Organic wastewater treatment system and treatment method

Abstract

The present application relates to the technical field of organic wastewater treatment, and particularly relates to an organic wastewater treatment system and a treatment method, which comprises an electrolysis reaction tank, a combined reactor, a dissolved gas component and an ozone generation component, and the organic wastewater treatment system comprises a first mode and a second mode; the first mode comprises that organic wastewater passes through the dissolved gas component and then returns to the electrolysis reaction tank, and the ozone generation component supplies gas to the electrolysis reaction tank through the dissolved gas component; the second mode comprises that liquid passes through the electrolysis reaction tank, the dissolved gas component and the combined reactor and then returns to the electrolysis reaction tank, and the ozone generation component supplies gas to the combined reactor through the dissolved gas component; the first mode and the second mode do not work at the same time. In the first mode, the relatively easy-to-oxidize and degrade substances in the organic wastewater are oxidized and degraded, and in the second mode, the relatively difficult-to-degrade and oxidize substances are subjected to deep treatment in the ultraviolet+hydrogen peroxide+ozone pressurized coupling oxidation mode, so that the oxidation efficiency is improved, the equipment size is reduced and the control is simple.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of organic wastewater treatment, and particularly relates to an organic wastewater treatment system and a treatment method. BACKGROUND

[0002] Biodegradation of high-concentration organic wastewater consumes a large amount of dissolved oxygen, causing the receiving water body to be anoxic, thereby causing a large number of aquatic plants and animals to die and water quality and the environment to deteriorate. Meanwhile, high-concentration organic wastewater contains a large amount of refractory and toxic organic substances, such as benzene, nitrobenzene, halogenated compounds, azo dyes, phenols and other organic refractory pollutants. These substances accumulate in the natural environment such as water and soil, and finally enter the human body, endangering human health.

[0003] Biological treatment technology is one of the most common methods in an organic wastewater pollution treatment system. Through the metabolic action of microorganisms, organic matter in organic wastewater is oxidized, decomposed and adsorbed, and is converted into harmless stable substances, so that the water quality is purified. However, this method is limited by the concentration of organic matter, and can only treat low-concentration organic wastewater. High-concentration coking organic wastewater and organic wastewater containing oil, ammonia, phenols and other organic matter need to be diluted and pretreated. In addition, microorganisms are sensitive to environmental changes, and water quality has a huge impact on the treatment effect of biological methods. If the water contains heavy metals, toxic substances and the like, the growth of microorganisms will be inhibited, and even the microorganisms will be inactivated, thereby prolonging the treatment time, increasing the operation cost and reducing the organic wastewater treatment efficiency. SUMMARY

[0004] (I) Objectives

[0005] The present application aims to provide an organic wastewater treatment system and a treatment method capable of improving the treatment efficiency of high-concentration organic wastewater and being pollution-free to the ecological environment.

[0006] (II) Technical solutions

[0007] To solve the above problems, the present application provides an organic wastewater treatment system, comprising: an electrolysis reaction tank, a combined reactor, a dissolved gas component and an ozone generation component,

[0008] The organic wastewater treatment system comprises a first mode and a second mode;

[0009] The first mode comprises that organic wastewater passes through the dissolved gas component and then returns to the electrolysis reaction tank, and the ozone generation component supplies gas to the electrolysis reaction tank through the dissolved gas component;

[0010] The second mode comprises that liquid passes through the electrolysis reaction tank, the dissolved gas component and the combined reactor and then returns to the electrolysis reaction tank, and the ozone generation component supplies gas to the combined reactor through the dissolved gas component.

[0011] The first mode and the second mode are not simultaneously operated.

[0012] In another aspect of the present application, preferably, the electrolysis reaction tank comprises a reaction tank body, a slag blocking component, a slag scraping component and an electrolysis component; the electrolysis component is arranged in the reaction tank body, the slag blocking component covers the top surface of the reaction tank body, and the slag scraping component scrapes the slag intercepted by the slag blocking component.

[0013] In another aspect of the present application, preferably, the combined reactor comprises a pressure vessel tank and an ultraviolet lamp, the ozone generation component, the dissolved gas component and the pressure vessel tank are sequentially communicated, and the ultraviolet lamp is arranged in the pressure vessel tank.

[0014] In another aspect of the present application, preferably, the electrolysis component comprises an anode, a cathode and a power supply, and the anode material is titanium-based iridium oxide-iridium oxide material.

[0015] In another aspect of the present application, preferably, further comprising an air compressor and a dosing component, the air compressor is connected with the ozone generation component and the combined reactor respectively, and the dosing component is connected with the electrolysis reaction tank and the combined reactor respectively.

[0016] When the first mode, the air compressor supplies air to the ozone generation component, and the dosing component adds chemicals to the electrolysis reaction tank.

[0017] When the second mode, the air compressor supplies air to the ozone generation component and the combined reactor respectively, and the dosing component adds chemicals to the combined reactor.

[0018] In another aspect of the present application, preferably, further comprising a filtering component, which is communicated with the electrolysis reaction tank.

[0019] In another aspect of the present application, preferably, a method for treating organic wastewater, the method for treating organic wastewater utilizes the organic wastewater treatment system as described above to treat organic wastewater, and the method comprises the following steps:

[0020] Step 100: in the first mode, the organic wastewater is put into the electrolysis reaction tank, flocculants and chlorine ion concentration regulators are added in the electrolysis reaction tank, electrolysis cycle is carried out, and a first reaction product is obtained;

[0021] Step 200: the first reaction product is put into the combined reactor to carry out oxidation reaction, and a second reaction product is obtained;

[0022] Step 300: in the second mode, H2O2 is added in the combined reactor to carry out oxidation-electrolysis cycle, and a third reaction product is obtained;

[0023] Step 400: in the first mode, the third reactant is put into the electrolysis reaction tank, and an electrolysis cycle is carried out to obtain a fourth reactant, and the cycle is ended.

[0024] In another aspect of the present application, preferably,

[0025] The step 100 of adding the flocculating agent in the electrolysis reaction tank comprises:

[0026] According to the quality of the organic wastewater, a predetermined proportion of flocculating agent is weighed, and the predetermined proportion is 0.1-0.5 kg of flocculating agent per ton of wastewater, and the flocculating agent comprises polyacrylamide;

[0027] The weighed flocculating agent is diluted, and the dilution ratio is 0.1%-0.5% to obtain the diluted flocculating agent;

[0028] The diluted flocculating agent is added to the electrolysis reaction tank at a rate of 200 ml / h;

[0029] The step 100 of adding the flocculating agent in the electrolysis reaction tank comprises:

[0030] The chloridion concentration regulator is added to the electrolysis reaction tank to make the chloridion concentration in the electrolysis reaction tank reach 5000 mg / L.

[0031] In another aspect of the present application, preferably, the step 300: in the second mode, H2O2 is added to the combined reactor to carry out an oxidation-electrolysis cycle to obtain a third reactant comprises:

[0032] The pressure in the combined reactor is 0.4 MP;

[0033] The amount of H2O2 added is:

[0034] V(H2O2) = M(COD mg) / C(H2O2 mg / ml),

[0035] Wherein, V(H2O2) represents the volume of H2O2 added, M(COD mg) represents the mass of chemical oxygen demand in the organic wastewater, and C(H2O2 mg / ml) represents the concentration of H2O2.

[0036] In another aspect of the present application, preferably, it further comprises:

[0037] Step 500: the fourth reactant is filtered by a high-pressure pump and a filter.

[0038] (III) Beneficial effects

[0039] The above technical solutions of the present application have the following beneficial technical effects:

[0040] The present application processes organic wastewater through a first mode and a second mode, in the first mode, the organic wastewater is oxidized and degraded, in the second mode, the more difficult to degrade oxidized substances are subjected to deep processing in the coupling oxidation mode of ultraviolet + hydrogen peroxide + ozone (pressurized), so as to improve the oxidation efficiency, reduce the equipment size and simplify the control. BRIEF DESCRIPTION OF DRAWINGS

[0041] Figure 1 is a schematic diagram of the overall structure of an embodiment of the present application;

[0042] Figure 2 is a graph of the changes of COD, color, and pH in the organic wastewater of Example Three with reaction time;

[0043] Figure 3 is a graph of the changes of COD, color, and pH in the organic wastewater of Example Four with reaction time;

[0044] Figure 4 is a graph of the changes of COD, color, and pH in the organic wastewater of Example Five with reaction time;

[0045] REFERENCE NUMERALS:

[0046] 1: electrolytic reaction tank, 2: combined reactor, 3: dissolved gas component, 4: ozone generation component, 5: air compressor, 6: dosing component, 1-1: reaction tank body, 1-2: slag blocking component, 1-3: slag scraping component, 1-4: electrolysis component, 2-1: pressure vessel tank, 2-2: ultraviolet lamp. DETAILED DESCRIPTION

[0047] To make the objectives, technical solutions and advantages of the present application clearer, further detailed description will be given below in conjunction with specific embodiments and with reference to the drawings. It should be understood that these descriptions are only exemplary and are not intended to limit the scope of the present application. In addition, in the following description, the description of well-known structures and technologies is omitted to avoid unnecessary confusion of the concept of the present application.

[0048] In the drawings, schematic diagrams of layer structures according to embodiments of the present application are shown. These drawings are not drawn to scale, in which certain details are exaggerated for the purpose of clarity, and certain details can be omitted. The shapes of various regions, layers shown in the drawings, and their relative sizes and positional relationships can deviate in actuality due to manufacturing tolerances or technical limitations, and regions / layers with different shapes, sizes, relative positions can be additionally designed by those skilled in the art according to actual needs.

[0049] Obviously, the described embodiments are part of the embodiments of the present application, rather than all the embodiments. Based on the embodiments in the present application, all other embodiments obtained by those skilled in the art without creative labor fall within the scope of protection of the present application.

[0050] In the description of the present application, it should be noted that the terms "first", "second", "third" are only for the purpose of description, and cannot be understood as indicating or implying relative importance.

[0051] In addition, the technical features involved in the different embodiments of the application described below can be combined with each other as long as there is no conflict between them.

[0052] The present application will be described in more detail below with reference to the accompanying drawings. In each of the drawings, the same elements are denoted by similar reference numerals. Each part of the drawings is not drawn to scale for the sake of clarity.

[0053] Embodiment one

[0054] An organic wastewater treatment system, Figure 1 The overall structure of one embodiment of the present application is shown in the schematic diagram as shown in the figure, Figure 1 including: electrolytic reaction tank 1, combined reactor 2, dissolved gas component 3 and ozone generation component 4,

[0055] The organic wastewater treatment system includes a first mode and a second mode;

[0056] The first mode includes organic wastewater from the electrolytic reaction tank 1 through the dissolved gas component 3 to the electrolytic reaction tank 1, and the ozone generation component 4 supplies gas to the electrolytic reaction tank 1 through the dissolved gas component 3;

[0057] In the first mode, to increase the oxidation effect, the ozone generation component 4 supplies gas to the electrolytic reaction tank 1 through the dissolved gas component 3, further, the ozone generation component 4 supplies gas to the bottom of the electrolytic reaction tank 1 through the dissolved gas component 3, increases the ozone coupling oxidation, and improves the oxidation efficiency. Further, in this embodiment, under the condition of ozone aeration, the electrode oxidation degradation is carried out for 1-2h, and the organic matter in the organic wastewater is oxidized into CO2 and H2O;

[0058] The second mode includes liquid from the electrolytic reaction tank 1, the dissolved gas component 3 and the combined reactor 2 to the electrolytic reaction tank 1, and the ozone generation component 4 supplies gas to the combined reactor 2 through the dissolved gas component 3; In the second mode, the relatively difficult degradable oxidized substances are treated in depth in the ultraviolet + hydrogen peroxide + ozone (pressurized) coupling oxidation mode, and the oxidation efficiency is improved,

[0059] The first mode and the second mode do not work at the same time.

[0060] Further, in the embodiment, the electrolysis reaction tank 1 comprises a reaction tank body 1-1, a slag blocking component 1-2, a slag scraping component 1-3 and an electrolysis component 1-4; the electrolysis component 1-4 is arranged in the reaction tank body 1-1, the slag blocking component 1-2 covers the top surface of the reaction tank body 1-1, and the slag scraping component 1-3 scrapes the slag intercepted by the slag blocking component 1-2.

[0061] Further, in the embodiment, the combined reactor 2 comprises a pressure vessel tank 2-1 and a UV lamp 2-2, the ozone generating component 4, the gas dissolving component 3 and the pressure vessel tank 2-1 are sequentially communicated, and the UV lamp 2-2 is arranged in the pressure vessel tank 2-1.

[0062] Further, the electrolysis component 1-4 comprises an anode, a cathode and a power supply, the anode material is titanium-based iridium oxide-iridium oxide material. Further, the cathode material is 304 steel plate, and the electrode spacing is 20 mm; because the electrode spacing is reduced, the inter-electrode resistance is reduced, thereby reducing the energy consumption of electrochemical treatment, which is beneficial to the removal of COD, but too low spacing is easy to cause short circuit, which has a great influence on the safety of the equipment;

[0063] Further, in the embodiment, the electrolysis component 1-4 adopts a suspended fixed particle electrode string, which can increase the treatment capacity of the unit area of organic wastewater, save the equipment cost, and the electrode string is convenient to take out and regenerate the particle electrode;

[0064] Further, the anode surface modified polypyrrole can not only improve the anode oxidation efficiency by adsorbing pollutants, but also can adsorb small molecular organic pollutants with low concentration and dispersion, so as to ensure that the organic matter is completely removed;

[0065] Further, the air compressor 5 is connected with the ozone generating component 4 and the combined reactor 2 respectively, and the dosing component 6 is connected with the electrolysis reaction tank 1 and the combined reactor 2 respectively;

[0066] When the first mode, the air compressor 5 supplies air to the ozone generating component 4, and the dosing component 6 adds medicine to the electrolysis reaction tank 1;

[0067] When the second mode, the air compressor 5 supplies air to the ozone generating component 4 and the combined reactor 2 respectively, and the dosing component 6 adds medicine to the combined reactor 2.

[0068] Further, in the embodiment, a filtering component is further included, and the filtering component is communicated with the electrolysis reaction tank.

[0069] In the first mode, the organic wastewater is oxidized and degraded, and the photon energy of the ultraviolet lamp in the second mode can directly open and cut the covalent bond in the organic molecule, activate the organic molecule in the sewage, and decompose it into ions, free atoms, and excited molecules. And the ultraviolet lamp and the ozone generator jointly produce continuous photosensitive reaction to ensure that the organic matter is completely removed.

[0070] Example Two

[0071] An organic wastewater treatment method using the organic wastewater treatment system as described above to treat organic wastewater, the method comprising the following steps:

[0072] Step 100: In the first mode, the organic wastewater is put into the electrolysis reaction tank, a flocculating agent and a chlorine ion concentration regulator are added to the electrolysis reaction tank, and electrolysis is carried out to obtain a first reaction product;

[0073] Further, in the embodiment, adding a flocculating agent to the electrolysis reaction tank comprises:

[0074] According to the quality of the organic wastewater, a predetermined proportion of the flocculating agent is weighed, and the predetermined proportion is 0.1-0.5 kg of flocculating agent per ton of sewage. The flocculating agent includes polyacrylamide;

[0075] The weighed flocculating agent is diluted at a dilution ratio of 0.1%-0.5% to obtain a diluted flocculating agent;

[0076] The diluted flocculating agent is added to the electrolysis reaction tank at a rate of 180-220 ml / h;

[0077] The step 100 of adding a chlorine ion concentration regulator to the electrolysis reaction tank comprises:

[0078] The chlorine ion concentration regulator is added to the electrolysis reaction tank to a chlorine ion concentration of 4500-5500 mg / L in the electrolysis reaction tank.

[0079] The reaction time of step 100 is not limited here, and the reaction time can be determined by the color of the first reaction product,

[0080] High-concentration organic wastewater passes through the reaction tank body, and a flocculating agent is added through the dosing component. The flocculating reaction is carried out, and the suspended matter after the flocculating reaction can be brought out of the water body by the electrolysis-generated micro-bubbles, floated on the surface of the residue blocking component, and scraped into the waste residue tank through the residue scraping component. It can also be intercepted by the residue blocking component when the organic wastewater passes through the dissolved gas component 3 after the electrolysis reaction tank 1 and then enters the electrolysis reaction tank 1, and scraped into the waste residue tank through the residue scraping component;

[0081] Increasing the concentration of chloride ions in the organic wastewater is conducive to accelerating the removal of COD, and the effect of chloride ion concentration on COD removal is mainly due to the indirect oxidation mechanism of the reaction system for COD removal, and the chloride ion concentration is undoubtedly an important influencing parameter; alternatively, in the present embodiment, when the concentration of chloride ions in the electrolysis reaction tank is 4500-5500 mg / L, the COD removal rate is higher;

[0082] Here, the current density of the electrolysis reaction in step 100 is not limited, and alternatively, the current density is 25 mA / cm under the condition that the electrode plate spacing is 2 cm 2 ~ 65.35 mA / cm 2 The increase in current density improves the yield of chlorine gas, because chlorine gas is the substance that generates the subsequent oxidant for removing organic pollutants, and the current density within the scope of the present embodiment helps to increase the COD reduction speed in the biochemical effluent, i.e., the amount of COD removed per unit time increases;

[0083] Step 200: placing the first reactant into a combined reactor for oxidation reaction to obtain a second reactant;

[0084] Here, the reaction time of step 200 is not limited, and alternatively, in the present embodiment, the reaction time of step 200 is 1-2 h, and here, the specific content of the component for oxidation in the combined reactor is also not limited, and alternatively, it can be a pressure vessel tank, an ozone generator, and a ultraviolet lamp for simultaneous oxidation, or it can be one or two components for oxidation; due to the modular design between devices, different modules or the number of modules can be selected to improve the treatment efficiency according to different organic wastewater concentrations and water quantities;

[0085] Step 300: in the second mode, adding H2O2 in the combined reactor for oxidation-electrolysis cycle to obtain a third reactant; comprising:

[0086] The pressure in the combined reactor is 0.3-0.5 MP;

[0087] The amount of H2O2 added is:

[0088] V(H2O2) = M(COD mg) / C(H2O2 mg / ml),

[0089] wherein V(H2O2) represents the volume of H2O2 added, M(COD mg) represents the mass of chemical oxygen demand in the organic wastewater, and C(H2O2 mg / ml) represents the concentration of H2O2;

[0090] When the combined reactor is in operation, the low-pressure ultraviolet mercury lamp can emit ultraviolet light at 254 nm and 185 nm simultaneously, and the photon energy of the light at the two wavelengths can directly open and cut the covalent bonds in the organic molecules, so that the organic molecules in the sewage are activated and decomposed into ions, free atoms, excited molecules, etc. At the same time, the light energy of the ultraviolet light at 185 nm can combine the oxygen in the air into ozone; and the light energy of the ultraviolet light at 254 nm can decompose the ozone into oxygen and active oxygen. This photochemical oxidation process is continuous, and under the irradiation of the two short-wave ultraviolet lights, the ozone is continuously generated and decomposed, and the active oxygen atoms are continuously generated and more and more, the active oxygen atoms have strong oxidation effect, and at the same time, combined with the chemical oxidation effect of hydrogen peroxide, the reaction occurs outside the gas bubbles to generate ·OH, ·H, ·HO2 and other free radicals with strong oxidation ability, and these free radicals with high oxidation activity and strong oxidants and the activated organic molecules (i.e. hydrocarbons and ammonia nitrogen) have an oxidation reaction, which can oxidize and degrade the organic pollutants to generate volatile gases (such as CO2, CO, H2O, NO, N2, etc.) to escape, so as to completely remove the organic pollutants and ammonia nitrogen in the organic wastewater;

[0091] Step 400: In the first mode, the third reactant is put into the electrolysis reaction tank, and an electrolysis cycle is performed to obtain a fourth reactant, and the cycle is ended; the reaction time is 1-2 h;

[0092] Step 500: After the cycle is ended, the fourth reactant is filtered by using a high-pressure pump and a filter.

[0093] In the reaction process in this embodiment, the electrolysis is first used to remove the suspended solids and colloidal substances in the organic wastewater by using the electrolytic flotation effect, and then the photochemical reaction efficiency and the preliminary removal of the pollutants in the organic wastewater are used to perform a deep treatment on the organic wastewater in the combined oxidation process, and the waste residue generated in the deep treatment process is removed by using the electrolytic flotation for a second time, so that the purpose of deep treatment of the high-concentration organic wastewater is achieved, and the treatment method has high flexibility, high treatment efficiency, no secondary pollution and low cost.

[0094] Example Three

[0095] An organic wastewater treatment method, which is performed by using the organic wastewater treatment system as described above, and the method comprises the following steps:

[0096] Step 100: In the first mode, the organic wastewater is put into an electrolysis reaction tank, a flocculant and a chlorine ion concentration regulator are added into the electrolysis reaction tank, and an electrolysis cycle is performed to obtain a first reactant;

[0097] 0.1 kg of flocculant is added for each ton of sewage according to a preset proportion, and the flocculant comprises polyacrylamide.

[0098] The weighed flocculant is diluted at a dilution ratio of 0.1% to obtain a diluted flocculant;

[0099] The diluted flocculant is added to the electrolysis reaction tank at a rate of 180 ml / h;

[0100] The current density is 25 mA / cm under the condition of a plate spacing of 2 cm 2 ;

[0101] The step 100 of adding a chloride ion concentration regulator in the electrolysis reaction tank includes:

[0102] The chloride ion concentration regulator is added to the electrolysis reaction tank to a chloride ion concentration of 4500 mg / L in the electrolysis reaction tank.

[0103] The reaction is carried out until the first reactant is clear;

[0104] Step 200: Put the first reactant into the combined reactor for oxidation reaction to obtain the second reactant; the reaction time is 1 h, and the pressure vessel tank, ozone generator, and ultraviolet lamp are simultaneously used for oxidation;

[0105] Step 300: In the second mode, H2O2 is added to the combined reactor for oxidation-electrolysis circulation to obtain the third reactant; including:

[0106] The pressure in the combined reactor is 0.3 MP;

[0107] The amount of H2O2 added is:

[0108] V(H2O2)=M(COD mg) / C(H2O2 mg / ml),

[0109] Wherein, V(H2O2) represents the volume of H2O2 added, M(COD mg) represents the mass of chemical oxygen demand in the organic wastewater, and C(H2O2 mg / ml) represents the concentration of H2O2;

[0110] Step 400: In the first mode, the third reactant is put into the electrolysis reaction tank for electrolysis circulation to obtain the fourth reactant, and the cycle is ended; the reaction time is 1 h;

[0111] Step 500: After the cycle is ended, the fourth reactant is filtered by using a high-pressure pump and a filter.

[0112] Example Four

[0113] An organic wastewater treatment method, which utilizes the organic wastewater treatment system as described above to treat organic wastewater, and the method comprises the following steps:

[0114] Step 100: in the first mode, the organic wastewater is put into an electrolysis reaction tank, a flocculating agent and a chlorine ion concentration regulator are added into the electrolysis reaction tank, an electrolysis cycle is carried out, and a first reaction product is obtained;

[0115] According to a preset proportion, 0.3 kg of flocculating agent is put into each ton of wastewater, and the flocculating agent includes polyacrylamide;

[0116] The weighed flocculating agent is diluted at a dilution ratio of 0.3%, and a diluted flocculating agent is obtained;

[0117] The diluted flocculating agent is added into the electrolysis reaction tank at a rate of 200 ml / h;

[0118] Under the condition that the distance between the electrode plates is 2 cm, the current density is 45 mA / cm 2 ;

[0119] The step 100 of adding the chlorine ion concentration regulator into the electrolysis reaction tank includes:

[0120] The chlorine ion concentration regulator is added into the electrolysis reaction tank to make the chlorine ion concentration in the electrolysis reaction tank reach 5000 mg / L.

[0121] The reaction is carried out until the first reaction product is clear and transparent;

[0122] Step 200: the first reaction product is put into a combined reactor for oxidation reaction, and a second reaction product is obtained; the reaction time is 1.5 h, and the pressure vessel tank, the ozone generator and the ultraviolet lamp simultaneously perform oxidation;

[0123] Step 300: in the second mode, H2O2 is added into the combined reactor to perform an oxidation-electrolysis cycle, and a third reaction product is obtained; including:

[0124] The pressure in the combined reactor is 0.4 MP;

[0125] The amount of H2O2 added is:

[0126] V(H2O2)=M(COD mg) / C(H2O2 mg / ml),

[0127] Wherein, V(H2O2) represents the volume of H2O2 added, M(COD mg) represents the mass of the chemical oxygen demand in the organic wastewater, and C(H2O2 mg / ml) represents the concentration of H2O2;

[0128] Step 400: in the first mode, the third reaction product is put into an electrolysis reaction tank, an electrolysis cycle is carried out, and a fourth reaction product is obtained, and the cycle is ended; the reaction time is 1.5 h;

[0129] Step 500: After the cycle, the fourth reactant is filtered by a high-pressure pump and a filter.

[0130] Example Five

[0131] An organic wastewater treatment method using the organic wastewater treatment system as described above, the method comprising the following steps:

[0132] Step 100: In the first mode, the organic wastewater is put into the electrolytic reaction tank, a flocculant and a chlorine ion concentration regulator are added, an electrolytic cycle is carried out, and a first reactant is obtained;

[0133] 0.5 kg of flocculant is added per ton of sewage according to a preset ratio, and the flocculant includes polyacrylamide;

[0134] The weighed flocculant is diluted at a dilution ratio of 0.5%, and a diluted flocculant is obtained;

[0135] The diluted flocculant is added to the electrolytic reaction tank at a rate of 220 ml / h;

[0136] The current density is 65 mA / cm 2 under the condition that the plate spacing is 2 cm;

[0137] The step 100 of adding a chlorine ion concentration regulator in the electrolytic reaction tank includes:

[0138] The chlorine ion concentration regulator is added in the electrolytic reaction tank to a chlorine ion concentration of 5500 mg / L in the electrolytic reaction tank.

[0139] The reaction is carried out until the first reactant is colorless and transparent;

[0140] Step 200: The first reactant is put into a combined reactor for oxidation reaction, and a second reactant is obtained; the reaction time is 2 h, and the pressure vessel tank and the ozone generator simultaneously carry out oxidation;

[0141] Step 300: In the second mode, H2O2 is added in the combined reactor for oxidation-electrolysis cycle, and a third reactant is obtained; including:

[0142] The pressure in the combined reactor is 0.5 MP;

[0143] The amount of H2O2 added is:

[0144] V(H2O2) = M(COD mg) / C(H2O2 mg / ml),

[0145] Where V(H2O2) represents the volume of H2O2 added, M(COD mg) represents the mass of chemical oxygen demand in organic wastewater, and C(H2O2 mg / ml) represents the concentration of H2O2;

[0146] Step 400: In the first mode, the third reactant is placed into the electrolytic reaction cell for electrolytic cycling to obtain the fourth reactant, and the cycle ends; the reaction time is 2 hours.

[0147] Step 500: After the cycle is completed, the fourth reactant is filtered using a high-pressure pump and a filter.

[0148] Figure 2 , Figure 3 and Figure 4 The changes in COD, color, and pH of the organic wastewater in Examples 3, 4, and 5 are shown respectively with respect to reaction time. Example 4 is used as an example. Figure 3 As shown, the COD concentration of organic wastewater shows a continuous decreasing trend with the extension of reaction time. The COD removal rate is relatively fast in the first 30 minutes, reaching 54.5%. This is partly because the proportion of organic matter that is more easily oxidized by electrochemical processes is larger in the initial stage of electrolysis, so the COD degradation rate is faster at this time. Subsequently, as the proportion of organic matter that is difficult to be electrochemically oxidized increases, the COD degradation rate gradually decreases. The system has a significant effect on color removal. After 30 minutes of reaction, the color can be reduced to 10 times or less. The higher the current density, the better the color removal effect in the same time period. During the oxidation process, the pH value of organic wastewater fluctuates slightly in the first 30 minutes, and then shows a continuous increasing trend with the extension of electrolysis time.

[0149] It should be understood that the specific embodiments described above are merely illustrative or explanatory of the principles of the invention and do not constitute a limitation thereof. Therefore, any modifications, equivalent substitutions, improvements, etc., made without departing from the spirit and scope of the invention should be included within the protection scope of the invention. Furthermore, the appended claims are intended to cover all variations and modifications falling within the scope and boundaries of the appended claims, or equivalent forms of such scope and boundaries.

[0150] The present invention has been described above with reference to embodiments thereof. However, these embodiments are merely illustrative and not intended to limit the scope of the invention. The scope of the invention is defined by the appended claims and their equivalents. Various substitutions and modifications can be made by those skilled in the art without departing from the scope of the invention, and all such substitutions and modifications should fall within the scope of the invention.

[0151] Although the embodiments of the present application have been described in detail, it should be understood that various changes, substitutions and alterations can be made hereto without departing from the spirit and scope of the application as defined by the appended claims.

[0152] Obviously, the above-described embodiments are only examples for clearly illustrating the present application, but not for limiting the embodiments. Based on the above description, other different forms of changes or variations can be made by those skilled in the art. Here, it is not necessary or possible to enumerate all the embodiments. The obvious changes or variations derived therefrom are still within the protection scope of the present application.

Claims

1. A method for treating organic wastewater based on an organic wastewater treatment system, characterized in that, The organic wastewater treatment system includes: an electrolytic reaction tank (1), a combined reactor (2), a dissolved gas component (3), and an ozone generating component (4). The organic wastewater treatment system includes a first mode and a second mode; The first mode includes organic wastewater flowing from the electrolysis reactor (1) through the dissolved gas component (3) and then to the electrolysis reactor (1), and the ozone generating component (4) supplying gas to the electrolysis reactor (1) through the dissolved gas component (3); The second mode includes liquid flowing from the electrolysis reactor (1), the dissolved gas component (3) and the combined reactor (2) back to the electrolysis reactor (1), and the ozone generating component (4) supplying gas to the combined reactor (2) through the dissolved gas component (3); The first mode and the second mode do not work simultaneously; The electrolytic reaction tank (1) includes a reaction tank body (1-1), a slag-blocking component (1-2), a slag-scraping component (1-3), and an electrolysis component (1-4); the electrolysis component (1-4) is disposed inside the reaction tank body (1-1), the slag-blocking component (1-2) covers the top surface of the reaction tank body (1-1), and the slag-scraping component (1-3) scrapes away the slag intercepted by the slag-blocking component (1-2); The combined reactor (2) includes a pressure vessel (2-1) and an ultraviolet lamp (2-2). The ozone generating component (4), the dissolved gas component (3), and the pressure vessel (2-1) are connected in sequence. The ultraviolet lamp (2-2) is installed inside the pressure vessel (2-1). The organic wastewater treatment method includes the following steps: Step 100: In the first mode, organic wastewater is placed into an electrolysis reactor, flocculant and chloride ion concentration regulator are added to the electrolysis reactor, and electrolysis is carried out to obtain the first reactant; Step 200: The first reactant is placed in a combined reactor for oxidation to obtain the second reactant; Step 300: In the second mode, H2O2 is added to the combined reactor to carry out an oxidation-electrolysis cycle to obtain a third reactant; Step 400: In the first mode, the third reactant is placed into the electrolytic reaction cell for electrolytic cycling to obtain the fourth reactant, and the cycle ends; The addition of flocculant to the electrolytic reaction tank in step 100 includes: Weigh out a predetermined proportion of flocculant according to the quality of the organic wastewater. The predetermined proportion is 0.1 to 0.5 kg of flocculant per ton of wastewater. The flocculant includes polyacrylamide. The weighed flocculant is diluted to a ratio of 0.1% to 0.5% to obtain the diluted flocculant. The diluted flocculant is added to the electrolytic reaction tank at a rate of 180-220 ml / h; The addition of a chloride ion concentration regulator to the electrolytic reaction cell in step 100 includes: A chloride ion concentration regulator is added to the electrolytic reaction cell to bring the chloride ion concentration in the electrolytic reaction cell to 4500-5500 mg / L.

2. The organic wastewater treatment method based on an organic wastewater treatment system according to claim 1, characterized in that, The electrolysis components (1-4) include an anode, a cathode, and a power source, wherein the anode material is a titanium-based ruthenium oxide-iridium oxide material.

3. The organic wastewater treatment method based on an organic wastewater treatment system according to claim 1, characterized in that, It also includes an air compressor (5) and a dosing unit (6), wherein the air compressor (5) is connected to the ozone generating unit (4) and the combined reactor (2) respectively, and the dosing unit (6) is connected to the electrolytic reaction tank (1) and the combined reactor (2) respectively; In the first mode, the air compressor (5) supplies air to the ozone generating unit (4), and the dosing unit (6) adds chemicals to the electrolytic reaction tank (1); In the second mode, the air compressor (5) supplies air to the ozone generating unit (4) and the combined reactor (2) respectively, and the dosing unit (6) adds chemicals to the combined reactor (2).

4. The organic wastewater treatment method based on an organic wastewater treatment system according to claim 1, characterized in that, It also includes a filter element, which is connected to the electrolytic reaction cell.

5. The organic wastewater treatment method based on an organic wastewater treatment system according to claim 1, characterized in that, Step 300: In the second mode, H2O2 is added to the combined reactor to perform an oxidation-electrolysis cycle, obtaining a third reactant comprising: The pressure in the combined reactor is 0.3–0.5 MPa; The amount of H2O2 added is: V(H2O2)=M(COD mg) / C(H2O2mg / ml), Where V(H2O2) represents the volume of H2O2 added, M(CODmg) represents the mass of chemical oxygen demand in organic wastewater, and C(H2O2mg / ml) represents the concentration of H2O2.

6. The organic wastewater treatment method based on an organic wastewater treatment system according to claim 1, characterized in that, Also includes: Step 500: Filter the fourth reactant using a high-pressure pump and a filter.

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