Classifications

• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F11/00—Treatment of sludge; Devices therefor
  • C02F11/18—Treatment of sludge; Devices therefor by thermal conditioning
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F11/00—Treatment of sludge; Devices therefor
  • C02F11/02—Biological treatment
  • C02F11/04—Anaerobic treatment; Production of methane by such processes
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F1/00—Treatment of water, waste water, or sewage
  • C02F1/02—Treatment of water, waste water, or sewage by heating
  • C02F1/025—Thermal hydrolysis
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F2201/00—Apparatus for treatment of water, waste water or sewage
  • C02F2201/002—Construction details of the apparatus
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F2209/00—Controlling or monitoring parameters in water treatment
  • C02F2209/02—Temperature
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F2209/00—Controlling or monitoring parameters in water treatment
  • C02F2209/03—Pressure
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F2301/00—General aspects of water treatment
  • C02F2301/06—Pressure conditions
  • C02F2301/066—Overpressure, high pressure
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F2303/00—Specific treatment goals
  • C02F2303/06—Sludge reduction, e.g. by lysis
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
  • Y02W10/00—Technologies for wastewater treatment
  • Y02W10/30—Wastewater or sewage treatment systems using renewable energies

Definitions

• the present invention relates to a method and a device for the continuous thermal hydrolysis of sludges containing organic matter, mixed or not with other liquid waste containing organic matter.
• This sludge can for example be derived from the treatment of domestic wastewater (sewage sludge, grease resulting from pretreatment), or from the treatment of industrial wastewater, or from waste materials, grease traps.
• the term "sludge” will subsequently be used in the document. Such sludge has a dryness of between 10 and 50% by weight.
• Sludges from the treatment of wastewater can be treated biologically, including anaerobic digestion.
• the hardly biodegradable organic material is degraded into compounds which can then be more easily degraded biologically.
• this subsequent biological degradation can be done by digestion in a closed reactor operating in anaerobic called digester.
• anaerobic digesters can only function properly if they operate at a suitable and constant temperature, generally requiring a heating system, and only if they are properly stirred. This mixing is all the easier as the incoming sludge in the digester is fluid, that is to say of low viscosity.
• thermal hydrolysis processes are known in the prior art, some being implemented by treating one by one, that is to say discontinuously, given amounts of sludge to be hydrolysed (operation in "batch” mode). ) While other processes are designed to allow a continuous treatment, or at least semi-continuously, the sludge to be hydrolysed.
• thermal hydrolysis treatment techniques for continuous or semi-continuous sludge mention may be made of the techniques described in EPI patent document 198424 and those described in patent document WO2009 / 121873.
• the sludge is fed to a reactor where it passes for a period of 5 to 60 minutes at a temperature between 130 ° C and 180 ° C.
• the sludge hydrolyzed by such treatment is then cooled by means of a heat exchanger to ensure that the temperature thereof is low enough to prevent the biomass of a digester to be destroyed.
• the energy thus recovered makes it possible to preheat the sludge before entering the thermal hydrolysis reactor.
• This technique uses re-vaporization steps whose management can in practice be difficult and constraining for the user. In addition these re-vaporization steps give the process in question a semi-continuous character rather that continuous.
• This method has the advantage of being a truly continuous process. However, although it has considerably improved the treatment of sludge by thermal hydrolysis that existed on the market, it does have some disadvantages.
• the critical phase of the process corresponds to the transfer and condensation of steam in the sludge. Indeed, if this step is not performed correctly, the performance of the thermal hydrolysis process can be considerably degraded both in terms of chemical reaction in economic terms, the amount of steam to be used is then greater.
• the thermal hydrolysis processes on dewatered sludge are therefore hampered by the difficulty of effectively injecting the sludge into the sludge and, consequently, the difficulty of ensuring their mixing, as soon as the sludge is too viscous. Since sludge is viscous by nature, the greater the dryness, the more difficult it is for the steam to be injected into the sludge, to be mixed with it and to give up its energy to cause the thermal hydrolysis of the compounds which are not readily biodegradable.
• the hydrolysis reactors have a significant length. At this important length corresponds a residence time of sludge and steam in the important reactor. Thus, it is possible to optimize the energy transfer coefficient of the steam to the sludge. However, such large reactor lengths involve high manufacturing costs.
• the objective of the present invention is to propose a method, and a device associated with the implementation of this method, making it possible to improve the performance of the technology disclosed in WO2009 / 121873, considered here as the closest prior art. of the invention which will be described below.
• an object of the present invention is to describe such a method and such a device that allow the treatment of sludge intended to be thermally hydrolyzed and having dryness rates higher than the maximum dryness rate that can be hitherto actually implemented. by the prior art, and without degrading the performance of digestion conventionally following the thermal hydrolysis of sludge.
• An object of the present invention is also to provide such a method and such a device for obtaining homogeneous temperatures of the mixture of sludge and steam inside the reactor in order to achieve high thermal hydrolysis performance and to overcome the mechanical constraints on reactors related to inhomogeneous temperatures.
• Yet another object of the invention is to describe such a method and such a device which allow the sludge to be sanitized.
• dynamic injector-mixer in the present description is intended to mean any mixer consisting of a chamber, preferably cylindrical, continuously receiving said sludge, steam injection means directly in said chamber and means for causing vigorous stirring, thanks to motorized mechanical means, the different phases entering the room.
• the stirring is strong enough to obtain a monophasic mixture of sludge and steam.
• such means may advantageously consist of blades mounted on an axis of rotation mu by a rotor rotating at a speed greater than 500 rpm, preferably between 1000 rpm and 2000 rpm.
• mechanical stirring means are not intended to push the material into the chamber but only to agitate it. Thus, when they include pale, they are shaped, according to the knowledge of those skilled in the art, so that their setting in motion does not cause advance of the material in the room.
• the residence time of the material in the dynamic injector-mixer is short.
• the preferably cylindrical chamber of the injector-mixer therefore advantageously has a small volume. Corollary the loss of load of this material during its passage in it is weak. In practice this pressure drop must be less than 10%.
• the injector-mixer implemented in the context of the invention is thus different from simple mixers constituted by a tank provided with stirring means in which the residence time of the material is long and which makes it possible to treat only a given amount of it at a time.
• This injector-mixer is also distinguished from simple sludge conveying devices, for example auger.
• the invention proposes mixing the pressurized water vapor with the sludge to be hydrolysed in order to obtain a perfect monophasic mixture of heated sludge upstream of the thermal hydrolysis step subsequently carried out in a reactor. tubular.
• the phases of mixing the sludge with the pressurized water vapor is clearly distinct from the thermal hydrolysis phase, one and the other of these phases being moreover carried out in separate equipment.
• the monophasic mixture produced prior to the thermal hydrolysis allows the water vapor to condense in the sludge at the level of the dynamic injector-mixer.
• This homogeneous mixture is then conveyed to the reactor in which it can flow in a piston stream.
• Presenting itself in a monophasic liquid phase it enters the reactor at a uniform or almost uniform temperature in the reactor, at which temperature the thermal hydrolysis of the biologically degradable compounds can be effected efficiently and optimized.
• this monophasic mixture which contains the hydrolysed organic matter is brought to a temperature and a concentration, by dilution if necessary, allowing its subsequent digestion.
• the invention clearly differs from the prior art and in particular from patent document WO20069 / 121873 by the characteristic that the mixture of the sludge to be hydrolysed with the steam is upstream of the thermal hydrolysis reactor and not within this one.
• the perfect mixture of steam and sludge makes it possible to uniformly reduce the viscosity thereof and thus to overcome the mechanical effects associated with sludge shearing.
• Obtaining a homogeneous single-phase mixture of heated sludge upstream of the reactor, obtained from sludge to be hydrolysed and steam, in a dynamic injector-mixer has the advantage of being able to treat sludge to be hydrolyzed. having a high dryness, and especially a dryness greater than 20% by weight.
• said single-phase mixture has, at the outlet of said injector-mixer, a temperature of between 100 ° C. and 200 ° C. (ie the temperature in the reactor allowing the thermal hydrolysis of the organic matter present in said sludge) and a pressure of between 1 bar a and 25 bar a. It will be noted that in the context of the present description the unit of pressure is the absolute bar (bar a).
• said single-phase mixture has, at the outlet of said injector-mixer, a temperature of between 150 ° C. and 170 ° C. (ie the temperature in the reactor allowing the thermal hydrolysis of the organic material present in said sludge) and a pressure comprised between between 5 bar a and
• the water vapor that will be used to produce the single-phase mixture of steam and sludge will have a temperature of between 100 ° C. and 220 ° C. and a pressure of greater than 1 bar. 23 bar a. Most preferably, a temperature of this water vapor of between 180 ° C and 200 ° C and a pressure of between 10 bar and 16 bar a.
• the amount of steam thus provided to the sludge will depend on the one hand on the dryness of the latter and on their concentration of organic matter to be hydrolysed.
• the residence time of the single-phase mixture within the reactor will, as indicated below, be sufficient to allow the thermal hydrolysis of the organic material to be carried out, but in principle will preferably be between 10 minutes and 2 hours, and preferably between all, between 20 and 40 minutes.
• the residence time of said single-phase mixture in the reactor will be at least 20 minutes, and the temperature of said mixture in the reactor will be at least 100 ° C so that the method according to the invention will also allow sanitizing said sludge, all of them then seeing the steam for a sufficiently long time and at a sufficiently high temperature.
• a temperature above 70 ° C for at least 20 minutes applied to the sludge is necessary to sanitize them.
• the step of cooling the single-phase mixture at its outlet from the tubular reactor to a temperature allowing the subsequent digestion of the hydrolysed organic matter it contains will be carried out by adding water and / or sludge and / or through the use of heat exchanger, which will also dilute this monophasic mixture.
• Such a dilution is indeed necessary to allow a good subsequent digestion of these thermally hydrolyzed sludge.
• This mixture will then reach a sufficiently low temperature and be sufficiently diluted to respect the biology of the digester.
• the method according to the invention comprises prior steps of dehydration and homogenization of the sludge with a view to their transport to the dynamic injector-mixer, these preliminary steps leading to sludge having a dryness of between 10 and 50% by weight, advantageously between 20% and 35% by weight, of dry matter.
• these preliminary steps leading to sludge having a dryness of between 10 and 50% by weight, advantageously between 20% and 35% by weight, of dry matter.
• the method comprises a step consisting in adapting the conditions of implementation of the dynamic mixture as a function of the dryness of the sludge.
• the dynamic mixing injector includes a rotor with blades
• the speed of rotation of these blades can be modified according to this dryness so as to allow the realization of a monophasic mixture even when this dryness will be high.
• this also covers any device for implementing the previously described method comprising: means for supplying sludge containing organic matter, means for supplying water vapor under pressure, a tabular thermal hydrolysis reactor, means for injecting water and / or dilution sludge provided downstream of said tubular reactor cooling means provided downstream of said tubular reactor, characterized in that it comprises at least one dynamic injector-mixer provided upstream of said tubular thermal hydrolysis reactor and depressurizing means provided downstream of said cooling means.
• Such a device according to the present invention is clearly distinguished from the prior art disclosed in WO2009 / 121873 by the characteristic that a dynamic injector-mixer is provided upstream of the tubular reactor of technical hydrolysis and not integrated into the hydrolysis reactor thermal.
• a dynamic injector-mixer is provided upstream of the tubular reactor of technical hydrolysis and not integrated into the hydrolysis reactor thermal.
• Such a device according to the invention therefore makes it possible to treat sludge in a smaller reactor volume by thermal hydrolysis, which has a significant economic advantage compared to the prior art.
• the device according to this will advantageously be provided with a dynamic injector-mixer which has a chamber provided with a blade rotor whose rotational speed can be adapted according to the dryness of the sludge as indicated above and in practice rotating at more than 500 rpm and preferably between 1000 rpm and 2000 rpm. It will be noted that the geometry of the blades can itself be adapted as a function of the dryness and the viscosity of the sludge.
• the embodiments of this technique given in this patent document recommend carrying out this reactor horizontally.
• a sludge inlet at one end of the tubular reactor is provided, with an injection of steam in the vicinity of this end, an outlet of the hydrolysed sludge being provided at the other end. end of this tubular reactor, cooling water injection means being provided at this second end.
• the tubular thermal hydrolysis reactor has a first vertical portion extended by a second horizontal part longer.
• each of these preferred embodiments has a relatively long horizontal part results from the need to bring the sludge into contact with the steam for a sufficiently long residence time so that not only the thermal hydrolysis occurs but beforehand thereto, within the tubular reactor, the water vapor injected at the beginning of the reactor can condense in the sludge in order to transfer thereto the energy necessary for their hydrolysis.
• the steam injection taking place upstream of the reactor is, thanks to the use of the dynamic mixer injector, a perfectly mixed monophasic mixture which arrives therein; so that the reactor in question no longer has to act as a condenser but only a thermal hydrolysis reactor. Its volume can therefore be reduced compared to the prior art. Indeed, in it, the reactor must act as both a condenser and a reactor which gives it a volume and in particular a long length.
• the thermal hydrolysis reactors implemented may have various forms.
• the tubular thermal hydrolysis reactor will be vertical and will have an inlet at its lower end and an outlet at its upper end.
• this tubular thermal hydrolysis reactor will have a first vertical section directly extended by a second vertical section, the inlet of the reactor being provided at the foot of the first vertical section and the outlet of the reactor being provided at the foot of said second vertical section.
• first vertical section directly extended by a second vertical section
• first vertical section covers achievements that there is no straight horizontal section provided between the first vertical section and the second section vertical. Indeed, such a horizontal section is useless in the measure wherein the tubular reactor of the device according to the invention is a thermal hydrolysis reactor and not a reactor also acting as a condenser.
• said tubular thermal hydrolysis reactor has a first vertical section connected to a second vertical section, the inlet of the reactor being provided at the head of said first vertical section and the outlet of said reactor being provided at the foot of said second vertical section.
• the device according thereto also comprises a heat exchanger provided downstream of the reactor.
• the device comprises a pump or a valve, preferably an eccentric screw pump, intended to maintain the pressure in the tubular thermal hydrolysis reactor.
• FIG. 1 represents a schematic view of a device for the thermal hydrolysis of sludge according to the invention (surrounded by a dotted line) integrated in an installation including a digester provided downstream thereof;
• FIG. 2 represents a tubular thermal hydrolysis reactor form that can be placed within the scope of the present invention;
• FIG. 3 represents another form of tubular thermal hydrolysis reactor that can be placed within the scope of the present invention;
• FIG. 4 represents another form of tubular thermal hydrolysis reactor that may be used in the context of the present invention;
• FIG. 1 represents a schematic view of a device for the thermal hydrolysis of sludge according to the invention (surrounded by a dotted line) integrated in an installation including a digester provided downstream thereof;
• FIG. 2 represents a tubular thermal hydrolysis reactor form that can be placed within the scope of the present invention;
• FIG. 3 represents another form of tubular thermal hydrolysis reactor that can be placed within the scope of the present invention;
• FIG. 4 represents another form of tubular thermal hydrolysis reactor that may be used in the
• FIG. 5 represents a graph showing firstly the evolution of the temperature in the tubular reactor of a prior art installation in accordance with the patent documents WO2009 / 121873 not integrating a dynamic mixer injector but in which the steam and the sludge are fed to the reactor head, and on the other hand the change in temperature in the tubular reactor of an installation corresponding to the invention integrating a dynamic mixer injector in which the steam and the sludge are mixed and then transported as a homogeneous single-phase mixture at the top of the reactor.
• a device according to the invention is described schematically.
• This device 1000 is integrated in an installation including a digester 9 which is not part as such of the device according to the invention.
• Such an installation can be used to implement a lysis-digestion (LD) process, but it will be noted that it will also be possible to integrate the method according to the invention in known configurations of the prior art called digestion-lysis. (DL) or digestion-lysis-digestion (DLD), knowing that in the so-called DL configuration a portion of the sludge is hydrolysed and then returns to the digester.
• DL digestion-lysis-digestion
• DLD digestion-lysis-digestion
• centrifuged sludge is conveyed by a pipe 1 to a hopper 2 provided with two worm to homogenize. These two worm screws are also used to feed the feed pump 3 supplying the sludge to the dynamic injector-mixer 4.
• the dehydrated and homogenized sludge from the hopper 2 are thus pumped through the pump 3 in a pipe serving as means for feeding these slurries to the dynamic injector-mixer 4.
• This dynamic injector-mixer 4 is also provided with steam injection means 100 generated by a steam generator not shown in FIG. 1.
• the injector-mixer comprises a cylindrical chamber provided with stirring means consisting of blades mounted on an axis of rotation mu by a rotor rotating at a speed between 1000 rpm and 2000 rpm, this speed being adjustable according to the dryness of the sludge .
• the residence time of the material transiting continuously in the mixer injector is short and in practice less than 10 minutes.
• the blades do not advance the material in the chamber but only shake it vigorously
• a washing water inlet 200 is provided upstream of the dynamic injector-mixer 4. With such water supply means 200, the dynamic injector-mixer can be cleaned if necessary.
• a pipe is used to convey the single-phase mixture produced therein to a thermal hydrolysis reactor 5.
• the treatment in this thermal hydrolysis reactor 5 is carried out at a temperature of between 165 ° C and 180 ° C, the inside of the reactor being maintained at a pressure of between 8 bar and 10 bar a (in this respect, it will be noted that lower or higher temperatures and pressures may be in particular according to the dryness of the sludge).
• a water inlet 101 located at the inlet of the reactor 5 is provided to be able to bring cleaning water into the reactor during cleaning phases that can be performed at the start of the installation or during maintenance phase of it.
• a purge 102 is provided for evacuating any incondensable gases.
• the hydrolysed sludge in the reactor 5 is then conveyed via a pipe to a heat exchanger 7. Before reaching this heat exchanger 7 cooling and dilution water is fed into the hydrolysed sludge by means of injection 201. If necessary, this dilution can also be done after the exchanger 7.
• the depressurizing member 8 which, by definition, generates a pressure drop, makes it possible to maintain the pressure prevailing in the thermal hydrolysis reactor 5.
• This body is, in the context of this example, constituted by an eccentric screw pump provided between the heat exchanger and the digester. In other embodiments it may be constituted by a valve or any other member to perform this function.
• the thermally hydrolyzed sludge is sent to the digester 9 where they can be easily digested because they have undergone thermal hydrolysis.
• FIG. 1 of an installation incorporating a device according to the invention is a schematic representation.
• the form of the reactor 5 in which the thermal hydrolysis of the monophasic mixture of sludge and steam is performed may take different forms. Three of these forms are given with reference to FIGS. 2, 3 and 4.
• the reactor 5 has a vertical shape.
• the reactor is provided in its lower part with a feed of single-phase mixture of sludge heated with steam 501 and in its upper part with an outlet of the reactor 502.
• a purge 503 is provided to evacuate any incondensable gases and means for measuring the pressure of the temperature inside the reactor are also provided in the upper part thereof.
• the thermal hydrolysis reactor has a first vertical section provided at its base with a single-phase mixture of sludge and steam 401, connected directly to a second vertical part provided at its foot with a evacuation 402 of hydrolysed sludge.
• a purge 403 is provided at the junction between these two vertical parts to evacuate any incondensable gases.
• Means for measuring the pressure and the temperature in the reactor are also provided. Note that in this configuration, the second vertical section portion is directly connected to the first vertical section without horizontal section between the two.
• the thermal hydrolysis reactor has a first vertical section provided at its head with a single-phase mixture of sludge and steam 601, connected directly to a second vertical part provided at its foot with a evacuation 602 of hydrolysed sludge.
• a purge 603 is provided at the junction between these two vertical parts to evacuate any incondensable gases.
• Means for measuring the pressure and the temperature in the reactor are also provided. Note that in this configuration, the second vertical section portion is directly connected to the first vertical section without horizontal section between the two.
• FIG. 5 shows the evolution over time of the temperature prevailing inside the thermal hydrolysis reactor: on the one hand in the context of the invention implementing a dynamic injector-mixer planned upstream of the reactor thermal hydrolysis; and, - On the other hand in the context of a similar installation according to the prior art in which dynamic injector-mixer is not used, the steam being injected at the bottom of the reactor.
• the temperature prevailing inside the reactor increases progressively until reaching and maintaining the set temperature allowing the optimized thermal lysis of the hydrolyzable organic compounds. contained in the treated sludge.
• the temperature observed in the reactor is immediately that of the injected steam. It then undergoes significant variations. This reflects the fact that, in the art according to this prior art, it does not systematically occur intimate mixture of steam with the sludge. On the contrary, the temperature fluctuations observed in the reactor reflect the existence of poly-phase flows within it. In the example described here, the steam being injected at a speed (in practice greater than
• the mixture reaching this reactor is perfectly monophasic liquid and homogeneous. It can therefore flow in piston flow in it.
• the set temperature is maintained throughout the residence time in the reactor. The energy of the steam is therefore optimally transferred to the sludge and the hydrolysis of the hardly biodegradable compounds can be carried out efficiently.
• the quantity of theoretical energy for hydrolyzing a given quantity of sludge corresponds more or less to the quantity actually used to obtain this hydrolysis.
• the calculation of the energy necessary to increase the temperature of a fluid of a temperature A at a temperature B is easy to achieve.
• the calculated theoretical vapor flow rate was 25 kilograms of steam at 13 bar per hour and the tests showed that it was exactly this steam flow that was actually necessary to hydrolyze effectively. sludge.
• the invention makes it possible to use reactors having a volume between 20 and 25% less than the reactor volumes of the prior art.

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