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    • 专利摘要:
    The invention relates to a process for the continuous hydrothermal carbonization of sludges containing organic matter, comprising a hydrothermal reaction step implemented in a reactor (4) comprising the following steps: a sludge introduction step in which sludge is introduced into the reactor (4) through a first inlet (11), - an endogenous steam injection step in which steam is injected into the reactor (4) through a second inlet (15) separate from the first inlet (11), - an extraction stage in which at least a portion of the sludge contained in the reactor (4) is continuously extracted by a sludge outlet (16), - a preheating stage in which one raises the temperature of the sludge before introduction into the reactor (4) to a preheating temperature above 70 ° C. The invention also relates to a device for implementing such a method.
    公开号:FR3037057A1
    申请号:FR1555149
    申请日:2015-06-05
    公开日:2016-12-09
    发明作者:Pierre Emmanuel Pardo；Jean-Louis Bourdais
    申请人:Degremont SA；
    IPC主号:
    专利说明:

    [0001] TECHNICAL FIELD The present invention relates to a method and a device for hydrothermal carbonization. The field of the invention is more particularly but not limited to that of the treatment of sludges heavily loaded with organic materials, for example from urban or industrial wastewater remediation processes, or network cleaning operations. Such treatment aims to reduce the volume of sludge, to stabilize them biologically and physicochemically and to produce valuable by-products. The invention relates more particularly to the field of the method and device for continuous hydrothermal carbonization of sludge containing organic material. State of the Prior Art The state of the art has developed two families of treatments: - thermal hydrolysis, - hydrothermal carbonization. The technique of thermal hydrolysis of sludge was developed by Porteous at the beginning of the 20th century. This technique uses pressurized reactors operating in sequence. Typically, the sludge is pumped into a first reactor in which steam produced by a boiler is injected until a temperature of about 180 ° C is reached at a pressure of 1.5 MPa inside the reactor. This first reactor, the temperature is then maintained for 30 minutes and the sludge is discharged under their own pressure through a heat exchanger. This heat exchanger is used to recover heat contained in the sludge leaving the first reactor and to heat the sludge before entering a second reactor. Many changes and improvements have since been made to improve productivity and ensure continuous operation. The hydrolysed sludge, that is to say having undergone such treatment in a reactor, are then subjected to biological treatments, for example anaerobic digestion to reduce the quantities of sludge by producing biogas. The technique of hydrothermal carbonization (HTC) is similar to thermal hydrolysis but is not intended to prepare sludge for digestion, it is aimed at the transformation of sludge into carbon-carbon bio-coal of high quality, by the use of heat and pressure generally higher than in thermal hydrolysis, and ensuring sludge residence time longer than for thermal hydrolysis (a few hours) and generally in the presence of a reagent. The HTC technique also makes it possible to produce biocharbon, a product similar to humus, which can be used to amend agricultural soils and store CO2. The hydrothermal carbonization technique was described in 1913 by Friedrich Bergius, and earned him the Nobel Prize in Chemistry in 1931. Patent FR3010403 is known from the state of the art and describes a method and a device for hydrolysis. method of sludge containing organic material, said method comprising the steps of: simultaneously providing an injection of recovery vapor into said sludge and a mixture of said sludge with said recovery vapor by means of a primary dynamic mixer-injector to obtain a primary uniform mixture; simultaneously injecting live steam into said primary uniform mixture and mixing said primary uniform mixture with said live steam by means of a secondary dynamic mixing injector so as to obtain a secondary uniform mixture; conveying said secondary uniform mixture to a pressurized tubular reactor and causing substantially uniform flow of said secondary uniform mixture into said tubular reactor at a sufficient residence time and at a temperature sufficient to permit thermal hydrolysis of the material organic present in this secondary uniform mixture; Producing said recovery vapor within recovery steam generating means from said secondary uniform mixture obtained at the outlet of said tubular reactor; cooling said secondary uniform mixture to its outlet from said recovery steam generating means at a temperature permitting further digestion of the hydrolysed organic material contained therein. US Pat. No. 8,673,112 also discloses a method for thermal hydrolysis comprising: (i) feeding biomass (in particular sludge) in an approximately continuous manner so as to undergo a first preheating step and preheat it, (ii) entrain sequentially the biomass preheated in at least two reactors, (iii) heat and pressurize a reactor by adding steam, (iv) keep the reactors at a certain temperature and pressure for a certain time, (y) bring the biomass heated and under pressure from the reactors in a first decompression tank without any substantial reduction in pressure and fast decompression of the biomass, by means of a nozzle, in order to disintegrate it, (vi) transfer the biomass of the first decompression tank into a second decompression tank whose pressure is lower than the pressure of the first decompression tank, 2 (Vii) and bring the biomass thus treated into a downstream plant for further processing. This US patent US8673112 also relates to a device for the heat treatment of biomass. International Patent Application WO2014135734 discloses a method which operates continuously for the thermal hydrolysis of organic material, comprising a preheating step, a subsequent reaction step and a depressurizing step. The preheating step comprises a recirculation of the organic material to be hydrolysed in a first recirculation circuit; the reaction step comprises recirculating in a second recirculation circuit the organic material extracted from the first recirculation circuit by subjecting it to a certain pressure and a certain temperature; and the depressurizing step comprises decompressing the organic material extracted continuously from the second circuit. Disadvantages of Prior Art Solutions The prior art solutions, particularly from International Patent Application WO2014135734, are more suitable for thermal hydrolysis applications followed by a bacterial digestion step. For such applications, the pressure and temperature levels within the reactor are relatively moderate, of the order of 0.6 MPa and 160 ° C. For applications of hydrocarbon type, the pressure and temperature levels are significantly higher, of the order of 3 MPa and 200 ° C. As a result, the solution of a mixing injector at the reactor inlet is not suitable for the application of hydrocarbonization. Indeed, to achieve the required temperatures, it is necessary to bring more steam which leads to a dilution detrimental to the proper functioning of the reactor, as well as downstream post-processing equipment. The pressure and temperature requirements lead to high stresses on the injection equipment, inducing leakage and corrosions detrimental to the life of the equipment. Furthermore, increasing the temperature of sludge injected into the reactor by preheating reduces their apparent viscosity, to dryness unchanged, until a viscosity close to that of water is obtained, the dryness being defined by the content of materials. dry biomass or sludge. In the solution proposed by US Pat. No. 8,673,112, the installation requires a plurality of reaction vessels, which considerably complicates the installation and is not compatible with continuous operation. The object of the present invention is to solve at least one of the aforementioned problems or disadvantages. SUMMARY OF THE INVENTION For this purpose, the invention proposes a process for continuous hydrothermal carbonization of sludges containing organic matter, said sludge having a dryness of between 10 and 30%, said process comprising a step hydrothermal reaction reaction carried out in a reactor (and preferably at least one cooling step in which the sludge having undergone the hydrothermal reaction stage are cooled), the hydrothermal reaction step comprising the following steps: introduction of sludge in which the sludge is introduced into the reactor through a first inlet, an endogenous steam injection stage in which steam is injected into the reactor through a second inlet, an extraction stage in which continuously at least a portion of the sludge contained in the reactor by a sludge outlet, this method further comprising a step of pre heating in which the temperature of the sludge is raised prior to introduction into the reactor to a preheating temperature above 70 ° C, the second inlet being distinct from the first inlet. The term "endogenous" refers to the fact that the steam is injected into the sludge contained in the reactor, as opposed to the term "exogenous" referring to an injection of steam into the sludge located outside the reactor.
    [0002] In this description, the expression "continuous extraction" is understood to mean a continuous extraction with a possibly variable flow rate, preferably driven by operating parameters of the reactor. Such continuous extraction may be temporarily interrupted when the regulations have not been able to recover the equilibrium of the hydrothermal carbonization process. Continuous extraction is not a sequential extraction, and is not a batch or batch extraction. The preheating step may comprise a microwave injection step in which microwaves are injected into the sludge before being introduced into the reactor. In one embodiment, the preheating step may comprise an exogenous steam injection step in which steam is injected into the sludge before being introduced into the reactor, and the method further comprises a step additional heating in which the temperature of the sludge having undergone the preheating stage is raised before being introduced into the reactor by transferring to these sludge the heat contained in the sludge extracted from the reactor. The preheating step may comprise a recirculation step in which a fraction of the sludge contained in the reactor 10 is taken and in which this fraction is mixed with the sludge before being introduced into the reactor. Preferably, the process may further comprise a circulation stage in which a mixture consisting of the sludge contained in the reactor and the steam injected into the circulating reactor is placed in the reactor. The method according to the invention may further comprise a step of heating water in which heat is transferred from the sludge extracted from the reactor to water via a heat exchanger, and in which the thus heated water is used to produce all or part of the steam used in the endogenous steam injection step. The invention also relates to a continuous hydrothermal carbonization device for sludges containing organic material, said sludge having a dryness of between 10 and 30%, this device comprising a reactor comprising: a first inlet arranged to introduce the sludge into the sludge; reactor, a second inlet arranged for injecting directly into the steam reactor, a sludge outlet arranged to extract the reactor continuously at least a portion of the sludge it contains, this device further comprising a preheating means upstream of the first inlet, the preheating means being arranged to receive the sludge before introduction into the reactor and to raise the temperature of the sludge it receives to a preheating temperature greater than 70 ° C, the second entrance being distinct from the first entrance. According to an advantageous characteristic, the preheating means may be arranged to inject microwaves into the sludge it receives. According to another advantageous characteristic, the preheating means may be arranged to inject steam into the sludge it receives, and the device may furthermore comprise additional heating means arranged to transfer heat contained in the extracted sludge. the sludge reactor downstream of the preheating means and upstream of the reactor, so as to raise the sludge temperature downstream of the preheating means and upstream of the reactor. According to yet another advantageous characteristic, the device may comprise a recirculation loop arranged to take a fraction of the sludge contained in the reactor and to mix this fraction with the sludge received by the preheating means.
    [0003] The device according to the invention may furthermore comprise a heat exchanger and a boiler, this heat exchanger being arranged to transfer heat contained in the sludge extracted from the reactor to water circulating between this heat exchanger and the heat exchanger. boiler, the boiler being arranged to supply all or part of the steam injected into the reactor through the second inlet. DESCRIPTION OF THE FIGURES AND EMBODIMENTS Other advantages and particularities of the invention will appear on reading the detailed description of implementations and non-limitative embodiments, and the following appended drawings: FIG. schematic of a first variant of the device according to the invention, FIG. 2 represents a schematic view of a second variant of the device according to the invention, FIG. 3 represents a schematic view of a third variant of the device according to FIG. FIG. 4 represents a schematic view of a fourth variant of the device according to the invention. The embodiments described below being in no way limiting, it will be possible to consider variants of the invention including a selection of characteristics described, isolated from the other characteristics described (even if this selection is isolated at within a sentence including these other features), if this selection of features is sufficient to confer a technical advantage or to differentiate the invention from the prior art. This selection comprises at least one feature, preferably functional without structural details, or with only a portion of the structural details if this portion alone is sufficient to provide a technical advantage or to differentiate the invention from the state of the art. earlier. In the present description of embodiments and variants, steam is by default water vapor. By default, any pressure indicated in the present description is an absolute pressure.
    [0004] FIG. 1 is an example of a continuous hydrothermal sludge carbonization device according to the invention. This device comprises a reactor 4 arranged to implement a hydrothermal reaction step.
    [0005] This hydrothermal reaction step comprises the following steps: a sludge introduction stage in which the sludge is introduced into the reactor 4 through a first inlet 11, an endogenous steam injection stage in which steam is injected in the reactor 4 by a second inlet 15, an extraction stage in which at least a portion of the sludge contained in the reactor 4 is continuously extracted by a sludge outlet 16. Thus, in the reactor 4: 30 the first inlet 11 is arranged to introduce the sludge into the reactor 4, the second inlet 15 is arranged to inject directly into the reactor 4 of the steam, the sludge outlet 16 is arranged to extract from the reactor 4 continuously at least a portion of the sludge that it contains. The sludge injected into the reactor 4 through the first inlet 11 is conveyed as described below. In the first place, sludge containing organic matter is introduced into the device through an inlet e from, for example, a hopper (not shown) to be conveyed in a conduit 1a, for example by gravity. The sludge arriving in the duct 1a typically has a solids content by dry weight of between 10 to 30%, typically between 18 and 24%. This sludge is conveyed via duct 1 to a preheating means 2 continuously by means of an apparatus (not shown) such as a pump, a screw, a gravity-fed apparatus, a mechanical conveyor or any means allowing supplying the sludge by means of preheating 2 upstream of the first inlet 11. The preheating means 2 is arranged to receive the sludge before it is introduced into the reactor 4 and to raise the temperature of the sludge it receives up to at a preheating temperature above 70 ° C. The preheating means 2 thus makes it possible to carry out a preheating step in which the temperature of the sludge is raised before they are introduced into the reactor 4 up to this preheating temperature.
    [0006] In the embodiment of FIG. 1, the preheating means 2 is arranged to inject microwaves into the sludge it receives. Thus, the preheating step comprises a microwave injection step in which microwaves are injected into the sludge before being introduced into the reactor 4. This microwave injection step 25 makes it possible to raise the temperature of the sludge up to the preheating temperature. The preheating means 2 is therefore a microwave heating equipment, whose power is adapted to pass the sludge, introduced at room temperature, at a temperature of about 70 ° C.
    [0007] The preheating means 2 preferably comprises a non-metallic tubular enclosure (not shown), for example made of a polymer such as glass fiber reinforced polyester ("SVR") or polypropylene homopolymer ("PPH"). This tubular enclosure passes through an action zone (not shown) in which microwaves are generated which continuously heat the sludge conveyed in this tubular enclosure. The materials of the preheating means 2 are adapted to the low pressure sludge conveyed in the tubular enclosure, close to atmospheric pressure, typically less than 2 bar, and their temperature, preferably less than 90 ° C.
    [0008] The tubular enclosure of the preheating means 2 is preferably closed or protected by a metal grid capable of confining the microwaves. The sludge is then conveyed to a pump 3 by a pipe 1b connecting the preheating means 2 and the pump 3, then to the reactor 4 10 via a conduit 1c connecting the pump 3 and the first inlet 11 of the reactor 4. The means of preheating 2 can operate continuously or in batch (or "batch"). In the case of continuous operation of the preheating means 2, the sludge and the microwaves interact throughout their path in the pipe 1b upstream of the pump 3. The sludges entering the device containing 70 at 90% water, they constitute a particularly favorable environment for heating by microwaves, the microwaves being able to go deep into the sludge and thus excite water molecules that they contain.
    [0009] The preheating temperature is preferably between 60 and 150 ° C depending on the needs of the process. From an optimum point of view, this preheating temperature is 70 ° C., such a preheating temperature making it possible to substantially reduce the viscosity of the sludge and being compatible with the materials typically used to form the pump 3. Thus, the sludge having undergone the preheating stage are liquefied. The liquefied sludge is introduced into the reactor 4, which is a hydrothermal carbonization reactor, by the first inlet 11 under the effect of the driving force produced by the pump 3.
    [0010] Preferably, the sludge is injected directly and continuously into the reactor 4 in such a way that it is rapidly integrated into the mixture contained in the reactor 4, this mixture consisting of the sludge contained in the reactor 4 and the steam injected into the reactor 4. 4. In this embodiment, the second sludge introduction inlet 15 is distinct from the first steam injection inlet 11 in the reactor 4. Preferably, the method further comprises a step of circulation in which the mixture is circulated within the reactor 4. In the present description, the term "circulation" of sludge, a mixture or a liquid in the reactor 4 designates any movement of these sludges, of this mixture or liquid in the reactor 4.
    [0011] In the present description, the term "circulation path" refers to the path along which any such movement is made in the reactor. In the present description, the expression "putting into circulation" of the sludge, the mixture or a liquid in the reactor means the creation or maintenance, directly inside the reactor 4, of the circulation ( ie the movement) of the sludge, mixture or liquid in the reactor, preferably independently of the amplitude and the direction of the rate of sludge introduction into the reactor 4 by the first inlet 11.
    [0012] This circulation is carried out by circulating means which typically comprise a circulator (not shown), for example to pale, arranged to circulate the sludge in the interior of the reactor 4 along the circulation path. By "circulation means" or "circulator" sludge, 25 of the mixture or a liquid in the reactor, is meant in the present description means arranged to create or maintain directly inside the reactor 4 the circulation (ie the movement) of the sludge, the mixture or the liquid, preferably independently of the amplitude and the direction of the rate of sludge introduction into the reactor 4 by the first inlet 11. According to variants not shown, this circulator may comprise: - an agitator with one or more blades, and / or - a screw, and / or - a pump, and / or a sludge recirculation loop, and / or - a bubbling . Thanks to the liquefaction of the sludge upstream of the reactor 4, their interaction with the steam injected into the reactor 4 is greatly facilitated and this vapor rapidly condenses in the mixture, making it possible to obtain the desired temperature, typically of the order from 160-250 ° C, preferably from 180-200 ° C. Typically, the pressure and the temperature of the steam injected into the reactor 4 by the second inlet 15 are respectively of the order of 0.6-4 MPa and 160-250 ° C., preferably of 2-2.5 MPa. and 215225 ° C. According to this embodiment of the invention, the reactor 4 comprises a reagent inlet 12 connected to a reagent injection conduit 5, for injecting into the reactor 4 a reagent, for example an acid such as the sulfuric acid. Such an injection of reagent promotes the carbonization reactions of the sludge in the reactor 4. Preferably, the interior space of the reactor 4 receiving the sludge is configured to form a degassing volume (not shown) in an upper part of this interior space (That is, a portion of altitude higher than other parts of this interior space). In this degassing volume, the mixture does not circulate. This degassing volume is arranged to recover incondensable gases. The reactor 4 is also provided with an output of the incondensables 13 connecting the degassing volume to a discharge pipe 30. This output of the incondensables 13 is typically controlled by a valve to control the pressure in the reactor 4. The output of sludge 16 is arranged to extract from reactor 4 continuously at least part of the sludge it contains. The device of FIG. 1 also makes it possible to implement at least one cooling step in which the sludges having undergone the hydrothermal reaction stage are cooled. The at least one cooling step is described below. The device is arranged to carry out a water heating step in which heat contained in the sludge extracted from the reactor 4 is transferred to the water via heat exchanger 6, and in 3037057 - 13 - which uses the thus heated water to produce the steam used in the endogenous steam injection step. To do this, the device of Figure 1 comprises a heat exchanger 6 connected to the sludge outlet 16 by the conduit ld. This device 5 also comprises a boiler 22 connected to this heat exchanger 6 via a pipe 21. This heat exchanger 6 is designed to transfer heat contained in the sludge extracted from the reactor 4 to water flowing between this heat exchanger. heat 6 and the boiler 22 through the conduit 21. The boiler 22, powered by another energy source (not shown), 10 is arranged to supply the steam injected directly into the reactor 4 via a conduit 23 connected to the second inlet 15. The water circulating in this heat exchanger 6 is typically heated to a temperature between 120 and 260 ° C, typically between 160 and 170 ° C. This water heated in the heat exchanger 6 is fed to the boiler 22 via the pipe 21 which will produce the steam directly injected into the reactor 4 via the second inlet 15. The water arriving via a pipe 20 into this heat exchanger heat 6 has a quality adequate for the production of steam (softening, demineralisation, etc.). This heat exchanger 6 may be of any type suitable for such an exchange, for example of tube-in-tube, flue tube, calender tube type, etc. Such a heat-recovery water heating step 25 contained in FIGS. sludge extracted from the reactor 4 allows a reduction in the energy consumption of the device. The device of Figure 1 also comprises a cooling equipment 7 arranged to cool the sludge extracted from the reactor 4 from the heat exchanger 6 by the duct connecting them. Thus, this cooling equipment 7 is mounted downstream of the heat exchanger 6. The sludge partially cooled by the heat exchanger 6 is conveyed via the duct 1c in this cooling equipment 7 which carries out a final cooling step. This cooling equipment 7 is implemented so that the temperature of the sludges 3037057 - 14 - then conveyed to a final dehydration treatment module 10 via the ducts 1f, 1g reach a defined temperature before they arrive in this module 10. This defined temperature is typically between 40 and 90 ° C, typically between 60 and 70 ° C.
    [0013] In order to carry out this final cooling step, the cooling equipment 7 may be an exchanger in which the sludge flows on the one hand and a fluid of the water, air or any available cooling fluid type on the other hand. Such a cooling fluid arrives in this cooling equipment or exchanger 7 through a conduit 24 and out of a conduit 25. The type of exchanger is for example a tube-type exchanger in a tube or tube in the flue gas circuit. At the outlet of this cooling equipment 7, the sludge arrives in a depressive element 9 via the pipe 1f, allowing these sludges to reach a pressure close to atmospheric pressure before the final treatment of dehydration in the module 10. The depressant 9 and the final dehydration treatment module 10 are connected to each other via the conduit 1g. This pressure-reducing member 9 can be a pump, a valve, a diaphragm or any accessory making it possible to lower the pressure of the sludge. In the solutions of the prior art providing a mixing injector upstream of the reactor, is injected into the reactor a homogeneous substance whose dryness is decreased (it contains more water due to the supply of steam). In these solutions, there is no interaction, inside the reactor, between sludge and the injected vapor. The invention is essentially distinguished from the solutions of the prior art by the simultaneous use of: 1) the preheating of the sludge upstream of the reactor 4 by means other than steam only, which makes it possible to reduce their viscosity without reducing their dryness and decrease the need for heating in the reactor 4, 2) decoupling: a) the introduction of sludge into the reactor 4 by the first inlet 11, these introduced sludge being preheated to reduce their viscosity 3037057 - 15 - , maintain their dryness and reduce the energy supply requirements within the reactor 4, b) the injection of steam into the reactor 4 by the second inlet 15 distinct from the first inlet 11. Optionally, the steam can be injected not via a single input 15 but via several separate inputs (not shown), so as to optimize the interaction zones between the mixture in the reactor 4 and the steam i njected, and optimize the regulation of temperature conditions within the reactor 4. Each of these 10 separate steam injection inputs can be equipped with a valve for fine control of the steam injection conditions and therefore the operation of the reactor 4. They may in particular be distributed over a circulation path of the mixture within the reactor 4, 15 3) of the preheating of the water for the production of the steam injected into the reactor 4. In such an embodiment of the invention, the mixture and the interactions between the preheated sludge and the steam injected into the reactor 4 are only inside the reactor 4. This interaction between sludge and steam not only makes it possible to increase the temperature of the sludge circulating in the reactor 4 by heat exchange, but also to create a mixing of the sludge due to the turbulence occurring in the meeting areas of the circulating mixture and the back vapor. Finally, such a decoupling makes it possible to optimally control the quality of the injected vapor, especially in the case of a large volume reactor, for long treatments, of the order of 3 hours of travel time within the reactor. typically required for hydrothermal carbonization, compared to the 30 minutes average circulation time required for thermal hydrolysis.
    [0014] Therefore, the liquefaction of the sludge by the microwaves greatly facilitates the homogenization of the mixture in the reactor 4, which simplifies the reactor 4 from the point of view of its design (it may for example consist of a simple piping circulating in piston flow, not shown). 3037057 - 16 - The preheating of the steam by the heat exchanger 6 makes it possible to optimize the thermal consumptions. In addition, the heat exchanger 7 can be used for the production of external energy.
    [0015] Moreover, if the price of electricity is low, the embodiment of FIG. 1 is of great economic interest. Figures 2 and 3 show a second and a third embodiment of the invention.
    [0016] Several of the components of the device of FIGS. 2 and 3, in particular the reactor 4 and its operation, are similar in these second and third embodiments and in the first embodiment described above. Thus, Figures 2 and 3 are essentially described in their differences from Figure 1. In this second and third embodiment, the preheating means 2 is arranged to inject steam into the sludge it receives. More specifically, the preheating step comprises an exogenous steam injection step in which steam is injected into the sludge prior to introduction into reactor 4 to raise its temperature to preheat temperature. More than a preheating, these embodiments make it possible to recover thermal heat injected into the system. Indeed, the devices of FIGS. 2 and 3 furthermore comprise additional heating means 91, 92, 93, 94 arranged to transfer heat contained in the sludge extracted from the reactor 4 to the sludges downstream of the preheating means 2 and upstream of the reactor 4, so as to raise the temperature of the sludge downstream of the preheating means 2 and upstream of the reactor 4. These additional heating means 91, 92, 93, 94 thus make it possible to implement a step of additional heating in which the temperature of the sludge having undergone the preheating stage is raised before introduction into the reactor 4 by transferring to the sludge heat contained in the sludge extracted from the reactor 4. Thus, the preheating of the sludge takes place by a dual system: on the one hand, by an exogenous steam injection via the preheating means 2; on the other hand, by additional heating via the additional heating means 91, 92, 93, 94. In both cases, the principle consists in recovering heat from the sludge extracted from the reactor 4 and using this heat to preheat the In these embodiments (FIGS. 2 and 3), the device comprises a heat exchanger 7 arranged to transform water circulating in this heat exchanger 7 into steam using heat contained in the sludge extracted from the reactor 4, this vapor being the vapor injected into the sludge upstream of the reactor 4 by the preheating means 2. To do this, this water circulates in a conduit 25 connecting this heat exchanger 7 to the preheating means 2. This heat exchanger 7 serves to produce saturated or slightly superheated steam intended to be injected into the sludge flowing upstream of the reactor 4 by means of preheating. Heating 2. Typically, the steam thus produced has a pressure of between 0.1 and 1 MPa, preferably between 0.15 and 0.3 MPa. The heat exchanger 7 is of the fume tube boiler type or consists of any other exchanger capable of producing saturated steam.
    [0017] The water circulating in the heat exchanger 7 arrives via a conduit 21b with a quality compatible with the desired steam production, especially in terms of softening, demineralization ... The sludge arriving in the preheating means 2 through the duct is mixed therein with low pressure steam, typically between 0.1 and 1 MPa, through a dynamic or static mixing device in view of the small amounts of steam used (typically 5-25% of steam versus sludge in terms of mass). This vapor typically has a temperature between 100 and 120 ° C, and a pressure between 0.15 and 0.3 MPa.
    [0018] The heat exchanger 7 is sized to produce a quantity of vapor suitable for: a) cooling the sludge extracted from the reactor 4 and reducing the temperature of the sludge passing through this heat exchanger 7. Typically, the temperature of the sludge exiting the heat exchanger 7 is of the order of 100-120 ° C; 3037057 - 18 - b) preheating the sludge upstream of the reactor 4 so that they are sufficiently liquefied at the outlet of the preheating means 2. Typically, the temperature of the sludge at the outlet of the preheating means 2 is of the order 50-140 ° C, preferably 70-90 ° C.
    [0019] 5 downstream of the pump 3 connected to the preheating means 2 via the conduit 1b, the sludge is conveyed to an exchanger 91 via a conduit 1c1 connecting the pump 3 and this exchanger 91. The liquefaction of the sludge during the preheating step promotes a good heat exchange in the exchanger 91.
    [0020] The pump 3 conveys the liquefied sludge under pressure to the exchanger 91, at a pressure corresponding to the operating pressure within the reactor 4, increased by the pressure drops of the exchanger 91 situated downstream of this pump 3. This pressure is typically P - reactor + Ppertes 15 where Ppertes denotes the pressure losses of the exchanger 91 and the ducts here and 1c2 (the duct 1c2 connecting the exchanger 91 to the first inlet 11 of the reactor 4), typically between 0.1 to 1 MPa, Preactor means the nominal operating pressure of the reactor 4, typically between 0.6 and 3 MPa. The second embodiment (FIG. 2) and the third embodiment (FIG. 3) are distinguished by the nature of the additional heating step: in the mode of FIG. 2, this additional heating is of the indirect type; in the mode of Figure 3, this additional heating is direct type. In the second embodiment (FIG. 2), the sludge is heated by exchanger 91 by heat transfer of these sludges with a coolant circulating in a loop 94, under the effect of a pump 92, between this exchanger 91 which is mounted upstream of the reactor 4 and an exchanger 30 93 mounted downstream of the reactor 4. This heat transfer fluid is heated by heat exchange in the exchanger 93 where it recovers heat contained in the sludge extracted from the reactor 4. While circulating in the loop 94, the heat thus recovered in the sludge extracted from the reactor 4 is transferred to the sludge flowing in the exchanger 91 upstream of the reactor 4.
    [0021] This heat transfer fluid is heated in the loop 94 at a temperature typically corresponding to the temperature of the reactor 4 decreased from 20 to 80 ° C, typically 40 ° C, which also corresponds to the preheating temperature in the conduit. 1c2 added from 20 to 80 ° C, typically 40 ° C. The exchanger 93 may be of any type but preferably of the tube 5 in tube type. The sludge cooled by the heat exchanger 93 is then conveyed to the heat exchanger 7 via a duct 1a. In the third embodiment (FIG. 3), the sludges circulating in the exchanger 91 coming from the pump 3 and intended for the reactor 4 are heated by direct heat transfer of the sludge extracted from the reactor 4 conveyed towards the same exchanger. 91 by the conduit ld. At the outlet of the exchanger 7, the sludge, which has a temperature that can go down to 100 ° C., is conveyed to a tertiary exchanger 6 via the pipe 1f. This tertiary exchanger 6 makes it possible to exchange heat between these sludges and water circulating in this tertiary exchanger 6. This water arrives in the tertiary exchanger 6 via a conduit 20 and exits through a conduit 21. water flowing in the duct 21, thus heated by heat exchange with the sludge in the tertiary exchanger 6, is then conveyed, via a bifurcation Y21: 20 on the one hand, to the duct 21b connected to the exchanger 7, d ' on the other hand, to a duct 21a connected to the boiler 22 operating according to the same principle as in the first embodiment of FIG. 1. Typically, this tertiary exchanger 6 is of any possible type and in particular tube in tube. The water arriving at this tertiary exchanger 6 via line 27 is of suitable quality (softened or demineralised) and at ambient temperature. The water leaving this tertiary exchanger 6 via line 21 is at a temperature of about 60-100 ° C., preferably 90 ° C. Preferably, this water leaving the tertiary exchanger 6 is stored in a buffer tank (not shown), for example at the bifurcation Y21. This buffer tank is for example a vessel adapted to the needs of the device in terms of endogenous or exogenous steam generation. This tertiary exchanger 6 makes it possible to reduce the sludge temperature to less than 90.degree. C., which prevents their vaporization during decompression in the depressurizing member 9. A last exchanger 8 can be added between the tertiary exchanger. 6 and the pressure reducing member 9 to further cool the sludge to the desired temperature before decompression. This latter exchanger 8 is thus connected to the tertiary exchanger 6 via a conduit 1g and to the pressure-reducing member 9 via a conduit 1h. This last exchanger 8 can be of any known type. It can cool the sludge with a water-like fluid, air or any other refrigerant entering the latter exchanger 8 through a conduit 26 and out through a conduit 27. The water in the conduit 27 may or may not be recovered for process needs. This latter exchanger 8 makes it possible on the one hand to produce sludge under optimum thermal conditions, and on the other hand to recover additional energy that can be used outside the described process. The pressure-reducing member 9 makes it possible to direct the carbonized sludge towards a suitable treatment. An example of a balance sheet is as follows: 1000 kg of sludge at 20% dryness and 15 ° C.
    [0022] 107 kg of steam at 0.13 MPa and 108 ° C are injected into the preheating means 2 to preheat the sludge at 85 ° C. The sludge is then preheated to 110 ° C. in the exchanger 91 before introduction into the reactor 4, and then 161 kg of steam at 25 MPa and 225 ° C. are injected into the reactor 4 to heat it to 190 ° C.
    [0023] At the outlet of the exchanger 93 (FIG. 2), the sludges having undergone the hydrothermal carbonization reaction have a temperature of 164 ° C., heating the coolant circulating in the loop 94 at 145 ° C. At the outlet of the exchanger 7, the sludge is at 105 ° C. At the outlet of the tertiary exchanger 6, the sludge is at 89 ° C.
    [0024] At the outlet of the last exchanger 8, the sludge is at 80 ° C. FIG. 4 represents a fourth embodiment of the invention in which the device comprises the same mechanical constituents as the device of the first embodiment, with the exception of the preheating means 2 connected to the reactor 4 by a loop b of FIG. 3037057 - 21 - recirculation. Thus, FIG. 4 is essentially described according to its differences with FIG. 1. The recirculation loop b is designed to take a fraction of the sludge contained in the reactor 4 and to mix this fraction with the sludge received by the preheating means 2 More specifically, this device makes it possible to carry out a preheating step which comprises a recirculation step in which a fraction of the sludge contained in the reactor 4 is taken up and in which this fraction is mixed with the sludge before being introduced into the reactor 4. this so as to raise their temperature up to the preheating temperature. Typically, the fraction of sludge arriving in the recirculation loop b has a temperature of between 50 and 140 ° C., preferably 70-90 ° C. The proportion of this fraction of recirculated sludge with respect to the quantity of sludge arriving in the preheating means 2 through the conduit 1a is determined and controlled to obtain sludge in the preheating means 2 at a target temperature. This proportion can be of the order of 100%. Typically, the proportion of treated or untreated doughs is also 10%, with 20 treated doughs being the flow rate of the recirculated sludge fraction which is injected into the stream. untreated cold sludge arriving in the preheating means 2 through the conduit 1a whose flow rate is untreated Tcibie corresponds to the preheating temperature referred to, for example 90 ° C, before introduction into the reactor 4 Tboues treated corresponds to the the temperature of the treated sludge, at the outlet of the reactor 4, for example 180 ° C. Untreated sludge corresponds to the temperature of the untreated sludge in the conduit 1a, at ambient temperature, for example 15 ° C. Of course, the invention is not limited to the examples which have just been described and many adjustments can be made to these examples without departing from the scope of the invention. For example, the recirculation loop b of FIG. In addition, the various features, shapes, variants and embodiments of the invention may be associated with each other in various combinations as far as possible. where they are not incompatible or exclusive of each other.
    权利要求:
    Claims (11)
    [0001]
    REVENDICATIONS1. Process for the continuous hydrothermal carbonization of sludges containing organic material, said sludge having a dryness of between 10 and 30%, said process comprising a hydrothermal reaction step carried out in a reactor (4), the hydrothermal reaction stage comprising the following steps: a sludge introduction step in which the sludge is introduced into the reactor (4) through a first inlet (11), an endogenous steam injection stage in which steam is injected into the reactor (4) by a second inlet (15), an extraction step in which at least a portion of the sludge contained in the reactor (4) is continuously extracted by a sludge outlet (16), characterized in that further comprises a preheating step in which the temperature of the sludge is raised prior to introduction into the reactor (4) to a preheating temperature above 70 ° C, and that the second input (15) is distinct from the first input (11).
    [0002]
    2. Method according to claim 1, characterized in that the preheating step comprises a microwave injection step in which microwaves are injected into the sludge before being introduced into the reactor (4).
    [0003]
    3. Method according to claim 1 or 2, characterized in that the preheating step comprises an exogenous steam injection step in which steam is injected into the sludge before being introduced into the reactor (4), and in that it further comprises an additional heating step in which the temperature of the sludge having undergone the preheating stage is raised before being introduced into the reactor (4) by transferring to these sludge the heat contained in the sludge extracted from the reactor (4). 3037057 - 24 -
    [0004]
    4. Method according to one of claims 1 to 3, characterized in that the preheating step comprises a recirculation step in which is taken a fraction of the sludge contained in the reactor (4) and in which this fraction is mixed with the sludges before their introduction into the reactor (4).
    [0005]
    5. Method according to one of claims 1 to 4, characterized in that it further comprises a circulation step in which is put a mixture consisting of the sludge contained in the reactor (4) and the 10 injected vapor in the reactor (4) circulating in the reactor (4).
    [0006]
    6. Method according to any one of the preceding claims, characterized in that it further comprises a step of heating water in which heat is transferred from the sludge extracted from the reactor (4) to the water through a heat exchanger (6), and wherein the water thus heated is used to produce all or part of the steam used in the endogenous steam injection step.
    [0007]
    7. A device for continuously hydrothermal carbonization of sludge containing organic material, said sludge having a dryness of between 10 and 30%, this device comprising a reactor (4) comprising: a first inlet (11) arranged to introduce the sludge in the reactor (4), - a second inlet (15) arranged to inject directly into the reactor (4) the steam, a sludge outlet (16) arranged to extract from the reactor (4) continuously at least one part of the sludge it contains, characterized in that it further comprises a preheating means (2) upstream of the first inlet (11), this preheating means (2) being arranged to receive the sludge before their introducing into the reactor (4) and raising the temperature of the sludge it receives to a preheating temperature above 70 ° C, and in that the second inlet (15) is distinct from the first inlet (11) . 35 3037057 - 25 -
    [0008]
    8. Device according to claim 7, characterized in that the preheating means (2) is arranged to inject microwaves into the sludge it receives. 5
    [0009]
    9. Device according to claim 7 or 8, characterized in that the preheating means (2) is arranged to inject steam into the sludge it receives, and in that it further comprises additional heating means (91, 92, 93, 94) arranged to transfer heat contained in the sludge extracted from the reactor (4) to the sludge downstream of the preheating means (2) and upstream of the reactor (4), so as to raise the sludge temperature downstream of the preheating means (2) and upstream of the reactor (4).
    [0010]
    10. Device according to one of claims 7 to 9, characterized in that it comprises a loop (b) for recirculation arranged to take a fraction of the sludge contained in the reactor (4) and to mix this fraction with the sludge received by the preheating means (2).
    [0011]
    11. Device according to any one of claims 7 to 10, characterized in that it further comprises a heat exchanger (6) and a boiler (22), the heat exchanger (6) being arranged to transfer the heat contained in the sludge extracted from the reactor (4) to the water circulating between this heat exchanger (6) and the boiler (22), the boiler (22) being arranged to supply all or part of the steam injected into the reactor (4) through the second inlet (15).
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    同族专利:
    公开号 | 公开日
    AU2016273355B2|2021-07-08|
    EP3152168A1|2017-04-12|
    US20170197858A1|2017-07-13|
    EP3760594A1|2021-01-06|
    CN106795022B|2021-08-03|
    EP3152168B1|2020-08-19|
    ES2821957T3|2021-04-28|
    US10538447B2|2020-01-21|
    PT3152168T|2020-09-24|
    WO2016193463A1|2016-12-08|
    CN106795022A|2017-05-31|
    FR3037057B1|2019-06-14|
    AU2016273355A1|2017-02-09|
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    优先权:
    申请号 | 申请日 | 专利标题
    FR1555149|2015-06-05|
    FR1555149A|FR3037057B1|2015-06-05|2015-06-05|METHOD AND DEVICE FOR HYDROTHERMAL CARBONIZATION WITH OPTIMIZED ENERGY EFFICIENCY|FR1555149A| FR3037057B1|2015-06-05|2015-06-05|METHOD AND DEVICE FOR HYDROTHERMAL CARBONIZATION WITH OPTIMIZED ENERGY EFFICIENCY|
    AU2016273355A| AU2016273355B2|2015-06-05|2016-06-03|Optimised energy efficiency hydrothermal carbonization method and device|
    CN201680002327.XA| CN106795022B|2015-06-05|2016-06-03|Hydrothermal carbonization method and apparatus for optimizing energy efficiency|
    ES16730725T| ES2821957T3|2015-06-05|2016-06-03|Optimized Energy Efficiency Hydrothermal Carbonization Device and Procedure|
    EP20190329.1A| EP3760594A1|2015-06-05|2016-06-03|Method and device for hydrothermal carbonisation with optimised energy efficiency|
    PT167307255T| PT3152168T|2015-06-05|2016-06-03|Optimised energy efficiency hydrothermal carbonization method and device|
    PCT/EP2016/062703| WO2016193463A1|2015-06-05|2016-06-03|Optimised energy efficiency hydrothermal carbonization method and device|
    EP16730725.5A| EP3152168B1|2015-06-05|2016-06-03|Optimised energy efficiency hydrothermal carbonization method and device|
    US15/325,019| US10538447B2|2015-06-05|2016-06-03|Optimised energy efficiency hydrothermal carbonization method and device|
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