• 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:
    A procedure for the treatment of slurries which comprises subjecting a liquid fraction thereof to a physical-chemical process in an essentially closed and sequential environment, first of coagulation, after flocculation and finally of filtration taking the appropriate measures so that at all times The separated liquid and solid parts remain acidic. An especially suitable reactor comprises a vessel with at least one first chamber prepared to subject the medium to be treated to a chemical coagulation process under controlled conditions of the pH level between 5 and 6.5; a second chamber in communication with the first chamber and prepared to subject a coagulated overflow of the first chamber to a chemical flocculation process under controlled conditions of the pH level below 6.8; and a third chamber in communication with the second chamber with a compartment for quieting the flocs with suspended solids and with a sieve device in which it overflows, for its separation, the contents of said compartment for quieting the flocs. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2737573A1
    申请号:ES201830672
    申请日:2018-07-04
    公开日:2020-01-14
    发明作者:Guardia Gener Romeu
    申请人:Rotecna SA；
    IPC主号:
    专利说明:

    [0001]
    [0002] A reactor, a system and a procedure for the treatment of liquid manure or digestates, especially suitable for the treatment of slurry
    [0003]
    [0004] Technical sector of the invention
    [0005] The invention belongs to the field of farm and related manure treatment, which pays special attention to how to condition a liquid fraction thereof for reuse.
    [0006]
    [0007] Background of the invention
    [0008] Liquids (purines) are the liquid formed by the urine of animals and what oozes from manure. In livestock farms, for example, in pigs, in practice, slurries consist of a mixture of solid and liquid dejections, that is, feces and urine, usually mixed with the water used to clean the stables.
    [0009]
    [0010] Liquid manures have traditionally been used as fertilizer elements, being recycled to become an organic fertilizer for cultivated land, with the consequent saving of chemical fertilizers and costs.
    [0011]
    [0012] The slurries have basic pHs, which favors emissions of ammonia and other GHG gases into the atmosphere, because in these mixing conditions there are uninterrupted reactions of product decomposition.
    [0013]
    [0014] When ammonia dissolves in water, an amount of it is converted into ammonium ions. The balance between ammonia and ammonium ions is expressed as follows: NH4 + OH- = NH3 H2O.
    [0015]
    [0016] It is known that the degree to which the ammonium ion is converted to ammonia depends on the pH of the solution. If the pH is low, more ammonia molecules are converted to ammonium ions (non evaporative). If the pH is high, the hydroxide ion abstracts a proton from the ammonium ion generating ammonia (evaporative).
    [0017]
    [0018] Taking advantage of this principle, different proposals for treatment of slurries that either favor the evaporation of ammonia for recovery, is the case of the procedures for extraction and thermal dehydration of volatile organic matter and ammoniacal nitrogen compounds, or ensure that it remains in the form of an ammonium ion , for example, the biological procedures of the nitrification / denitrification type that produce a biological sludge that contains the majority of phosphates. However, the presence of solid components in the slurry and the necessary contribution of energy and space for the implementation of some of these proposals mean that they are not efficient.
    [0019]
    [0020] Among the processes that seek to prevent the evaporation of ammonia, for example, the one described in patent document ES 2147975 is known, which comprises subjecting the liquid fraction of a solid-liquid separation stage to a physical-chemical coagulation treatment that employs coagulating agents in the presence of an acid so that the treatment is carried out at the pH value of the optimal reaction medium. This optimal pH is not exemplified, although it is commented that the use of sulfuric acid has the advantages of modifying the balance of ammonium salts towards more chemically and thermally stable ammonium sulfate such as ammonium carbonate (or ammonium bicarbonate); and that the sulfate element is evaluated agronomically in the recovered solid.
    [0021]
    [0022] Optionally, this coagulation treatment can be followed by a flocculation treatment, in this case without control of the pH value. As a coagulating agent, a mineral coagulating agent is proposed, which can be chosen from the group consisting of ferrous chloride, ferric chloride, ferrous sulfate, ferric sulfate, ferric chlorosulfate, aluminum sulfates or basic aluminum chlorosulfates; or an organic agent, a neutral polyelectrolyte 0 being listed as a candidate, most preferably, cationic. As a flocculating agent, at least one anionic polyelectrolyte is preferably mentioned.
    [0023]
    [0024] In document ES 2147975 the coagulation treatment and the flocculation treatment is carried out in different devices, so that after the coagulation treatment in the coagulation apparatus the medium to be treated is taken to the apparatus used for flocculation. The flocculant is injected into the stream of the medium being treated between the two devices.
    [0025]
    [0026] Then, at a later stage performed in another apparatus, a liquid / solid separation operation is carried out by a float or hydrocyclone (when animal feces are treated). The proposal is exemplified, in the case of pig droppings liquid, with a float device from which a separated sludge with 5.28% dry extract is obtained at 105 ° C.
    [0027]
    [0028] A solution capable of extracting a separated sludge with a higher dry extract value is of interest.
    [0029]
    [0030] Likewise, for the implementation of the proposal according to ES 2147975 a complex installation is required, equipped with pumping units, hydraulic connections and a notable space extension. For example, it is estimated that to separate 2000 Kg / h in the separation stage with the float device, at a rate of 6.6 Kg / m2h (Metcalf Eddy) it would take 303m2 of surface and provide suitable humidity conditions.
    [0031]
    [0032] It is also an object of the present invention a more compact and versatile solution, which can adapt to different livestock farms quickly and safely and that requires less space than known solutions.
    [0033]
    [0034] The solution pursued cannot also give up other basic objectives, such as the suppression of odors, essentially caused by volatile organic materials and bound elements (such as H2S and NH3); and phosphate removal from the recovered liquid fraction.
    [0035]
    [0036] Explanation of the invention.
    [0037] To solve the above-described drawbacks, a compact reactor for the treatment of liquid manure or digestates, especially suitable for the treatment of a liquid slurry part, comprising a closed container with at least three chambers for subjecting the solution, is disclosed. manure at three consecutive stages of treatment, and in particular - a first chamber with a liquid manure receiving input, prepared to subject the liquid manure to a chemical coagulation process under controlled conditions of the pH level between 5 and 6, 5;
    [0038] - a second chamber in communication with the first chamber, prepared to subject a coagulated overflow of the first chamber to a chemical flocculation process under controlled conditions of the pH level below 6.8; Y
    [0039] - a third chamber in communication with the second chamber and in which a compartment is formed for quieting the flocs with suspended solids formed in the second chamber; and a sieve device, preferably curved, over which the contents of the compartment to soothe the flocs are overflowing for separation, comprising In addition, the third chamber is an outlet for the recovered liquid fraction (Lr) that passes through the sieve device and collecting means of the recovered solid fraction (Sr) that slides through the sieve device with connection to the outside of the container.
    [0040]
    [0041] The reactor thus offers a compact solution that requires less space than conventional installations while being more versatile.
    [0042]
    [0043] Note that the reactor is adapted to control the pH of the medium being treated not only in the first but also in the second chamber, which allows to avoid an overflow of flocculant, as in the known procedures that do not implement any control to the In this respect, as is the case of the procedure described in ES 2147975. In fact, if after coagulation there is no pH control, the natural tendency of the flocculant is to raise the pH a bit and then it can exceed the PH 7 value which favors, undesirably, the generation of evaporative ammonia. Controlling the pH well in the second chamber also allows the necessary dose of flocculant to be adjusted and the pH of the medium at the outlet, both of the solid part and of the liquid part, is known for sure.
    [0044]
    [0045] The arrangement in chambers, hydraulically connected, and the passage through natural overflow between the first and the second chamber avoids subjecting the medium to overpressures that can impair the stability of the flocs, as occurs when having different devices to subject the medium to a treatment of coagulation and a flocculation treatment, which implies the use of pumping groups for the transfer of the medium between the different devices.
    [0046]
    [0047] In a variant of the invention the first chamber is equipped with at least first stirring means; an upper outlet, intended to allow the evacuation of gases; a first pH probe; and first means for the joint or separate dosing of a coagulant, an acidifier and an antifoam in the amount and proportions required to maintain the pH level between 5 and 6.5.
    [0048]
    [0049] Preferably, the coagulant comprises at least one of aluminum polyhydroxychlorosulfate (PACS) or aluminum hydroxychloride (PACI).
    [0050]
    [0051] In a variant of the invention, the second chamber is equipped with at least a few second stirring means; a second pH probe; and a few second means for the dosage of flocculant in the amount and proportions required to maintain the level of pH below 6.8.
    [0052]
    [0053] Preferably, the flocculant is a solid mixture of cationic, medium or high cationicity and high molecular weight flocculant with a minor part of an organic acid.
    [0054]
    [0055] As explained below, the first and second means for dosing coagulant and flocculant, respectively, as well as the acidifier and antifoam can comprise dosing pumps continuously or at intervals, as mandated by an associated control unit depending on the values pH snapshots of the medium measured in said first and second chambers and the target pH value for each chamber.
    [0056]
    [0057] According to one embodiment, the volume ratio V1 of the first chamber and V2 of the second chamber meets the ratio V1 <V2; and comprising the first and second agitator means both first and second propeller agitators or vertical shaft blades the ratio of the rotational speeds R1 of the first propeller agitator or blades and R2 of the second propeller agitator or blades meets the ratio R1> R2 . In practice, the agitation in the first chamber will be faster than that in the second chamber.
    [0058]
    [0059] In a variant of interest, which contributes to compacting the reactor, the third chamber is equipped with an overflow device, for communication between the compartment for quieting the flocs and the sieve device, adjustable in height to be able to control the level of the free surface of the medium in treatment in the first, second and third chambers by effect of communicating vessels.
    [0060]
    [0061] The surfaces of the container in contact with the liquid manure being treated may be polypropylene.
    [0062]
    [0063] Optionally, the container can comprise two attached chambers to prepare in situ the flocculant to be used in the second chamber.
    [0064]
    [0065] According to another aspect of the invention, a slurry treatment plant is disclosed, comprising a solid-liquid separator for obtaining a solid fraction and a liquid fraction of the slurries; and a reactor according to the invention, whose reception inlet is connected to the separator for feeding the liquid fraction of the slurries to the reactor, the separator being optionally arranged above the reactor.
    [0066] According to another aspect of the invention, a process for the treatment of slurries is disclosed, comprising the steps of a) mechanically separating a liquid fraction (L) from a solid fraction (S) from the slurries, obtaining a solid fraction (S) with 15-30% dryness; and b) subject the liquid fraction obtained to a physical-chemical process in an essentially closed and sequential environment, first of coagulation, after flocculation and finally of filtration taking the appropriate measures so that at all times the liquid and solid parts are kept in shape acid to, among other factors, favor the presence of ammonium ion and avoid ammonia emissions.
    [0067]
    [0068] The reactor of the invention is especially suitable for carrying out said step b).
    [0069]
    [0070] In one form of interest, step b) comprises the operations of b3) subjecting the obtained liquid fraction to a chemical coagulation process under cheerful agitation and controlled pH level conditions between 5 and 6.5; b4) subject the coagulate resulting from operation b3) to a chemical flocculation process under moderate agitation and controlled conditions of the pH level below 6.8; and b5) quieting flocks with suspended solids obtained from operation b4) and spilling them by overflow to a sieve device, preferably of the curved type, obtaining a recovered liquid fraction (Lr) that crosses the sieve device and a solid fraction (Sr) recovered slipping through the sieve device.
    [0071]
    [0072] Preferably, the solid fraction (Sr) recovered in operation b5) is mixed with the solid fraction (S) of the slurry obtained in operation a), obtaining a final solid capable of being dried, composted or used as fertilizer. .
    [0073]
    [0074] According to a preferred method of the process, in operation b3) the pH value of the material or the medium in the process of coagulation is monitored and a coagulant, an acidifier and an antifoam in the amount and proportions required to maintain the pH level between 5 and 6.5.
    [0075]
    [0076] Likewise, also preferably in operation b4) the pH value of the material or the medium in the flocculation process is monitored and a flocculant is dosed which is a solid mixture of cationic flocculant, medium or high cationicity and high weight molecular with a minor part of an organic acid.
    [0077] Brief description of the drawings
    [0078] Fig. 1 schematically shows an installation for the implementation of the method according to the invention;
    [0079] Figs. 2 and 3 show the compact reactor for the physical-chemical treatment of the liquid slurry fraction of the installation of Fig. 1, according to a side view and in section according to a longitudinal cutting plane, respectively.
    [0080]
    [0081] Detailed description of the invention
    [0082] Fig. 1 schematically shows an installation that exemplifies the invention. The parts of it are not represented at scale and the purpose of the scheme is only to provide the reader with the explanations that follow.
    [0083]
    [0084] That said, the installation of Fig. 1 comprises a raft 30 of farm slurries 33, preferably of the agitated type, from which and in a conventional manner by means of a pumping group 31 the slurries to be treated are driven to a solid separator 32 /liquid. This separator 32 can be, for example, a TECNAPUR® TP-01 separator, with a treatment flow of 5m3 / h.
    [0085]
    [0086] The solid obtained (S), with approximately 25% dryness, can be used to throw it into the field, it can be composted or it can be used for other uses, in the present example after mixing with a recovered solid (Sr) obtained at a later stage , as explained below.
    [0087]
    [0088] The characteristics of the slurry at the entrance and exit of this separator 32 are shown in Table 1.
    [0089]
    [0090]
    [0091] Table 1 : Example and characterization of the solid-liquid separation stage with TECNAPUR separator model TP-01.
    [0092]
    [0093] The resulting liquid fraction (L) (comprising 58.8% dry matter from the initial slurry) is conducted directly and without deposits to a compact reactor 100, the details of which will be explained below, and from this liquid fraction (L) you will obtain a recovered liquid fraction (Lr) and the recovered solid fraction (Sr) mentioned above.
    [0094]
    [0095] In the example installation, in the reactor 100 the 4,108 tons of the liquid fraction (L) obtained from the separator 32 were treated, with 7.36% of dry matter, from which 2.96 tons of fraction were obtained recovered liquid (Lr) with 1.7% dry matter (corresponds to dissolved solids) and 6.5 pH units; and 1.23 tons of solid fraction recovered (Sr) with 20.4% dry matter and 6.5 pH units.
    [0096]
    [0097] The characteristics of the liquid fraction (L) at the inlet of the reactor 100 and the liquid and solid fractions recovered (Lr) and (Sr), respectively, at the outlet of this reactor 100 are shown in Table 2.
    [0098]
    [0099]
    [0100]
    [0101] Table 2 : Example and characterization of the stage in the compact reactor.
    [0102]
    [0103] Under the conditions of the output pH, the ammonia is 99.99% non-evaporative and the emissions to the atmosphere of greenhouse gases (GHG) CH4, N2O, CO2, NOx, odors are eliminated. as well as a very important reduction of nitrogen and phosphorus of the liquid part.
    [0104]
    [0105] As advanced above, in the example installation the recovered solid fraction (Sr) is mixed with the solid fraction (S) of the first solid / liquid separation stage. The final balance of the slurry is summarized in Table 3.
    [0106]
    [0107]
    [0108]
    [0109]
    [0110] Table 3 : Final overall result of the treatment.
    [0111] The contribution of reactor 100 to achieve this balance is significant. In the reactor 100, the liquid fraction (L) obtained in the solid / liquid separator 32 is subjected to a physicochemical process in essentially closed and sequential environment, first of coagulation, after flocculation and finally of filtration taking the appropriate measures so that in at all times the liquid and solid parts remain acidic in order to, among other factors, favor the presence of ammonium ion and avoid ammonia emissions.
    [0112]
    [0113] This reactor 100, illustrated in Figs. 2 and 3, comprises a container 2 constructed with materials resistant to chemical reactions that occur inside. In the example, the reactor 100 is made of double-wall polypropylene and stainless steel AISI 316.
    [0114]
    [0115] It is characteristic of the reactor 100 that the vessel 2 has internal divisions, that is, it is compartmentalized, three chambers being determined to subject the liquid fraction (L) that comes from the solid / liquid separator 32 to the three consecutive treatment stages. These three cameras are as follows:
    [0116]
    [0117] - a first chamber 3, which has a reception inlet 10 of the liquid fraction (L) to be treated, and is prepared to be subjected to a chemical coagulation process under controlled conditions of the pH level between 5 and 6.5;
    [0118]
    [0119] - a second chamber 4, in hydraulic communication with the first chamber 3, prepared to subject a coagulated overflow of the first chamber 3 to a chemical flocculation process under controlled conditions of the pH level below 6.8; Y
    [0120]
    [0121] - a third chamber 5, in hydraulic communication with the second chamber 4 and in which an interior compartment is formed for quieting 6 the flocs with suspended solids leaving the second chamber 4; and which is equipped with a sieve device 7, in the example of the preferably curved type, in which the contents of the compartment for quieting the flocs 6 overflow, the third chamber 5 further comprising an outlet 11 for the recovered liquid fraction (Lr) 8 which passes through the sieve device 7 and collecting means 9 of the recovered solid fraction (Sr) that slides through the sieve device 7 in connection with the outside of the container 2. The sieve device 7, which can be of triangular rod, has a Automatic cleaning system, not shown, and conducts flocculars without destroying to said collection means 9 which may comprise a thyme or auger conveyor.
    [0122]
    [0123] The procedure that is carried out in the installation is as follows:
    [0124]
    [0125] The liquid fraction (L) of the slurry to be treated is obtained by means of the solid / liquid separator 32. Said separator 32 is arranged superimposed on the reactor 100, said liquid fraction (L) being able to feed by gravity to the reactor 100, penetrating the first chamber 3 through the reception inlet 10, whose discharge mouth is submerged in the treatment medium .
    [0126]
    [0127] This first chamber 3 is equipped with first stirring means 12 with a set of blades 12a and with first means for the joint or separate dosing of a coagulant, an acidifier and an antifoam in the amount and proportions required to maintain the level of pH of the medium between 5 and 6.5. Although in essence the container 2 is a closed container and the treatment medium is not in contact with the atmosphere, the first chamber 3 has an upper outlet 13 intended to allow the evacuation of gases.
    [0128]
    [0129] The arrangement of these first means for the dosage 15 is schematic in Fig. 3. The dosage by means of separate pipes or injectors is of interest, as well as being able to locate the supply point in an area close to the mouth of the inlet reception.
    [0130]
    [0131] The first chamber 3 has a first pH probe 14 capable of monitoring the pH of the treatment medium, continuously or at intervals. The pH value is sent to a control unit, not shown, which seeks the joint or separate dosage of the coagulant, the acidifier and the antifoam in the quantities and proportions required to maintain said pH level between 5 and 6.5. In practice, the control unit will regulate the operation of two drive pumps for these products.
    [0132]
    [0133] In the example, the coagulant comprises at least one of aluminum polyhydroxychlorosulfate (PACS) or aluminum hydroxychloride (PACI). These coagulants have different solid bases in hydrolytic reactions with respect to conventional coagulants and the practice has revealed in an unpredictable way that PAC flocs tend to be groups of small spheres and chain structures smaller than 25 mm in size, while flocs obtained with conventional coagulants, aluminum sulfate type, are usually spongy and porous structures with a size of 25 to 100 mm. This difference causes PACs to produce less turbidity in suspension than aluminum sulfate.
    [0134]
    [0135] Advantageously, since PACs are more efficient than aluminum sulfate, given its greater capacity to remove suspended solids, it requires less dose: depending on the type of the nature of the slurry, it can substitute 1.5 to 2.0 parts of grade A aluminum sulfate and 3.5 to 3.9 of grade B aluminum sulfate.
    [0136]
    [0137] In the case of aluminum hydroxychloride, Al2 (OH) 5Cl2.5H2O, this is an inorganic salt of multinuclear aluminum (PAC) capable of forming flocs faster and more perfectly with sedimentation speed and clarifying power, achieving higher removals of turbidity with respect to other mononuclear aluminum salts such as aluminum sulfate.
    [0138]
    [0139] Aluminum hydroxychloride is commercially presented as a slightly viscous liquid of light amber color, sometimes opalescent and astringent dulzaino flavor. It has the advantage of its easy handling and dosing without leaving unwanted insoluble residues, unlike conventional granulated coagulants that must be dissolved and in many cases leave residues that damage the dosing equipment.
    [0140]
    [0141] In short and with respect to conventional coagulants, aluminum hydroxychloride improves the rate of floc formation; allows a higher sedimentation speed, protects dosing equipment; and requires shorter mixing times to coagulate.
    [0142]
    [0143] In addition to the above, aluminum hydroxychloride tends to rapidly acidify the medium as a function of the dose, which results in this procedure of interest in wanting to maintain the pH of the medium in acidic values.
    [0144]
    [0145] The acidifier can be selected sulfuric or hydrochloric acid.
    [0146]
    [0147] However, the conditions in chamber 3 are optimal to produce an exothermic reaction with rupture processes due to destabilization processes, molecular breakage of complexes forming small clots, with immediate elimination of microorganisms and pathogens, precipitation and uptake of phosphorus and metals, odor reduction, immediate transformation from ammonia to ammonia and reduction of CH4 emissions, favoring formation of ammonium sulfate and the agglutination of subsequent organic matter.
    [0148]
    [0149] The first chamber 3 of the reactor 100 is hydraulically connected to the second chamber 4 by means of a pipe 23 arranged in the upper part of the first chamber 3 but preferably at a level below the free surface of the medium in the first chamber 4.
    [0150]
    [0151] The pipe 23 is in the layered example and flows into the second chamber 4 at an intermediate level. The pipe 23 can have a vertical branch that communicates with the outside of the container 2.
    [0152]
    [0153] The second chamber 4 is equipped with a second stirring means 16 with a set of blades 16a and with a second means for dosing 18 of flocculant in the amount and proportions required to maintain the pH level below 6.8. In the example, the flocculant is supplied within the vertical branch of the pipe 23, the supply point being located at the level or below the horizontal section of the pipe 23.
    [0154]
    [0155] The second chamber 4 has a second pH probe 17 capable of monitoring the pH of the treatment medium, continuously or at intervals. The pH value is sent to the control unit referred to above, or to another associated control unit, which seeks the dosage of the flocculant in the amount required to maintain said pH level below 6.8. In practice, this control unit will regulate the operation of a discharge pump for the flocculant product.
    [0156]
    [0157] In the example, the flocculant is a solid mixture of cationic flocculant, medium or high cationicity and high molecular weight with a minor part of an organic acid. Table 4 characterizes flocculants with these characteristics.
    [0158]
    [0159]
    [0160]
    [0161]
    [0162] Table 4 : Optimal flocculants for the implementation of the invention.
    [0163]
    [0164] Commercial products that meet these characteristics usually incorporate between 2.5% of muramic acid, 2.5 % adipidic acid, or different mixtures, of acetic acid, citric acid. The invention accordingly contemplates using in combination with the selected flocculant less than 10% in proportion to an acid, such as an organic acid buffer.
    [0165]
    [0166] In the example, the capacity of the first chamber 3 is 600 liters and the capacity of the second chamber 4 is 800 liters.
    [0167]
    [0168] In the example, the stirring carried out in the first chamber 3 is a rapid stirring and the stirring carried out in the second chamber 4 is a slow stirring. In the reactor 100 the speed of rotation of the vanes 12a and 16a can be regulated to govern the speed of rotation to the optimum values. In the context of the present invention, rapid agitation is considered to be obtained at rotation rates between 700 and 1500 rpm; and a slow agitation which is obtained at speeds of rotation below 300 rpm.
    [0169]
    [0170] However, the conditions in the second chamber 4 are optimal for very large and heavy floccules to be formed that contain all suspended solids.
    [0171]
    [0172] Said second chamber 4 is in hydraulic communication with a third chamber 5 by means of a passage 24 arranged at an intermediate level that embeds a compartment for quieting 6 the flocs formed in the third chamber 5 and equipped with an overflow device 19 through which the starches are they pour onto the sieve device 7. The overflow device 19 is preferably height-adjustable to be able to control the level of the free surface of the medium being treated in the first, second and third chambers 3, 4 and 5 by effect of communicating vessels.
    [0173]
    [0174] The compartment for quieting the flocs 6, or calming chamber, is of a small volume and is not agitated, contributing to a better grouping and compaction of the flocs before the separation that takes place in the sieve device 7.
    [0175]
    [0176] The flocs are poured naturally and continuously on the sieve device 7 and separated by rolling the solid towards the bottom of the sieve device 7, which contributes to drying it in the path without being destroyed. The solid that reaches the bottom of the sieve device will constitute the recovered solid fraction (Sr) that is continuously removed by the collecting means 9 at a maximum of 2000 kg / h.
    [0177] The liquid part that passes through the sieve device 7 will constitute the recovered liquid fraction (Lr) and is devoid of suspended solids, presenting a reduction in color to a light orange hue. This recovered liquid fraction (Lr) is continuously extracted from reactor 100 and can be subjected to further treatments and / or sent to a raft.
    [0178]
    [0179] The reactor 100 is preferably equipped with an automatic cleaning system 7a of the sieve device 7. This automatic cleaning system 7a (schematically illustrated in Fig. 3) can consist of a series of nozzles suitable for launching liquid jets on the sieve device 7.
    [0180]
    [0181] In the present example, the energy consumption associated with the pumping group 31, the separator 32 and the physical-chemical system inside the reactor 100 is less than 5 KW / h for a maximum flow rate of 15 m3 / hour, which represents a remarkable energy saving compared to other known procedures, especially with respect to those that employ the electrocoagulation technique or that employ centrifugal devices.
    [0182]
    [0183] The reactor 100 exemplifying the invention comprises a first and a second added chambers 21 and 22, contiguous, to produce in situ and continuously the flocculant used in the flocculation stage carried out in the second chamber 4.
    [0184]
    [0185] The first added chamber 21 incorporates a receiving hopper of about 60 liters capacity, in which the cationic flocculant in powder format of the parameterized type is added in Table 4.
    [0186]
    [0187] This powdered flocculant is dosed with a heated visinfin operated by a geared motor with speed regulation capability, to control the amount of powdered flocculant to be supplied to the first added chamber 21
    [0188]
    [0189] In the same first added chamber 21, in the example of about 600 liters of capacity, water is supplied from the network, at a controlled rate of approximately 1200 liters / hour with a rotameter and mixed with the flocculant powder, stirring the medium by blade agitator that rotates at a speed of approximately 200 rpm. Through communicating vessels, the stirred medium passes to the second added chamber 22 and is also subjected to agitation, where the mixture has just matured to be able to be dosed into the second chamber 4.
    [0190] By controlling the amounts of dust and water it is possible to achieve the optimum concentration of flocculant. In the example, concentrations of 0.1% have been satisfactory.
    [0191]
    [0192] As an alternative, the use of a pulse counter flowmeter is also contemplated before the rotameter enters so that it is possible to dose an emulsion flocculant (highly concentrated liquid mixture but more expensive in economic terms) instead of dust. In this case, the pulse counter would be connected to a pulse pump to dose the emulsion flocculant from a container or container to be introduced into the first added chamber 21.
    权利要求:
    Claims (16)
    [1]
    1. - A reactor (100) for the treatment of liquid manure or digestates, especially suitable for the treatment of a liquid part of slurry, comprising a closed container (2) with at least three chambers to subject the manure to three consecutive stages of treatment, and specifically
    - a first chamber (3) with a reception inlet (10) of the liquid manure to be treated, prepared to subject the liquid manure to a chemical coagulation process under controlled conditions of the pH level between 5 and 6.5;
    - a second chamber (4) in communication with the first chamber (3), prepared to subject a coagulated overflow of the first chamber to a chemical flocculation process under controlled conditions of the pH level below 6.8; Y
    - a third chamber (5) in communication with the second chamber (4) and in which it is formed - a compartment for quieting (6) flocks with suspended solids formed in the second chamber (4); Y
    - a sieve device (7), preferably curved, over which the contents of the compartment for overflowing (6) the flocs overflow for separation, further comprising the third chamber (5) an outlet (11) for the liquid fraction (Lr) recovered (8) through the sieve device (7) and collecting means (9) of the recovered solid fraction (Sr) that slides through the sieve device (7) with connection to the outside of the container (2).
    [2]
    2. - A reactor (100) according to claim 1, characterized in that the first chamber (3) is equipped with at least
    - first stirring means (12);
    - an upper outlet (13), intended to allow the evacuation of gases;
    - a first pH probe (14); Y
    - First means for dosing (15) together or separately of a coagulant, an acidifier and an antifoam in the amount and proportions required to maintain the pH level between 5 and 6.5.
    [3]
    3. - A reactor (100) according to the preceding claim, characterized in that the coagulant comprises at least one of aluminum polyhydroxychlorosulfate (PACS) or aluminum hydroxychloride (PACI).
    [4]
    4. - A reactor (100) according to any one of the preceding claims, characterized in that the second chamber (4) is equipped with at least
    - a few second stirring means (16);
    - a second pH probe (17); Y
    - a few second means for the dosage (18) of flocculant in the amount and proportions required to maintain the pH level below 6.8.
    [5]
    5. - A reactor (100) according to the preceding claim, characterized in that the flocculant is a solid mixture of cationic flocculant, of medium or high cationicity and of high molecular weight with a minor part of an organic acid.
    [6]
    6. - A reactor (100) according to claims 3 and 4, characterized in that the ratio of volumes V1 of the first chamber (3) and V2 of the second chamber 4 meets the ratio V1 <V2; and because the first and second agitator means (12 and 16) comprising first and second propeller agitators or blades (12a, 16a) of vertical axis comprise the ratio of the rotational speeds R1 of the first propeller agitator or blades (12a) and R2 of the second propeller stirrer or blades (16a) meets the ratio R1> R2.
    [7]
    7. - A reactor (100) according to any one of the preceding claims, characterized in that the third chamber (5) is equipped with an overflow device (19), for communication between the compartment for quieting (6) the flocs and the sieve device (7), adjustable in height to be able to control the level of the free surface of the liquid manure being treated in the first, second and third chambers (3, 4 and 5) by effect of communicating vessels.
    [8]
    8. - A reactor (100) according to any one of the preceding claims, characterized in that the surfaces of the container in contact with the liquid manure being treated are polypropylene.
    [9]
    9. - A reactor (100) according to any one of the preceding claims, characterized in that the vessel (2) comprises two additional chambers, attached (21, 22), prepared to prepare in situ the flocculant dosed to the second chamber (4) .
    [10]
    10. - An installation for the treatment of slurry, which comprises
    - a solid-liquid separator (32) to obtain a solid fraction and a liquid fraction of slurry; Y
    - a reactor (100) according to any one of claims 1 to 9, whose reception inlet (10) is connected to the separator (32) for feeding to the reactor (100) of the liquid fraction of the slurries,
    the separator being arranged above the reactor (100).
    [11]
    11. - A process for the treatment of slurries comprising the steps of a) mechanically separating a liquid fraction (L) from a solid fraction (S) of the slurry, obtaining a solid fraction (Se) with 15-30% of dryness; Y
    b) subject the liquid fraction (L) obtained to a physical-chemical process in an essentially closed and sequential environment, first of coagulation, after flocculation and finally of filtration taking the appropriate measures so that at all times the separated liquid and solid parts they remain acidic to, among other factors, favor the presence of ammonium ion and avoid ammonia emissions.
    [12]
    12. - A method according to the preceding claim, characterized in that step b) comprises the operations of
    b3) subject the obtained liquid fraction to a chemical coagulation process under cheerful agitation and controlled conditions of the pH level between 5 and 6.5;
    b4) subject the coagulate resulting from operation b3) to a chemical flocculation process under moderate agitation and controlled conditions of the pH level below 6.8; b5) quench flocks with suspended solids obtained from operation b4) and spill them by overflow to a sieve device (7), preferably of the curved type, obtaining a recovered liquid fraction (Lr) (8) that crosses the sieve device (7 ) and a recovered solid fraction (Sr) that slides through the sieve device (7).
    [13]
    13. - A method according to the preceding claim, characterized in that the solid fraction (Sr) recovered in operation b5) is mixed with the solid fraction (S) of the slurry obtained in operation a), obtaining a final solid capable of being drying, intended for composting or to be used as fertilizer.
    [14]
    14. - A method according to any one of claims 11 to 13, characterized in that in operation b3) the pH value of the coagulation material or medium is monitored and because a coagulant is dosed together or separately, an acidifier and antifoam in the amount and proportions required to maintain the pH level between 5 and 6.5.
    [15]
    15. - A method according to the preceding claim, characterized in that the coagulant comprises at least one of aluminum polyhydroxychlorosulfate (PACS) or aluminum hydroxychloride (PACI) and one of sulfuric acid or hydrochloric acid.
    [16]
    16. - A method according to any one of claims 11 to 15, characterized in that in operation b4) the pH value of the material or the medium in the process of flocculation is monitored and that a flocculant is dosed which is a solid mixture of cationic flocculant, medium or high cationicity and high molecular weight with a minor part of an organic acid.
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    同族专利:
    公开号 | 公开日
    EP3819264A1|2021-05-12|
    ES2737573B2|2020-05-20|
    WO2020008093A1|2020-01-09|
    CA3104439A1|2020-01-09|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    ES2088749A1|1995-01-13|1996-08-16|Mulet Pitarch Dionisio M|Installation for purifying porcine waste and the like|
    ES2259257A1|2004-05-07|2006-09-16|Miguel Sierra Sanchez|Purines integral processing sequene comprises filtration, compaction homogenization and e.g. reverse osmosis|
    FR2744119B1|1996-01-29|1998-04-10|Rhone Poulenc Chimie|PROCESS FOR TREATING AQUEOUS LIQUID EFFLUENTS CONTAINING ORGANIC AND MINERAL MATERIALS FOR THEIR RECOVERY|
    CA2493615C|2002-07-26|2009-08-04|Gurunathan Lakshman|Hog manure treatment system|
    ES2302575B1|2005-06-13|2009-05-29|Josep Tapias Parcerisas|PROCEDURE AND DEVICE FOR THE TREATMENT OF PURINS.|
    WO2012109737A1|2011-02-17|2012-08-23|Anaergia Inc.|Organics and nutrient recovery from anaerobic digester residues|
    PL2874957T3|2012-07-20|2018-03-30|Kemira Oyj|Method of treating a digestate from a biogas process|
    法律状态:
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    申请号 | 申请日 | 专利标题
    ES201830672A|ES2737573B2|2018-07-04|2018-07-04|A reactor, system and procedure for treating liquid manure or digestates, especially suitable for treating slurry|ES201830672A| ES2737573B2|2018-07-04|2018-07-04|A reactor, system and procedure for treating liquid manure or digestates, especially suitable for treating slurry|
    EP19737805.2A| EP3819264A1|2018-07-04|2019-07-02|Reactor, system and method for the treatment of liquid manure or digestates, especially suitable for the treatment of slurry|
    PCT/ES2019/070465| WO2020008093A1|2018-07-04|2019-07-02|Reactor, system and method for the treatment of liquid manure or digestates, especially suitable for the treatment of slurry|
    CA3104439A| CA3104439A1|2018-07-04|2019-07-02|A reactor, a system and a method for the treatment of liquid manure or digestates, especially suitable for the treatment of slurry|
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