment gas stream.

8) Module according to any one of the preceding claims, characterized in that it comprises a device (19) provided for advancing the biomass (B) on said horizontal fixed bed (L) of the inlet opening (11). ) towards the discharge opening (12). 9) Biomass processing system on substantially horizontal fixed bed, said system comprising:

an inlet opening (233) of said biomass (B) to be treated on said horizontal fixed bed (L, L1),

a single reactor (23) for treating biomass, comprising a first and a second module (231, 232) according to any one of claims 1 to 9, communicating with each other:

Said first pyrolysis module (231) pyrolyzing said biomass (B) admitted by said inlet opening (233) with a gaseous treatment stream and comprising first means for extracting the gaseous pyrolysis stream; charge,

Said second gasification module (232), carrying out a gasification of said biomass (B) from said first module (231) by said gaseous treatment stream and comprising second extraction means of the charged gaseous gas flow,

an outlet opening (235) for residues from the gasification of the biomass.

10) System according to claim 9, characterized in that it further comprises a charged charge pyrolysis gas flow circuit (GPC) in the sky of the reactor (23), wherein said charged pyrolysis gas stream (GPC) is oxidized in the presence of oxidant (C) to obtain the gaseous flow of biomass treatment.

11) System according to claim 10, characterized in that the feed circuit of the charged pyrolysis gas stream (GPC) in the reactor sky (23) comprises a device (264), by venturi effect, of biomass pulverulent (BP) in the sky of the reactor (23).

12) System according to claim 11, characterized in that it comprises means for maintaining the pulverulent biomass (BP) in the form of a fluidized bed. 13) System according to any one of claims 10 to 12, characterized in that it further comprises means for injecting an oxidizer into the sky of the reactor (23).

14) System according to any one of claims 10 to 13, characterized in that it comprises at least one heat exchanger (28) provided for recovering, at least in part, the thermal energy of the charged gasification gas stream (GGC ).

15) System according to any one of claims 10 to 14, characterized in that it comprises a drying module (21,22) of biomass (B) disposed upstream of the reactor (23).

16) System according to any one of claims 10 to 15, characterized in that it comprises means for separating (29) at least one gaseous component in the gaseous gasification gas flow (GGC).

17) System according to any one of claims 10 to 16, characterized in that it comprises a drying module (25) of liquid biomass (BL), said drying module (25) of the liquid biomass (BL) comprises means for atomizing, in said module, liquid biomass (BL) in the form of fine droplets treated with a gaseous drying flow (GS), said drying producing pulverulent biomass (BP) sprayed in the sky of the reactor (23) to be pyrolyzed and carbonated.

18) System according to any one of claims 10 to 17, characterized in that the pyrolysis module (231) and the gasification module (232) are superimposed, said pyrolysis module (231) being disposed above said module of gasification (232), in said gasification module (232) the biomass (B) having a flow direction opposite to the direction of flow of said biomass (B) in the pyrolysis module, said system further comprising at least one opening of passage (238) allowing the gaseous treatment stream to pass from the pyrolysis module (231) into the gasification module (232)

19) Process for the gasification of biomass on a substantially horizontal fixed bed by a gaseous treatment stream, said process comprising the following steps:

pyrolysis of the biomass in a so-called pyrolysis module by said gaseous treatment stream; gasification of the biomass in a so-called gasification module by said gaseous treatment stream, said pyrolysis and gasification modules being in communication with each other and arranged in a single reactor, each of said modules comprising several zones (14), so-called process, said method further comprising

an injection of said treatment gas stream into the sky of said modules, said injection being common to the treatment zones of each of said modules,

at the level of each of said treatment zones, an extraction of the charged pyrolysis gas stream as a function of the biomass thickness present at said zone, such that said extraction is carried out with a substantially constant loss of charge for the all of said treatment areas (14), and

an extraction of the charged gaseous gas flow, said extraction being carried out with a substantially constant loss of charge for each of said treatment zones of said gasification module.

20) The method of claim 19, characterized in that it further comprises an introduction of the biomass on the horizontal fixed bed and an extraction of the residues of the gasification.

21) Method according to any one of claims 19 or 20, characterized in that it comprises an injection of the gas stream of pyrolysis charged (GPC) in the sky of the reactor (23), wherein said charged pyrolysis gas stream (GPC) is oxidized in the presence of oxidant (C) to obtain the treatment gas stream.

22) A method according to claim 21, characterized in that it further comprises an injection of pulverulent biomass into the air of the reactor, said pulverulent biomass being driven by the charged pyrolysis gas stream (GPC), by venturi effect.

23) Method according to claim 22, characterized in that it comprises a gasification of the pulverulent biomass in the sky of the reactor (23).

24) Method according to any one of claims 22 or 23, characterized in that the pulverulent biomass (BP) is in the form of a fluidized bed.

25) Method according to any one of claims 19 to 24, characterized in that it further comprises injecting an oxidizer in the sky of the reactor (23).

26) Method according to any one of claims 19 to 25, characterized in that it comprises at least one heat exchange to recover, at least in part, the thermal energy of the gaseous gasification gas flow (GGC).

27) Method according to any one of claims 19 to 26, characterized in that it comprises a step of drying the biomass (B) before the pyrolysis step.

28) Method according to any one of claims 19 to 27, characterized in that it comprises a step of drying a liquid biomass (BL) in a drying module (25), said liquid biomass (BL) being atomized in said drying module (25) in the form of fine droplets treated with a gaseous drying flow (GS), said drying Producing pulverized biomass (BP) sprayed in the sky of the reactor to be pyrolyzed and gasified.

29) Process according to any one of claims 19 to 28, characterized in that it comprises a step of separating at least one gaseous component (GS1, GS2, GS3) present in the gasification gas feed stream (GGC) .