• 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:
    Procedure and plant for slurry treatment. The present invention concerns a method for treatment of slurry comprising three successive stages of filtering and separation of solid particles, the latter being an electrocoagulation stage, and subsequent pelletization of the obtained solid fraction mixed with lignocellulosic or ligneous materials, the stage being of filtering and intermediate separation a physical-chemical separation stage by means of a coagulant and flocculant supply, in aqueous dispersion and by a subsequent separation of an ultra-fine solid fraction by means of a centrifuge equipment. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2626598A1
    申请号:ES201600326
    申请日:2016-04-12
    公开日:2017-07-25
    发明作者:José Luis ZARRALANGA PETRIZ；Ignacio TOBARUELA DELGADO
    申请人:Instr Financieros Y Economicos Soc Ltda；Instrumentos Financieros Y Economicos Ltda Soc；
    IPC主号:
    专利说明:

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    DESCRIPTION
    Procedure and plant for treatment of slurry.
    Technique Field
    The invention is part of the technical sector of the treatment of animal slurry in particular of pig purln, for the valorization of waste from farms in the agro-livestock industry, by eliminating a significant proportion of nitrogen compounds, eliminating greenhouse gases ( CO2, CH4), and elimination of other contaminants in the form of gas (NH3, NH4, NOx) that cause odors and the use of the resulting residue in the form of combustible biomass.
    The invention also refers to a plant for the treatment of pig manure, where the said treatment procedure is implemented.
    State of the art
    Various backgrounds are known that propose the use of pig manure as organic fertilizer, together with purified water for various purposes, which is a benefit for farmers and agricultural land. However, a problem arises in the so-called areas of high concentration of pig farms, where there is not enough agricultural land nearby for an adequate recovery of pig manure as fertilizer.
    To reduce the polluting load of the liquid agricultural waste, oxidation techniques are applied (electro-oxidation, ozone, hydrogen peroxide or electro-deionization with appreciable energy consumption, or evaporation, so that a part of the dissolved gases escapes the uncontrolled atmosphere, maintaining significant emission levels if additional recovery systems are not included.
    From US 7156999 (B2), a mop is known for treating animal purln comprising a stage of subjecting at least a part of the purln to a first stage of passive biological flotation in a flotation unit, with a residence time comprised between 4 and approximately 24 hours, with the presence of a polymer, to yield a first solid fraction and a first floating liquid fraction and to carry out a subsequent treatment stage selected from a group comprising subjecting the purln to a stage of separation of larger thick solid particles 0.05 mm before making a first flotation to provide a liquid fraction that is part of said slurry, and subject the said liquid fraction to a subsequent solid-liquid separation stage that provides a final liquid fraction.
    Patent ES 2395664 (B1) describes a system for the elimination of slurry impurities generated in pig farms comprising a separation of solids-liquids in a press filter after whose operation the liquid fraction is sent to a float-flocculation tank of the that the resulting liquid matter is passed through an electrocoagulation equipment for the separation of the floating sludge from the precipitated sludge and the treated effluent passes to a process where caustic soda is added to increase the PG, to pass to an electro stage -oxidation. Said electro-oxidation is complemented with an active zeolite-carbon filtration phase and a reverse osmosis to separate salts and other impurities from the liquid obtaining a treated and clean water. On the other hand, the solid phases resulting from the different stages are used to convert them into a fertilizer or fertilizer for the land. This application
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    It does not deal with the elimination of CO2 emissions from the methanization of the existing carbon in the solid fraction used as an organic fertilizer and the emission of NOx by the nitrogen compounds existing in both the solid fraction and the liquid used as irrigation water enriched in said nitrogen compounds.
    WO 20006134453 (A1) describes the production of a fertilizer from the treatment of purines by electrolysis and with ozone injection. This treatment does not prevent the methanization of the organic fraction of the slurry and therefore does not reduce the CO2 emission associated with said methanization. The same happens with the nitrogen fraction present in the fertilizer obtained, since the treatment does not reduce the emission of nitrogen-based GEl generated during the treatment or after its deposition on an agricultural surface.
    Patent ES 2292310 (B1) describes a system for the treatment of effluents by electrocoagulation.
    Patent ES 2473440 (B1) refers to a slurry treatment process which comprises all the steps included in the preamble of the claim of this patent application, using an electrocoagulation equipment as described in the previous patent ES 2292310 ( B1). In this procedure the final liquid fraction is left with a very low content of nitrogen-generating compounds or precursors of GEl, and of remains of dissolved organic matter, phosphorus and other inorganic contaminants such as heavy metals, etc., and especially also of organic pollutants, such as fauna and microbial or fungal flora, remains of medication and organic matter in general, obtaining an effluent treated with a highly reduced pollutant load and low environmental impact. On the other hand, the decanted solids and sludge or supernatants of the process are sent to pellet to obtain combustible biomass or, if its humidity is excessive to a solid-liquid separator to subsequently pass to pelletization.
    The present invention is an improvement of the procedure described in this last patent, which is achieved by the realization of an additional ultrafine filtration phase, which guarantees that the effluent that reaches the electrocoagulation equipment has a particle size below 20 microns, that is to say, the number of solid non-conductive particles present in the effluent to be electrocoagulated is reduced, in addition to carrying out a system of continuous execution of the process under computerized control.
    Brief description of the invention
    The present invention concerns a process for the treatment of animal slurries, especially pig slurries. It will be understood that the slurries are a residue that contains feces, urine and water from the washing of the cochiqueras and that may include food scraps, plant debris, seeds, etc.
    The proposed method comprises the following steps, which are themselves known in this sector of the art, in particular for having been implemented in the aforementioned patent ES 2473440 (B1):
    a) solid-liquid physical separation of a liquid effluent from a tank with agitation, containing slurry, generated a first solid fraction and a first filtered liquid fraction;
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    b) physical-chemical separation of the first liquid fraction obtained in step a) providing a second solid fraction and a second liquid fraction;
    c) electrocoagulation of the second liquid fraction obtained in step b) providing a solid third fraction and a third liquid fraction; Y
    d) pelletizing the solid fractions obtained at least in steps a) and b) in the presence of some ligneous or lignocellulosic materials,
    Ace! then, successive stages of separation and filtering allow to extract said first, second and third solid fractions from the initial liquid effluent, leaving a third fraction filtered liquid free of said solid fractions as the final result of the described process.
    In a novel way, the present method also proposes that said stage b) of physical-chemical separation comprises:
    • controlled dosing and contribution of a coagulant to said first liquid fraction;
    • controlled dosage and contribution of a flocculant, in aqueous dispersion to said first liquid fraction, downstream of the coagulant contribution point; Y
    • treatment of said first liquid fraction, dosed with coagulant and flocculant, in a device that provides a second ultra-fine filtrate (particle size smaller than 20 microns) by separating an ultra-thin solid fraction from a second liquid fraction .
    In a preferred embodiment, said second ultra-fine filtering will be carried out by means of an endless screw centrifuge which pushes the solid fraction towards one end while a drum with micro holes rotates at high speed (speed of the order of 4,500 revolutions / minute) by evacuating a liquid phase by centrifugal force.
    These improvements in stage b) allow the elimination of a second ultra-thin solid fraction, leaving a second fraction of liquid much better filtered, which has an impact on the performance of the electrocoagulation stage favoring, by preventing the sacrificial anodes used (from Al or Fe) receive an excessive load of particles affecting the reaction of oxidation and release of Al3 + and Fe3 + ions, responsible for the formation of basic salts or insoluble hydroxides that will separate from the liquid fraction. With this contribution, a very significant improvement in the system's performance is achieved, and resulting in a third fraction that is much better purified than with the previously known methods.
    According to a further realization of the proposed method, steps a) to c) are carried out continuously and are automatically controlled by a control center with computing means and specific software which apart from supporting the management of the installation in continuous, sends different alarms in case of any anomaly in the equipment of the plant. These alarms can be transmitted through various media / communication systems to a remote point, for example by wiring, wireless signal (wifi, bluetooth). They can also be received on portable and / or remote devices, such as a mobile phone receiver, for example.
    In this way, control over the incidents of the slurry treatment procedure is available and in addition, the procedure can be influenced by
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    remote control from another terminal or, at least in part, from a mobile phone. In said control center said alarms are also received as well as the level values of a series of deposits of the treatment plant through which the aforementioned first and second liquid fractions are successively filtered, said control center also receiving the rotation speed values of said centrifugal equipment, which is proposed to be a centrifuge with screw screw. In particular, if said centrifuge is not at a predetermined rate of rotation, the process of the different steps described in continuous is not started.
    In accordance with the proposed procedure, it is envisaged that said first liquid fraction integrates solid particles in suspension of a size smaller than 0.45 or 0.65 mm, and is obtained by filtration by means of a mesh in a screw filter separator equipment, that will operate under a flow with the particularity of providing a flow of effluent to be treated greater than the treatment capacity. This excessive supply of liquid effluent will generate a return circulation to a first effluent tank of all the liquid effluent supplied to the separator equipment and not filtered because it exceeds its treatment capacity. In said first effluent tank, an agitator will subject the stored liquid effluent to agitation to avoid decantation.
    As indicated above, it is further proposed that said second liquid fraction, resulting from the additional stage of ultra-fine filtration, contain an effluent with a load of suspended solids with a particle size of less than 20 microns.
    From this it follows that the first stage of solid-liquid risic separation will eliminate particles of a size greater than 0.45 or 0.65 mm, which will form the first solid fraction, and that the physical-chemical separation stage will eliminate particles of a size between 20 microns and the above 0.45 or 0.65 mm, which will make up the second ultra-thin solid fraction.
    It is envisaged that said first liquid fraction is stored in a homogenization tank, where it is homogenized by liquid recirculation, and from which said first liquid fraction, homogenized, is pumped into a centrifuge-filtered equipment, which will preferably be a device of centrifuge. In a particular example, said centrifuge equipment is a screw screw centrifuge. Said second liquid fraction is conducted, after its chemical-chemical separation, to a regulation tank from where it is pumped to one or more electrocoagulation equipment. Said regulation tank has a level sensor, whose value is a priority in the chained maintenance of the different stages continuously. That is, the value reported by said level sensor to the control center is a priority parameter used in determining the operating parameters of other equipment of the treatment plant controlled by said control center.
    Additionally, it is proposed to provide a dosage and contribution of an antifoam to the second liquid fraction upstream of said regulation tank.
    Each of said electrocoagulation equipment has sacrificial anodes that release Al3 + or Fe (2 + / 3 +) ions, performing a continuous treatment of an adjustable flow rate of the second liquid fraction to be treated. In addition, a regulation of the distance between anode and cathode of the heads of said equipment is provided, which determines the maintenance of an intensity of the electrocoagulation current at a constant and predetermined value defined from said control center.
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    As for said pelletization stage of the solid fractions, it preferably comprises a treatment of the solids of said solid fractions in a rotating drum with heat input and with mixing of said solid fractions with a crushed lignocellulosic material, the proportion of material being lignocellulosic not exceeding 50% of the final mixture. The minimum presence of lignin must be at least 10% in dry matter of the total mixture. This can be achieved with a smaller proportion of wooden elements that have a higher lignin content.
    In an embodiment example, the proportions of solid fraction and lignocellulosic material can be 50% / 50%, respectively.
    The resulting mixed product after passing through the rotating drum has a maximum humidity of 20%, and is subsequently subjected to a compression binding process, preferably by means of an extruder compressor.
    Said compression agglutination process comprises the addition, to the product resulting from the mixing of solid and lignocellulosic fraction, of glycerin and optionally also of starch.
    The aforementioned treatments have been proposed by the fact that the pig purln by itself does not agglutinate it, that is to say the particles do not stick together. Providing a lignocellulosic charge, and subsequently glycerin and possibly starch, to the process, said agglutination is guaranteed.
    Other features of the invention will appear in the following detailed description of an embodiment example.
    Brief description of the figures
    The foregoing and other advantages and characteristics will be more fully understood from the following detailed description of an example of embodiment with reference to the attached drawings, which should be taken by way of illustration and not limitation, in which:
    Fig. 1 shows a scheme of a pig slurry treatment plant that applies the procedure proposed by this invention. The figure shows the main equipment of the plant and, in a continuous line, the transport conduits of the effluents to be treated that contain slurries that communicate said equipment, and in a broken line the conduits of the solid fractions separated from said effluents to treat, without including in this scheme the data connections of the aforementioned treatment plant to a control center equipped with computer means and plant management software to guarantee continuous operational operation, nor the part of the plant responsible for producing the compression agglutination procedure of the solid fraction;
    Fig. 2 shows the same scheme as Fig. 1, in which the main equipment of the plant is shown, and the data connections of said equipment with a control center, without having included in the present scheme the conduits for transporting the liquids to be treated or the solid fraction conduits separated from said liquids;
    Fig. 3 illustrates a diagram of the portion of the plant responsible for producing the process of agglutination by compression of the solid fraction and preparation of pellets or combustible biomass, from the solid fraction separated from the liquid
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    treated in the plant shown in Figs. 1 and 2, showing in a broken line the path of the solid fraction treated.
    Detailed description of an embodiment example
    Fig. 1 shows, according to an exemplary embodiment with an illustrative non-limiting character, a scheme of the treatment plant of effluents L0 containing slurries, separating solid fractions S1, S2 and S3 (S4 meeting of S1 and S2 ) usable of some first L1 and second L2 liquid fractions, and collecting a final liquid fraction L3 capable of being used for irrigation, in a reception raft 18.
    The proposed plant includes:
    • an effluent raft 10 containing slurries, intended to store liquid effluents L0 containing slurries;
    • a supply line 40 for the supply of liquid effluents L0 from the effluent reservoir 10 to a first effluent tank 11, which is conducted by a feed pump 20;
    • a first effluent tank 11, intended to store the liquid effluent L0 supplied through said first conduit 40, said first effluent reservoir 11 being provided with an agitator 23, and connected by a first conduit 41 which allows the contents of the first effluent tank 11 to the second line 42 by means of a first pump 21;
    • a screw filter separator equipment 12, fed through said second conduit 42 with a flow of liquid effluent L0 with a flow to be treated greater than the treatment capacity of said screw filter 12, which has a motor of screw 24 that drives the rotation of the screw of the separator equipment 12;
    • a third line 43 which returns the flow of liquid effluent L0 supercharged to the separator equipment 12 and not treated by it, to the tank 11;
    • a fourth line 44 that conducts a first liquid fraction L1, obtained from the solid-liquid physical separation produced in the separator equipment 12 to a tank 13 or homogenization tank;
    • a first conveyor 50 that conducts a first solid fraction S1, obtained from the solid-liquid physical separation produced in the separator equipment 12 to a solid collection tank D1:
    • a homogenization tank 13 by recirculation of liquid, fed through said fourth conduit 44 with the first liquid fraction L1;
    • a fifth line 45 which conducts said first liquid fraction L1 after having been homogenized in the homogenization tank 13, driven by a second pump 22 to a centrifuge equipment 14;
    • a sixth branch line 46 that connects the fifth line 45 with the fourth line 44;
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    • a coagulant dispenser 30 that introduces a controlled supply of coagulant A1 to said first liquid fraction L1 conducted through said fifth conduction 45;
    • a flocculant dispenser 31 that introduces a controlled supply of flocculant A2 mixed with a controlled supply of mains water, supplied through a water line 60, to said first liquid fraction L1 conducted through said fifth line 45;
    • a screw screw centrifuge equipment 14 fed through said fifth conduit 45 which provides, together with the coagulant and flocculant, a physical-chemical separation of the first liquid fraction L1 providing a second ultra-fine filtration, resulting in a second liquid fraction L2 with a particle size of less than 20 microns, and a second solid fraction S2 ultra-fine;
    • a seventh conduit 47 leading said second liquid fraction L2 towards a regulation tank 15;
    • a second conveyor 51 that conducts a second solid fraction S2, from the screw screw centrifuge 14, which is mixed with the first solid fraction S1 producing a fourth solid fraction S4 that accumulates in the solid collection tank D1;
    • an antifoam dispenser 32 that introduces a controlled supply of antifoam A3 to said second liquid fraction L2 conducted through said seventh conduit 47;
    • a regulation tank 15 fed with said second liquid fraction L2 through said seventh conduit 46;
    • an eighth conduit 48 leading said second liquid fraction L2 to one or more electrocoagulation equipment 16, 17;
    • one or more electrocoagulation equipment (which may be as described in patent ES 2292310 (B1)), in the present example a first and second electrocoagulation equipment 16 and 17, which are fed with said second liquid fraction L2 a through said eighth conduit 48, by means of third and fourth pumps 25 and 26, wherein said electrocoagulation equipment 16 and 17 include sacrificial anodes that release Al3 or Fe ions (2 + / 3 +), performing a treatment in continuous of an adjustable flow of the second liquid fraction L2 to be treated, and which also allow a regulation of the distance between anode and cathode determining maintenance of the intensity of the electrocoagulation current at a constant and predetermined value; these electrocoagulation equipment 16 and 17 provide a third liquid fraction L3 purified and a third solid fraction S3 resulting from the basic salts or insoluble hydroxides formed in the solution by the release of metal ions, insoluble compounds that precipitate in the form of flocculation and that they absorb an important part of organic substances that exist in the solution by decontaminating the resulting water or liquid fraction L3, cited;
    • a ninth conduit 49 collects the said third liquid fraction L3 produced in the electrocoagulation equipment 16 and 17 and leads it to a reception raft 18;
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    • one or more conveyors, in this example a third and a fourth conveyors 53 and 54, collect the said third solid fraction S3 produced in electrocoagulation equipment 16 and 17;
    • a reception raft 18 is fed with the third liquid fraction L3 through said eighth conduction 48.
    In order to achieve a correct regulation of the different equipment that make up the proposed treatment plant, a control center 80 with computation means (including at least one computer) is included, as shown in Fig. 2, where they receive the values of different sensors integrated in the plant that include a first level 70 sensor located in the first effluent tank 11, a second level 71 sensor located in the homogenization tank 13, and a third level 72 sensor located in the regulation tank 15, to which the aforementioned first and second liquid fractions L1 and L2 are successively filtered, said computer also receiving the rotation regime values of said centrifugal equipment (14) screw auger.
    All these data obtained by the control center 80 allow to know the operating parameters of the plant, and allow said control center 80 to take, by means of control algorithms included in said specific software, decisions to modify operating parameters of the plant. plant. Preferably, the control center 80 will implement said modifications of operating parameters through automated actuators controlled by said control center 80, such as for example solenoid valves, pumps, or by modifying actuation parameters of said pumps, of coagulant dosers 30 , flocculant 31 or antifoam, electrocoagulation equipment, etc.
    Figure 3 shows, schematically, the treatment given to said fourth solid fraction S4 and solid fraction S3 in order to achieve its use by converting it into pellets 57 usable as fuel.
    In a first stage, said solid fraction (S3 + S4) is mixed with a crushed lignocellulosic material S5 in an exemplary embodiment, and both materials are introduced into a rotating drum 90 with heat input 91, where they are mixed and dry
    The resulting product is a dry solid product S6 which is extracted from said rotating drum, and to which a controlled supply of glycerin A4 is added, by means of a glycerin dispenser 33, and a controlled supply of A5 starch is also added by means of a starch dispenser 34. Then said dry solid product S6 with glycerin A4 and starch A5 is subjected to a compression agglutination process, by means of an extruder compressor 92, which converts said product into pellets 57 suitable as combustible biomass.
    As will be apparent, the equipment shown in Figure 3 can also be connected and controlled by the control center 80 shown in Figure 2.
    权利要求:
    Claims (20)
    [1]
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    1. Procedure for treatment of slurry, in particular pig slurry, which comprises the following stages:
    a) solid-liquid physical separation of a liquid effluent (L0) containing slurry, generating a first solid fraction (S1) and a first filtered liquid fraction (L1):
    b) physical-chemical separation of the first liquid fraction (L1) obtained in step a) providing a second solid fraction (S2) and a second liquid fraction (L2);
    c) electrocoagulation of the second liquid fraction (L2) obtained in step b) providing a third solid fraction (S3) and a third liquid fraction (L3); Y
    d) pelletizing of the solid fractions (S1, S2 and S3) obtained at least in stages a) and b) in the presence of ligneous or lignocellulosic materials (56),
    characterized because
    • stage b) of physical-chemical separation includes:
    • controlled dosage and contribution of a coagulant (A1) to said first liquid fraction (L1):
    • controlled dosage and contribution of a flocculant (A2), in aqueous dispersion to said first liquid fraction (L1), downstream of the coagulant contribution point (A 1): and
    • treatment of said first liquid fraction (L1), dosed with coagulant (A1) and flocculant (A2), in a device that provides a second liquid fraction (L2) by performing a second ultra-fine filtration by separating a solid fraction ( S2) ultra-fine, so that said second liquid fraction L2 has a particle size much lower than that of the particles of liquid fraction L1.
    [2]
    2. Method according to claim 1, characterized in that said second ultra-fine filtering is carried out by means of a centrifuge equipment (14).
    [3]
    3. Method according to claim 2, characterized in that said centrifugation equipment is a screw screw centrifuge equipment.
    [4]
    Method according to any one of the preceding claims, characterized in that steps a) to c) are carried out continuously, and are automatically controlled by a control center (80) with computing means with at least one computer and associated specific software. , where the level values of a series of deposits (11, 13, 15) are received through which the aforementioned first and second liquid fractions (L1 and L2) are successively filtered, said computer also receiving the values of rotation speed of said centrifugal equipment (14) screw screw.
    [5]
    5. Method according to claim 1, characterized in that said first liquid fraction (L1) comprises a size of solid particles in suspension of less than 0.45 or 0.65 mm, and is obtained by filtration by means of a mesh in a separating equipment (12 ) screw filter operating under a flow rate with an effluent flow (L0) to be treated higher than
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    treatment capacity and providing a return circulation to a first effluent tank (11) where it is subjected to agitation.
    [6]
    Method according to any one of claims 1 to 3, characterized in that said second liquid fraction (L2) comprises a particle size of less than 20 microns.
    [7]
    Method according to any one of claims 1 to 3, characterized in that said first liquid fraction (l1) is stored in a homogenization tank (13), by recirculation of liquid, from where it is pumped into the centrifuge equipment (14) screw screw
    [8]
    8. Procedure according to revindication 4, characterized in that said second liquid fraction (L2) is conducted to a regulation tank (15) from where it is pumped to one or more electrocoagulation equipment (16, 17), and because said regulation tank (15) has a level (72), whose value is a priority in the chained maintenance of the different stages continuously.
    [9]
    9. Procedure according to revindication 8, characterized in that it comprises a dosage and contribution of an antifoam (A3) to the second liquid fraction (l2) upstream of said regulation tank (15).
    [10]
    10. Procedure according to revindication 2 or 3, characterized in that said electrocoagulation is performed in an electrocoagulation equipment (16, 17) in the presence of sacrificial anodes that release Al3 + or Fe (2 + / 3 +) ions, performing a continuous treatment of an adjustable flow rate of the second liquid fraction (L2) to be treated and with a regulation of the distance between anode and cathode determining maintenance of the intensity of the electrocoagulation current at a constant and predetermined value defined from said center control (80).
    [11]
    Method according to any one of claims 1 to 3, characterized in that said pelletization step comprises a treatment of the solids of said solid fractions (S1, S2 and S4) in a rotating drum (90) with heat input (91) and with a proportion of lignocellulosic material (S5) not exceeding 50% of the final mixture with said solid fractions producing a resulting mixed product with a maximum humidity of 20%, which is subsequently subjected to a compression binding process.
    [12]
    12. Procedure according to revindication 11, characterized in that said lignocellulosic material is crushed with a predetermined particle size.
    [13]
    13. Method according to revindication 11, characterized in that said compression agglutination process comprises the addition, to the product resulting from the mixing of solid fraction (S1, S2 and S4) and lignocellulosic (S5), of glycerin (A4).
    [14]
    14. Procedure according to revindication 13, characterized in that an amount of starch (A5) is additionally used as binder.
    [15]
    15. Plant for the treatment of slurry, in particular pig slurry, characterized in that it comprises:
    • a first effluent reservoir (11), intended to store a liquid effluent L0 containing slurries, supplied through a first conduction (40), said first effluent reservoir (11) being provided with a stirrer (23), and connected to a
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    first conduction (41) which allows the contents of said tank (11) to be supplied to a second conduction 42 by means of a first pump 21;
    • a screw filter separator device (12), fed through said second conduction (42) with a flow of liquid effluent L0 with a flow to be treated greater than the treatment capacity of said screw filter (12) and with a third conduction (43) that returns the flow of supercharged liquid effluent L0 to the separator equipment (12) and not treated by it, to the tank (11);
    • a homogenization tank (13) that receives said first liquid fraction L1;
    • a fifth conduction (45) that conducts said first liquid fraction L1 after having been homogenized in the homogenization tank (13), driven by a second pump (22) to a device that performs a second ultra-fine filtration;
    • a coagulant dispenser (30) that introduces a controlled supply of coagulant A1 to said first liquid fraction L1 conducted through said fifth conduction
    (Four. Five);
    • a flocculant dispenser (31) that introduces a controlled supply of flocculant A2 mixed with a controlled supply of mains water, supplied through a water pipe (60), to said first liquid fraction L1 conducted through said fifth conduction (45);
    • a screw auger centrifuge equipment (14) fed through said fifth conduction (45) which provides, together with the coagulant and the flocculant, a physical-chemical separation of the first liquid fraction L1 providing said second ultra-fine filtrate , resulting in a second liquid fraction L2 with a particle size smaller than 20 microns, and a second solid fraction S2 ultra-thin, which are fed to an electrocoagulation equipment (16, 17), and
    • a control center (80) with computing means with at least one computer and associated specific software, where the level values of said series of deposits (11, 13) are received through which the aforementioned vehicles are transported first and second liquid fractions (L1 and L2) successively filtered, said computer also receiving the rotation regime values of said centrifugal equipment (14) screw auger.
    [16]
    16. Plant according to revindication 15, characterized in that it also includes a
    seventh conduction (47) leading said second liquid fraction L2 into a regulation tank (15), sandwiched between the screw screw centrifuge (14) and the electrocoagulation equipment (16, 17), a metering dispenser being arranged
    defoamer (32) which introduces a controlled supply of defoamer A3 to said second liquid fraction L2 conducted through said seventh conduction (47).
    [17]
    17. Plant according to revindication 15, characterized in that said electrocoagulation equipment (16 and 17) includes slaughter nodes that release Al3 or Fe ions (2 + / 3 +), performing a continuous treatment of an adjustable flow of the second liquid fraction L2 to be treated, and which also allow a regulation of the distance between anode and cathode determining maintenance of the intensity of the electrocoagulation current at a constant and predetermined value, providing these electrocoagulation equipment (16 and 17 ) a third liquid fraction L3 purified and a third solid fraction S3.
    [18]
    18. Plant according to one of claims 15 to 17, characterized in that one or more conveyors collect the solid fractions produced in the separation equipment (12), centrifugation equipment (14), and electrocoagulation equipment (16, 17), a some deposits (D1, D2).
    5
    [19]
    19. Plant according to any one of claims 15 to 18, characterized in that it comprises a rotating drum (90) with heat input (91), where the solid products (S1, S2, S3 and S4) are mixed and dried with lignocellulosic materials crushed (S5), and because it also includes an extruder compressor (92) in which they are agglutinated by
    10 buy these solid products (S1, S2, S3 and S4).
    [20]
    20. Plant according to revindication 19, characterized in that it comprises means for a controlled supply of glycerin A4, by means of a glycerin dispenser (33), and optionally for an additional controlled supply of starch A5 by means of a
    15 starch dispenser (34) in a supply conduction of said solid products (S1, S2, S3 and S4), to the extruder compressor (92) which provides useful pellets such as combustible biomass.
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    同族专利:
    公开号 | 公开日
    EP3459910A1|2019-03-27|
    ES2626598B1|2018-05-04|
    WO2017178671A1|2017-10-19|
    EP3459910A4|2020-01-08|
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    FR3005651B1|2013-05-16|2017-03-31|Concept Rolland Dev|PROCESS FOR TREATING EFFLUENTS OF LIVESTOCK AND DEVICE THEREOF|
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    EP17781970.3A| EP3459910A4|2016-04-12|2017-04-12|Slurry processing method and plant|
    PCT/ES2017/000043| WO2017178671A1|2016-04-12|2017-04-12|Slurry processing method and plant|
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