Method for the treatment of organic waste

Abstract

The invention relates to a method for hydrotreating a mixture M1 comprising at least organic matter, the method comprising: a) pressurising the mixture M1 to a pressure ranging from 20 to 350 bar, in order to obtain a stream M1p; b) a step of heating the mixture M1p to a temperature ranging from 170 to 430°C, in order to obtain a mixed stream M2; c) introducing at least one fraction of the stream M2 into a hydrotreatment reactor by a tangential injection allowing a cyclonic movement; and d) recovering downstream of the reactor a stream M3 enriched with soluble materials and a stream M4 depleted of soluble materials.

Description

ORGANIC WASTE TREATMENT PROCESS TECHNICAL FIELD OF THE INVENTION

[0001] The invention relates to the field of biomass treatment, in particular sludge from sewage treatment plants, food and agri-food waste, manure digestates and agricultural residues. TECHNICAL BACKGROUND

[0002] Hydrothermal biomass treatments are becoming increasingly common. They require high temperatures. It is therefore essential to control temperatures in order to obtain the desired biomass quality.

[0003] Thus, controlling the temperatures and residence times of the process is extremely important to achieve the desired result. Temperatures that are too high or too low, residence times that are too short or too long either do not allow the desired reactions to occur or lead to unwanted side reactions that result in an overall degradation of the desired performance or, worse, in the production of a residue whose treatment costs will be significant.

[0004] In particular, the heating stage of hydrothermal treatments is a major cause of these side reactions due to the long residence time at intermediate temperatures which can lead to the formation of unwanted compounds such as oils, tars or derivatives close to coal. This heating stage is all the longer as the temperatures to be reached are high, in particular when the temperatures to be reached are close to or higher than the temperature of supercritical water.

[0005] Furthermore, in the state of the art, heating is often carried out via a “tube in tube” type exchanger to recover the output heat in order to reduce the quantity of heat required for the process. However, in this type of exchanger, the low thermal conduction of the product to be heated leads to a very significant temperature variation inside the product and therefore different process conditions between the different parts of the product leading to unwanted parasitic reactions.

[0006] There is therefore a need to provide a process for hydrotreating a mixture, such as biomass, allowing better heat exchanges and less formation of unwanted compounds such as oils, tars or derivatives close to coal.

[0007] The invention relates to a process for hydrotreating a mixture M1 comprising at least organic matter, said process comprising:

[0008] a) Pressurizing the mixture M1 to a pressure ranging from 20 to 350 bars, in order to obtain a flow M1p,

[0009] b) a step of heating the mixture M1p to a temperature ranging from 170 to 430°C, in order to obtain a flow of mixture M2,

[0010] (c) an introduction of at least a fraction of the M2 flow into a hydrotreatment reactor by a tangential injection allowing cyclonic movement,

[0011] d) recovery downstream of the reactor of an M3 stream enriched in soluble materials and an M4 stream depleted in soluble materials.

[0012] Preferably, the recovery of the M3 stream during step d) is carried out through at least one filter, said filter comprising at least one filtration layer preferably having a mesh size of less than 100 µm, preferably less than 50 µm, more preferably less than 40 µm, said filter preferably being in the hydrotreatment reactor.

[0013] Preferably, step b) comprises at least one step of injecting water ES at a temperature of at least 374°C into the flow of mixture M1p in order to obtain the flow M2, the injected water preferably being at a pressure of at least 225 bars.

[0014] According to one embodiment, the recovery of the M3 stream during step d) is controlled by determining the pressure difference between the pressure in the hydrotreatment reactor and the pressure in the M3 stream downstream of the filter and downstream of the reactor.

[0015] According to one embodiment, the hydrotreatment reactor is maintained at a temperature ranging from 170°C to 430°C.

[0016] Preferably, the recovery of the M3 stream is implemented in the upper part of the hydrotreatment reactor, via a vertical outlet line, and the recovery of the M4 stream is implemented in the lower part of the reactor.

[0017] According to one embodiment, the method further comprises, downstream of the filter and downstream of the reactor, a step e) of injecting water at a temperature of at least 374°C into the flow M3, counter-current to said flow, where appropriate said water preferably being at the same temperature and at the same pressure as the water injected during step b).

[0018] Preferably, when the counter-current water injection of step e) is implemented, then the outlet of the reactor in the lower part is opened in order to extract a flow M4.

[0019] According to one embodiment, the mixture flow M2 is introduced into the reactor with a speed ranging from 0.5 to 20 m / s, preferably from 0.5 to 15 m / s, preferably from 2 to 10 m / s.

[0020] According to one embodiment, the method further comprises: at least one heat exchange step X1 making it possible to recover heat from the flow M3 to at least partially heat the water intended to be injected in step b), a cooled flow M5' then being obtained, and optionally comprising at least one additional water heating step, downstream of the heat exchange X1 making it possible to heat the water to the temperature of at least 374°C before its injection in step b) and where appropriate before its injection into the water e), and optionally at least one heat exchange step X2 making it possible to recover heat from the flow M5' to heat the mixture M1p upstream of the water injection of step b), a cooled flow M5' then being obtained.

[0021] According to one embodiment, the method further comprises:at least one step of cooling at least a fraction of the stream M5' or, where appropriate, the stream M5'' making it possible to obtain steam and a stream M6 comprising hydrotreated organic matter, anda step of injecting at least a portion of said steam to preheat the mixture M1 upstream of step a) of pressurizing, said mixture M1 preferably being preheated to a temperature ranging from 50 to 170°C, preferably from 50 to 90°C,optionally a step of cooling at least a fraction of the stream M6 to obtain a cooled stream M6' and optionally a step of digesting the stream M6'.

[0022] According to one embodiment, the hydrotreatment reactor comprises an excess thickness which resists abrasion on at least a portion of its internal surface.

[0023] The invention also relates to an installation for implementing the hydrotreatment method according to the invention, said installation comprising: a mixture supply line M1, a pressurizing pump 2 supplied by the mixture supply line M1 and comprising a mixture outlet line M1p, a heating device 11 downstream of the pump 2 comprising an inlet for the mixing line M1p and an outlet for the flow line M2, a hydrotreatment reactor 1 comprising at least one inlet E1 for the flow M2, an outlet S1 for the flow M3 enriched in soluble matter and an outlet S2 for the flow depleted in soluble matter, the inlet E1 being configured so as to introduce a cyclonic movement into the reactor 1 via the inlet E1.

[0024] According to one embodiment, the hydrotreatment reactor 1 further comprises: at least one first filter F1, said first filter being arranged in such a way that the flow M3 enriched in soluble matter passes through the filter before leaving the reactor via the outlet S1, and optionally at least one second filter F1', said second filter F1' being arranged in such a way that the flow M3' enriched in soluble matter passes through said second filter F1' before leaving the reactor 1 via an outlet S1',

[0025] preferably, the outlets S1 and S1' are located in the upper part of the hydrotreatment reactor 1 and preferably allow vertical extraction, from the bottom to the top of hydrotreated organic matter, respectively M3 and M3'.

[0026] According to one embodiment, the heating device 11 comprises at least one water injection device ES in the mixing line M1p, said installation preferably further comprising: a heat exchanger 6 downstream of the hydrotreatment reactor 1, said heat exchanger making it possible to recover the heat in the flow line M3, possibly combined with the flow line M3', to obtain a flow M5' and to transfer this heat to the water upstream of the water injection device ES, and possibly a water heating device 7, downstream of the heat exchanger 6 and upstream of the water injection device ES,

[0027] said installation preferably further comprising: optionally a heat exchanger 8 making it possible to recover heat from the mixture M5' to obtain a mixture M5'' and to transfer this heat to the mixture M1p upstream of the water injection device ES, A cooling device 4 supplied by at least a fraction of the flow M5' or where appropriate M5'' making it possible to produce steam and a cooled flow M6, An injection device 3 of said steam produced into the mixture flow M1 upstream of the pressurization pump 2, Optionally a cooling device 9 downstream of the cooling device 4 supplied by at least a fraction of the flow M6 making it possible to cool at least a fraction of the flow M6 to obtain a flow M6', and Optionally a digester 5 supplied by the flow M6'.

[0028] The invention thus allows the biomass to be heated very quickly by direct heating, which subsequently allows the desired process conditions to be controlled.

[0029] The invention makes it possible to maintain the thermal recovery of the process by heating the water in supercritical conditions in order to minimize the overall thermal consumption of the process.

[0030] The cyclonic movement helps improve the quality of the hydrotreated organic matter.

[0031] The invention also makes it possible to separate the residence times between the massive particles constituting the biomass and for which the chemical reaction times (in particular solubilization) must be longer and the solubilized molecules which must be removed more quickly from the reactor to avoid secondary reactions, for example repolymerization.

[0032] Biomass has a certain viscosity. However, viscosity makes heat exchange difficult. Since water has a lower viscosity than any other biomass, heating the water will result in a smaller recovery exchanger and therefore a lower cost.

[0033] The invention proposes injecting supercritical water directly into the flow of organic matter M1. Thus, the thermal shock between the organic matter (M1), part of which is cellular content, and the very hot supercritical water will cause local cavitations due to the difference in local density and therefore local pressure. These cavitations allow immediate release of the cellular content into the aqueous matrix and therefore, subsequently, in the hydrotreatment reactor, immediate reactions of the proteins and sugars contained in the bacteria. BRIEF DESCRIPTION OF THE FIGURES

[0034] represents an installation according to an embodiment of the method according to the invention.

[0035] represents an installation according to an embodiment of the method according to the invention.

[0036] represents an installation according to an embodiment of the method according to the invention.

[0037] represents an installation according to an embodiment of the method according to the invention.

[0038] represents an installation according to an embodiment of the method according to the invention.

[0039] represents an installation according to an embodiment of the method according to the invention. DETAILED DESCRIPTION OF THE INVENTION

[0040] The invention relates to the hydrothermal treatment of a mixture M1 comprising organic matter.

[0041] Mixture M1 is typically a biomass. Biomass can be pasty or liquid, and can include sewage sludge, food and agri-food waste, and especially manure digestate and agricultural residues.

[0042] The invention relates to a process for hydrotreating a mixture M1 comprising at least organic matter, said process comprising:

[0043] a) Pressurizing the mixture M1 to a pressure ranging from 20 to 350 bars, preferably at least 150 bars, in order to obtain a flow M1p,

[0044] b) a step of heating the mixture M1p to a temperature ranging from 170 to 430°C, preferably from 250 to 350°C, in order to obtain a flow of mixture M2,

[0045] c) an introduction of at least a fraction of the mixture flow M2, preferably the entire flow M2, into a hydrotreatment reactor by a tangential injection allowing a cyclonic movement,

[0046] d) extraction from the reactor of an M3 flow enriched in soluble materials and an M4 flow depleted in soluble materials.

[0047] For the purposes of the present invention, the expression "at least a fraction of a mixture or stream" has the same meaning as the expression "all or part of said mixture or stream". When referring to a part of said mixture or stream, this expression refers to a certain proportion of said mixture or stream. For example, for the purposes of this expression "each fraction of the mixture" or "each fraction of the stream" will have the same composition.

[0048] For the purposes of the present invention, the expression "where appropriate of step X" introduces a characteristic present when step X is present.

[0049] For the purposes of the present invention, the expression “where applicable of the flow X” introduces a characteristic present when the flow X is present. Pressurization step a)

[0050] The method according to the invention comprises a step of pressurizing the mixture M1 preferably to a pressure ranging from 20 to 350 bars, preferably from 50 to 300 bars, preferably from 150 to 270 bars, preferably from 170 to 220 bars, said mixture M1 possibly already being under pressure before step a).

[0051] In particular, pressurization allows mixture M1 to be brought to a pressure sufficient for the mixture to be in a predominantly liquid phase. More specifically, the pressure in mixture M3 will typically be greater than the saturated vapor pressure of said mixture M3 to maintain the water in the liquid phase.

[0052] For the pressurization step, a pump can be provided on the M1 mixing line.

[0053] Downstream of the pressurization, a flow of M1p mixture is obtained. Heating step b)

[0054] The method of the invention comprises a step of heating the mixture M1p to a temperature ranging from 170 to 430°C, preferably from 250 to 350°C, making it possible to obtain a flow of mixture M2.

[0055] This heating can be implemented in one or more stages. A sub-stage can be heating by an external heat flow (electric heating, heat exchanger by a hot fluid (gas / liquid), microwave, etc.) or water injection.

[0056] Thus, according to a preferred embodiment, the heating step b) comprises at least one step during which water ES at a temperature of at least 374°C is injected into the mixture stream M1p in order to obtain a mixture stream M2 comprising water and organic matter. The mixture M2 will typically also comprise inorganic matter.

[0057] Water injection can, for example, be implemented at an angle ranging from 15° to 90°, preferably from 45 to 90°, or even from 45 to 75°, relative to the flow arrival line M1p.

[0058] According to one embodiment, the mixture M1p during the water injection of step b) is at a temperature ranging from 90°C to 300°C. In this case, the heating step b) may optionally comprise a sub-step of heating by an external heat flow (electric heating, heat exchanger by a hot fluid (gas / liquid), microwave, etc.).

[0059] Upstream of step b), the injected water will typically be at a pressure higher than the pressure of the M1p mixture.

[0060] According to a preferred embodiment of the invention, the water injected in step b) is at a pressure of at least 225 bars. According to this embodiment, the injected water will then be called “supercritical water”.

[0061] According to one embodiment, the heating step b) of the method comprises two sub-steps: a first sub-step of heat exchange between the flow M1p and flow M3, said flow M3 having optionally been subjected to one or more heat exchanges between the outlet of the reactor and this heat exchange with M1p, a second sub-step of injection of ES water at a temperature of at least 374°C and preferably at a pressure of at least 225 bars, in the flow line M1p downstream of the first sub-step.

[0062] According to one embodiment, the method of the invention comprises at least one step of heating the water making it possible to obtain water at a temperature of at least 374°C upstream of its injection in step b).

[0063] According to one embodiment, the method according to the invention comprises a step of pressurizing the water to a pressure of at least 225 bars followed by at least one step of heating the water to obtain water at a temperature of at least 374°C upstream of its injection in step b).

[0064] Preferably, at least one water heating step is implemented by heat exchange with the heat of at least a fraction of the stream M3 comprising hydrotreated organic matter leaving the hydrotreatment reactor, the stream thus cooled will be called stream M3' at the end of this heat exchange (it could be the heat exchange step X1 described below).

[0065] At the outlet of the injection between water and mud M1p, a static turbulator (e.g. chosen from propeller, blades, pipe bends, or combinations thereof) can also be introduced to increase turbulence and rapid heat exchange between mud and water and prevent mud and water from remaining in separate flows (to avoid laminar hydraulic lines).

[0066] Thus, according to one embodiment of the invention, upstream of step c), the mixture M2 is introduced into a static turbulator, said static turbulator then being located upstream or at the inlet of the hydrotreatment reactor.

[0067] According to one embodiment, a static turbulator is present upstream or at the inlet of the hydrotreatment reactor in order to increase the turbulence in the mixture M2.

[0068] According to a particular embodiment, the flow line M2, downstream of the water injection when it is present, comprises one or more pipe bends upstream of the hydrotreatment reactor. Mixing flow introduction step M2 c)

[0069] The method according to the invention comprises a step of introducing the M2 stream into a hydrotreatment reactor.

[0070] According to the method of the invention, the introduction of at least a fraction of the M2 flow into a hydrotreatment reactor is implemented by a tangential injection allowing a cyclonic movement.

[0071] According to the process of the invention, before entering the hydrotreatment reactor, the diameter of the reactor inlet pipe will be chosen so that the inlet speeds into the reactor are sufficient to cause the cyclonic movement of the particles of the mixture M2 without causing excessive turbulence, preferably the reactor inlet speed will be 0.5 to 20 m / s, preferably 0.5 to 15 m / s, preferably 2 to 10 m / s.

[0072] The cyclonic movement has several advantages. Due to the tangential feed, an azimuthal velocity is given to the multiphase flow. This azimuthal velocity drives the higher density particles towards the periphery of the reactor. A vortex is created in the hydrotreatment reactor, hence a centrifugation effect which adds to the gravity effect, increasing the efficiency of the separation of the flow of the hydrotreated organic matter M3 (soluble matter) from the rest, the rest being insoluble matter, of higher density, which continues to be hydrotreated by a residence time greater than that of the M3 matter or which will be rejected via the M4 outlet during the backflush.

[0073] The hydrotreatment reactor is advantageously maintained at a temperature ranging from 170°C to 430°C. For example, this temperature maintenance can be carried out via a peripheral heat exchange with a hot fluid, the implementation of the equipment inside a furnace maintained at temperature, the implementation of an electric heating collar.

[0074] According to one embodiment, the hydrotreatment reactor comprises an excess thickness which resists abrasion on at least a portion of its internal surface, in particular at the altitude close to that of the tangential injection of the flow M2. Thus, said excess thickness may only be present on a portion of the hydrotreatment reactor, in particular the portion in contact with the flow M2 during its injection into the reactor.

[0075] In the context of the process of the invention, control of the flow rates of the injected water, preferably supercritical water, and of the M1p mixture is advantageously implemented and will typically allow the new mixture (mixture called M2) to have a residence time in the hydrotreatment reactor ranging from 1 minute to 30 minutes, preferably 10 minutes to 15 minutes.

[0076] Step of recovering an M3 flow and an M4 flow d)

[0077] Downstream of the hydrotreatment reactor, an M3 stream enriched in soluble matter and an M4 stream depleted in soluble matter are recovered.

[0078] The M3 stream may be recovered downstream of one or more filters, said filter(s) being able to be present in the reactor and / or downstream of the reactor on the M3 stream line.

[0079] According to an advantageous embodiment of the invention, the recovery of the M3 stream enriched in soluble materials during step d) is carried out through at least one filter, preferably said at least one filter is present in the hydrotreatment reactor.

[0080] When the filter is present in the hydrotreatment reactor, this makes it possible to increase the filtering surface area and to have filters with a larger specific surface area, particularly in comparison with a filter present in the piping.

[0081] Additionally, when the filter is outside the hydrotreating reactor, it can be either in the piping or in another reactor downstream of the hydrotreating reactor, but in both cases the filter will clog faster than when the filter is in the hydrotreating reactor.

[0082] The filter limits the size of solid particles in the flow of hydrotreated organic matter M3, also called flow enriched in soluble matter.

[0083] The filter may comprise one or more filtration layers, which may optionally have different mesh sizes, preferably the external filtration layers have mesh sizes larger than the internal filtration layers.

[0084] According to one embodiment, the filter has a mesh size of less than 100 µm, preferably less than 50 µm, more preferably less than 40 µm. When the filter comprises several filtration layers, then the finest mesh will preferably have a size of less than 100 µm, preferably less than 50 µm, more preferably less than 40 µm.

[0085] According to a particular embodiment, a second filter is present in the hydrotreatment reactor or downstream of the hydrotreatment reactor on a flow outlet line M3' separate from the flow line M3. Thus, the second filter is configured such that material enriched in soluble materials is extracted from the reactor via this second filter. This second flow extracted via the second filter will be called M3'. The second filter will allow hydrotreated material (enriched in soluble materials) to be extracted when the first filter is saturated and while the first filter is being cleaned. Once the first filter is cleaned, it will resume its filtration role. This second outlet of material enriched in soluble materials will thus advantageously be open during the backflush period implemented on the first filter.

[0086] Advantageously according to this embodiment, the second filter will have a mesh size different from that of the first filter (filter allowing the extraction of the M3 flow), preferably a mesh size larger than that of the first filter.

[0087] Thus, according to this embodiment, the second filter will preferably have a mesh size of less than 200 µm, preferably less than 100 µm.

[0088] According to a particular embodiment, the first filter has a mesh size less than 40 µm and the second filter has a mesh size less than 100 µm.

[0089] This second filter may also comprise one or more filtration layers which may optionally have mesh sizes of different sizes, preferably the external filtration layers have mesh sizes larger than the internal filtration layers. When the second filter comprises several filtration layers, then preferably the finest mesh has a size of less than 200 µm, preferably less than 100 µm.

[0090] According to one embodiment, the recovery of the M3 stream during step d) is controlled by determining the pressure difference between the pressure in the hydrotreatment reactor and the pressure in the M3 stream at the outlet of the reactor downstream of the filter. According to one embodiment, the recovery of the M3 stream is carried out, typically by opening a valve V1 on the M3 stream line downstream of the filter, as long as the pressure difference is less than a predetermined threshold value, for example when the pressure difference is less than 10 bars.

[0091] This pressure difference check ensures that the filter is not excessively clogged.

[0092] According to one embodiment, the extraction of the M3 stream is implemented in the upper part of the hydrotreatment reactor, by a vertical outlet line (with respect to gravity). Thus, according to this embodiment, the M3 stream is preferably extracted by a flow circulating from the bottom to the top (with respect to gravity).

[0093] Preferably, the hydrotreatment reactor comprises at least one outlet in the upper part, at least one outlet in the lower part, and optionally at least a second outlet in the upper part.

[0094] For the purposes of the present invention, the expression "lower part" is opposed to the expression "upper part". Thus, an exit in the upper part will be located at a higher altitude than the exit in the lower part. Similarly, an exit in the upper part will be located at a higher altitude than an entrance in the lower part.

[0095] The method of the invention thus comprises an introduction of a flow M2, an extraction of a flow M3 and an extraction of a flow M4. Preferably, the inlet of mixture M2 is via an inlet E1 of the hydrotreatment reactor, the outlet of flow M3 is via an outlet S1 and the outlet of flow M4 is via an outlet S2.

[0096] Thus, according to an advantageous embodiment, the inlet E1 is located at a lower altitude than the outlet S1 and the inlet E1 is located at a higher altitude than the outlet S2 to extract the flow M4.

[0097] When a second filter is present, a flow M3' is extracted from the reactor via a third outlet S1', distinct from outlets S1 and S2. Thus, preferably, according to this embodiment, outlet S1' is located at an altitude higher than inlet E1, inlet E1 itself being at an altitude higher than outlet S2. Preferably, outlets S1 and S1' are at similar or even identical altitudes.

[0098] All of these configurations (E1, S1, S2 and where applicable S1') thus make it possible to optimize residence times and promote the solubilization of the material in the reactor.

[0099] According to one embodiment, the method further comprises a step e) during which water ES2 at a temperature of at least 374°C is injected into the flow line M3 leaving the hydrotreatment reactor downstream of the filter, preferably said water is at a pressure of at least 225 bars, more preferably said water injected into the flow line M3 is, where appropriate (i.e. when step b) comprises an injection of water ES) at the same temperature and at the same pressure as the water injected into the flow M1p during step b).

[0100] Thus, this injection of water ES2, preferably supercritical water, is implemented counter-currently to the flow M3 leaving the hydrotreatment reactor. According to one embodiment, this water injected into the flow line M3 counter-currently is obtained by the same method as that described for the water injected in step b) (advantageously heat exchange X1 then additional heating).

[0101] Typically, during this countercurrent water injection into the M3 stream, the M3 stream is no longer extracted from the hydrotreatment reactor, typically by closing a valve V1 present downstream of the hydrotreatment reactor and downstream of the filter on the M3 stream outlet line. The ES2 water injection then typically takes place between the filter and the valve V1.

[0102] This injection of ES2 water into the M3 stream allows a backflush of the first filter to be carried out. This washing step can be implemented at the same time as the recovery of the M4 stream via the lower outlet of the reactor, for example by opening a V2 valve on the M4 stream line. Thus, this countercurrent injection of ES2 water can be triggered when the pressure difference between the pressure in the hydrotreatment reactor and the pressure in the M3 stream at the reactor outlet downstream of the filter exceeds a certain predetermined threshold, for example from 10 bars.

[0103] According to an embodiment of the method of the invention, when a counter-current injection of water ES2, preferably supercritical water, is implemented in the flow M3, then preferably the reactor further comprises an outlet in the lower part and the outlet of the reactor in the lower part is open (during said water injection), via the opening of a valve V2 downstream of the hydrotreatment reactor on the flow line M4, in order to extract a flow M4 depleted in soluble matter.

[0104] For the purposes of the present invention, the term “flow enriched in soluble materials” means a flow comprising a mass proportion of soluble materials greater than the mass proportion of soluble materials in the mixture M2.

[0105] For the purposes of the present invention, the term “flow depleted in soluble materials” means a flow comprising a mass proportion of soluble materials lower than the mass proportion of soluble materials in the mixture M2.

[0106] For the purposes of the present invention, a soluble material will be a material obtained after filtration in a 40 µm filter (material not retained by said 40 µm filter) then drying of an initial material.

[0107] Thus, according to one embodiment, the ratio between the concentration of soluble materials of the flow M3 and the concentration of soluble materials of the flow M4 is at least 2, preferably at least 4, more preferably at least 6, or even at least 10.

[0108] According to an embodiment implementing a second filter, during backwashing of the first filter, the flow outlet M3 is closed (for example by means of a valve V1) and it is possible for a flow M3' enriched in soluble matter to be extracted from the reactor via the second filter during said backwashing of the first filter.

[0109] Preferably, each of the flow outlets M3 and M3' is located in the upper part of the reactor, in order to allow a vertical outlet of the flow, from bottom to top.

[0110] Thus, according to this embodiment, a first valve V1 is present on the flow outlet M3 and a second valve V1' is present on the flow outlet M3'. Preferably according to this embodiment, when the first valve V1 is open, then either the second valve V1' is open or the valve V2 is open or both valves V1' and V2 are open.

[0111] According to the embodiment implementing two filters, said filters can be (i) in the hydrotreatment reactor or (ii) downstream of the hydrotreatment reactor or (iii) one of the two filters can be in the reactor and the other filter can be downstream of the reactor. According to this embodiment, two streams enriched in soluble matter M3 and M3' are then obtained downstream of the hydrotreatment reactor and downstream of said filters. Advantageously, the two stream lines M3 and M3' are combined, typically downstream of the valves V1 and V1'.

[0112] According to a particularly advantageous embodiment, the method of the invention further comprises at least one heat exchange step X1 making it possible to recover heat from the flow M3, possibly combined with the flow M3' to at least partially heat the water W1 intended to be injected for the heating step b). Downstream of the heat exchange X1, the flow M3 (possibly combined with the flow M3') which will have been cooled will be called flow M5' and the water W1 which will have been heated will be called water W2.

[0113] Typically, according to this embodiment, the method of the invention further comprises at least one step of heating the water W2, downstream of said heat exchange X1, making it possible to heat the water to a temperature of at least 374°C before its injection in step b).

[0114] When the method of the invention comprises a heat exchange step X1, said heat exchange step X1 is preferably carried out with water having a pressure of at least 225 bars, it will thus preferably be carried out after a step of pressurizing the water W1 to a pressure of at least 225 bars.

[0115] Preferably, according to the embodiment implementing two filters, the heat exchange X1 is implemented downstream of the recombination of the flow lines M3 and M3'.

[0116] According to one embodiment, the method of the invention further comprises a heat exchange step X2 making it possible to recover heat from the flow M5' to heat the mixture M1p upstream of the water injection of step b) of the method. This heat exchange then makes it possible to obtain a cooled flow M5''.

[0117] The M1p flow downstream of the X2 heat exchange could typically have a temperature ranging from 90 to 170°C.

[0118] Said heat exchange step X2 may be combined with another external heating step to heat the mixture M1p to the desired temperature when implementing step b), this may in particular involve heating by injecting water to a temperature of at least 374°C.

[0119] The M5'' flux can typically have a temperature ranging from 100 to 200°C.

[0120] Preferably, according to this embodiment, the hydrotreatment process according to the invention further comprises: a step of cooling at least a fraction of the stream M5'' making it possible to obtain steam and a stream M6 enriched in soluble materials, and a step of injecting at least a portion of said steam to preheat the mixture M1 upstream of step a) of pressurizing.

[0121] The cooling step can be implemented using a cooling device chosen from a heat exchanger integrated or not in a rankine, flash, scrubber cycle, preferably using a flash.

[0122] The steam produced during cooling is, according to this embodiment, used to preheat the mixture M1 upstream of step a) of pressurizing.

[0123] Preferably, according to this embodiment, the mixture M1 is preheated upstream of the pressurization step a) to a temperature ranging from 50 to 170°C, preferably from 50 to 90°C, using the steam resulting from the cooling of at least a fraction of the flow M5''. It should be noted that the mixture M1 may possibly already be under pressure, before step a) defined in the invention.

[0124] The invention thus allows for better optimization of the viscosity of the biomass undergoing high-pressure treatments. Indeed, the difficulty of pumping at these high pressures requires a minimum viscosity of the biomass to be pumped in order to meet the specifications of very high-pressure pumps.

[0125] By injecting steam into the M1 mixture, all possibilities are used to reduce the viscosity of the biomass to an acceptable value for pumping technologies while minimizing the dilution of the biomass which can cause additional costs in the sizing of downstream equipment (residence time to be respected, etc.).

[0126] According to one embodiment, the cooling of at least a fraction of the flow M5' or where appropriate M5'' is carried out at a pressure regulated as a function of the preheating temperature of the mixture M1 upstream of the pressurization step a).

[0127] Indeed, pressure and temperature are linked for saturated steam. Maintaining a constant pressure makes it possible to control the temperature of the steam and therefore the maximum temperature that can be reached by the product heated by the steam (mixture M1 in the case of the invention).

[0128] For example, the pressure can be maintained between 2 and 10 bars.

[0129] According to one embodiment, the method according to the invention further comprises an additional step of cooling at least a fraction of the M6 ​​stream (enriched in soluble matter) to obtain a M6' stream followed by a step of introducing said M6' stream into a digester to enable the digestion of the organic matter contained in the M6' stream.

[0130] The additional cooling step makes it possible, for example, to cool the M6 ​​flow to a temperature less than or equal to 100°C, preferably less than or equal to 60°C, more preferably less than or equal to 40°C.

[0131] According to one embodiment, the cooled M6' stream is then introduced into a digester to undergo a digestion step.

[0132] Digestion can be carried out according to any digestion method known to those skilled in the art.

[0133] According to one embodiment, the treatment method according to the invention comprises at least one anaerobic digestion step implemented on the M6' stream.

[0134] Anaerobic digestion can be mesophilic or thermophilic.

[0135] When mesophilic digestion is implemented, then the temperature in the digester ranges from 33°C to 37°C and the residence time is 16 to 22 days.

[0136] When thermophilic digestion is implemented, then the temperature in the digester ranges from 55° to 60°C and the residence time is 10 to 12 days.

[0137] Residence time and temperature are two factors influencing the proper degradation of sludge and therefore the optimization of energy production.

[0138] When the flow to be digested is sufficiently liquid, digestion can be of the UASB type and residence times reduced.

[0139] At the end of the digestion stage, biogas is obtained.

[0140] This biogas typically comprises a mixture consisting essentially of methane, carbon dioxide and water. The biogas may optionally comprise other gases, such as hydrogen, oxygen, nitrogen, hydrogen sulfide, but these other gases collectively represent less than 10% by weight of the biogas, of the total weight of the biogas.

[0141] According to one embodiment, at least a fraction of the M3 flow enriched in soluble materials leaving the reactor is sent to one or more subsequent treatment stages.

[0142] In the embodiment implementing two filters, the two flow lines M3 and M3' are advantageously recombined upstream of the subsequent processing steps.

[0143] Among the subsequent treatments that can be implemented, mention may be made of an additional heating step, a hydrothermal gasification step. According to this embodiment, the heat exchange(s) (X1, X2) described in the present invention and the digestion described in the invention will be implemented where appropriate, downstream of said subsequent treatments.

[0144] According to a particular embodiment of the invention, the method comprises:

[0145] a) Pressurizing the mixture M1 to a pressure of at least 40 bars, in order to obtain a flow M1p,

[0146] b) a heating step comprising at least one injection of water at a temperature of at least 374°C and at a pressure of at least 225 bars into the flow of mixture M1p in order to obtain a flow M2 comprising water and organic matter,

[0147] (c) an introduction of at least a fraction of the M2 flow into a hydrotreatment reactor by a tangential injection allowing cyclonic movement,

[0148] (d) recovery downstream of the reactor of an M3 flow enriched in soluble materials and an M4 flow depleted in soluble materials,

[0149] said method further comprising:a step of pressurizing water W1 to a pressure of at least 225 bars,a heat exchange step X1 downstream of said pressurizing of water, making it possible to recover heat from the flow M3 to at least partially heat the water W1 intended to be injected in step b), making it possible to obtain, downstream of the exchange X1, a cooled flow M5' and a flow of heated water W2,an additional heating step implemented on the flow of heated water W2, downstream of said heat exchange X1, making it possible to heat the water to a temperature of at least 374°C before its injection in step b),a heat exchange step X2, downstream of the heat exchange X1, making it possible to recover heat from the flow M5' to heat the mixture M1p upstream of the water injection of step b) of the method, this heat exchange X2 then making it possible to obtain a flow M5'' cooled.

[0150] According to a particular embodiment of the invention, the method comprises:

[0151] a) Pressurizing the mixture M1 to a pressure ranging from 20 to 350 bars, in order to obtain a flow M1p,

[0152] b) a heating step comprising at least one injection of water at a temperature of at least 374°C and at a pressure of at least 225 bars into the flow of mixture M1p in order to obtain a flow M2 comprising water and organic matter,

[0153] (c) an introduction of at least a fraction of the flow M2 into a hydrotreatment reactor via an inlet E1 by a tangential injection allowing a cyclonic movement,

[0154] d) recovery of an M3 flow enriched in soluble matter downstream of a filter present in the reactor or downstream of the reactor, said filter having a mesh size of less than 40 µm,

[0155] e) a step of injecting water at a temperature of at least 374°C into the flow line M3 downstream of the reactor and downstream of the filter, counter-current to said flow M3, said water being at the same temperature and at the same pressure as the water injected during step b),

[0156] said hydrotreatment reactor further comprising:a first outlet S1 configured to extract material M3 enriched in soluble materials,a second outlet S2 configured to extract material M4 depleted in soluble materials,

[0157] said method further comprising a recovery, via a third outlet S1' different from S1, of a flow enriched in soluble materials M3' downstream of a second filter present in the reactor or downstream of the reactor, said second filter having a mesh size greater than that of the first filter,

[0158] the E1 entrance being located at an altitude lower than the S1 and S1' exits and at an altitude higher than the S2 exit,

[0159] said method being characterized in that when water is injected during step e), then: no flow M3 is extracted from the reactor and a flow M4 is extracted from the reactor, preferably a flow M3' is extracted from the reactor.

[0160] According to a particular embodiment of the invention, the method comprises:

[0161] a) Pressurizing the mixture M1 to a pressure ranging from 20 to 350 bars, in order to obtain a flow M1p,

[0162] b) a heating step comprising at least one injection of water at a temperature of at least 374°C and at a pressure of at least 225 bars into the flow of mixture M1p in order to obtain a flow M2 comprising water and organic matter,

[0163] (c) an introduction of at least a fraction of the flow M2 into a hydrotreatment reactor via an inlet E1 by a tangential injection allowing a cyclonic movement,

[0164] d) recovery of an M3 flow enriched in soluble matter downstream of a filter present in the reactor or downstream of the reactor, said filter having a mesh size of less than 40 µm,

[0165] e) a step of injecting water at a temperature of at least 374°C into the flow line M3 downstream of the reactor and downstream of the filter, counter-current to said flow M3, said water being at the same temperature and at the same pressure as the water injected during step b),

[0166] said hydrotreatment reactor further comprising:a first outlet S1 configured to extract material M3 enriched in soluble materials,a second outlet S2 configured to extract material M4 depleted in soluble materials,

[0167] said method further comprising:a step of pressurizing water W1 to a pressure of at least 225 bars,recovery, via a third outlet S1' different from S1, of a flow enriched in soluble matter M3' downstream of a second filter present in the reactor or downstream of the reactor, said second filter having a mesh size greater than that of the first filter,a heat exchange step X1 downstream of said pressurizing of water, making it possible to recover heat from the flow M3, possibly combined with M3', to at least partially heat the water W1 intended to be injected in step b), making it possible to obtain, downstream of the exchange X1, a cooled flow M5' and a flow of heated water W2,an additional heating step implemented on the flow of heated water W2, downstream of said heat exchange X1, making it possible to heat the water W2 to the temperature of at least 374°C before its injection in step b),a step heat exchange X2,downstream of the heat exchange X1, making it possible to recover heat from the flow M5' to heat the mixture M1p upstream of the water injection of step b) of the process, this heat exchange X2 then making it possible to obtain a cooled flow M5''.,

[0168] the E1 entrance being located at an altitude lower than the S1 and S1' exits and at an altitude higher than the S2 exit,

[0169] said method being characterized in that when water is injected during step e), then: no flow M3 is extracted from the reactor and a flow M4 is extracted from the reactor, preferably a flow M3' is extracted from the reactor.

[0170] The invention also relates to an installation for implementing the hydrotreatment process according to the invention.

[0171] The drawings illustrate embodiments of the invention, without limiting its scope.

[0172] The installation according to the invention comprises: a mixture supply line M1, a pressurizing pump 2 supplied by the mixture supply line M1 and comprising a mixture outlet line M1p, a heating device 11 downstream of the pump 2 comprising an inlet for the mixing line M1p and an outlet for the flow line M2, downstream of the water injection device ES, a hydrotreatment reactor 1 comprising at least one inlet E1 for the flow M2 and at least one outlet S1 for the flow M3 and at least one outlet S2 for the flow M4, the inlet E1 being configured so as to introduce a cyclonic movement of the flow M2 into the reactor 1 via the inlet E1.

[0173] According to one embodiment of the installation, the heating device 11 is chosen from one or more elements among: a water injection device, an external heating device, said external heating device being able to be chosen from an electric heating device, a heat exchanger by a hot fluid (gas / liquid), a microwave heating device, or a combination of these.

[0174] According to a preferred embodiment of the invention, the heating device 11 comprises at least one water injection device ES into the mixing line M1p. This embodiment is illustrated in the Figures.

[0175] According to one embodiment, the heating device 11, 11' comprises a heat exchanger 8 and a water injection device ES in the mixing line M1p, preferably, the heat exchanger 8 is upstream of the water injection device ES. This embodiment is illustrated in the.

[0176] As illustrated in, according to one embodiment, the installation according to the invention comprises: a mixture supply line M1, a pressurization pump 2 supplied by the mixture supply line M1 and comprising a mixture outlet line M1p, a heating device 11 comprising a device for injecting water ES into the mixture line M1p downstream of the pressurization pump 2, a hydrotreatment reactor 1 comprising at least one inlet E1 for the flow M2, at least one outlet S1 for the flow M3 and at least one outlet for the flow M4, the inlet E1 being configured so as to introduce a cyclonic movement into the reactor 1 via the inlet E1.

[0177] According to one embodiment, the hydrotreatment reactor 1 further comprises at least one filter F1, the filter preferably being arranged within the reactor, on the flow outlet line M3 arranged in such a way that the hydrotreated organic matter M3 passes through the filter before leaving the reactor via the outlet S1.

[0178] Illustrates an advantageous embodiment of the invention in which a filter F1 is present in the reactor 1, such that the flow M3 passes through the filter F1 before being extracted from the reactor 1. According to one embodiment, the filter F1 comprises at least one mesh of size less than 100 µm, preferably less than 50 µm, more preferably less than 40 µm.

[0179] A valve V1 may be present downstream of reactor 1 in order to control the flow M3 leaving the reactor.

[0180] It also illustrates the cyclonic movement.

[0181] Also illustrates an advantageous embodiment of the invention in which the installation further comprises a second water supply line ES2 in the flow M3 at the outlet of the reactor 1. The water supply line ES2 is configured to introduce water, preferably supercritical water, counter-current to the flow M3.

[0182] Also illustrates an advantageous embodiment of the invention in which the reactor 1 comprises an outlet S1 in the upper part and an outlet S2 in the lower part of the reactor 1.

[0183] Advantageously, the installation further comprises a control unit for controlling the water injection ES2 and the outlet S2. Indeed, preferably, the outlet S2 is open (thanks to the valve V2) when water is injected via the supply line ES2.

[0184] Illustrates an embodiment of the method according to the invention implementing a heat exchange X1 as defined in the invention. The installation illustrated in shows a heat exchange step via a heat exchanger 6. The heat exchanger 6 makes it possible to recover the heat present in the flow M3 leaving the hydrotreatment reactor 1 to transfer it to the water in order to preheat the water.

[0185] According to an embodiment illustrated in the, the installation according to the invention comprises:

[0186] - a heat exchanger 6 downstream of the hydrotreatment reactor, said heat exchanger 6 making it possible to recover the heat from the flow M3 to obtain a cooled flow M6' and to transfer this heat to the water W1 upstream of the water injection device ES to obtain a flow of heated water W2,

[0187] - a water heating device 7, downstream of the heat exchanger 6 and upstream of the water injection device ES, said heating device 7 being supplied by the water W2 and making it possible to obtain water ES at a temperature of at least 374°C.

[0188] Preferably, when the installation comprises a water injection line ES2, said water ES2 is introduced into the flow line M3 via a water supply line leaving the heating device 7 (case 1a) or leaving a branch of the water supply line ES.

[0189] According to an embodiment not shown, the installation according to the invention comprises on the water supply line W1, a pressurization pump advantageously making it possible to bring the water to a pressure of at least 225 bars.

[0190] According to one embodiment, the installation further comprises a static turbulator 10 supplied by the flow line M2, said static turbulator being upstream of the hydrotreatment reactor 1. The mixture leaving the turbulator 10 supplies the hydrotreatment reactor 1. This embodiment is illustrated in the.

[0191] The static turbulator may be chosen from a propeller, blades or elbows or combinations thereof. Thus, for example, the mixing flow supply line M2 located between the water injection device ES and the hydrotreatment reactor 1 may comprise one or more elbows making it possible to provide turbulence, thus improving the exchanges between the water and the sludge.

[0192] As illustrated in, the turbulator 10 may be a system of elbows.

[0193] According to the embodiment illustrated in the, the installation further comprises a second filter F1', another outlet in the upper part of the reactor 1, outlet S1', allowing the extraction of a flow M3' comprising the hydrotreated organic matter (flow enriched in soluble matter). A valve V1' may also be present in order to control the extraction of the flow M3'.

[0194] Preferably, the filter F1' has a mesh size of less than 200 µm.

[0195] According to a particular embodiment, the filter F1 comprises a filtration layer having a mesh size less than 40 µm and the filter F1' comprises a filtration layer having a mesh size less than 100 µm.

[0196] Preferably, the outlet S1 and the outlet S1' are located in the upper part of the hydrotreatment reactor 1 and preferably allow vertical extraction, from the bottom to the top of hydrotreated organic matter, respectively M3 and M3'.

[0197] Preferably, according to this embodiment, the installation comprises a line for injecting the flow M3' into the flow line M3 downstream of the valve V1, and where appropriate upstream of the heat exchanger 6, thus making it possible to recombine the flow lines M3 and M3'.

[0198] Illustrates an embodiment of the method according to the invention. The installation illustrated in includes:

[0199] - a heat exchanger 6 downstream of the hydrotreatment reactor 1, said heat exchanger making it possible to recover the heat from the flow M3, possibly combined with the flow M3', to obtain a flow M5' and to transfer this heat to the water W1 upstream of the heating device 7, making it possible to obtain heated water W2,

[0200] - a water heating device 7, downstream of the heat exchanger 6 supplied by the heated water W2 and upstream of the water injection device ES,

[0201] - a cooling device 4 supplied by at least a fraction of the flow M5' making it possible to produce steam and a cooled flow M6,

[0202] - a device 3 for injecting said steam produced into the mixture flow M1 upstream of the pressurizing pump 2, said injection device 3 possibly being a reactor,

[0203] - a cooling device 9 downstream of the cooling device 4 making it possible to cool at least a fraction of the flow M6 to obtain a flow M6', and

[0204] - a digester 5 fed by the M6' flow.

[0205] Illustrates an embodiment of the method according to the invention. The installation illustrated in includes:

[0206] - a heat exchanger 6 downstream of the hydrotreatment reactor 1, said heat exchanger making it possible to recover the heat from the flow M3, possibly combined with the flow M3', to obtain a flow M5' and to transfer this heat to the water W1 upstream of a heating device 7, making it possible to obtain heated water W2,

[0207] - a water heating device 7, downstream of the heat exchanger 6 supplied by the heated water W2 and upstream of the water injection device ES,

[0208] - a heat exchanger 8 for recovering heat from the mixture M5' to obtain a mixture M5'' and transferring this heat to the mixture M1p upstream of the water injection device ES,

[0209] - a cooling device 4 supplied by at least a fraction of the flow M5' making it possible to produce steam and a cooled flow M6,

[0210] - a device for injecting said steam produced into the mixture flow M1 upstream of the pressurizing pump 2, said injection device 3 possibly being a reactor,

[0211] - a cooling device 9 downstream of the cooling device 4 making it possible to cool at least a fraction of the flow M6 to obtain a flow M6', and

[0212] - a digester 5 fed by the M6' flow.

[0213] According to an embodiment illustrated in the, the heating device 11, 11' comprises a heat exchanger 8 and a water injection device ES. According to the embodiment illustrated in the, the heating step b) of the method comprises two sub-steps: a first sub-step of heat exchange between the flow M1p and flow M3, said flow M3 having optionally been subjected to one or more heat exchanges between the outlet of the reactor and this heat exchange with M1p, a second sub-step of injection of water ES at a temperature of at least 374°C and preferably at a pressure of at least 225 bars, in the flow line M1p downstream of the first sub-step.

[0214] According to an embodiment not shown in the Figures, the installation according to the invention further comprises at least one post-treatment device supplied by at least a fraction of the flow M3 downstream of the hydrotreatment reactor 1. When the installation further comprises at least one heat exchanger 6, then said post-treatment device is upstream of said heat exchanger 6. Preferably, said post-treatment device is chosen from a complementary heating step, a hydrothermal gasification step.

Claims

A process for hydrotreating a mixture M1 comprising at least organic matter, said process comprising:Pressurizing the mixture M1 to a pressure ranging from 20 to 350 bars, in order to obtain a flow M1p,a step of heating the mixture M1p to a temperature ranging from 170 to 430°C, in order to obtain a flow of mixture M2,an introduction of at least a fraction of the flow M2 into a hydrotreatment reactor by tangential injection allowing cyclonic movement,a recovery downstream of the reactor of a flow M3 enriched in soluble matter and of a flow M4 depleted in soluble matter. Hydrotreatment process according to claim 1, wherein the recovery of the M3 stream during step d) is carried out through at least one filter, said filter comprising at least one filtration layer preferably having a mesh size of less than 100 µm, preferably less than 50 µm, more preferably less than 40 µm, said filter preferably being in the hydrotreatment reactor. Hydrotreatment process according to claim 1 or 2, in which step b) comprises at least one step of injecting ES water at a temperature of at least 374°C into the flow of mixture M1p in order to obtain the flow M2, the injected water preferably being at a pressure of at least 225 bars. Hydrotreatment process according to any one of claims 1 to 3, in which the recovery of the M3 stream during step d) is controlled by determining the pressure difference between the pressure in the hydrotreatment reactor and the pressure in the M3 stream downstream of the reactor, where appropriate downstream of the filter and downstream of the reactor. A hydrotreatment process according to any one of claims 1 to 4, wherein the hydrotreatment reactor is maintained at a temperature ranging from 170°C to 430°C. Hydrotreatment process according to any one of claims 1 to 5, in which the recovery of the M3 stream is carried out in the upper part of the hydrotreatment reactor, via a vertical outlet line, and the recovery of the M4 stream is carried out in the lower part of the reactor. Hydrotreatment process according to any one of claims 2 to 6, further comprising, downstream of the filter and downstream of the reactor, a step e) of injecting water at a temperature of at least 374°C into the flow M3, counter-current to said flow, where appropriate said water preferably being at the same temperature and at the same pressure as the water injected during step b). Hydrotreatment process according to claim 7, wherein, when the countercurrent water injection of step e) is implemented, then the outlet of the reactor in the lower part is opened in order to extract a flow M4. Hydrotreatment process according to any one of claims 1 to 8, wherein the mixture flow M2 is introduced into the reactor with a speed ranging from 0.5 to 20 m / s, preferably from 0.5 to 15 m / s, preferably from 2 to 10 m / s. Hydrotreatment process according to any one of claims 3 to 9, further comprising at least one heat exchange step X1 making it possible to recover heat from the flow M3 to at least partially heat the water intended to be injected in step b), a cooled flow M5' then being obtained, and optionally comprising at least one additional water heating step, downstream of the heat exchange X1 making it possible to heat the water to the temperature of at least 374°C before its injection in step b) and where appropriate before its injection into the water e), and optionally at least one heat exchange step X2 making it possible to recover heat from the flow M5' to heat the mixture M1p upstream of the water injection of step b), a cooled flow M5' then being obtained. Hydrotreatment process according to claim 10, further comprising:at least one step of cooling at least a fraction of the stream M5' or where appropriate of the stream M5'' making it possible to obtain steam and a stream M6 comprising hydrotreated organic matter, anda step of injecting at least a portion of said steam to preheat the mixture M1 upstream of step a) of pressurizing, said mixture M1 preferably being preheated to a temperature ranging from 50 to 170°C, preferably from 50 to 90°C,optionally a step of cooling at least a fraction of the stream M6 to obtain a cooled stream M6' and optionally a step of digesting the stream M6'. Hydrotreatment process according to one of claims 1 to 11, in which the hydrotreatment reactor comprises an excess thickness which resists abrasion on at least a portion of its internal surface. Installation for implementing the hydrotreatment process according to any one of claims 1 to 12, said installation comprising: a mixture supply line M1, a pressurizing pump (2) supplied by the mixture supply line M1 and comprising a mixture outlet line M1p, a heating device (11) downstream of the pump (2) comprising an inlet for the mixing line M1p and an outlet for the flow line M2, a hydrotreatment reactor (1) comprising at least one inlet E1 for the flow M2, an outlet S1 for the flow M3 enriched in soluble matter and an outlet S2 for the flow depleted in soluble matter, the inlet E1 being configured so as to introduce a cyclonic movement into the reactor (1) via the inlet E1. Installation according to claim 13, in which the hydrotreatment reactor (1) further comprises: at least one first filter F1, said first filter being arranged in such a way that the flow M3 enriched in soluble matter passes through the filter before leaving the reactor via the outlet S1, and optionally at least one second filter F1', said second filter F1' being arranged in such a way that the flow M3' enriched in soluble matter passes through said second filter F1' before leaving the reactor (1) via an outlet S1', preferably, the outlets S1 and S1' are located in the upper part of the hydrotreatment reactor 1 and preferably allow a vertical extraction, from the bottom to the top of hydrotreated organic matter, respectively M3 and M3'. Installation according to claim 13 or 14, in which the heating device (11) comprises at least one water injection device ES in the mixing line M1p, said installation preferably further comprising: a heat exchanger (6) downstream of the hydrotreatment reactor (1), said heat exchanger making it possible to recover the heat in the flow line M3, possibly combined with the flow line M3', to obtain a flow M5' and to transfer this heat to the water upstream of the water injection device ES, and optionally a water heating device (7), downstream of the heat exchanger (6) and upstream of the water injection device ES, said installation preferably further comprising: optionally a heat exchanger (8) making it possible to recover heat from the mixture M5' to obtain a mixture M5'' and to transfer this heat to the mixture M1p upstream of the water injection device ES,A cooling device (4) supplied with at least a fraction of the flow M5' or where appropriate M5'' making it possible to produce steam and a cooled flow M6,A device (3) for injecting said steam produced into the mixture flow M1 upstream of the pressurizing pump (2),Optionally a cooling device (9) downstream of the cooling device (4) supplied with at least a fraction of the flow M6 making it possible to cool at least a fraction of the flow M6 to obtain a flow M6', andOptionally a digester (5) supplied with the flow M6'.,

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