WO2014154466A1 - Procédé et dispositif d'hydrolyse thermique en continu - Google Patents
Procédé et dispositif d'hydrolyse thermique en continu Download PDFInfo
- Publication number
- WO2014154466A1 WO2014154466A1 PCT/EP2014/054388 EP2014054388W WO2014154466A1 WO 2014154466 A1 WO2014154466 A1 WO 2014154466A1 EP 2014054388 W EP2014054388 W EP 2014054388W WO 2014154466 A1 WO2014154466 A1 WO 2014154466A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reactor
- sludge
- thermal hydrolysis
- mixture
- temperature
- Prior art date
Links
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
- 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.
- 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 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%.
- 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.
- 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.
- 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 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 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.
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Molecular Biology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
Claims
Priority Applications (11)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP14709237.3A EP2978715A1 (fr) | 2013-03-25 | 2014-03-06 | Procédé et dispositif d'hydrolyse thermique en continu |
RU2015145809A RU2654013C2 (ru) | 2013-03-25 | 2014-03-06 | Способ и устройство для непрерывного термического гидролиза |
AU2014243326A AU2014243326B2 (en) | 2013-03-25 | 2014-03-06 | Process and device for continuous thermal hydrolysis |
JP2016504548A JP6458001B2 (ja) | 2013-03-25 | 2014-03-06 | 有機物を含有する汚泥を連続的に熱加水分解する方法 |
CA2906159A CA2906159C (fr) | 2013-03-25 | 2014-03-06 | Procede et dispositif d'hydrolyse thermique en continu |
MX2015013302A MX369384B (es) | 2013-03-25 | 2014-03-06 | Procedimiento y dispositivo de hidrolisis termica continua. |
US14/779,746 US10322959B2 (en) | 2013-03-25 | 2014-03-06 | Process and device for continuous thermal hydrolysis |
KR1020157026628A KR102067167B1 (ko) | 2013-03-25 | 2014-03-06 | 연속적인 열적 가수분해의 방법 및 장치 |
CN202010285763.0A CN111302602B (zh) | 2013-03-25 | 2014-03-06 | 连续热水解的方法和装置 |
CN201480018093.9A CN105050967A (zh) | 2013-03-25 | 2014-03-06 | 连续热水解的方法和装置 |
HK16105400.5A HK1217476A1 (zh) | 2013-03-25 | 2016-05-11 | 連續熱水解的方法和裝置 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1352686A FR3003558B1 (fr) | 2013-03-25 | 2013-03-25 | Procede et dispositif d’hydrolyse thermique en continu |
FR1352686 | 2013-03-25 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2014154466A1 true WO2014154466A1 (fr) | 2014-10-02 |
Family
ID=48856786
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/EP2014/054388 WO2014154466A1 (fr) | 2013-03-25 | 2014-03-06 | Procédé et dispositif d'hydrolyse thermique en continu |
Country Status (12)
Country | Link |
---|---|
US (1) | US10322959B2 (fr) |
EP (1) | EP2978715A1 (fr) |
JP (1) | JP6458001B2 (fr) |
KR (1) | KR102067167B1 (fr) |
CN (2) | CN111302602B (fr) |
AU (1) | AU2014243326B2 (fr) |
CA (1) | CA2906159C (fr) |
FR (1) | FR3003558B1 (fr) |
HK (1) | HK1217476A1 (fr) |
MX (1) | MX369384B (fr) |
RU (1) | RU2654013C2 (fr) |
WO (1) | WO2014154466A1 (fr) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107074601A (zh) * | 2014-10-31 | 2017-08-18 | 威立雅水务技术支持公司 | 用于热水解污泥的方法和设备 |
US11453608B2 (en) | 2017-05-11 | 2022-09-27 | Bl Technologies, Inc. | Method for pre-conditioning sludge |
Families Citing this family (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
ES2570812B1 (es) * | 2014-11-19 | 2017-09-05 | Aquatec, Proyectos Para El Sector Del Agua, S.A.U. | Procedimiento para la hidrólisis térmica en continuo de materia orgánica y una instalación apta para la puesta en práctica del procedimiento |
FR3032193B1 (fr) * | 2015-02-02 | 2020-01-31 | Degremont | Optimisation d'un procede de traitement de pulpe |
CN105923969A (zh) * | 2016-07-13 | 2016-09-07 | 同济大学 | 连续式污泥高温热水解装置 |
CN106237879A (zh) * | 2016-08-31 | 2016-12-21 | 上海同济普兰德生物质能股份有限公司 | 一种高干度污泥管式蒸汽喷射浆化装置及方法 |
CN110650810A (zh) * | 2017-03-15 | 2020-01-03 | 碧奥新能源有限公司 | 用于将进料至沼气反应器的原料卫生化的卫生化单元和方法 |
CN107867787A (zh) * | 2017-12-23 | 2018-04-03 | 北京达源环保科技有限公司 | 用于污泥热水解处理的旋流式反应器 |
CN110272177A (zh) * | 2019-07-09 | 2019-09-24 | 上海东振环保工程技术有限公司 | 一种工业园区污水厂生化剩余污泥减量方法及应用 |
CN112876022B (zh) * | 2021-01-19 | 2022-05-27 | 重庆科技学院 | 一种利用热固载体处理轧钢油泥的热解装置 |
Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20080223793A1 (en) * | 2007-03-16 | 2008-09-18 | Ch2M Hill, Inc. | Treatment of Particulate Biodegradable Organic Waste by Thermal Hydrolysis Using Condensate Recycle |
WO2009121873A1 (fr) * | 2008-03-31 | 2009-10-08 | Krüger Off-Shore A/S | Appareil et procédé d’hydrolyse thermique continue de matériel biologique |
EP2177280A2 (fr) * | 2008-10-16 | 2010-04-21 | Hermann Dauser | Procédé et dispositif d'hydrolyse discontinue de substrats organiques |
AT509319A4 (de) * | 2010-05-25 | 2011-08-15 | Biogas Systems Gmbh | Verfahren und vorrichtung zur hydrolyse von vorzugsweise festen, organischen substraten |
Family Cites Families (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3687646A (en) * | 1970-12-21 | 1972-08-29 | Texaco Development Corp | Sewage disposal process |
SU1564196A1 (ru) * | 1987-07-28 | 1990-05-15 | Северо-Кавказский Филиал Всесоюзного Научно-Исследовательского Института Гидролиза Растительных Материалов | Способ двухстадийного гидролиза растительного сырь |
US4983296A (en) * | 1989-08-03 | 1991-01-08 | Texaco Inc. | Partial oxidation of sewage sludge |
NO310717B1 (no) * | 1999-05-31 | 2001-08-20 | Cambi As | Fremgangsmate og anordning for kontinuerlig hydrolyse av avlopsvann |
JP2005205252A (ja) * | 2004-01-20 | 2005-08-04 | Kobe Steel Ltd | バイオマスを含む高濃度スラリー、および高濃度スラリーの製造方法、並びにバイオマス燃料の製造方法 |
JP4812261B2 (ja) * | 2004-05-10 | 2011-11-09 | 日鉄環境エンジニアリング株式会社 | 高濃度有機性物質中の固形分の可溶化処理方法、及び高濃度有機性物質の処理方法 |
CZ17066U1 (cs) * | 2006-07-24 | 2006-12-12 | Coramexport S. R. O. | Zařízení pro diskontinuální nebo kontinuální hydrolýzu organické hmoty |
CN102428044A (zh) * | 2009-03-18 | 2012-04-25 | 克莉雅沃特泰科有限公司 | 污泥水解设备、使用该设备的方法及在该污泥水解设备中提供的接触式热交换单元和蒸汽式热交换单元 |
CN101979349B (zh) * | 2010-08-06 | 2012-05-30 | 安徽合协生态环境科技有限公司 | 一种污泥管式热水解处理方法及其装置 |
JP5347133B2 (ja) * | 2010-08-30 | 2013-11-20 | 株式会社テクノプラン | 汚泥処理方法及び汚泥処理システム |
CN102381820B (zh) * | 2011-09-20 | 2012-12-05 | 福州开发区三水环保科技有限公司 | 基于水热改性技术的污泥处理工艺 |
CN102417285B (zh) * | 2011-10-20 | 2013-05-01 | 同济大学 | 一种高含固生物污泥连续热水解装置与方法 |
CN102515454B (zh) * | 2011-12-22 | 2013-09-25 | 湖北国新天汇能源有限公司 | 采用旋转方式实现热水解发酵处理的装置与方法 |
CN102718377B (zh) * | 2012-06-21 | 2013-09-11 | 上海同济普兰德生物质能股份有限公司 | 一种城市污泥除砂消毒预处理的装置与方法 |
PL2774894T3 (pl) * | 2013-03-08 | 2016-03-31 | Aquatec Proyectos Para El Sector Del Agua S A U | Ciągły sposób termicznej hydrolizy materiału organicznego oraz instalacja umożliwiająca realizację sposobu |
-
2013
- 2013-03-25 FR FR1352686A patent/FR3003558B1/fr active Active
-
2014
- 2014-03-06 AU AU2014243326A patent/AU2014243326B2/en active Active
- 2014-03-06 WO PCT/EP2014/054388 patent/WO2014154466A1/fr active Application Filing
- 2014-03-06 KR KR1020157026628A patent/KR102067167B1/ko active IP Right Grant
- 2014-03-06 CN CN202010285763.0A patent/CN111302602B/zh active Active
- 2014-03-06 CN CN201480018093.9A patent/CN105050967A/zh active Pending
- 2014-03-06 CA CA2906159A patent/CA2906159C/fr active Active
- 2014-03-06 MX MX2015013302A patent/MX369384B/es active IP Right Grant
- 2014-03-06 EP EP14709237.3A patent/EP2978715A1/fr active Pending
- 2014-03-06 RU RU2015145809A patent/RU2654013C2/ru active
- 2014-03-06 US US14/779,746 patent/US10322959B2/en active Active
- 2014-03-06 JP JP2016504548A patent/JP6458001B2/ja active Active
-
2016
- 2016-05-11 HK HK16105400.5A patent/HK1217476A1/zh unknown
Patent Citations (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20080223793A1 (en) * | 2007-03-16 | 2008-09-18 | Ch2M Hill, Inc. | Treatment of Particulate Biodegradable Organic Waste by Thermal Hydrolysis Using Condensate Recycle |
WO2009121873A1 (fr) * | 2008-03-31 | 2009-10-08 | Krüger Off-Shore A/S | Appareil et procédé d’hydrolyse thermique continue de matériel biologique |
EP2177280A2 (fr) * | 2008-10-16 | 2010-04-21 | Hermann Dauser | Procédé et dispositif d'hydrolyse discontinue de substrats organiques |
AT509319A4 (de) * | 2010-05-25 | 2011-08-15 | Biogas Systems Gmbh | Verfahren und vorrichtung zur hydrolyse von vorzugsweise festen, organischen substraten |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN107074601A (zh) * | 2014-10-31 | 2017-08-18 | 威立雅水务技术支持公司 | 用于热水解污泥的方法和设备 |
US11453608B2 (en) | 2017-05-11 | 2022-09-27 | Bl Technologies, Inc. | Method for pre-conditioning sludge |
Also Published As
Publication number | Publication date |
---|---|
US20160185640A1 (en) | 2016-06-30 |
JP6458001B2 (ja) | 2019-01-23 |
US10322959B2 (en) | 2019-06-18 |
CN111302602A (zh) | 2020-06-19 |
KR20150133207A (ko) | 2015-11-27 |
KR102067167B1 (ko) | 2020-01-17 |
MX369384B (es) | 2019-11-06 |
EP2978715A1 (fr) | 2016-02-03 |
AU2014243326B2 (en) | 2018-03-15 |
HK1217476A1 (zh) | 2017-01-13 |
CA2906159A1 (fr) | 2014-10-02 |
CN105050967A (zh) | 2015-11-11 |
RU2015145809A (ru) | 2017-05-03 |
FR3003558B1 (fr) | 2015-04-24 |
FR3003558A1 (fr) | 2014-09-26 |
JP2016517792A (ja) | 2016-06-20 |
RU2654013C2 (ru) | 2018-05-15 |
MX2015013302A (es) | 2015-12-15 |
AU2014243326A1 (en) | 2015-11-12 |
CN111302602B (zh) | 2023-04-28 |
CA2906159C (fr) | 2020-02-11 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP3041796B1 (fr) | Procede et dispositif d'hydrolyse thermique en continu avec recirculation de vapeur de recuperation | |
WO2014154466A1 (fr) | Procédé et dispositif d'hydrolyse thermique en continu | |
EP3087038B1 (fr) | Procede d'hydrolyse thermique en continu de boues a forte siccite | |
EP1360151B1 (fr) | Procede pour l'hydrolyse thermique des boues | |
RU2566997C2 (ru) | Способ и устройство для гидролиза предпочтительно твердых органических субстратов | |
EP2009353A1 (fr) | Procédé de préparation d'une charge mixte contenant de la biomasse et une coupe hydrocarbonnée lourde en vue d'une gazeification ultereure | |
WO2013167469A1 (fr) | Procede et installation pour l'hydrolyse thermique des boues | |
EP3152167A1 (fr) | Procédé et dispositif de carbonisation hydrothermale à mélange optimisé de boue et vapeur | |
EP3212582B1 (fr) | Procédé et installation pour l'hydrolyse thermique des boues | |
EP3152166A1 (fr) | Reacteur de carbonisation hydrothermale a melange optimise de boue et vapeur | |
EP3328802B1 (fr) | Procede et installation pour l'hydrolyse thermique semi-continue des boues | |
WO2015135932A1 (fr) | Procede de traitement de dechets organiques par oxydation hydrothermale | |
WO2013011447A1 (fr) | Procédé et installation pour effectuer en continu l'hydrolyse de matières organiques, en particulier de boues produites lors du traitement des eaux | |
FR2799456A1 (fr) | Dispositif de traitement de l'eau destine a augmenter la solubilite de l'oxygene dans l'eau potable ultra pure | |
WO2024068894A1 (fr) | Procede de traitement de dechets organiques | |
EP3247489A1 (fr) | Procédé et installation de production d'un produit poreux en poudre | |
FR2894248A1 (fr) | Dispositif de destruction oxydative de la matiere insoluble de boue d'epuration par couplage thermique et ultrasons. | |
FR3140364A1 (fr) | Procede de traitement de dechets organiques | |
FR2947043A1 (fr) | Dispositif de sechage d'un dechet et procede correspondant. | |
WO2018184123A1 (fr) | Procede et installation pour extraire de l'anhydride carbonique au cours d'un traitement de dechets par oxydation par voie humide | |
CH706345B1 (fr) | Procédé et dispositif de traitement par oxydation par voie humide de déchets liquides radioactifs contenant des charges de matières diverses. | |
FR3118631A1 (fr) | Dispositif et procédé pour la production d’acides gras volatils à partir de coquilles de mollusques présentant des corps mous ou de la chair | |
FR2947044A1 (fr) | Dispositif de sechage de dechets par evaporation et procede correspondant. |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 201480018093.9 Country of ref document: CN |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 14709237 Country of ref document: EP Kind code of ref document: A1 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2014709237 Country of ref document: EP |
|
ENP | Entry into the national phase |
Ref document number: 2906159 Country of ref document: CA |
|
WWE | Wipo information: entry into national phase |
Ref document number: MX/A/2015/013302 Country of ref document: MX |
|
ENP | Entry into the national phase |
Ref document number: 20157026628 Country of ref document: KR Kind code of ref document: A Ref document number: 2016504548 Country of ref document: JP Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 2015145809 Country of ref document: RU Kind code of ref document: A |
|
ENP | Entry into the national phase |
Ref document number: 2014243326 Country of ref document: AU Date of ref document: 20140306 Kind code of ref document: A |
|
WWE | Wipo information: entry into national phase |
Ref document number: 14779746 Country of ref document: US |