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    • 专利摘要:
    Method for the treatment of wastewater based on photooxidation by ultraviolet light. It is a new process for the treatment of water in general from the olive oil, agri-food, chemical, pharmaceutical, hospital, natural or residual industries contaminated by pesticides or other chemical compounds of different nature, with a medium organic load and high, with complex physical-chemical composition and difficult to be treated by other purification routes. The process is passed through a main stage that is a photo-oxidation that takes place in a photoreactor that receives enough artificial ultraviolet light to be fully illuminated. The process can be formed by a series of operations: Flocculation (A) - sedimentation (B) to induce the separation of a part of the organic matter for its later use in composting, followed by a photooxidation (C) induced by artificial ultraviolet light , either heterogeneously with energetic oxidants such as hydrogen peroxide or other peroxides, or homogeneously with energetic oxidants in the presence of liquid metal ion catalysts, such as iron salts, then a neutralization step (D) with a basic agent and applying coagulants/flocculants of mineral or organic origin followed by a decanting operation (D) and filtration-adsorption (E), which allows obtaining a treated water with a quality close to drinking. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2673673A1
    申请号:ES201631664
    申请日:2016-12-23
    公开日:2018-06-25
    发明作者:Gassan HODAIFA MERI；Cristina AGABO GARCÍA
    申请人:Universidad Pablo de Olavide；
    IPC主号:
    专利说明:

    Method for wastewater treatment based on ultraviolet light photooxidation
    FIELD OF THE INVENTION
    The present invention falls within the technical field of water treatment, and refers in particular to a process for the treatment of industrial wastewater with a high organic load and difficult to treat by conventional methods. The Method for the treatment of these waters applies a photooxidation that is carried out in a folorereactor that receives ultraviolet light.
    STATE OF THE TECHNIQUE
    Currently, wastewater treatment is based on conventional methods. Conventional processes can be summarized in different treatments: pretreatment, primary, secondary or biological, and tertiary. These methods mentioned above, are mostly applied to the treatment of urban wastewater and to a lesser extent in the treatment of industrial wastewater. They are characterized by the need to make high investments in infrastructures that occupy enough surface and labor to ensure the correct operation of the process.
    On the other hand, there are other methods that are called 'unconventional' that are currently studied at the research level but with little implementation at the industrial level, due to the little practical information in this regard, as they are not optimized processes at the industrial level, and considering them expensive without real reliable studies on their implementation. As unconventional methods can be mentioned ozonation, ozonation with hydrogen peroxide (O¡ H20 2), ozone-ultraviolet (O, lUV), H, O, / UV and O, lH, O, / UV, catalytic ozonation ( O, lCat.), Fenton (Fe "/ H, O,) and FotoFenton (Fe2 + IH20 2 / UV) and electrochemical methods.
    In this invention a process for the treatment of wastewater has been designed. Specifically, for the treatment of industrial wastewater difficult to treat (000> 3000 mg 0 2 / L) as is the case of wastewater from the olive oil industries and the processing of table olives. In the case of olive oil production there are different extraction systems, discontinuous system (press) and continuous system using a horizontal centrifuge (Decanter) that can contain three outputs "process known as three-phase" or two outputs "process known as two-phase "(FIGURE 1)
    More than 97% of the world's olive production is concentrated in the Mediterranean basin, with Spain being the main world producer (7.87) (106 tons), followed by Italy, Greece, Turkey, Morocco and Tunisia. Globally, the production of olives in 2013 exceeded 20) (106 tons (Food and Agriculture Organization of the United Nations-Statistics Division, 2016. http://faostat3.fao.org).
    More than 11 million hectares of olive trees are cultivated in the world, spread across five continents. Currently, 47 countries in which olive oil is produced. Olives grown for olive oil production are harvested from October to April in the northern hemisphere and from April to July in the southern hemisphere, although 98 percent of the world's olives are harvested in the Mediterranean region. There are approximately 12,000 olive oil mills in the world, more than 80 percent of which use centrifugal systems, where the centrifugal system using a two-outlet decanter is the most used in Spain. On the other hand, olive oil is consumed in more than 160 countries (International Olive-oil Council, 2016. 'MVW.internationaloliveoil.org).
    Olives usually reach oil mills with societies such as soil, leaves, branches, pesticide residues, small stones, etc. Therefore, as in all agri-food industries, it is necessary to apply a stage of pretreatment and conditioning of the raw material based on the washing of olives and the separation of these unwanted components, which causes the generation of a wastewater called "wastewater for washing olives" with a variable composition according to the protocol applicable in each oil mill in relation to the amount of water used and the frequency of renewal thereof. The olive oil obtained at the exit of the decanter also usually carries some impurities and remains of vegetation water that is necessary to separate it by washing oil in vertical centrifuges, which implies the generation of a wastewater called “wastewater from washing oil". In addition to these two main streams, other small amounts of wastewater are usually generated in the receiving hoppers and in the machine area.
    Currently, the olive oil industries do not have wastewater treatment plants generated at the different points of the olive oil extraction process. On the other hand, the current solution to this environmental problem is based on the management of wastewater through the use of evaporation rafts throughout the year or its limited use in irrigation of the olive grove itself. This fact is due to the lack of clear and mandatory environmental legislation that regulates its treatment although in Spain Royal Decree 849/1986, of April 11, which approves the Regulation of the Public Hydraulic Domain, which develops the titles Preliminary, 1, IV, V, VI and VII of Law 29/1985, of August 2, on Water has classified industrial activities and has established that the manufacture of olive oil is of class 3 and the characteristic parameters that they must be considered, as a minimum, in the estimation of the treatment of the discharge to public channel (Table 1). In this sense, the Confederation of Guadalquivir has also been resolving over the years in favor of spacing the oil and olive wash waters from the two-phase system on exclusively agricultural surfaces. The 2002/2003 campaign resolution specifies the following maximum parameters pH = 6-9, suspended solids <500 mg / I and DaD <2000 mg O2 / 1.
    Subsequently, this resolution has been modified over the years in terms of the parameter of the chemical oxygen demand up to DaO values <1000 mg O2 / 1 (Resolution of the year 2006).
    On the other hand, Royal Decree 1620/2007, of December 7, which establishes the legal regime for the reuse of purified water, establishing quality criteria according to their uses: urban, agricultural, industrial, recreational and environmental. The increase in this requirement will eventually lead to zero discharge, which would make the situation of the industries difficult.
    During the years 2001 to 2006 our research team has carried out a study of the characterization of the wastewater of the oil mills that operate with the two outlets system, registering pH values between 5 and 7, solids suspended in very variable quantities, values of DaD between 0.5 and 10000 mg O2 / 1 and DB05 values between 200 and 3000 mg 0, / 1.
    Between 2013 and 2016 And within the activities and tasks established in the Project of Excellence "Application of advanced oxidation technologies in the treatment of oil and olives wash waters, Ref .: AGR-7092" funded by the Ministry of Economy, Innovation, Science and Employment of the Junta de Andalucía and 5 of the Ministry of Economy and Competitiveness. The composition of these waters has varied according to the parameter as follows: pH ;;; 4.40-9.00, conductivity
    electric = 0.175-30.7 mS / cm, Turbidity = 134-5088 FTU, 000 = 474-44500 mg 0, / 1, TOC = 49-25000 mg / l.
    10 Table 1. Main characteristic parameters that should be considered, as a minimum, in the estimation of the treatment of the discharge.
    Parameter Maximum value
    pH 6.5-9.5
    Suspended solids, mg / I 300
    Sedimentable materials, mUI 2
    Thick solids missing
    OB05, mg / l 300
    000 mg / l 500
    Temperature, oC 3
    Color Invaluable in dissolution 1/40
    Aluminum (mg / I) 2
    Arsenic (mg / l) 1.0
    Barium (mgll) twenty
    Boron (mg / l) 10
    Cadmium (mg / l) 0.5
    Chromium 111 ((mg / l) 4
    Chrome VI (mg / l) 0.5
    Iron (mg / i) 10
    Manganese (mg / l) 10
    Nickel (mg / l) 10
    Mercury (mg / l) 0.1
    Lead (mg / l) 0.5
    Selenium (mg / l) 0.1
    Tin (mg / l) 10
    Copper (mg / l) 10
    Zinc (mg / l) twenty
    Metal toxics 3
    Cyanides (mg / I) one
    Chlorides (mg / l) 2,000
    Sulfides (mg / l) 2
    Sulfites (mg / l) 2
    Sulfates (mg / l) 2,000
    Fluorides (mg / I) 12
    Total phosphorus (mg / l) twenty
    Idem (K) 0.5
    Ammonia (mg / I) fifty
    Nitric Nitrogen (mg / I) twenty
    Oils and fats (mg / l) 40
    Phenols (mgll) one
    Aldehydes (mg / l) 2
    Detergents (mg / I) 6
    Pesticides (mg / I) 0.05
    ..
    (K) If the discharge occurs to lakes or reservoirs, the limit is reduced to 0.5 in the pretrial of eutrophic outbreaks.
    This variation in the physicochemical composition of the wastewater is due to the variation in the operating conditions between the different oil mills at the time of olive oil extraction, in addition to other reasons such as varieties of
    5 olives, origin of soil or tree, climatology, etc. All this makes clear the need for an effective treatment process that responds to the needs that our current society demands. As a solution to the problem posed, there is a procedure for sewage treatment, (ES2282043) where the Fenton reaction is described as a stage
    10 main of the purification process and is indicated for wastewater with average organic load up to 10000 mg O2 / 1.
    This invention presented is a more efficient new process that can treat wastewater with a high organic load up to 50,000 mg O2 / 1 and with an oxidation reactor degradation time of less than 30 minutes, producing a treated final water High quality very similar to drinking.
    DESCRIPTION OF THE INVENTION This is a process for wastewater treatment in general
    20 (from the olive oil, agri-food, chemical, pharmaceutical, hospital, natural or wastewater industries contaminated by pesticides or other chemical compounds of different natures, ..) without limitation by origin, with a medium and high organic load, with complex physicochemical composition and difficult to be treated by other means of purification.
    The main stage of the process is a chemical photooxidation, which allows a degradation of organic matter greater than 90%, in a very short degradation time (15-30 min) obtaining water at the exit of the process with a quality very close to potable. A turbidity of less than 10 FTU and mineral content that allows its discharge into public channels, use in different types of irrigation or its reuse in industrial processes that current European regulations allow. This process is characterized by the low cost of investment in equipment, very small land to occupy with a high productivity in final treated water. The process can be optimized and controlled remotely without the need for a fixed daily opera hand. The process allows the control of the degree of degradation of organic matter, which allows the control of the consumption of chemical reagents.
    Future treatment plants based on this process will be versatile, so that they can be used to purify wastewater from different sources, so that the investment made can be profitable in the event that the process is installed in industries that operate seasonally. (campaigns to collect the raw material), as is the case of the agri-food industries and specifically those of oil mills.
    DETAILED DESCRIPTION OF THE INVENTION This is a process for the treatment of wastewater in general (from the olive and agri-food oil industry, chemical, pharmaceutical, hospital, natural or wastewater contaminated by pesticides or other chemical compounds of different natures , ...) without limitation by origin, with a low, medium and high organic load, with complex physical-chemical composition and difficult to be treated by other means of purification.
    The process goes through a main stage which is a photooxidation that is carried out in a photoreactor that receives artificial ultraviolet light sufficient to be fully illuminated. The operations that make up the process may vary depending on the origin of the wastewater.
    In general, the process can be formed by a series of operations such as: Flocculation (A) -seeding (8) to induce the separation of a part of the organic matter for later use in composting, followed by a photooxidation induced by ultraviolet light artificial (C), then a neutralization stage (D) adjusting to pH between 6 and 9 with a basic agent and applying coagulants / flocculants of mineral or organic origin, followed by a decanting operation (D), then a filtration stage -absorption (E) to eliminate the rest of organic and inorganic matter that could not be separated by the previous stage (flocculation (D) sedimentation (E »), which allows to obtain a treated water with a quality close to drinking, suitable of being reused in the industrial process itself, for the different types of irrigation set in European regulations or being poured into public channels.
    The design of the main stage, where more degradation / elimination of organic matter contained in the wastewater is achieved (DOOeliminated and COTeliminated> 80%), can be carried out in different ways:
    i) In the case of treating wastewater with a relatively low organic load
    (DOO <1000 mg 0 2 / L) can be performed by applying a photolysis (ultraviolet light
    artificial alone) or photolysis supported with the presence of some oxidizing agent.
    ii) In the case of treating residual water with a medium organic load (1000 mg
    0 2 / L <000 <10000 mg 0 2 / L) it is necessary to use changing ultraviolet light
    and oxidizing agent.
    iii) For wastewater with high organic loads (10,000 mg 02 / L <000 <
    50,000 mg 0 2 / L) the solution will be based on the joint use of light
    u Itraviol eta / cata I izador / age nte oxi da nte.
    In the case of wastewater with medium and high organic loads the photoxidation reaction can be carried out in the photoreactor in a homogeneous way, using energy oxidizing agents such as hydrogen peroxide (H20 2) or other oxidizing peroxides (potassium peroxymethyl sulfate, KHSOs, persulfate of sodium, Na2S20 S, etc.) and metallic catalysts in a liquid state such as iron (Fe), titanium (Ti), manganese (Mn), ... and its variants, or in a heterogeneous way using, apart from the agents energy oxidants mentioned above, solid state metal catalysts such as iron oxides, titanium, manganese, etc. or said catalysts supported on organic supports such as activated carbon, olive bone, etc. or in inorganic supports such as silica gel, zeolites or other synthesized mineral supports.
    The photoreactor used in the chemical oxidation stage in the homogeneous phase with the objective of eliminating organic matter can be of different types: (1) Agitated tank reactor with one or more ultraviolet lamps submerged vertically, horizontally, or even inclined with or without recirculation, (2) Tubular type reactor with a
    or more ultraviolet lamps submerged in the center of the tubular reactor or placed on the walls thereof with or without recirculation, (3) Agitated tank type reactors, such as those mentioned above, placed in series with or without recirculation. (4) Unitary or series bubble column type reactors with one or more ultraviolet lamps submerged vertically, horizontally, or even inclined with or without recirculation, (5) Other types of reactors such as rectangular with one or more ultraviolet lamps submerged vertically, horizontally, or even inclined with or without recirculation.
    The photoreactor used in the stage of chemical oxidation in the heterogeneous phase with the objective of eliminating organic matter may be of the same types mentioned in the photoreactor operating in the homogeneous phase with the following specifications in relation to the catalyst: (i) The catalyst may be suspended in wastewater. (ii) The catalyst can be placed in the blades used in the agitation system. (iii) The catalyst can be placed at the bottom of the reactor (in the case of unitary or series stirred tank type reactors), in the form of one or more vertical, horizontal or inclined bars. (iv) The catalyst can be fixed inside oxidation-resistant plastic meshes or inside stainless steel meshes.
    In the case of treating wastewater with a very high organic load with a DaO greater than 50,000 mg 02 / L, other operations based on membrane technology, ion exchange, ultrasound, etc. could be incorporated.
    DESCRIPTION OF THE FIGURES
    Figure 1. Olive oil production systems (Discontinuous: Press and continuous using "Decanter" horizontal centrifuges with 3 outputs or 2 outputs).
    Figure 2. Collect the essential unit operations that form the treatment process: A) Reception-homogenization-flocculation tank for wastewater, oil washing (1) and olives washing (2) or wastewater of any kind, and formation of pellets by the addition of an organic flocculant or inorganic coagulant (3). B) Decanter, regardless of the type to be used, for the separation of the solid phase (4) and obtaining a clear phase that passes to the next operation. C) Photooxidation in which organic matter is degraded and transformed into carbon dioxide, water and other simpler products. The photooxidation is carried out in a photoreactor that will be equipped with a sufficient number of lamps (5) that emit ultraviolet light and that allow the complete illumination of the reactor. Several streams are added to this reactor, at least one of them will be the oxidant to be used (6) and the other the catalyst used (7). The residence time in the photoreactor to carry out the degradation of the organic matter is 15-30 min. Once the oxidation stage is finished, the treated water passes to a neutralization-f1oculation tank (O), where the pH is adjusted with a alkaline solution (8) and an organic formula (9) is added. Then the water is passed to a Decanter
    (E) which allows the separation of treated water from sludge (10) formed by the effect of the fluid (9). At the outlet of the Decanter (E) the treated water passes through a filtration-adsorption column (s) through a filter body that can be any porous material such as sea sand, olive bone, wood crushed, etc. or a mixture of different filter materials and adsorbents such as a mixture of sea sand and activated carbon. At the end of this process, the final treated water (11) is obtained with sufficient quality to be used in irrigation, in the process itself or simply to be poured into public channels.
    Figure 3. This is a schematic drawing of a stirred tank photoreactor and the possible positions of the ultraviolet lamps: Horizontal (A) and inclined (B) position. In addition, the vertical position shown in Figure 2 ..
    Figure 4. This is a schematic drawing of a possible photoreactor, regardless of its type, with recirculation.
    Figure 5. It shows a schematic drawing of a tubular photoreactor with different positions of the ultraviolet lamps: Central lamp (s) or several ultraviolet lamps placed on the wall of the photoreactor.
    Figure 6. Schematic drawing shows possible configurations of the photoreactor in the case of operating using a heterogeneous reaction. i) Using solid catalyst in suspension (in this case the reactor would be as shown in Figure 2). ii) Solid catalyst placed at the bottom of the photoreactor (A). iii) Solid catalyst placed in the form of bars (vertical, horizontal or inclined) submerged in the photoreactor (8). Catalyst placed on the surface of the stirring blades (C).
    EXAMPLES
    EXAMPLE 1: Treatment of wastewater difficult to treat with medium and high organic load following a series of operations that includes an essential stage where maximum degradation of organic matter is performed based on a photooxidation.
    The process that describes the treatment of wastewater difficult to treat with medium and high organic load following a series of operations that includes an essential stage where maximum degradation of organic matter is performed based on a photooxidation. However, this process can be used by making some modifications to treat low medium organic water.
    The treatment process consists of the following essential unit operations (Figure 2): wastewater from oil washing, olive washing, wastewater obtained during cleaning of the machine areas and water generated in the area of the receiving hoppers of olives ° raw wastewater generated in industrial processes in general, can be incorporated into the new treatment process without prior modifications, or mixed with each other, in case there is more than one effluent of wastewater generated, with the aim of controlling the load organic at the entrance of the treatment process. They are introduced into the reception-homogenization-flocculation tank (A) where they are flocculated and passed to the Decanter
    (B) for the separation of the solid-liquid phases, the solid phase or sludge (4) is treated by composting and the liquid phase with an organic load less than the initial phase is passed to photoxidation (C) using artificial ultraviolet light (5). ), and adding an energy oxidant (6), such as hydrogen peroxide, and a liquid or solid catalyst (7), such as ferric chloride 'FeCI3' or iron oxide 111 'HFe02' depending on the type of reaction. Water obtained after photooxidation will accumulate in a neutralization-flocculation tank (O) where the pH will be adjusted to a value that can vary between 6 and 9 using an alkaline solution, such as sodium hydroxide (8), and add a flocculant (9) to flocculate the organic matter that has been suspended. The removal of organic matter and catalyst residues, in the case of a homogeneous reaction, will be carried out in a Decanter (E). The creamy sludge generated (10) will be returned to the head of the process, to the homogenization-f1oculation reception tank (A). Then the flocculated water will be passed to a filtration-adsorption operation (F) using as a filter body a mixture of sea sand and activated carbon. The treated water will have a reduction in DOO of over 95%.
    In the stages of reception-homogenization-f1oculation (A) and decantation (B) of the raw wastewater, inorganic coagulants, such as Bentonite and Smectite and / or organic flocculants, such as those produced by the company Nalca, can be used. The removal rates in the case of inorganic coagulants can reach up to 18% of the initial DOO, 20% of initial COD and 30% of initial turbidity. In the case of organic formulants, the removal percentages can reach 20% of the initial DOO, 40% of initial COD and 74% of the initial turbidity.
    The photooxidation stage can be carried out in different ways depending on the composition of the wastewater to be treated:
    one. In the case of a mixture of oil and olive wash waters with a relatively low organic load (000 = 1388 mg 0 2 / L, COT = 215 mg / L, Total Nitrogen 'NT' = 23.1 mg / L ). Applying oxidation with ultraviolet light only (photolysis) is more than enough to reduce its organic load to 000 = 269 mg O, / L, TOC = 79 mg / L, NT = 16.5 mg / L. This treated water can be used in irrigation or poured into public channels. However, in the case of mixtures of waste water from oil and olives washing with a medium-high organic load (000 = 18661 mg O, / L, COT = 4057 mg / L, NT = 71, 3 mg / L) . A photolysis allows to obtain a water with the following parameters: 000 = 12754 mg O, / L, COT = 2972 mg / L, NT = 37 mg / L. In this case, the photolysis treatment is not enough to use the water in irrigation, or in the process itself, or to pour into public channels and the application of a more aggressive photooxidation combining ultraviolet light, hydrogen peroxide with or without catalyst.
    2. In the case of using a mixture of oil and olive wash waters with a high organic load (COD = 8780 mg O, / L, COl = 1063 mg / L, Total Nitrogen 'NT' = 35 mg / L and phenolic compounds total = 38.3 mg / L). The quality of the final water obtained, after a photooxidation with oxidizing agent and catalyst (UV / FeClj H20 2), the separation of the solid-liquid phases by natural sedimentation without f10culant or coagulant, will be the following: COD = 121 mg O, / L, COl = 18.8 mg / L, Total nitrogen 'NT' = 4.7 mg / L, total phenolic compounds = 0.11 mg / L and turbidity = 1.21 FTU). Final water with sufficient quality for irrigation, discharged into a public channel.
    3. In the previous example, but with the addition of a coagulant or f10culant in the neutralization operation (O) and then solid-liquid phase separation (E), the quality of the final water will be as follows: DaO = 30.2 mg 02 / L, TOC = 6.9 mg / L, Total Nitrogen 'NT' = 3.87 mg / L, total phenolic compounds = 0.29 mg / L and turbidity = 1.65 FTU). Final water with quality close to drinking enough for irrigation, discharged into a public channel. If, in addition, filtration-adsorption (F) is applied, the resulting water may have sufficient quality for reuse in the industrial process itself.
    The photoreactor (F), in addition to the configuration shown in Figure 2, can be configured with ultraviolet lamps in a horizontal or inclined position, according to Figure 3. The configuration of the photoreactor with recirculation, regardless of its type will be as shown in the scheme of Figure 4.
    The photoreactor can be tubular tubular (Figure 5) with different positions of the ultraviolet lamps: Central lamp (s) or several ultraviolet lamps placed on the wall of the photoreactor.
    If the photoreactor operates using a heterogeneous reaction, its configuration may be (Figure 6): i) Using solid catalyst in suspension (in this case the reactor would be as shown in Fig. 1). ii) Solid catalyst placed at the bottom of the photoreactor (A). iii) Solid catalyst placed in the form of bars (vertical, horizontal or inclined) submerged in the photoreactor (B). Catalyst placed on the surface of the stirring blades (C).
    权利要求:
    Claims (13)
    [1]
    1. Industrial wastewater treatment procedure, characterized by being able to treat wastewater with a mainly medium organic load
    or high (000> 5 g O, / L) and comprising (figure 2):
    [8]
    8. pretreatment based on a stage of f10culation (A) -seeding (8) by the addition of coagulants or f10culants (3);
    b. photooxidation using artificial ultraviolet light (5), oxidizing agent (6) and a catalyst (7) as a key operation, to reduce the organic matter content of wastewater in a very short time of 15-30 min (C);
    C. neutralization-f1oculation (D) by adjusting the pH with a basic solution (8) and adding ph10culants (9);
    d. settling (E) of water formulated to separate solids (10);
    and. filtration (F) of treated and formulated water. This filtration is performed on a filtration column (F) that contains a filter body that can be sea sand, olive bone, zeolite, or a combination of different adsorbent materials.
    [2]
    2. Process of degradation of the organic load in industrial wastewater, according to claim 1, characterized by the use of a homogeneous photooxidation reaction, using artificial ultraviolet light alone or in combination with a liquid energy oxidant and / or a catalyst, in the form of ions metallic in liquid state.
    [3]
    3. Method of elimination of the organic load in industrial wastewater, according to claim 1, characterized by the use of a heterogeneous photooxidation reaction, using artificial ultraviolet light combined with a liquid energy oxidant and a solid form catalyst or metal ions in mineral supports like silica gel or zeolite.
    [4]
    Four. Procedure for eliminating the organic load in industrial wastewater, according to claim 2 and 3, characterized by the use of some of the following oxidation energy agents: hydrogen peroxide, potassium peroxymethyl sulfate, KHSOs, sodium persulfate, Na2S20 a.
    [5]
    5. Process of elimination of the organic load in industrial wastewater, according to claim 2, characterized by the use as catalyst of the oxidation of any of the following compounds: FeCI3 ferric chloride, iron, ferrous or ferric salts, or as the product of a chemical reaction in a liquid state.
    [6]
    6. Wastewater treatment method according to claim 3, characterized by the use of metal oxides such as manganese oxide, Mn02, or iron oxide 111, HFe02, or other iron salts, ferrous or ferric, immobilized in organic supports such as active or inorganic carbon such as silica gel-FeCI3.
    [7]
    7. Wastewater treatment method according to claim 1, 2, 3, characterized by the use of a photoreactor or several series photoreactors stirred or tubular tank type with or without recirculation.
    [8]
    8. Wastewater treatment method according to claim 7, characterized by the placement of the ultraviolet lamps vertically, horizontally or inclined in the stirred tank reactor or in the central position or on the walls in the case of the use of the tubular reactor.
    [9]
    9. Wastewater treatment process according to claims 3 and 7, characterized by the placement of the catalyst at the bottom of the reactor, such as vertical or horizontal bars that cross the reactor body, supported on the agitator blades or simply the catalyst loose and suspended in the reaction mixture.
    [10]
    10. Wastewater treatment method according to claim 1, characterized by the direct entry of wastewater to the pretreatment stage, tank A, or prior natural sedimentation by gravity in homogenization rafts.
    [11 ]
    eleven . Wastewater treatment method according to claim 1, characterized by filtration of the water from the decanter E in adsorption-filtration columns using combined filtering body of sea sand and activated carbon, or any other filtering and / or adsorbent body of organic or mineral origin. This operation can be carried out in a single filter or several in parallel or in series.
    [12]
    12. Wastewater treatment method according to previous claims, characterized by the use of other operations (use of membranes, ion exchangers) with the aim of refining or adjusting the quality of the treated water to the final destination of the waters obtained especially, when it is about reuse in the process itself or as regenerated drinking water.
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    同族专利:
    公开号 | 公开日
    ES2673673B1|2019-01-04|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    ES2282043A1|2006-03-28|2007-10-01|Leopoldo Martinez Nieto|Method for purification of sewage from oil mills or chemical industries involves natural sedimenting or eliminating solids in suspension of water|CN111517447A|2020-05-09|2020-08-11|张海兵|Industrial wastewater catalytic oxidation equipment based on Internet of things|
    CN113105046A|2021-04-28|2021-07-13|四川大学|Method for synchronously removing organic pollutants and suspended matters in water|
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