• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    It is a method and a device for treating an organic effluent (2, 31). The effluent is supplied with a continuous flow at a flow rate q (m3 / h), via a first enclosure (5) maintained at a first determined pressure (P1), and / or directly through a first restriction (7), a second enclosure or vessel (10, 33, 55) maintained at a second average pressure (P2; P '; P1' '; P2' ') determined by injecting air (11, 31, 54) into said second enclosure at a flow rate Q (Nm3 / h), to obtain an emulsion (13, 57) in said second enclosure, a determined pressure drop is created in the optionally modified emulsion by a second and / or a third restriction or a valve ( 61) for supplying a third chamber (22, 39, 62) maintained at a determined third pressure (P3; P '; P3' ') in the zone (79) immediately downstream of said second or third restriction and / or valve (61) and a flocculant (24, 45, 78) is injected into said zone of the third enclosure, and then said emulsion is degassed atmospheric pressure and recovering the emulsion thus degassed in a filter device or decanting.
    公开号:FR3013701A1
    申请号:FR1361696
    申请日:2013-11-27
    公开日:2015-05-29
    发明作者:Patrice Capeau；Pascal Gendrot
    申请人:Orege SA；
    IPC主号:
    专利说明:

    [0001] The present invention relates to a process for the treatment of an organic effluent, and more particularly to the treatment, conditioning, coagulation, flocculation and oxidation of emulsions, water and organic effluents. strongly colloidal and / or liquid sludge, by bursting, dispersion and diffusion thereof within a gas under pressure. It also relates to a treatment device (conditioning, coagulation, flocculation and oxygenation) of emulsions, strongly colloidal waters and / or liquid sludges using such a process. The invention finds a particularly important, though not exclusive, application in the field of reducing the volume of organic or biological sludges for processing or subsequent use. Methods for separating solid matter in suspension from the liquid effluent in which it is present are already known. Existing techniques for extracting water from sludge are essentially compaction which increases the content (% by weight of the total mixture) to solid compound of the order of 5%, centrifugation or filtration which increases the solubility of the mixture. both the solid compound content of 18 to 25%, and finally the drying (by combustion or spreading for several weeks) which increases the solid content of 90 to 95%, and this knowing that the the weight content of solid compound of the sewage sludge before the treatment is generally between 0.1 to 1% of the total weight of the effluent. All these known treatments of the prior art have drawbacks, either related to the fact that desiccation is not sufficient (compaction, centrifugation, filtration) or related to the treatment time (drying) or the high energy consumption ( combustion).
    [0002] Also known (FR 2 175 897) is a sludge waste treatment method in which a sealed circuit comprising a vessel is supplied, a circuit in which it is recirculated for several tens of minutes by introducing an oxygen-containing gas into the circuit. upstream of the tank. The retention of the activated sludge in the tank for a period of time sufficient to allow supersaturation by the oxygen-containing gas is indicated as allowing substantial removal of suspended solids. Such a method, in addition to being long, implements a rather complicated device, source of many clogging. A method of collisional decolloiding of at least two flows opposite in a small chamber in which air is blown is also known. Although quite effective this process is essentially applicable to very mineralized sludge (ie having one% of organic material on 100% by weight of dry matter less than 5 to 15%). Also known (FR 2 966 818) is a method for separating liquid from slurry material in which slurry and high volume air are injected into a low volume enclosure. The process allows the separation of water bound to organic colloids. Such a method, however, does not allow the removal of certain elements contaminating organic sludge, for example loaded with ammonia. The drying of the sludge obtained with such treatment can also be improved, a gain would be only a% in dryness compared to the prior art resulting in significant savings in transport and disposal cost. Thus, for users of sludge treatment plant, the return on investment in operating cost justifies very quickly a small improvement. The present invention aims to provide a method and a device which better than those previously known to the requirements of the practice, in particular in that it will allow improved dehydration, in particular when it is used in combination with techniques known centrifugation or pressing / filtration, and while allowing a better decontamination of sludge including ammonia loaded, very quickly, the use of the method according to the invention requiring only a few seconds or minutes before obtaining 'a result. In particular, this process makes it possible to obtain excellent results for very organic sludges, that is to say essentially charged with phospholipids, polysaccharides, bacterial residues, volatile fatty acids, etc. It is also possible to obtain optimized efficiency when combined with a complementary separation tool disposed downstream of the device (band filter or centrifugation), improving more than 10% desiccation, for example by 25%. With the invention, the existing installations can be easily improved, and this at low cost due to a low power consumption and the reasonable use in quantity of the utilities used (compressed air, reagent_). In addition, the method uses a simple device 15 whose continuous operation has few operating constraints, unlike devices of the prior art such as centrifuges for example. The invention also makes it possible to obtain a solid residue, in the form of a dehydrated porous slab, without odor, or with a humus odor, which is particularly easy to reuse and / or to spread. For this purpose, the invention notably proposes a method for treating an organic effluent, characterized in that it feeds with said effluent in a continuous flow at a flow rate q (m3 / h), via a first chamber or container maintained at a first determined pressure, and / or directly through a first restriction, a second chamber maintained at a second determined average pressure by injecting air into said second chamber at a flow rate Q (Nm3 / h), for to obtain an emulsion in said second chamber, a determined pressure drop in the (optionally modified) emulsion is created by a second and / or a third supply restriction of a third chamber maintained at a determined third pressure in the zone located immediately downstream of said second or third restriction or the valve, and a flocculant is injected into said zone of the third chamber, and then said emulsion is degassed. atmospheric pressure and the emulsion 10 thus degassed is recovered, after filtration and / or decantation in the form of a thickened sludge. By mean pressure is meant a mean pressure on the volume of the enclosure. Thus the injection of air into the stream of the effluent itself introduced with a restriction causing a loss of charge, creates a violent suction of the air flow passage. In the main part of the device, the emulsion is mud (dispersed phase) in the air (continuous phase) which coats it. In the presence of a slight depression, there is a very good dispersion of the sludge in the gas bed, knowing that the passage through the restriction zones the pressure is locally strong and can lead to a reversal of the proportions. In these zones, the pressure rises and the air penetrates better the mud, thus probably accentuating the exceptional porosity effect observed with the invention. Thanks to these phenomena of emulsion and / or inversion of emulsions, the air comes into contact with the sludge intimately, the flocculation freezing the air / water pair in a manner favorable to the deodorization, the flotation of the flocs. of sludge and their dehydration. It has thus been possible to observe a high porosity of the sludge flocs with millimetric bubbles (from 1 to 5 mm) whereas, during a conventional flotation, micrometric bubbles are created and serve as a surface-active medium for the organic matter. In these known cases, the material rises to the surface at a speed of a few meters per hour, causing the bubbles to burst on the surface of the float possibly allowing the flocs to fall in the middle zone and then at the bottom of the tank, the mud having a density slightly higher than water. With the invention, the flocs themselves have a much lower density than water (mud density of 0.6 to 0.9 g / cm 3). This very specific characteristic allows the sludge to have a high quality of flotation, carried out with an improved speed which makes perennial phase separation. According to one embodiment, means for providing shocks / dispersion in the gaseous fluidized bed are provided. For example, each enclosure is embellished with simple hydraulic systems such as walls perpendicular to the flow, spring systems of the raschig rings, etc. Advantageously, the effluent is introduced into a small enclosure (first or second enclosure), corresponding for example to a volume of 0.5% of the volume of effluent passed per hour, (flow rate) ie 50 1 for 10m3 / h of sludge, for example 30 1, or even less than or equal to 5 1. This allows a loss sudden charge in the mud flow for example fed by pumps of 10 bar of water height. This first enclosure (or the second enclosure) is for example closed by a reduced outlet forming 5 venturi, to maintain it at an overpressure 4 bar absolute, for example 5 bar absolute. The outlet of the first chamber is therefore effected by a first and / or second restriction favorable to the penetration of air into the effluent, injected downstream of the restriction, for example at 10 Nm 3 / h in the second pregnant. Downstream, more or less immediate of this first restriction a second restriction at the head of a third enclosure and / or a third restriction at the head of a fourth enclosure are for example provided. According to the embodiment of the invention more particularly described here, and downstream more or less immediate of this second restriction (some 20 centimeters, 1 m or a few meters) it is also injected a flocculant that can trap micro bubbles and millimeters in contact with the suspended material. A very interesting phenomenon of immediate sludge flotation then occurs with a rate of rise of 50 or even 100 and more m / h. In comparison, conventional sludge flotation techniques allow a climbing speed of 2 to 6 m / h. This unexpected phenomenon makes it possible to constitute a self-draining material from colloidal sludge.
    [0003] In advantageous embodiments, one and / or more of the following provisions are additionally and / or in addition: the first chamber is of volume less than 5,300 cm 3, or even 30 l first pressure being between 4 and 10 bar absolute, the flow q being between 5 m3 / h and 30 m3 / h, the second pressure being between 1.2 bar and 4 bar absolute, the air flow Q being understood between 5 Nm3 / h and 200 10 Nm3 / h, and the third pressure being between 1.05 bar and 2 bar absolute; an intermediate chamber is emulsified between the second and third chambers; A second injection of air is injected downstream of the first injection into said intermediate chamber, situated between the second and third chambers at a flow rate Q 'for example between 50 and 200 Nm3 / h or more (ie> 200 Nm3 / h for example 500 Nm3 / h or 1000 Nm3 / h); the first, second and / or third restrictions are formed by venturis; the second enclosure is a column of average diameter d and of height H> 10 d, for example a column> 2 m, for example 3 m, for example 5 ill; the flocculant is a polymer injected at the immediate exit (a few centimeters, for example between 5 cm and 10 cm) from the second or third restriction; a part of the flocculated emulsion is recycled to the first chamber, for example in 1 / 10th and 1 / 5th of the flow rate or between 5% and 30% of the sludge volume output from the device, for example 10% or 20%. This makes it possible to lower the overall consumption of polymer; the sludge is treated downstream of the tubular chamber by centrifugation, filtration and / or pressing; - The injected air can be heated. The invention also proposes a device implementing the method as described above. It also relates to a device which comprises means for supplying effluent (for example slurries) in continuous flow at a flow rate q, via a first chamber maintained at a first predetermined pressure, and / or directly through a 15 first restriction, a second chamber maintained at a second predetermined pressure, air injection means in said second chamber at a flow rate Q (Nm3 / h), to obtain an air / effluent emulsion in said second chamber, 20 a second restriction arranged to create a determined pressure drop in the emulsion and a third chamber maintained at a determined third pressure in the zone immediately downstream from said second restriction and means for injecting a flocculant into said zone of the third enclosure, means for degassing said emulsion at atmospheric pressure and means for recovering the emulsion thus degassed in a device filtration or decantation. Advantageously, it further comprises an intermediate chamber between the second and third enclosures and means for injecting air downstream of the first injection into said intermediate enclosure. Also advantageously the first and second restrictions are formed by venturis.
    [0004] In another advantageous embodiment the second enclosure is a column of average diameter d and height H> 10 d. Alternatively, a shock enhancer may be added between the sludge particles. For example, it can be used up to 10%, 5%, 1% of the MS content of the sludge. 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). Oxygenation reagents can also be provided. The invention will be better understood on reading the following description of embodiments given hereinafter by way of non-limiting examples. The description refers to the accompanying drawings in which: Figure 1 is a block diagram of a device according to the embodiment of the invention more particularly described herein. Figure 2 is an embodiment of another device according to the invention. Figure 3 shows another embodiment of a device according to the invention. FIG. 1 schematically shows a sludge thickener device 2 sucked by means 3 (pump) from a reservoir or storage tank 4. The device 1 comprises a first small volume enclosure 5, for example cylindrical or cubic, 5 for example of volume 10 1, liquid slurry receiving, for example at a first determined pressure P1 slightly lower than the pressure Po output of the feed pump 3, due to the pressure drops of the supply circuit 6 (flexible tube 10 for example). The flow rate q of the pump is for example between 5 m 3 / h and 50 m 3 / h for example 10 m 3 / h, and the first determined pressure P 1 is 2 bars absolute, Po being for example 2.2 bars absolute. The enclosure 5 comprises at its outlet a restriction 7, for example formed by a round orifice or nozzle 8, for example of diameter 2 cm, in an intermediate wall 9, of separation with a second enclosure 10, of greater volume. , for example 200 1. The second chamber 10, for example cylindrical, is at a second pressure P2 (for example 1.8 bar absolute) and is fed for example in the lower part by air 11 with a very high flow rate. 500 Nm3 / h, and a pressure of several bars, for example 5 bars creating in the chamber 12 formed by the enclosure an emulsion 13 of mud droplets 14 which is evacuated via a second similar restriction 15 or the same as restriction 7. The injection of air into the emulsion just after the introduction of the sludge into the chamber facilitates the mixing which takes place in the accelerating portion after the nozzle (air ejector effect ).
    [0005] The second restriction 15 opens on an intermediate chamber 18, for example of larger volume, for example 500 1, formed by a cylinder 19 whose interior is at a third pressure P3, for example 1.6 bar absolute. A second air injection 20 in the lower part of this intermediate chamber further increases the parcelling or dilution of the sludge in the air, the injection being done for example at a flow rate Q 'of 200 Nm3 / h, with for example 50 Nm3 / h <Q '<Q. As for the intermediate enclosure 18, in the embodiment described here, via a third restriction or nozzle 21, a third enclosure 22, also cylindrical, for example with a height of 3 m, at a fourth decreasing P4 pressure of the inlet of the enclosure in 23 to 1.2 bar to the atmospheric pressure in the upper part. The fourth enclosure comprises a flocculant feed 24 (for example a known polymer) at a flow rate q ', for example a function of the type and flow rate of the sludge, which may be appreciated by those skilled in the art in a manner known per se. to obtain good flocculation. The sludge is then discharged, for example, gravitarily via a pipe 25 vented in a filter bag 26, the purified water 27 being discharged downwards and the thickened sludge being recovered for example by shoveling to form thickened blocks 29, for example by a factor of 20 with respect to the liquid slurry 2 at the inlet (T of MS multiplied by 20 before draining into the filter bag).
    [0006] FIG. 2 shows another embodiment of a device 30 for treating liquid sludge 31 introduced at an end portion 32 of a container 33 that is elongate about an axis 34 and of a 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 150 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 2 absolute bars.
    [0007] The air is fed at a very high flow rate Q 'for example 100 Nm3 / h, the sludge being introduced at a flow rate Q for example 10 m3 / h. The sludge 31 bursts in the air which is under overpressure, a slight low pressure AP existing between the container at the arrival of the sludge at 35 and the outlet of the sludge emulsion downstream 37 of the container. At the outlet of the container 33 there is a venturi 38 and / or a control valve generating a pressure drop, for example 0.4 bar, the sludge emulsion being here discharged in a tubular enclosure 39 comprising a first cylindrical portion 40 of diameter of (for example d '= d) which is at a pressure P'1 <P', for example here of 1.6 bars (in the example taken), in which can be injected, downstream of the venturi and close to it (for example to 10 cm to allow a good mixing), a reagent at 41, and / or air again (tapping 42).
    [0008] In this embodiment, the tubular enclosure also comprises a second cylindrical portion 43, separated from the first portion 40 by a second venturi 44, said second portion being of diameter d "with for example d = d = d. Downstream of the venturi 44, and close to it (1 to 10 cm) is provided a supply 45 flocculant, with means known in themselves (dosing pump etc ...), and a vent 46 of in the atmosphere and / or an outlet 47 of mud open to the atmosphere, the pressure P'2 in this second part is therefore very rapidly brought to atmospheric pressure, for example 1.3 bar at the outlet of the venturi for move rapidly to 1 bar = 1 atmosphere at exit 47, the emulsion becoming after the addition of flocculant an emulsion of air in the flakes of sludge, which flow gravitarily on the end. The total length of the enclosure L2 '^ -' 11 + 12, for example is 10 m, with 11 = 3 m and 12 = 7 m, but other values are possible, the proportion between 11 and 12 being in Generally, but not exclusively, such as 11 <12. The device 30 further comprises a filter 48 and / or a settling tank for evacuation of purified water 49 at the bottom and 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 at the bottom, in liquid slurry, and below this stitching 53, supplied with high-flow compressed air by a second stitch 54.
    [0009] More specifically, the container is formed by a vertical column 55 comprising a first part forming a tank 56 for mixing / stirring very violent air and mud, small for example cylindrical height hl = 50 cm and diameter d1 30 cm is a volume of the order of 35 1, to obtain the first emulsion 57 of droplets 58 of broken mud. This emulsion of drops in a strong upward flow of air under pressure then enters a cylindrical pipe 59, extending the reservoir 56, of smaller diameter d2 <d1 for example of 10 cm in diameter and which extends over a length h2 for example 1 m (with L1 = hl + h2).
    [0010] In this air column, 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 12 is advantageously dimensioned for this purpose by those skilled in the art.
    [0011] At the top 60 of the enclosure, a regulating valve 61 and / or a valve is provided for evacuation towards a tubular enclosure 62. The pressure of the emulsion 57 changes from Pi "(for example 3 bars) into the reservoir initial 56, P2 "(2,890 bar) slightly lower than P1 in the upper part of the column 59 of the container, at the valve 61, with OP" = P2 "- Plrr = a few millibars, then at the exit of the valve P3 "= 2 bars (due to the pressure drop of the valve) .more precisely the enclosure 62 comprises a first section 63 of length 13 for example 5 m, which ends with a venturi 64 passing the pressure P3 "'<P3" at the end 65 of the first section at a pressure P4 "in a second section 66 of the granite slope enclosure, provided with a vent 67, the section 66 being of length 14, for example 1 m , with L2 = 13+ 14. The section 66 is connected to the suspension material separation filter 69 of the liquid part 70, which is emptied in the opposite direction. inu in 71, in a manner known in itself.
    [0012] According to the invention the enclosure comprises flocculant feed means 72 from a preparation tank 74 by mixing and mixing. 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. P3 "is here and for example increased from P2" 2 bar to P3 "= 1.4 bar, P4" being meanwhile at atmospheric pressure, or substantially at atmospheric pressure because of the vent 67. In this embodiment, it has also been provided a complementary air inlet 77, injected for example 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.
    [0013] The two sections 63 and 66 are for example cylindrical of the same diameter d3 for example equal to the average diameter of the container for example d1 + d2. 2 For 10 m3 / h of liquid sludge, an air flow of at least 60 Nm3 / h, whatever the mode of injection, the container having a section of 200 mm for a height of 5 m, 10 m , 30 m or more, we observe a stripping effect (in Anglo-Saxon language) (pulling trapped gases) very strong, the air being intimately mixed with the mud. As regards the flocculant, a polymer, for example a cationic polymer, will preferably be used. Example, for a sludge containing 7 g / l of MS, 50 g of crude polymer is used, for example prepared at 5 g / l, ie an injection of 10 l of solution per m 3 of sludge. The injection takes place immediately out of the container column. Alternatively, a shock-improving reagent can 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. In some applications, for example when the sludge contains a lot of organic fatty acids or that these sludge is sludge from the methanizer, excellent results are indeed observed.
    [0014] For example in proportions of 1 1 of H 2 O 2 or 1 1 of S 2 O 8 per 1 m 3 of sludge containing 40 g / l of MS. There may also be a supply of reagent for the coagulation of complementary organic materials. For example, for a slurry of 11 g / l of MS and 8% of MV (Volatile matter is organic matter / dry matter) (about organic matter / dry matter ( )) And for 500 ml of sludge, it is brought 1 ml of FeCl 3 (10% solution) either at the introduction of the liquid into the column or before the introduction of flocculant (after column). By way of example, tests were carried out on biological sludge with a band filter, from sludge 15 charged with 26 to 30 g / l in MS with: Q '= 50 to 80 Nm3 / h P = 1.7 bar pressure of the container / reactor Q = 3 to 15 m 3 / h At the exit of the process, dry porous sludge is obtained with accelerated drying and a dryness of 25 to 35%. It is thus observed that, surprisingly and simply by decantation, the water allows its untied water to evacuate directly gravity. The sludge then dries progressively from 100 g / l DM after the first hour to 130 g / l after 2 h, 160 g / l after 5 h, 350 g / 1 after 1 month. (big bag). Other examples of treatment according to the method used, by recovery on filtering bucket or filter bags (big bag in the English language) give: Filter dump; Ex 2: 130 g / l after 20h and 180 g / l after 8 days Filter tipper; Ex 3: 100 g / l after 5 h, 130 g / l after 7 d.
    [0015] Big bag; Ex 4: 100 g / l after 24 h, 115 g / l after 7 d and 221 g / l after 1 month. Big bag; Ex 5: 144 g / l after 24 h, 154 g / l after 7 d and 459 g / l after 1 month. Big bag; Ex 4: 120 g / 1 after 24h (when it rained all night) and 402 g / 1 after 1 month. Note that the sludge treated according to the invention is initially liquid. Up to 30 g / 1 dilution is not required a priori. But if the sludge is denser, for example above 40 g / 1, it will be possible to dilute the inlet of the device to allow proper operation of the pumping of the sludge, which is remembered as an organic sludge, c that is to say the rate of MO (Organic Matter) on the rate of MS (Suspended Material) is between 65% and 85%. By organic material is meant essentially phospholipids, polysaccharides, proteins, alkalis, alkaline earth metals and / or metals etc. Hereinafter another example of operation is given, this time with reference to the simplified FIG. gets rid of the first portion of the speaker). Container 33 forms a first tube-shaped chamber 20 cm in diameter and 50 cm in length, into which a flow rate of Q = 10 m 3 / h is introduced into an organic sludge (from a station clarifier). communal purification) at 6 g / l of MS and compressed air at 50 Nm3 / h of air at 1.9 bar with a booster. A 5 cm2 orifice closes this chamber for a length of 10 cm.
    [0016] Immediately downstream from it, a flocculant is introduced into the chamber 43, for example dosed at 10 g / l. The pressure post orifice drops gradually to reach the atmosphere after a few meters. For example: the chamber 43 which forms a post-orifice chamber 10 is also a pipe 3 m long and 20 cm in diameter. At the end of the enclosure, all of the flows join, for example, a filter bag (filter 50) at the cut-off point of 500 μm immediately giving a dryness of 10% (or 100 g / l) and a clear filtrate. in 49 of 50 mg of oxygen (O 2) per liter (COD). The reactants are introduced by liquid metering pumps. Conventionally, the more concentrated the sludge, the more the reagents must be prepared diluted. The output of the device is carried out in the atmosphere. But the venting may optionally be regulated in one embodiment of the invention, so as to recover the pressure of the downstream separation apparatus. Downstream devices are classic. It is found that their effectiveness on dehydration is improved by at least 3%, for example for a centrifuge which gives a result of 23% dryness or 230 g / l of MS, the device placed upstream can reach in fine at least 26% dryness is 260 g / 1 DM. Downstream devices are: - Filter bags (100, 300, 500 μm or more) open or closed - Floats - Mechanical thickeners - Screw presses - Band filters - Centrifuges - Press filters At the outlet, the sludge can of course 10 to be used on the ground, without or after composting, alone or with green or other wastes. They can also be dried on single or solar drying beds. It is interesting to note that the sludge obtained is "non-odorous" and does not ferment over time (anaerobic fermentation). In fact, the enormous dilution with air allows the sludge to have a high dehydration power, due to the presence of air bubbles. The results obtained with the device 1 according to the invention were given below in Tables I, II, III, combined downstream with indicated apparatus, at different sludge rates. TABLE I: Device + band filter Siccité test Flow rate Flow rate Pressing Salt capacity Remarks Length Air slurry P outlet L2 sludge inlet Nm3 / h bar filter device M3 / h 2 10 7.8 80 1, 7 14 Diluted slurry 6m 3 10 7.8 95 1.2 16.5 Diluted slurry 3m TABLE II: Device 1 + big bag Test Type of test Date of test Immediate Siccity Siccity at A 1 month 1 d TO Indicator without device only big bag filter 05 / 04 8% 10% 22% TESTS 10 Device Mid-April 10 to 11% 14.5 to 45.9% DAYS + big filter bag 15.5% 53.5% Flow rate from 3 to 12 m3 / h It can be seen that thanks to an optimized concentration of sludge obtained with the invention, for example from 70 to 130 g / l of MS, it will very favorably maximize the dehydration function by tools such as centrifuges or a filter press, allowing significantly improve their performance. Indeed, the untied water has been extracted by the method described above, this can almost always improve at least 100 g / 1, the rate of MS sludge output.
    [0017] As is obvious and as also follows from the above, the present invention is not limited to the embodiments more particularly described. On the contrary, it encompasses all the variants and in particular those in which the number of portions and / or sections of enclosure is different, for example greater than three, or the container is horizontal with only one section.
    权利要求:
    Claims (12)
    [0001]
    REVENDICATIONS1. Process for the treatment of an organic effluent (2, 31), characterized in that it feeds with said effluent in a continuous flow at a flow rate q (m3 / h), via a first chamber (5) maintained at a first determined pressure (P1), and / or directly through a first restriction (7), a second chamber or container (10, 33, 55) held at a second mean pressure (P2; P '; Pl "; P2") determined by injecting air (11, 31, 54) into said second chamber at a flow rate Q (Nm3 / h), to obtain an emulsion (13, 57) in said second enclosure, a determined pressure drop 15 is created. in the emulsion optionally modified with a second and / or third restriction or a valve (61) for supplying a third chamber (22, 39, 62) maintained at a determined third pressure (P3; P '; P3 " ) in the zone (79) immediately downstream of said second or third restriction and / or valve (61) and injecting a floc lant (24, 45, 78) in said zone of the third chamber, then said emulsion is degassed at atmospheric pressure and the emulsion thus degassed is recovered in a filtration or decanting device.
    [0002]
    2. Method according to claim 1, characterized in that the first chamber (7) is of volume less than 3200 cm3, the first pressure being between 4 and 10 bar absolute, in that the flow q is between 5 m3 the second pressure (P2, P ', Pi ", P2") is between 1.2 bar and 4 bar absolute, the air flow rate being between 5 Nm3 / h and 200 Nm3 / h, and the third pressure (P3; P '; P3 ") is between 1.05 bar and 2 bar absolute.
    [0003]
    3. Method according to any one of the preceding claims, characterized in that emulsified feeds an intermediate chamber (18, 40) between the second (10, 33) and third enclosures (22, 43).
    [0004]
    4. Method according to any one of the preceding claims, characterized in that a second injection of air downstream of the first injection into an intermediate chamber located between the second and the third chamber at a flow Q '.
    [0005]
    5. Method according to any one of the preceding claims, characterized in that the first, second and / or third restrictions (7, 38, 21, 44) are formed by venturis.
    [0006]
    6. Method according to any one of the preceding claims, characterized in that the second enclosure or container (10, 33) is a column of average diameter d and height H> 10 d.
    [0007]
    7. Process according to any one of the preceding claims, characterized in that the flocculant is a polymer injected at the immediate outlet of the valve (61) of the second (44) or third (21) restriction.
    [0008]
    8. Method according to any one of the preceding claims, characterized in that a part of the flocculated emulsion is recycled into the first chamber.
    [0009]
    9. Device (1) for continuous treatment of a sludge (2), characterized in that it comprisesmeans (3) for supplying said continuous flow sludge at a flow rate q, via a first enclosure (5) maintained at a first determined pressure, and / or directly through a first restriction (7), a second chamber or container (10, 33, 55) maintained at a second predetermined pressure, means for injecting air into said second enclosure at a flow rate Q, to obtain an emulsion in said second enclosure, a second restriction or a third restriction (21, 44), or a valve (61) arranged to create a determined pressure drop in the emulsion and a third enclosure (22, 39, 62) maintained at a determined third pressure in the zone immediately downstream of said second restriction and means for injecting a flocculant (24, 45, 78) into said zone of the third enclosure, means (46, 66) for degassing ladit emulsion at atmospheric pressure and means for recovering the emulsion thus degassed in a device (26, 48, 68) for filtration or decantation.
    [0010]
    10. Device according to claim 9, characterized in that it further comprises an intermediate chamber (18, 40) between the second (10, 33) and third (22, 43) enclosures and air injection means (20, 42) downstream of the first injection into said intermediate enclosure.
    [0011]
    11. Device according to any one of claims 9 and 10, characterized in that the first, second and / or third restrictions are formed by venturis.
    [0012]
    12. Device according to any one of claims 9 to 11, characterized in that the second chamber (10) is a column of average diameter d and height H> 10 d.
    类似技术:
    公开号 | 公开日 | 专利标题
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    同族专利:
    公开号 | 公开日
    US9908802B2|2018-03-06|
    AR098536A1|2016-06-01|
    MA39050B1|2017-07-31|
    IL245791D0|2016-07-31|
    EP3094394B8|2018-06-13|
    CN106457074A|2017-02-22|
    CA2931574C|2021-10-26|
    PH12016500986A1|2016-06-20|
    SG11201604204UA|2016-07-28|
    FR3013701B1|2017-07-21|
    ES2664848T3|2018-04-23|
    NO3094394T3|2018-06-09|
    MY179737A|2020-11-12|
    AU2014356279B2|2018-10-04|
    HUE037223T2|2018-08-28|
    JP2016538124A|2016-12-08|
    EA033771B1|2019-11-25|
    HRP20180510T1|2018-05-04|
    EP3094394A1|2016-11-23|
    KR20160088430A|2016-07-25|
    MA39050A1|2016-11-30|
    US20160376182A1|2016-12-29|
    SI3094394T1|2018-06-29|
    CA2931574A1|2015-06-04|
    WO2015079177A1|2015-06-04|
    AU2014356279C1|2019-01-31|
    AU2014356279A1|2016-06-09|
    TN2016000193A1|2017-10-06|
    PL3094394T3|2018-07-31|
    RS57031B1|2018-05-31|
    ZA201603426B|2019-03-27|
    MX2016006682A|2017-01-16|
    EP3094394B1|2018-01-10|
    CN106457074B|2019-01-04|
    KR102307272B1|2021-09-29|
    DK3094394T3|2018-04-23|
    EA201600351A1|2017-08-31|
    JP6514207B2|2019-05-15|
    引用文献:
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    KR100581752B1|2003-05-07|2006-05-22|한상배|The Aerators with the Functions of Mixing, Aeration, Intermittent Aeration and Advanced Waste Water Treatment Methods with using these Aerators|
    CN1258485C|2003-12-23|2006-06-07|清华大学|Process for treating waste water by aerobic-anaerobic microbic repeated coupling|FR3052450B1|2016-06-08|2020-01-10|Veolia Water Solutions & Technologies Support|IMPROVED PROCESS FOR DEHYDRATION OF SLUDGE ASSISTED BY FLOCCULATING REAGENT AND PLANT FOR THE IMPLEMENTATION OF SUCH A PROCESS.|
    CN110545890B|2017-04-17|2022-02-01|切弗朗菲利浦化学公司|System and method for treating reactor polymerization effluent|
    CN109775873A|2019-01-28|2019-05-21|农业部环境保护科研监测所|A kind of jet-flow aeration sewage-treatment plant|
    CN110590106A|2019-09-20|2019-12-20|青海天普伟业环保科技有限公司|Sludge advanced treatment equipment and use method thereof|
    法律状态:
    2015-11-18| PLFP| Fee payment|Year of fee payment: 3 |
    2016-11-09| PLFP| Fee payment|Year of fee payment: 4 |
    2017-11-08| PLFP| Fee payment|Year of fee payment: 5 |
    2018-11-06| PLFP| Fee payment|Year of fee payment: 6 |
    2019-11-04| PLFP| Fee payment|Year of fee payment: 7 |
    2021-08-06| ST| Notification of lapse|Effective date: 20210705 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1361696A|FR3013701B1|2013-11-27|2013-11-27|METHOD AND DIPSOSITIVE FOR TREATING AN ORGANIC EFFLUENT|FR1361696A| FR3013701B1|2013-11-27|2013-11-27|METHOD AND DIPSOSITIVE FOR TREATING AN ORGANIC EFFLUENT|
    ARP140104421A| AR098536A1|2013-11-27|2014-11-26|PROCEDURE AND TREATMENT DEVICE OF AN ORGANIC EFFLUENT|
    DK14814979.2T| DK3094394T3|2013-11-27|2014-11-27|Process and device for treating organic sludge|
    SG11201604204UA| SG11201604204UA|2013-11-27|2014-11-27|Method and device for treating an organic effluent|
    EA201600351A| EA033771B1|2013-11-27|2014-11-27|Method and device for treating organic effluents|
    MA39050A| MA39050B1|2013-11-27|2014-11-27|Process and device for treating an organic effluent|
    KR1020167016764A| KR102307272B1|2013-11-27|2014-11-27|Method and device for treating an organic effluent|
    ES14814979.2T| ES2664848T3|2013-11-27|2014-11-27|Procedure and device for treating an organic sludge|
    RS20180348A| RS57031B1|2013-11-27|2014-11-27|Method and device for treating an organic sludge|
    MX2016006682A| MX2016006682A|2013-11-27|2014-11-27|Method and device for treating an organic effluent.|
    AU2014356279A| AU2014356279C1|2013-11-27|2014-11-27|Method and device for treating an organic effluent|
    NO14814979A| NO3094394T3|2013-11-27|2014-11-27|
    CA2931574A| CA2931574C|2013-11-27|2014-11-27|Method and device for treating an organic effluent|
    PCT/FR2014/053066| WO2015079177A1|2013-11-27|2014-11-27|Method and device for treating an organic effluent|
    PL14814979T| PL3094394T3|2013-11-27|2014-11-27|Method and device for treating an organic sludge|
    JP2016534650A| JP6514207B2|2013-11-27|2014-11-27|Method and apparatus for organic wastewater treatment|
    TN2016000193A| TN2016000193A1|2013-11-27|2014-11-27|METHOD AND DEVICE FOR TREATING AN ORGANIC EFFLUENT|
    MYPI2016701903A| MY179737A|2013-11-27|2014-11-27|Method and device for treating an organic sludge|
    EP14814979.2A| EP3094394B8|2013-11-27|2014-11-27|Method and device for treating an organic sludge|
    CN201480065255.4A| CN106457074B|2013-11-27|2014-11-27|The processing method and equipment of organic emission|
    US15/039,832| US9908802B2|2013-11-27|2014-11-27|Method and device for treating an organic effluent|
    HUE14814979A| HUE037223T2|2013-11-27|2014-11-27|Method and device for treating an organic sludge|
    SI201430617T| SI3094394T1|2013-11-27|2014-11-27|Method and device for treating an organic sludge|
    ZA2016/03426A| ZA201603426B|2013-11-27|2016-05-19|Method and device for treating an organic effluent|
    IL245791A| IL245791D0|2013-11-27|2016-05-23|Method and device for treating an organic effluent|
    PH12016500986A| PH12016500986A1|2013-11-27|2016-05-26|Method and device for treating an organic effluent|
    HRP20180510TT| HRP20180510T1|2013-11-27|2018-03-27|Method and device for treating an organic sludge|
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