Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
  • B01D21/0084—Enhancing liquid-particle separation using the flotation principle
• • 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
  • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
  • C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
  • B01D21/02—Settling tanks with single outlets for the separated liquid
  • B01D21/08—Settling tanks with single outlets for the separated liquid provided with flocculating compartments
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
  • B01D21/24—Feed or discharge mechanisms for settling tanks
  • B01D21/2494—Feed or discharge mechanisms for settling tanks provided with means for the removal of gas, e.g. noxious gas, air
• • 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
  • C02F1/24—Treatment of water, waste water, or sewage by flotation
• • 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
  • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
  • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
  • C02F1/56—Macromolecular compounds
• • 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
  • C02F1/72—Treatment of water, waste water, or sewage by oxidation
  • C02F1/74—Treatment of water, waste water, or sewage by oxidation with air
• • 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
  • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
  • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
• • 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
  • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
  • C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
  • C02F11/143—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using inorganic substances
  • C02F11/145—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using inorganic substances using calcium compounds
• • 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
  • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
  • C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
  • C02F11/147—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using organic substances
• • 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
  • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
• • 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
  • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
  • C02F1/5281—Installations for water purification using chemical agents
• • 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
  • C02F2209/38—Gas flow rate
• • 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
  • C02F2209/40—Liquid flow rate
• • 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
  • C02F2303/02—Odour removal or prevention of malodour

Definitions

• the present invention relates to a method for treating liquid sludge by injecting air into a sludge stream.
• the invention finds a particularly important, although not exclusive, application in the field of thickening and / or reducing the volume of sludge resulting from a water treatment and / or accumulated in industrial water settling ponds. .
• Sludge thickeners (FR 2 729 383) are already known which make it possible to improve the dryness of compact sludge by means of mechanical scrapers moving on the permeable bottom of storage tanks.
• Sludge thickening processes resulting from water treatment by flocculation / decantation requiring superficial degassing, the injection of a refloculation reagent into the sludge and finally a thickening into at least one lamellar thickener are also known.
• the thickening is provided mechanically and can not avoid frequent clogging.
• Static thickening systems formed by settling tanks are also known.
• the present invention aims to provide a method and a device that better than those previously known to the requirements of practice, in particular in that it does not use mechanical systems likely to seize or systems causing a structural change sludge to treat, but hydraulic systems, as well as inexpensive reagents (compressed or supercharged air, or conventional flocculant), and while allowing a sludge decontamination, quickly, the use of the method of thickening according to the invention requiring only a few seconds or minutes.
• the invention starts from the principle of a treatment or / and thickening in continuous or semi-continuous (by alternating batch) of a sludge, in which one feeds with the slurry a chamber in continuous flow by injecting simultaneously air with a large flow (several tens, or even hundreds of Nm 3 / h) resulting in velocities V of the obtained emulsion important at the location of the meeting between the air and the mud (V> lOm / s ) (for example 50 m / s), the emulsion being formed of a multitude of sludge droplets in the strong stream of air, a determined pressure drop is created in the emulsion by shrinking in and / or out of the enclosure, a flocculant is injected after such a shrinkage, said emulsion is degassed at atmospheric pressure and the whole is recovered in a filtration or decantation device.
• the in-line sludge is also rapidly concentrated downstream in a spillway vessel.
• the invention notably proposes a method for treating and conditioning liquid sludge, in which a first sludge emulsion is created in a pressurized in-line container fed by the sludge continuously at a first flow rate Q (m3 / h) by shocking the sludge with air injected into the container at a flow rate Q '(Nm3 / h), with Q'> 5Q, and then discharged at the outlet of the vessel via a body generating a pressure drop before recovery of the emulsion and degassing and then filtering or allowing the suspended solids of the emulsion thus obtained to be separated by separating them from the liquid part which is continuously emptied, characterized in that injecting the slurry and the air in a first zone of the container, and then evacuates the emulsion thus formed to a second region of the container extending over a first predetermined length L j ⁇ air injection and mud in the first zone and the length Li being suitable for constituting said first
• the evacuation is done in an enclosure extending over a second determined length L 2 , in which at least one flocculant is injected, in order to obtain in said enclosure a second air emulsion in the coagulated and flocculated sludge,
• said second emulsion is degassed at least in part by venting the chamber.
• the first zone is a small volume particularly confined between two side walls (as in a venturi or a pipe restriction for example) and for example less than 0.005 m 3 .
• continuous semi is meant by successive batches, which are substituted one after the other on the fly, or substantially without stopping, to allow treatment in continuous or semi-continuous, thereby allowing an excellent rate.
• the first emulsion is rather a sludge emulsion.
• a sludge emulsion By this is meant an emulsion where the sludge is in disperse phase in the air which is the continuous phase.
• the second emulsion is rather a gas emulsion in the sludge, the flocculant having blocked micro and millimeter gas bubbles within the mud flakes.
• the particularly small size of the injection zone (for example 0.01 m 3 ) will allow an excellent mud / air mixture.
• first and second zones can be separated by a restriction (a venturi and / or an orifice) forming the two zones in two separate chambers.
• a restriction a venturi and / or an orifice
• the first determined length is greater than fifty centimeters, for example greater than 1 m, for example 1 m 50.
• the pressure brings an energy capable of destabilizing and breaking the electrostatic (Coulombian type) or dipolar (Van des Waals type) bonds and thus causing water to escape from the organic fractions.
• the following dispersion produces a movement of acceleration of the sludge and expansion or stretching towards the zone of lower pressure continuing the effect of destabilization and destructuring of the colloids and a breaking effect of the bonds.
• compression sequences and then depression are reiterated again to extend / simplify / produce the desired effects.
• the technical effect obtained by the invention is primarily related to the porosification of the sludge obtained by the shock of the sludge with air under the conditions of dimensions and active zones of the reactor, then the pressure drop between container and enclosure that will be dimensioned more precisely and naturally by the skilled person depending on the treated effluent, flow rates used and the flocculant used.
• Air is introduced into the mud flow thus causing a shock between the air and the sludge and pressure differentials for example as will be seen by a venturi system with air suction.
• the second determined length L_2 is greater than 1 m, more preferably greater than 2 m or 3 m, for example 5 m or more.
• the mean pressure P in the container is such that 1.5 bar ⁇ P ⁇ 10 bar and Q 'is such that Q ⁇ Q' ⁇ 100 Q, for example Q '> 50 Q;
• the emulsion is strongly degassed at the outlet of the container, for example inside a degassing chamber provided with stirring means;
• the in-line container is a column of average diameter d and height H> 10 d, the sludge being introduced at the bottom of the column into the gas bed created by the air injected at the level of said sludge feed (for example above or below);
• the slurry is thrown into the column on a wall or an internal screen of the receptacle to improve the bursting thereof in the gaseous flow.
• the outlet in the container of the sludge feed is advantageously located opposite a wall and / or screen, at a small distance, for example less than 5 cm;
• a static mixer is a system known in itself not powered, located in the sludge feed tube and comprising for example static stirring blades and / or oblique diaphragms etc .;
• the flocculant is a polymer injected at the immediate outlet of the container, before venting.
• At least one reagent taken from the sand, calcium carbonate, slaked lime, oxidation reagents and / or coagulation aid reagents is introduced upstream of the container in the mud flow; at least one reagent taken from sand, calcium carbonate, slaked lime, oxidation reagents and / or coagulation aid reagents is introduced downstream of the container;
• the enclosure is tubular with an average passage cross section equivalent to that of the container;
• the tubular enclosure comprises at least one element generating a pressure drop downstream of the outlet of the receptacle, at the outlet of which the flocculant is injected;
• the tubular enclosure comprises at least one second element generating a pressure drop upstream of the first generating element, at the outlet of which at least one reagent and / or air is introduced;
• a rapid and / or substantially instantaneous concentration (a few seconds or even minutes, for example seven to ten minutes) of sludge is obtained by flotation / settling of the flocculated emulsion in a concentrator capacity, the concentrated sludge being discharged continuously by example by overflow.
• the injected air is heated and / or mixed with water vapor.
• the air is injected against the flow of the sludge, or to form a helical flow possibly against the flow of sludge, or injected at right angles to the mud flow, or in the direction of the sludge flow.
• the invention also proposes a device implementing the method as described above.
• a liquid sludge treatment and conditioning device comprising an in-line container, means for feeding sludge to said container continuously at a first flow rate Q (m3 / h), means for supplying said container with air at a flow rate Q '(Nm3 / h), with Q'> 5Q, and filtering means and / or decantation of the emulsion and flocculated arranged to separate the liquid portion of the suspended matter and recover it continuously, characterized in that the sludge and air supply means of the container are arranged to inject the sludge and the air into a first zone of the container, then to convey the mixing on a first length Li to form a first emulsion of drops of mud in the air, in that it comprises an evacuation chamber of the first emulsion obtained in the container, the enclosure being tubular extending for a length determined L_2, comprising means for venting and means for injecting at least one flocculant into said tubular enclosure upstream with respect to said venting, so as
• length or L2 determined is meant a distance greater than 0.5 m, preferably 1 m, for example 2 m, 3 m and preferably greater than 5 m, for example 10 m.
• the first zone of the container is of a small volume less than 0.05 m 3, in particular confined between two lateral walls (small section) (between which the mud is thus introduced to exit towards the second zone of greater volume and / or wider section).
• the small volume is for example formed by a venturi and / or is part of injection means or a device for simultaneous injection of air and sludge.
• the in-line container is a column of average diameter d and height H> 10 d, the sludge being introduced at the bottom of the column into the gas bed created by the air injected at the level, for example a little below or a little above (one or a few centimeters) of said sludge feed.
• the column further comprises an internal screen disposed at the outlet of the injection means in the column, for bursting the mud jet.
• the device comprises a static mixer of the sludge upstream of the container.
• the enclosure comprises at least one element generating a pressure drop, for example a venturi.
• the invention further proposes a degassing chamber provided with stirring means located downstream of the container.
• the invention also provides a slab of solidified sludge obtained from an organic slurry of porosity equal to or similar to that of pumice.
• porosity By equals or the like is meant a porosity of + 20%, advantageously + 10%.
• the porosity is, for example, calculated in a manner known per se on samples prepared after extracting the fluids from the sample with, for example, an extractor known under the name Soxhlet or by vacuum distillation. The total total volume V is measured for example by measurement, then the solid volume, for example with a pyknometer.
• the porosity of pumice stone is around 85% ( ⁇ 5%).
• the density of the wafer is for example between 0.5 and 0.9 g / cm 3 '
• the wafer is obtained by the method and / or the device as described above.
• Figure 1 is a diagram illustrating a first embodiment of a device embodying the method according to the invention.
• Figure 2 is a diagram illustrating a second embodiment of a device according to the invention.
• Figure 3 is an operating diagram of a third embodiment of a device according to the invention.
• Figure 4 shows schematically a fourth embodiment according to the invention with degasser and concentrator.
• FIGS. 5A, 5B and 5C are front, side and top views of a device according to a fifth embodiment of the invention.
• Figure 6 is a partial side view of a device according to a sixth embodiment of the invention.
• FIGS. 7A, 7B and 7C are respectively a view from above and side views in section of the concentrator of FIG. 5.
• Figures 8A and 8B are top and side sectional views of a concentrator according to another embodiment of the invention.
• Figure 9 is a perspective view (and in transparency) of another concentrator / float embodiment usable with the invention.
• FIG. 1 shows a device 1 for treating and conditioning liquid sludge 2, for example pumped by a pump 3, from a reservoir 4 for storing, for example, contaminated sludge, with a high organic content and therefore generating, in particular, ammonia ( NH3).
• a device 1 for treating and conditioning liquid sludge 2 for example pumped by a pump 3, from a reservoir 4 for storing, for example, contaminated sludge, with a high organic content and therefore generating, in particular, ammonia ( NH3).
• NH3 ammonia
• the device comprises a container 5 formed by a tubular column 6 of diameter d for example between 30 cm and 50 cm.
• the sludge is injected at a flow rate Q for example of 20m 3 / hr by a penetrating tube 7 (provided with static mixing means not shown as a helical screw) in a first zone 8 located in the lower part 9 of the column 6, of small volume for example 1.
• the volume of the zone 8 is delimited by the portion of the chamber situated in the volumetric extension of the end 10 of the penetrating pipe 7 and by the facing wall 11, for example cylindrical , and located 5 cm from said end 10.
• the device 1 also comprises a supply 12 of air 13 at a flow rate Q '(Nm 3 / h) of the chamber 6 for example below the sludge feed (tubing 7). But the air can also be fed against the flow of the mud flow, for example by means of an internal helical ramp 12 '.
• the value of the gas flow rates is conventionally given in Nm 3 / h (cubic norm-meter / h), the volume (in Nm 3 / h) being considered here at its value reported at a pressure of 1 bar , a temperature of 20 ° C and 0% humidity as is naturally admitted and understood by those skilled in the art, an engineer in the field of chemical engineering.
• the air is at an overpressure P 'with respect to the average internal pressure of the column 6 and is injected at a flow rate Q' much higher than the sludge flow rate, for example 500 Nm 3 / h.
• the meeting of the air and the mud creates a first emulsion of mud 14, with bursting of the mud (dispersed drops) in the air, which emulsion then rises in the column of total height H, in a second zone 16 of a first length Li before reaching the top 17 of the column which comprises an output member 18, for example a valve and / or a control valve allowing a permanent overpressure of the first emulsion inside the enclosure, for example at an average pressure P of the order of 1.5 bar absolute, with a ⁇ between the bottom 9 and the top 17 of the column of a few millibars.
• the device 1 also comprises a tubular enclosure 19 for example of diameter such that 1 ⁇ 2 d ⁇ d ⁇ d evacuation of the first emulsion on a second determined length L2 by example of 3 m.
• the device 1 comprises means 21 known per se (dosing pump, preparation container, etc.) for introducing into the chamber 19, a flocculant 22, located for example near the enclosure (for example 5 cm from the member 18), for example formed by a polymer of known type, adapted by the skilled person depending on the treated sludge.
• the tubular enclosure allows a flow initially overpressure then gravitational or substantially gravitational (slope a) once the atmosphere of the emulsion operated by the vent 20.
• a valve 24 may optionally regulate this venting.
• the emulsion 23 then falls into tanks, here filter bags 25, 25 'for recovering the dewatered sludge 26 which floats on the surface, the clear water 27 being recovered at the bottom.
• the mud slices 28 extracted from the bags are then stored and / or spread. Surprisingly, they do not smell or smell humus.
• the separated water benefited from the same physicochemical treatment as the mud.
• the air is not trapped there, but its redox potential has risen, the colloidal fractions being fixed at the MO leaving a transparent water, of charge in MES and very weak organic matter.
• a turbidity of 5 to 10 NTU is obtained whereas with a band filter a much more turbid water of 25 to 35 NTU is obtained.
• the filter is also less viscous than in the prior art, with equal initial sludge quality.
• a measurement of the CST gives here of the order of 5 s, whereas the prior art obtains on the order of 10 s.
• O2 / I for a biological sludge filter and less than 200 mg / l for a digested sludge filter (for a filter of the same sludge obtained with a conventional centrifuge of 1000 to 3000 mg0 2 / l), as well as a MES content ⁇ 50 ppm for more than 1000 ppm with the prior art under equivalent conditions.
• FIG. 2 shows another embodiment of a device 30 according to the invention for treating liquid sludge 31 introduced to an end portion 32 of an elongated container 33 around an axis 34 and of determined height H. for example 1 m.
• the container is maintained at an average pressure P for example of 2 bars absolute, and is formed by a cylinder of diameter d for example of 300 mm.
• the sludge feeds a reduced zone 35, for example 10 1 located at the end portion 32 also fed to the end of the container and upstream of the introduction of the sludge by an air inlet 36 for example at a pressure P P, for example 3 bar absolute.
• the air is fed at a very high flow rate Q 'for example 100 Nm 3 / h, the sludge being introduced at a flow rate Q for example of 10 m 3 / h.
• the sludge 31 bursts in the air which is under overpressure, a slight depression ⁇ existing between the container at the arrival of the sludge at 35 and the outlet of the sludge emulsion downstream 37 of the container.
• the device 30 further comprises a filter 48 and / or a settling tank for evacuation of the purified water 49 at the bottom and the dewatered sludge 50 at the top.
• FIG. 3 shows a third embodiment of a device 51 according to the invention.
• the device 51 comprises a container 52 fed by a stitching 53 in the lower part, in liquid slurry, and below this stitching 53, fed with high-flow compressed air by a second stitch 54.
• the gas stream stripping (stripping in the English language) of the gases contained and / or from the sludge and in particular ammonia NH3, surprisingly and depending on the operating conditions and conditions.
• treated organic sludge almost complete elimination of unwanted gases ( ⁇ a few ppm) trapped in sludge.
• the length 1 2 is advantageously dimensioned to do this by the skilled person.
• a control valve 61 and / or a valve is provided for evacuation towards a tubular enclosure 62.
• the section 66 is connected to the suspension material separation filter 69 of the liquid part 70, which is continuously emptied at 71, in a manner known per se.
• the enclosure comprises flocculant feed means 72 from a preparation tank 74 by mixing and stirring.
• a metering pump 75 feeds the flocculant into the sludge emulsion which exits the container 52 at the outlet of the valve 61, or in the immediate vicinity (ie a few cm) in a zone 76 which is quite disturbed due to the pressure drop. generated by said valve 61.
• a complementary air inlet 77 for example injected sequentially with the flocculant by the stitching 78, or in parallel.
• the emulsion 79 at the outlet of the treatment with the flocculant becomes an emulsion of air in the thickened flocculated sludge.
• the two sections 63 and 66 are for example cylindrical of the same diameter d 3 for example equal to the average diameter of the container for example di + d2.
• a polymer for example a cationic polymer, will preferably be used.
• Example for a sludge containing 7 g / l of MS, use is made of 50 g of crude polymer, for example prepared at 5 g / l or an injection of 10 1 of solution per m 3 of sludge. The injection takes place immediately out of the container column.
• the sludge is then evacuated for example by gravity via a pipe (not shown) stoved in a filter bag (not shown) and the thickened sludge being recovered for example by shoveling to form blocks thickened by a factor of 50, for example with respect to the liquid sludge at the inlet (x MS multiplied by 50 before draining into the filter bag).
• a shock enhancer may be added between the sludge particles. It can for example be used up to 10%, 5%, 1% of the MS rate of the sludge, as seen previously.
• This reagent is, for example, sand, calcium carbonate, slaked lime, etc. It is introduced upstream of the column, for example into a mixing tank with the liquid slurry (not shown).
• Oxidation reagents can also be provided.
• FIG. 4 shows a device 80 for treating sludge 81 injected by a pump 82 into an in-line container 83.
• the container 83 comprises a first zone 84 of small volume ( ⁇ 50 1) formed by a first chamber 85, for example parallelepipedal or cylindrical into which is injected on the one hand the mud for example in the lower part at a flow rate Q for instance 10 m 3 / h and the other compressed air or supercharged 86 from a blower 87 to a flow Q '(for example 100 Nm 3 / h) for example through two side connections 88 opposite, perpendicular to the flow of sludge to form a first air / sludge emulsion 89.
• a first zone 84 of small volume ( ⁇ 50 1) formed by a first chamber 85, for example parallelepipedal or cylindrical into which is injected on the one hand the mud for example in the lower part at a flow rate Q for instance 10 m 3 / h and the other compressed air or
• the chamber 85 is for example at a pressure P of 5 bar absolute and is connected by a tubing 90 of smaller section than that of the chamber, for example by half (thereby forming a restriction causing a pressure drop to a second zone 91 formed by a second chamber 92, of substantially cylindrical, oblong or tubular shape by example of larger section than the chamber 85, for example twice the length Li, in which the first emulsion 89 obtained by the air / sludge mixture is at a lower pressure P ', for example 4.5 bars absolute.
• the device comprises an enclosure 93 formed of a tube 94 terminated by a degassing chamber 95 provided with stirring means 96.
• the tube 94 comprises a restriction valve 97, making it possible to modify the pressure in the chamber between its upstream part and its downstream part and is provided with means 98 for injecting a flocculant known in themselves downstream of the restriction. 97, to form a second flocked emulsion 99 degassed in the chamber 95.
• the degassing chamber 95 is for example a cylindrical reservoir of sufficient volume to evacuate the excess air, and feeds gravitarily through an outlet pipe 100 a concentrator apparatus or capacity 101 which will serve as a float.
• the degassed emulsion 99 arrives at the lower intermediate portion 102 of the apparatus and immediately separates into solid material 103 which rises to the surface and to transparent water 104 which is discharged gravitarily at 105, continuously in a first tank 106 of tronco shape. -cylindrical.
• the solid material 103 is evacuated in the upper part of the concentrator / float 101 for example by a narrowed chute 107 which discharges the solid material 108 by pumping (pump 109) to a centrifuging unit 110, with additional decantation in an auxiliary tank 111, residual water in 112.
• the reservoir 106 of the apparatus 101 is advantageously of small size (but not necessarily), that is to say and for example of a volume corresponding to 1% of the volume of sludge conveyed per hour, for example 100 1 for 10 Nm 3 / h.
• the tank is closed by the chute 107 of reduced or narrowed section to maintain a slight overpressure above an absolute bar, for example 1.2 bar.
• a float with a surface area of 1 m2 and a total volume of 1 m3 is capable of handling between 10 and 13 m3 / h of sludge and 200 to 250 kg / h of MS and removing a slurry of 80 to 120 g / 1 from MS.
• the mud At the time of rising the mud at a density of 0.6 to 0.9.
• the porosity is stable and such that even after centrifugation at 110, for example at 3000 T / min, the mud keeps a porosity allowing it to float on the water.
• the sludge in the tank 106, and / or in the auxiliary tank 111 can be extracted by scraping, overflow, continuous pumping or batch process (here it is the overflow by the chute which is more particularly described).
• the concentration apparatus can also be a column, a simple or more complex vessel equipped with a system for recovering floats and an overflow as will now be described with reference to the following figures.
• the sludge flotation is indeed so effective (it is the size of the bubbles, due to flocculation on the emulsion, which allows it, in comparison with a conventional float that pressurizes the flotation air and does not allow a speed climbing as strong and a mud as consistent), that a thick cake is obtained.
• centrifugal machines and filter presses allow the centrifugal machines and filter presses to operate in their optimum performance range and consequently to greatly improve the dryness of the dewatered sludge by at least 5 to 6% or even 10%.
• FIGS. 5A, 5B and 5C show another embodiment of an effluent treatment device 113 according to the invention.
• the device 113 comprises a sludge feed, via a pipe 114 provided with a control valve 115 and a mixer 116, a small cylindrical chamber 117 (for example 36 1) in part lower.
• the chamber 117 is also powered by two connections 118 for supplying compressed air. It is connected at the top to a second chamber 119, via a junction tubing 120, said second chamber being cylindrical and of volume for example 500 1. It is terminated in the upper part by a tubular enclosure 121 provided with a venturi 122, the output of which are connected means 123 for feeding by flocculating.
• the tubular enclosure 121 forms a bend and feeds at the top a degassing apparatus or chamber 124, open at 125 at atmospheric pressure and connected in the lower part 126, for example frustoconical, via a gravity supply pipe 127, to the capacity or concentrator apparatus 128.
• the concentrator apparatus 128 will be described more specifically with reference to Figs. 7A-7C. It comprises, in addition to its feed in the lower part 129 by the flocculated emulsion from the degasser apparatus 124, an outlet pipe 130 of the thickened sludge and a pipe 131 for the output of the transparent water obtained.
• the concentrator apparatus according to the embodiment of the invention described here does not act as a conventional float insofar as the pressure of the reactor is not high enough and consequently the size of the bubbles of air is not in the micrometer range but millimeter.
• the observed rate of climb is then estimated to be greater than 50 m / h, reaching 100 m / h or even 200 m / h.
• the device according to the embodiment of the invention more particularly described here is allow to concentrate the digested output digested sludge, which can then be stored in a stirred sludge tank prior to centrifugation.
• the invention therefore opens perspectives of size reduction of the tools of filtration (typically centrifuge), limiting investments.
• Sludge consists of primary sludge and biostyr wash sludge (addition of FeC13 and multiflo polymer input);
• the invention thus makes it possible to obtain remarkable sludge concentration performances of 80 g / l to 100 g / l.
• the implemented device is also very compact.
• a device for treating 15 m3 / h of sludge has a footprint less than 10m2 a 50 m3 / h device will not exceed 20 m2.
• MBR sludge reactor biological membrane
• the invention shows here performances up to 90g / l from a slurry at 40 g / 1.
• Figure 6 shows another embodiment of a container 131 according to the invention.
• the first zone 132 of small volume here is the central portion 133 of a venturi 134 formed on the pipe 135 of mud supply, the air injections being made by two symmetrical pipes 136, injecting in the flow direction for example with an angle a between 20 ° and 90 °, for example 30 ° via frustoconical narrowing 137 pricking on the central portion 133.
• the second zone 138 of the container is here formed by a pipe portion 139 of the mud feed pipe 135, connected, for example through a diaphragm 140 to adjust the pressure P, to a larger cylindrical chamber 141.
• diameter for example ten times the diameter of the pipe 135, all of the first and second zones extending over a length L for example 1 m before emulsion exit obtained from the top of the chamber 141, via a junction stitching with a valve or valve (not shown).
• Figs. 7A to 7C show the concentrator apparatus 128 of Fig. 5.
• This comprises a cylindrical tank 128 provided with an emulsion inlet by the pipe 127, bent, centered inside the tank at a level corresponding to one third of the height of the tank.
• the pipe is bent at 90 ° and ends with a funnel outlet 152 flared upwards to allow the rise of sludge bubbles 153 which constitute a layer 154 of height h adjustable according to the flow rate.
• the sludge rises in the tank at a speed of the order of 50 m / s and flows into a conical central funnel 155.
• the upper face 156 of the tank is inverted cone open at its center 157 to allow air to escape and allow compression of the slurry 158 between the inner face 159 of the inverted cone and the upper edge 160 of the periphery of the cone. 'funnel.
• the sludge then flows into the funnel and is evacuated in the lower part for gravity via a bent tube 161 terminated by the tubular 130.
• the clear water 162 is evacuated in the lower part 163 of the tank via a vertical tube 164 allowing siphoning (arrow 165) and the outlet in the upper part by the turbulence 131.
• FIGS. 8A and 8B show another embodiment of a concentrator apparatus 166 that can be used according to a variant of the invention.
• It comprises a cylindrical tank 167 fed with mud 168 from above through a plunger pipe 169 and centered with an end 169 for example located at one third or one quarter of the height of the tank.
• a deflection plate 170 makes it possible to raise the sludge at high speed to form a slug 171 of sludge which exits at the top 172 of the vessel comprising an outlet end 173 in the form of a truncated cone, the sludge being evacuated by a spillway. along the peripheral edge 174 in a reservoir annular device 175 and via an outlet pipe 176 in the lower part of said annular reservoir.
• the water 177 which remains in the lower part is in turn evacuated via an outlet turbulence 178.
• FIG. 9 shows another embodiment of a concentrator apparatus 180 formed by a parallelepipedic tank 181 provided at its center with an internal parallelepipedal chamber 182 defining a space 183 between the internal walls of the tank 181 and external chambers 182.
• the sludge arrives at the middle portion 184 of the chamber, mounts by flotation creating a mud plug of constant thickness and flows over the periphery 185 of the chamber in the annular peripheral portion 183 between the walls of the chamber and the vessel. .
• Water is discharged at 189 through an outlet located in the upper part of a vertical collector channel 190, functioning as a siphon water column.
• the present invention is not limited to the embodiments more particularly described. On the contrary, it embraces all the variants and in particular those where several devices are used one after the other.

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• Chemical & Material Sciences (AREA)
• Engineering & Computer Science (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Life Sciences & Earth Sciences (AREA)
• Hydrology & Water Resources (AREA)
• Environmental & Geological Engineering (AREA)
• Water Supply & Treatment (AREA)
• Organic Chemistry (AREA)
• General Chemical & Material Sciences (AREA)
• Health & Medical Sciences (AREA)
• Toxicology (AREA)
• Mechanical Engineering (AREA)
• Treatment Of Sludge (AREA)
• Separation Of Suspended Particles By Flocculating Agents (AREA)
• Separation Of Solids By Using Liquids Or Pneumatic Power (AREA)
• Degasification And Air Bubble Elimination (AREA)

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• 2014
  • 2014-11-27 CA CA2931572A patent/CA2931572C/fr active Active
  • 2014-11-27 KR KR1020167016765A patent/KR102292428B1/ko active Active
  • 2014-11-27 WO PCT/FR2014/053063 patent/WO2015079175A1/fr not_active Ceased
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  • 2014-11-27 EP EP14814976.8A patent/EP3094393B8/fr active Active
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