Classifications

• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
  • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
  • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
  • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
  • F23G5/10—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating electric
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
  • F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
  • F23G5/14—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating including secondary combustion
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2201/00—Pretreatment
  • F23G2201/10—Drying by heat
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2201/00—Pretreatment
  • F23G2201/90—Cooling
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2209/00—Specific waste
  • F23G2209/12—Sludge, slurries or mixtures of liquids
• • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
  • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
  • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
  • F23G2209/00—Specific waste
  • F23G2209/20—Medical materials

Definitions

• the present invention relates to the technical field of waste treatment and it aims, more particularly, although in a nonlimiting manner, the treatment of wet waste and, more specifically, among these sludges of various origins.
• the first relates to the water content which must necessarily be removed for a suitable treatment to lead to "inerting" of the residual dry products.
• insusceptible By the neologism "inerting”, it is necessary to understand any means to make such waste after treatment insusceptible to cause pollution by themselves or by leaching.
• This first difficulty is linked to the need to control energy expenditure, so that the cost of treatment is acceptable.
• the second difficulty is due to the pasty or muddy form of the waste which poses a hardly soluble problem of transfer within an installation, by the risks of clogging, solidification, vaulting which can intervene within the transfer circuits in particular. .
• the third difficulty relates to the establishment, conduct and control of a treatment process capable of safely and completely eliminating all the components of the waste likely to be destroyed by incineration. This is an objective that must necessarily be achieved in order to meet the requirements of regulatory, even legislative, texts aimed at eliminating, in the long term if not immediately, deposits and discharges in illegal or regulated access landfills.
• the prior art has proposed a number of methods for attempting to inert the waste. These processes can be classified into two main categories, called cold process and hot process.
• 3,677,404 consists in creating, in an incineration oven, a fluidized bed of inert mineral solid particles, for example formed of silica grains, such a bed being heated to a suitable temperature, by example close to 750 ° C.
• the particles circulate from the bottom of the bed to the upper level from which they are recycled to be incorporated into the waste.
• the mixture obtained is received in a filtration tower intended to allow the evacuation of at least part of the moisture.
• a low racking device is provided for extracting the mixture from the filtration tower and for directing it to the inlet of a feed system supplying, in the oven at the base of the fluidized bed, the mixture of heated particles.
• the waste-particle mixture will have the property of being put into circulation and of following, by a continuous supply of the furnace, an upward migration in the fluidized bed within which an incineration of the burnable components may intervene.
• the second is due to the fact that the mixture from the filtration tower has a heterogeneous character which is not favorable to the progress of a complete incineration process inside the bed.
• the third is that the fluidization of the bed is ensured by the exhaust gas from a burner responsible for raising and maintaining the inert recyclable particles in temperature.
• the exhaust gas from a burner responsible for raising and maintaining the inert recyclable particles in temperature In the case of a bed which is necessarily very high to impose a sufficient residence time, as is recommended, the incineration of the "burnable" components cannot really and effectively intervene due to a lack of oxygen. .
• the present invention aims to overcome the drawbacks listed above, in order to provide a method for inerting wet waste, and more particularly sludge, which is really efficient, relatively low energy consumer and which can make the subject to flexibility or suppleness of conduct, in particular by a self-adaptation of the temperature regulation of the bed taking into account the energy input resulting from the actual and complete combustion of the burnable components.
• extract, from the roof of the furnace, the gases produced which are directed to a treatment installation. and extracting the surplus from the fluidized bed from the upper level is characterized in that it consists in:. recycle the hot inert particles extracted from the bed to a mixing section of one unit,. admit in appropriate proportion the wet waste to be treated in said section, proceed to mixing in the section,. stir and move the mixture in a drying coating section where the waste agglomerates in a layer around the particles to form a gangue that is at least partly dried,. recycle the particles coated directly at the base of the bed and maintain the fluidization of the bed with a pressurized, oxygenated fluid, supplied at least at the base of the bed.
• Figure 1 is a schematic view illustrating an installation for implementing the method.
• Figure 2 is a schematic view showing an alternative embodiment of the installation.
• Figure 1 shows a first embodiment of an installation for the implementation of the treatment process.
• Such an installation comprises an oven 1 delimiting an enclosure 2 for confining a bed 3 of materials or of an inert mineral material, in particulate form.
• the enclosure 2 is made so that the bed 3 can rise over a relatively large height, for example between 1 m and 2.50 m.
• the inert mineral material selected is chosen from silica, alumina, lime, zircon, with a particle size favorable for fluidization.
• the particle size is, for example, between 100 and 2000 micrometers in average diameter.
• the bed 3 can be formed from a single mineral material or from a composition of several compatible with each other.
• the oven 1 comprises an insulating envelope 4 suitably formed to form a barrier limiting the propagation of calories from the interior of the oven to the surrounding environment.
• a tank 5 is mounted which delimits the enclosure 2.
• the tank 5 has a bottom 6 and a double bottom 6a defining between them a manifold 7 for inlet and pressure distribution, the function appears in the following.
• the double bottom 6a is provided with fluidization nozzles 8 opening inside the collector 7 which communicates with a circuit 9 adapted to supply an oxygenated gaseous fluid, under pressure, responsible for ensuring the fluidization of the bed 3.
• the fluid gaseous fluidization is, for example, supplied by a booster 10 whose outlet 11 can be connected to the circuit 9, either directly or indirectly through a heating system 12, of any suitable type, which can be , of preferably, a heat exchanger, the second circuit of which will be described below.
• the oven 1 furthermore comprises heating means 13 which are constituted by static means capable of heating the bed 3.
• Such means 13 are preferably constituted by electrical resistors, arranged between the tank 5 and the insulating envelope 4, being distributed over the entire height corresponding to that of the bed 3 at least, but preferably also over the height of a chamber 14 forming an enclosure sky and delimited inside the latter by the upper level of the bed 3.
• the chamber 14 communicates at its upper part with a chimney 15 passing through the insulating envelope 4 to ensure the extraction of the fumes and other gaseous products developing in the enclosure 2.
• the chimney 15 leads to a cyclone 16 for separating any dust, before being connected to the heating system 12 to take the second circuit of the latter then produced in the form of a dual-circuit exchanger.
• the exchanger 12 is also connected to a smoke treatment unit 17, produced in any known manner to provide pollution control.
• the circuit 9 comprises a branch branch 9a capable of passing through a heater 18 the outlet of which is connected to means 19 for supplying an oxidizer inside the enclosure 2.
• the means 19 are, for example, constituted by a rod 20, the end of which is provided with a diffuser 21 which may be situated just above the upper level of the bed 3 or at least partly inside the latter.
• the upper level of the bed 3 inside the enclosure 2 is determined by extraction means 25 which can involve active means, of the type of an extraction screw endless driven by a motor or passive means, such as an overflow through a level weir.
• the enclosure 2 is provided with means 26 for supplying waste to be treated.
• waste it is appropriate, within the meaning of the invention, to consider the term in its broadest sense to designate wet materials and more generally sludge.
• the supply means 26 may consist of a sheath containing a worm or a pneumatic transfer system. In all cases, the means 26 open out at the bottom of the tank 5, substantially at the level of the double bottom 6a and above the outlets of the nozzles 8.
• the supply means 26 are connected by a supply line 27 to a mixing unit 28 comprising a first inlet 29 reserved for the introduction of the waste to be treated and a second inlet 30 reserved for the introduction of a charge of mineral matter in particulate form directly from the means 25.
• the mixing unit 28 comprises a box 32 defining a trough or gutter 33 for, at least, a mixing screw 34 of the Archimedes type driven in rotation by an actuator 35.
• the gauge 33 defines a section or zone 36, so-called mixing, to which the inputs 29 and 30 lead.
• the input 29 is connected upstream to a device 37 for supplying waste which may be a buffer tank provided with extraction means, a grinder, a kneader, an agitator, or even a granulator, if the wet waste has been previously frozen.
• the gauge 33 delimits, after the zone 36, a zone or section 38, called coating-drying, which is overhung by a hood 39 connected to the smoke treatment circuit, for example between the heating system 12 and the processing unit 17.
• the gauge 33 is connected, opposite the section 36, to the line 27 with the interposition of a launching apparatus 40.
• the method according to the invention consists in heating 1 enclosure 2 by means of the means 13 so as to maintain a constant temperature, between 400 and 1000 ° C. and typically close to 900 ° C., imposed on the bed 3.
• the unit 28 When the desired temperature is reached and maintained by control and servo means which are not directly part of the object of the invention, the unit 28 is put into service.
• inert mineral particles at a suitable temperature are supplied, for example by an auxiliary circuit 30a to maintain a functional mode in a closed circuit.
• the inert particles come directly from the oven 2 by extraction from the upper level of the bed 3.
• the hot mineral particles are discharged into zone 36 where they are stirred by the rotation of the screw (s) 34.
• the zone 36 also receives by the input 29 a proportional quantity of waste which is thus mixed with the particles in the zone 36.
• the screw (s) 34 then maintain effective mixing of the mixture in the zone 38 where there is a gradual coating of the hot inert mineral particles which transfer their calories to the layer of waste gradually forming into a dry gangue of relatively small thickness. Given the large specific surface area of the particles, a high drying power of the waste occurs and the vapors produced are taken up by the hood and evacuated.
• the waste is completely incorporated by coating around the particles and the mixture thus obtained can be described as homogeneous.
• coated particles are then extracted from the box 28 and taken in charge by the launcher 40 to be conducted by the line 27 to the means 26 ensuring their introduction inside the bed 3 whose fluidized state is maintained by the intake oxygenated gaseous fluid, possibly heated, supplied by the booster 10 and delivered to the lower manifold of the tank 5.
• the coated particles are subjected to a thermal shock bringing the gangue of waste to ambient temperature of the fluidized bed.
• the ascending path is positively controlled in terms of residence time, since the particles and waste are trapped in a sort of fluid matrix whose homogeneity is ensured by the fact that the particles of mineral matter having been coated, are of the same nature and of the same particle size as those constituting the fluidized bed.
• This residence time which is consequently relatively long due to the height of the fluidized bed 3, can, depending on the operating parameters of the furnace, be in the region of several tens of minutes, or even several hours, during which the waste is subjected to the processing temperature. This temperature therefore promotes the combustion of the combustible parts of the waste, the oxidation of the oxidizable parts, and even the sublimation of the sublimable parts.
• the leachable products partially decompose in the gaseous phase, for example, the salts in the form of chloride, and this gaseous phase is evacuated from the treatment and reaction enclosure 2, via the chimney 15 to undergo there. a possible separation of the fine particles included inside the cyclone 16 before passing through the exchanger 12 making it possible to improve the energy balance of the installation in operation.
• the fumes are washed and decontaminated by the unit 17 operating in a manner known per se.
• the residual part of the waste in solid form can be partly burnt and partly oxidized by the effect of oxygen surrounding each of the particles and which comes from the gaseous fluid for fluidizing bed 3. It can be envisaged to improve the presence of oxygen inside the enclosure 2, in particular providing for a supply by the rod 20 to maintain, for example, in the headliner or chamber 14, a partial oxygen pressure greater than 2,000 Pascal, maintaining an oxidizing atmosphere.
• the oxidation of the residual part in solid form also occurs due to the temperature maintained inside the enclosure 2 and the long residence time which is imposed on the particles along an ascending path or path inside the fluidized bed 3.
• the supply, continuously or discontinuously, of the mixture to be treated has the consequence of increasing the mass of the fluidized bed 3, the surplus of which is taken up at a higher level by the extraction means 25.
• This surplus consists of the mineral matter in inert particulate form, or even the inert solid fraction of waste.
• the input into zone 36 may involve a proportion of particulate matter between 15 and 80% compared to waste.
• the recommended method involves the use of inert particles which can be described as carriers which, in the above case, rotate in a closed circuit to facilitate the hydrodynamics, handling and circulation of waste in the installation.
• the particles included also act as a vector of heat energy favoring, during mixing in the unit 28, the drying of wet waste.
• This arrangement makes it possible to treat a wide spectrum of wet waste, even going as far as direct treatment of organic and hospital waste by planning, for example to freeze it initially to allow grinding and / or granulation promoting incorporation into the inert material. recycled whose temperature at the outlet of the oven ensures rapid drying during the mixing phase in the unit 28.
• FIG. 2 shows an alternative embodiment in which the recirculation means 30 are directed, optionally after passing through a cooler 43, towards a separator 44 capable of ensuring, by any suitable means, such as centrifugation or mechanical stripping, the separation between the particulate inert material and the solid fraction of the waste together constituting the surplus extracted from the bed 3 by the means 25.
• the separated solid fraction is evacuated to a unit for conditioning or compacting final waste, such as 45, while the fraction of inert particulate matter is taken up by a line 46 to reach inlet 29.
• the invention finds a preferred application in the treatment of wastewater sludge.
• the invention is not limited to the examples described and shown since various modifications can be made without departing from its scope.

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• Engineering & Computer Science (AREA)
• Mechanical Engineering (AREA)
• General Engineering & Computer Science (AREA)
• Processing Of Solid Wastes (AREA)
• Treatment Of Sludge (AREA)
• Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
• Drying Of Solid Materials (AREA)

Applications Claiming Priority (3)

Publications (2)

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ID=9460666

Family Applications (1)

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Cited By (1)

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• 1995
  • 1995-02-24 EP EP95910598A patent/EP0746725B1/de not_active Expired - Lifetime
  • 1995-02-24 US US08/696,911 patent/US5806444A/en not_active Expired - Fee Related
  • 1995-02-24 ES ES95910598T patent/ES2133748T3/es not_active Expired - Lifetime
  • 1995-02-24 CA CA002183786A patent/CA2183786C/fr not_active Expired - Fee Related
  • 1995-02-24 DK DK95910598T patent/DK0746725T3/da active
  • 1995-02-24 DE DE69509506T patent/DE69509506T2/de not_active Expired - Fee Related
  • 1995-02-24 WO PCT/FR1995/000223 patent/WO1995023317A1/fr active IP Right Grant
  • 1995-02-24 AT AT95910598T patent/ATE179790T1/de not_active IP Right Cessation

Non-Patent Citations (1)

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