FR3056573A1 - CARBONACEOUS FILLING GASIFICATION METHOD IN AN IMPROVED YIELDED FLOW REACTOR - Google Patents

Abstract

The present invention relates to a process for the thermochemical conversion of a feedstock of carbonaceous material into a synthesis gas in order to produce a fuel or a fuel, in particular a liquid fuel, or another synthetic product, according to which a step of injecting the charge of carbonaceous material into an injection zone of a flow-type gasification reactor, preferably at temperatures of between 1400 and 1600 ° C, the charge being mixed in the injection zone, a gas or a mixture of pressurized carrier gas which is also a combustible gas or a mixture of combustible gas, whose concentration in the air is greater than its upper explosive limit (LSE).

Description

Holder (s): COMMISSIONER OF ATOMIC ENERGY AND ALTERNATIVE ENERGIES Public establishment.

Extension request (s)

Agent (s): NONY CABINET.

METHOD FOR GASIFICATION OF CARBONACEOUS MATERIAL LOAD IN AN IMPROVED FLOW REACTOR.

FR 3,056,573 - A1 _ The present invention relates to a process for thermochemical conversion of a charge of carbonaceous material into a synthesis gas in order to produce a fuel or a fuel, in particular a liquid fuel, or another synthesis product, according to which a step of injecting the charge of carbonaceous material is carried out in an injection zone of a gasification reactor of the entrained flow type, preferably at temperatures between 1400 and 1600 ° C., the charge being mixed in the injection area, to a gas or a mixture of carrier gas under pressure which is also a combustible gas or a mixture of combustible gases, the concentration of which in the air is greater than its upper explosive limit (LSE) .

Carbonaceous product - (coal, plastic, ...)

ÎPreparation and! pressurization T

Injection

Fuel gas (Pressurized fine gasification [pressurized rfE ^

Product of interest (fuel, ..

-4Synthesis (* - 7; <_ J Syngaz k purifies .T

Agent

Ί Decarbonation K; —I- I, —I Syngaz

CO, \ gasifying crude

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CARBONACEOUS MATERIAL LOAD GASIFICATION IN AN IMPROVED YIELD REACTOR

Technical area

The present invention relates to a process for the gasification of biomass and, more generally of charging carbonaceous material, in a gasification reactor of the entrained flow type, in order to produce fuels or fuels.

The invention aims to increase the profitability of the overall gasification process and more particularly to increase the material and energy yields of the process.

Although described with reference to biomass, for a conversion into a fuel or a fuel, in particular a liquid fuel, or another synthetic product, the invention can be used for the conversion of other charges of carbonaceous material (coal, pet coke, organic waste ...).

State of the art

The term carbonaceous charge designates any combustible material consisting of compounds containing carbon.

It can therefore be biomass, that is to say any inhomogeneous material of plant origin containing carbon, such as lignocellulosic biomass, forest or agricultural residues (straw), or household waste. All of these loads can be dry or wet.

It can also be a fossil fuel, such as coal.

It can also be combustible waste of industrial origin containing carbon, such as plastics.

It can also be a combination between these different charges.

The current processes under study or on an industrial pilot scale, allowing thermochemical conversion of biomass or other charges into liquid or gaseous fuel by chemical synthesis, necessarily include a step of gasification of the carbonaceous charge to obtain a synthesis gas containing carbon monoxide (CO) and hydrogen (EL).

The gasification stage proper is carried out continuously from the carbonaceous charge of different types and sizes, usually stored at atmospheric pressure.

The gasification of biomass and coal has been known for a long time. In general, it can be defined as a thermochemical transformation of biomass or coal by the action of heat in the presence of gasifying agents. We are looking to generate, after gasification, a mixture of so-called syngas which includes carbon monoxide and hydrogen (CO + H2) among others.

Thus, the processes of gasification of lignocellulosic biomass make it possible to generate a synthesis gas which makes it possible to produce downstream either liquid fuels or other organic products. This gasification takes place typically in the presence of water vapor at around 1400-1600 ° C for entrained flow reactors. Conventionally, these processes convert the carbon of the biomass with a gas leaving the gasifier with an average composition of 20-25% in CO, 8-12% in CLL, 18-22% in CO2 and approximately 38-42% in H2 and, organic compounds C2 to Ci6 plus inorganic compounds.

A major drawback of these methods is that the rate of conversion of carbon from biomass to CO currently achieved is not high enough since it is only around 35-40%. Another major drawback of these processes is that the CO2 emitted is currently lost, in particular in the end it is released into the atmosphere. However, any conversion of carbon from biomass, more generally from carbonaceous feedstock, into CO2 can be considered as a loss of reaction yield in order to obtain synthetic methane (SNG) or a liquid fuel (Diesel Fischer Topsch) in the end. or another organic product (methanol, dimethyl ether, etc.).

There are different operational or research gasification processes that can be grouped as follows: gasification in a counter-current fixed bed, in a co-current fixed bed, in a fluidized bed and finally, entrained flow gasification. .

In an entrained flow reactor (RFE), the combustion reaction takes the form of a flame, which implies a very specific biomass injection mode.

Indeed, it must be introduced into the reactor in atomized form, in suspension in a transport gas or carrier gas. The atomized jet is then brought into contact with the oxidizing agent, a mixture of oxygen and water vapor.

In order to obtain good combustion, the mixing with the oxidant must take place quickly and as homogeneously as possible.

This is why the injection technologies used play a vital role and have been the subject of numerous developments.

Synthesis reactions, where the synthesis gas, commonly known as "syngas", a mixture of H2 and CO, is transformed into fuel or product of interest, take place under pressure. Typically, the preferred pressure is of the order of 30 bars for a Fischer-Tropsch synthesis (FT).

In a continuous installation, the gasification stage upstream of the synthesis must also take place under pressure to avoid having to compress the syngas produced. This pressurization also makes it possible to minimize the investment cost by a significant reduction in the size of the gasification reactor and the non-investment in dedicated compressor.

We can cite here patent applications WO2013 / 87521, WO2013 / 45266 or WO2008 / 95977 which propose to inject solid biomass under pressure.

The biomass powder is pressurized before being injected into an RFE reactor.

However, injections of solid powder into an RFE reactor are difficult to carry out, in particular when it is desired to use a minimum of neutral carrier gas, of the CO2 or N2 type.

Indeed, the speed of the particles must be precise, that is to say sufficiently large to stabilize the flame in particular for the autothermal modes where one burns the carbonaceous load to bring the power necessary to the reactor RFE, but sufficiently small to respect a minimum residence time of the solid particles in the RFE reactor, in order to allow the gasification reaction to take place.

Specific hydrodynamic phenomena such as that known under the term "swirl" can also be used in the RFE reactor, to homogenize the mixture and the temperature.

An order of magnitude of the velocity of carbonaceous charge particles which is suitable in an RFE reactor is 5 to 10 meters per second (m / s).

The injection of a neutral carrier gas, such as nitrogen N2 or carbon dioxide CO2, is often used to reach these operating points. In particular, the technology for injecting coal in powder form into a gasification reactor with nitrogen as the carrier gas is known.

We can cite here the publications [1] to [3] which compare the results of solid injection, in particular for coal, with different neutral carrier gases: N2, Air, H2, CO2 and He. What emerges from these publications is the influence of the viscosity of the carrier gas as the most important criterion, with the conclusion that the higher the viscosity of the carrier gas, the better the fluidization of the particles.

Publication [4] mentions the recovery of CO2 produced by gasification and its recycling as a carrier gas for injection.

The major drawbacks of a carrier neutral gas for injecting powder into an RFE reactor are as follows:

- as mentioned above, it must be pressurized, which involves the use of electricity;

- it must be heated to the operating temperature of the RFE reactor, typically around 1500 ° C. The additional heating energy required is provided by burning either a higher amount of carbon resource (autothermal mode) or an auxiliary fuel (allothermic mode). This decreases the material yield, since there is less carbon from the biomass in the final fuel since part of it is transformed into CO2 via partial combustion;

- It dilutes the synthesis gas produced and must be separated from the latter, preferably before synthesis because the yields fall sharply otherwise.

The inventors of the present invention have made an inventory of the literature, including the scientific publications [1] to [4] already mentioned, which mentions the injection of solid particles into a neutral carrier gas.

We can group into two categories, the type of injection known in the literature, dispersed phase injection and dense phase injection.

With regard to the injection in dispersed phase, it is mentioned in the literature mainly relating to the injection of coal powder, that a consumption of several tonnes, typically 5 tonnes, of N2 or CO2 per tonne of solid injected is necessary. This corresponds to approximately 2% of the volume of solid in the carrier gas phase.

With regard to dense phase injection, it is mentioned in the literature that conveying using less carrier gas than the dispersed phase seems possible with good flowability of the powder.

In this case, consumption of 0.5 tonnes of CO2 per tonne of solid powder injected is thus commonly considered, which corresponds to 15 to 20% of the volume of solid in the carrier gas phase.

So far, it seems that no one has really quantified the impact of using neutral gas injected for gasification of carbonaceous feedstock in an RFE reactor.

Also, the inventors have thought of doing it, in order to have a real appreciation of the energy and material yield losses, and therefore of the impact on the cost of producing a fuel or a fuel.

Their energy consumption calculations show that an amount of 0.5 t of CO2 per tonne of carbonaceous charge, which corresponds to the case generally accepted in the prior art for a dense phase injection, represents a consumption of approximately 6% of the lower calorific value (PCI) contained in the biomass, with a distribution as follows:

- 1.5% for gas compression, due to the consumption of electricity,

- 3% for the rise in temperature of the neutral gas in the RFE reactor, this energy being able to be taken from the biomass, and

- 1.5% to separate the carrier gas from the synthesis gas obtained, due to the consumption of electricity, this separation not being profitable for nitrogen.

The inventors have also calculated the financial costs of producing a C5 + fuel, which is a mixture of diesel and naphtha, in the case of a plant producing bio-fuel from a ligno- biomass powder. gasified cellulosic in an RFE reactor.

The sensitivity study parameter is the quantity of neutral injection gas introduced into the reactor, with the following values considered: 0 for conveying powder without adding gas, which corresponds to a technically unrealistic case; 0.5 tonnes of CO2 per tonne of carbonaceous charge for conveying in dense phase; respectively 1, 2.5 and 5 tonnes of CO2 per tonne of carbonaceous charge for conveying in dispersed phase.

The results of these calculations are summarized in the table below:

Consumption per tonne of CO2 per tonne of charge carbonaceous 0 0.5 1 2.5 5 Cost of producing C5 + in allothermic mode (€ / l) -1.06 -1.21 -1.37 -2.00 > 3 Cost of producing C5 + in autothermal mode (€ / l) -1.10 -1.28 -1.48 -2.32 > 3

From this table, it can be seen that the impact of the quantity of neutral gas introduced is very significant on the final cost of a fuel of type C5 +.

There is therefore a need to improve the gasification process for a charge of carbonaceous material, in a gasification reactor of the entrained flow type, with a view to producing fuels or fuels, in particular with a view to increasing the profitability of the overall process and more particularly to increase the material and energy yields of the process, by reducing the impact of the use of a neutral gas as a carrier gas for injecting the charge into the reactor.

The general aim of the invention is to meet this need at least partially.

Statement of the invention

To do this, the subject of the invention is a process for thermochemical conversion of a charge of carbonaceous material into a synthesis gas with a view to producing a fuel or a fuel, in particular a liquid fuel, or another synthesis product, according to which performs a step of injecting the charge of carbonaceous material, in an injection zone of a gasification reactor of the entrained flow type, preferably at temperatures between 1400 and 1600 ° C., the charge being mixed in the injection area, to a gas or a mixture of carrier gas under pressure which is also a combustible gas or a mixture of combustible gases, the concentration of which in the air is greater than its upper explosive limit (LSE) .

Thus, the invention essentially consists in replacing all or part of the neutral gases used as a gas carrying the carbonaceous charge for injection into an RFE reactor with a combustible gas or a mixture of combustible gases, of methane type or gases obtained by the process and recovered downstream, in particular the top gases from a Fisher-Tropsch synthesis.

The inventors were against the reflexes of a person skilled in the art who never thought of using gas or a mixture of combustible gases for injection and pressurization because, de facto, he always considered the risks of 'flammability and explosion.

Surprisingly, the inventors have overcome this prejudice by substituting all or part of a neutral gas with a gas or mixture of combustible gases.

To ensure that there is no risk associated with this substitution, the combustible gas or mixture of combustible gases must feed the injector in which it is mixed with the carbonaceous charge powder, with a concentration in the air above its limit. higher explosiveness (LSE).

It is recalled here that according to the standards in force, the explosive limits of a combustible gas or vapor are the limit concentrations of the gas in the air which allow it to ignite and possibly explode. The explosion range is characterized by the lower explosion limit (LEL) and the upper explosion limit (LSE). Under the LEL the mixture is too poor in fuel to initiate a reaction. Above the LSE, the oxidizer is missing.

In particular, when it is desired to inject methane as a carrier gas into the RFE reactor, its concentration in the air at the level of the injector upstream of the reactor must be greater than 15% in order to be above his LSE.

The invention makes it possible to increase the material and energy yields but also the overall profitability of the process because for the same dimensioning of an RFE reactor as according to the state of the art, the quantity of synthesis gas which can be obtained is superior.

According to a first advantageous mode, the combustible gas or the mixture of combustible gases can be obtained at least in part by a process independent of the process for thermochemical conversion of the charge of carbonaceous material.

The combustible gas can advantageously be methane (CEE).

According to a second advantageous mode, alternative or in combination with the first variant, the combustible gas or the mixture of combustible gases can be at least partially one or more gases obtained by the process of thermochemical conversion of the charge of carbonaceous material. and recovered downstream from the gasification.

According to this second mode, it is advantageous to carry out, downstream of the gasification, a synthesis according to the Fischer-Tropsch process to produce liquid diesel, at least part of the gases known as overhead gases, originating from the Fischer synthesis being recovered then injected as a combustible gas or the carrier combustible gas mixture. When implementing the Fisher-Tropsch process, the recovered overhead gases can be sufficient on their own as injected combustible gases, even if an external supply of combustible gas is to be expected at least for the start-up of the installation implementing the method according to the invention.

Preferably, the pressure of the combustible gas or the mixture of combustible gas injected into the reactor is between 5 and 100 bars, typically equal to 30 bars.

More preferably, the ratio of mass flow rates between combustible gas or the mixture of combustible gas and carbonaceous charge is between 1 and 100%.

According to an advantageous variant, there is also carried out a step of pressurizing the powder of the carbonaceous charge by means of a combustible gas or of a mixture of combustible gases, upstream of the injection zone.

According to another advantageous variant, a neutral gas under pressure is circulated around the injection zone, the neutral gas being under overpressure relative to the pressure of the combustible gas or of the mixture of combustible gases.

Advantageously, the rate of combustible gas or of the mixture of combustible gases and / or the rate of oxygen in the injection zone is measured.

The charge of carbonaceous material can be biomass, preferably lignocellulosic.

The invention also relates to an installation for thermochemical conversion of carbonaceous material charge implementing continuously the process described above.

detailed description

Other advantages and characteristics of the invention will emerge more clearly on reading the detailed description of the invention given by way of illustration and not limitation, with reference to the following figures among which:

FIG. 1 is a schematic view of the principle of an installation for thermochemical conversion of a charge of carbonaceous material according to the state of the art, continuously implementing a gasification process in a reactor of the driven flow type, and a summary for the production of a product of interest such as a liquid fuel (BtL);

FIG. 2 is a diagrammatic view of the principle of an installation for thermochemical conversion of a charge of carbonaceous material according to the invention implementing continuously a gasification process in a reactor of the entrained flow type (RFE) and a synthesis for the production of a product of interest such as a liquid fuel (BtL);

FIG. 3 is a diagrammatic view of the principle of an installation for thermochemical conversion of a charge of carbonaceous material according to an alternative of the invention implementing continuously a gasification process in a reactor of the entrained flow type and a synthesis for the production of a product of interest such as a liquid fuel (BtL);

- Figure 4 is a schematic view showing a variant of the installation according to Figure 2;

- Figure 5 is a schematic view of an advantageous variant of a driven flow type reactor (RFE) according to the invention incorporating a pressurized enclosure with an independent neutral gas.

In the following description, the terms “inlet”, “outlet” “upstream”, “downstream” are used by reference with the direction of transfer of the charge of carbonaceous material and of the synthesis gas in the conversion installation putting implement the method according to the invention.

For the sake of clarity, the same references designating the same elements of an installation according to the state of the art and of an installation according to the invention are used for all of the figures 1 to 4.

As illustrated in FIG. 1, a continuous installation 1 according to the state of the art implements the process of gasification of a carbonaceous charge according to the invention for the synthesis of a product of fuel interest of synthesis.

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A gasification reactor 2 of the entrained flow type (RFE or EFR, acronym for "Entrained flow reactor") preferably operating at temperatures typically between 1400-1600 ° C and a pressure between 30 and 50 bars is supplied with continuous by the load from a suitable storage tank.

More specifically, the charge of carbonaceous material is prepared by grinding to be put into the form of a powder which is pressurized in a preparation and pressurization unit 3.

Continuous feeding can for example be carried out by means of at least one worm, advantageously as described in patent application WO 2005/092749.

The charge of prepared and pressurized carbonaceous material is mixed with a neutral carrier gas which is CO2, in an injector 4, the carrier CO2 conveying the charge in the RFE reactor 2.

As illustrated, the carrier CO2 comes from the crude synthesis gas mixture comprising, for the majority species, CO, CO2, H2O and FF obtained at the outlet of the RFE 2 reactor.

Thus, the crude synthesis gas mixture undergoes gas cleaning in a decarbonation device 5, adapted to extract the CO2. Preferably, the CO2 is removed from the gas mixture according to an amine absorption process implemented in device 5.

It is specified here that the absorption process with amines also called washing with amines is already widely tested on an industrial scale and that it consists in carrying out a capture of CO2 in a tower with amines, as solvent, typically towards 3040 ° C. Another commonly used process is methanol washing, known as Rectisol®, carried out at very low temperature, typically around -50 ° C and under pressure, typically around 30 bar.

Thus, the CO2 extracted from the raw synthesis gas is at the outlet of the device 5 pressurized in an ad hoc unit 6 then re-sent to the injector 4 in order to constitute the gas carrying the carbonaceous charge powder itself. even pressurized.

The cleaned synthesis gas is sent to a reactor 7 implementing a synthesis process, such as a Fischer-Tropsch synthesis.

To achieve a desired H2 / CO ratio, it is advantageous to reform the top gases from the Fischer-Tropsch synthesis in a suitable unit.

The reaction co-products can be recovered in an ad hoc unit 8.

After having noted by calculations the negative impact of the use of very significant recycled CO2 on the overall yield of the conversion process, as explained in the preamble, the inventors thought of replacing this neutral gas with a combustible gas as gas powder injection.

The combustible gas can advantageously be methane.

Thus, according to the invention, as illustrated in FIG. 2, a combustible gas or a mixture of combustible gas previously pressurized at the same operating pressure of the RFE reactor 2, feeds the injector 4 in order to constitute the gas carrying the powder of carbonaceous charge coming upstream from its pressurization unit 3.

The combustible gas or mixture of combustible gases used is introduced into the injector with a concentration in the air above its upper explosive limit (LSE).

The use of a gas or a mixture of combustible gases makes it possible to increase the material and energy yields but also the overall profitability of the process according to FIG. 1, because for the same dimensioning of the RFE 2 reactor, which is based on the quantity of gas introduced, it is possible to produce more syngas.

Preferably, the injection of the oxidant (O2) is only carried out at the level of the burner in the gasification reactor RFE 2, in order to avoid any contact between this oxidant (O2) and the combustible gas upstream of the RFE reactor enclosure.

An alternative to the process according to the invention is shown in FIG. 3: part of the pressurized combustible gas is obtained directly by the process and recovered in order to supply the injector 4 in addition to the independent combustible gases, such as methane.

The advantage of this alternative according to Figure 3 is a reduction in the consumption of fuel supplied from outside, such as methane (CLL). In particular, when the synthesis reactor 7 is provided for implementing a Fischer-Tropsch synthesis, then the overhead gases (mixture of C1-C4) can be reinjected into the injector 4.

FIG. 4 illustrates an advantageous variant of the invention according to which the pressurization of the charge of carbonaceous material in powder form is also carried out in unit 3 also with a combustible gas or a fuel mixture.

The gas or mixture of combustible gases which is used to pressurize the powder is preferably identical to that which feeds the injector 4, and preferably still recovered directly from the synthesis reactor 7.

In addition to the special precautions linked to the use of combustible gases, care is taken to ensure the inerting of the pressurization airlock of the pressurization unit 3 before pressurization by the gas or mixture of combustible gases.

As illustrated in FIG. 5, provision can be made to arrange an enclosure 8 upstream of the RFE reactor 2. The interior 80 of this enclosure 8 is pressurized by means of a neutral gas, such as argon, which makes it possible to '' prevent the combustible gases to be injected into the RFE 2 reactor from mixing with the air without control. Thus, if a possible leak occurs in this enclosure 8, i.e. upstream of the RFE reactor, the argon enters the RFE 2 reactor, which can be detected immediately. Preferably, the gas pressure within this enclosure 8 can be equal to that of the operating of the RFE reactor plus a value of a few bars, typically from 1 to 5 bars.

Although described with reference exclusively to biomass, the installation for converting into a fuel or a fuel, in particular a liquid fuel, or another synthetic product, the invention can be used for the conversion of other charges of carbonaceous material ( coal, pet coke, organic waste ...).

Other variants and improvements can be provided without departing from the scope of the invention.

The invention is not limited to the examples which have just been described; one can in particular combine together characteristics of the examples illustrated within variants not illustrated.

References Cited [1]: Haifeng Lu, Xiaolei Guo, Xin Gong, Xingliang Cong, Weibin Dong, Wanjie Huang "Effect of gas type on the fluidization and discharge characteristics of the pulverized coal", Powder Technology 217 (2012) 347-355;

[2]: Chunbao Xu, J.-X. Zhu "EFFECTS OF GAS TYPE AND TEMPERATURE ON FINE PARTICLE FLUIDIZATION", CHINA PARTICUOLOGY Vol. 4, Nos. 3-4, 114-121, 2006;

[3]: D. Geldart and A-R. Abrahamsen "Homogeneous Fluidization of Fine Powders 10 Using Various Gases and Pressures" Powder Technology. 19 (1978) 133-36;

[4]: Haifeng Lu, Xiaolei Guo, Shunlong Tao, Xin Gong; "A further study on effect of gas type on pulverized coal discharge", Powder Technology 281 (2015) 193-199.

Claims (12)

1. Method for thermochemical conversion of a charge of carbonaceous material into a synthesis gas with a view to producing a fuel or a fuel, in particular a liquid fuel, or another synthesis product, according to which an injection step is carried out. the charge of carbonaceous material in an injection zone of a gasification reactor of the entrained flow type, preferably at temperatures between 1400 and 1600 ° C., the charge being mixed in the injection zone, with a gas or a mixture of pressurized carrier gas which is also a combustible gas or a mixture of combustible gases, the concentration of which in the air is greater than its upper explosive limit (LSE). 2. Conversion process according to claim 1, the combustible gas or the mixture of combustible gases being obtained at least in part by a process independent of the thermochemical conversion process of the charge of carbonaceous material. 3. The conversion method according to claim 2, the combustible gas being methane (CPU). 4. Conversion method according to one of the preceding claims, the combustible gas or the mixture of combustible gases being at least partially one or more gases obtained by the thermochemical conversion process of the charge of carbonaceous material and recovered in downstream of gasification. 5. Conversion process according to claim 4, according to which a synthesis is carried out, downstream of the gasification, according to the Fischer-Tropsch process to produce liquid diesel, at least part of the gases called overhead gases, resulting from the synthesis Fischer being recovered and then injected as combustible gas or the carrier combustible gas mixture. 6. Conversion process according to one of the preceding claims, according to which the pressure of the combustible gas or the mixture of combustible gas injected into the reactor is between 5 and 100 bars, typically equal to 30 bars. 7. Conversion process according to one of the preceding claims, according to which the ratio of mass flow rates between combustible gas or the mixture of combustible gas and carbonaceous charge is between 1 and 100%. 8. Conversion method according to one of the preceding claims, according to which there is further carried out a step of pressurizing the powder of the carbonaceous charge using a combustible gas or a mixture of combustible gases, upstream of the injection area. 9. Conversion method according to one of the preceding claims, according to which a pressurized neutral gas is circulated around the injection zone, the neutral gas being under overpressure relative to the pressure of the combustible gas or of the gas mixture. combustible. 10. Conversion process according to one of the preceding claims, in which the rate of combustible gas or of the combustible gas mixture and / or the rate of oxygen in the injection zone is measured. 11. Conversion process according to one of the preceding claims, the charge of carbonaceous material being biomass, preferably lignocellulosic. 12. Installation (1) of thermochemical conversion of carbonaceous material charge intended to continuously implement the method according to any one of the preceding claims, comprising a gasification reactor (2) of the entrained flow type, preferably operating at temperatures between 1400 and 1600 ° C, the reactor comprising an injection zone (8), suitable for mixing the feedstock with a gas or a mixture of pressurized carrier gas which is also a combustible gas or a mixture of combustible gases, whose concentration in the air is higher than its upper explosive limit (LSE). 1/3 Reaction by-products (Recovery) * - Product * - of interest (fuel, ...) z- \ Summary * k J