CN216998076U - Industrial wastewater treatment system - Google Patents
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- CN216998076U CN216998076U CN202220534690.9U CN202220534690U CN216998076U CN 216998076 U CN216998076 U CN 216998076U CN 202220534690 U CN202220534690 U CN 202220534690U CN 216998076 U CN216998076 U CN 216998076U
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Abstract
The utility model discloses a treatment system of industrial wastewater, which comprises: the system comprises a water inlet adjusting tank, a hydrolysis acidification tank, an anaerobic fermentation tank, an aerobic aeration tank, a chemical advanced treatment unit, a filtering unit and a concentration unit; wherein the anaerobic fermentation tank comprises at least one anaerobic fermentation unit. The aerobic aeration tank comprises at least one aerobic aeration unit. The chemical depth treatment unit comprises one or more of the following devices: ozone oxidation treatment equipment, an electrochemical treatment pool, chemical catalytic oxidation treatment equipment, Fenton process treatment equipment and chemical specific reagent treatment equipment. The sodium chloride salt obtained by the system reaches or is superior to the national standard of industrial salt, and the obtained fresh water reaches or is superior to the standard of surface three types of water.
Description
Technical Field
The utility model relates to a wastewater treatment system, in particular to an industrial wastewater treatment system, and belongs to the technical field of wastewater treatment.
Background
The industrial wastewater comprises production wastewater, production sewage and cooling water, and refers to wastewater and waste liquid generated in the industrial production process, wherein the wastewater and the waste liquid contain industrial production materials, intermediate products, byproducts and pollutants generated in the production process, which are lost along with water. The industrial wastewater has various types and complex components. For example, the waste water from electrolytic salt industry contains mercury, the waste water from heavy metal smelting industry contains various metals such as lead and cadmium, the waste water from electroplating industry contains various heavy metals such as cyanide and chromium, the waste water from petroleum refining industry contains phenol, and the waste water from pesticide manufacturing industry contains various pesticides. With the rapid development of industry, the variety and quantity of waste water are rapidly increased, the pollution to water bodies is more and more extensive and serious, and the health and the safety of human beings are threatened. Therefore, the treatment of industrial wastewater is more important than the treatment of municipal sewage for environmental protection. Because industrial wastewater contains various toxic substances and pollutes the environment, the environmental pollution has great harm to human health, so that comprehensive utilization and harm conversion are developed, and corresponding purification measures are taken according to the components and concentration of pollutants in the wastewater for treatment and then the wastewater can be discharged.
The main pollution caused by industrial wastewater is: organic aerobic substance pollution, chemical poison pollution, inorganic solid suspended substance pollution, heavy metal pollution, acid pollution, alkali pollution, plant nutrient substance pollution, heat pollution, pathogen pollution and the like. Many pollutants have color, odor or easily-generated foam, so the industrial wastewater often presents an unpleasant appearance, large-area pollution of water is caused, the life and health of people are directly threatened, and the control of the industrial wastewater is particularly important.
The chemical industrial wastewater mainly comes from production wastewater discharged from petrochemical industry, coal chemical industry, acid-base industry, chemical fertilizer industry, plastic industry, pharmaceutical industry, dye industry, rubber industry and the like. The main measures for preventing and treating the chemical wastewater pollution are as follows: firstly, the production process and equipment are required to be reformed, pollutants are reduced, the wastewater is prevented from being discharged outside, and comprehensive utilization and recovery are carried out; the treatment degree of the wastewater which must be discharged is selected according to the water quality and requirements. The primary treatment mainly separates suspended solids, colloidal substances, floating oil or heavy oil and the like in water. The method of water quality and quantity regulation, natural precipitation, floating and oil separation can be adopted. The secondary treatment mainly removes biodegradable organic dissolved matters and partial colloid matters, reduces the biochemical oxygen demand and partial chemical oxygen demand in the wastewater, and generally adopts a biological method for treatment. In the waste water after biological treatment, a certain amount of COD (chemical oxygen demand) still remains, sometimes the waste water has higher color, smell and taste, or a three-stage treatment method is adopted for further purification due to high environmental sanitation standard requirements. The third-stage treatment is mainly used for removing organic pollutants which are difficult to biodegrade and soluble inorganic pollutants in the wastewater. The common methods include activated carbon adsorption method and ozone oxidation method, and ion exchange and membrane separation technology can also be adopted. Different treatment methods can be selected for various chemical industrial wastewater according to different water quality and water quantity and the requirement of the treated discharged water quality.
Hydroxypropyl methyl cellulose ether is high-polymerization cellulose ether which is prepared by taking cellulose, caustic soda, chloromethane and epoxypropane as main raw materials, is called HPMC for short, has a compound molecular weight of millions, is a macromolecular organic substance, and is widely applied to the industries of buildings, coatings, plastics and the like. A large amount of high-concentration and high-salinity organic chemical wastewater is generated in the production process, and the wastewater contains macromolecular substances such as methyl cellulose, cellulose and hydroxypropyl cellulose and also contains micromolecular substances such as propylene oxide, chloromethane, toluene and inorganic salt. The wastewater has the characteristics of high COD (chemical oxygen demand) content, high salt content, poor biodegradability and great harm to the environment, and if the wastewater is directly discharged without being treated, the wastewater brings serious harm to the ecological environment.
CN203319823U discloses a cellulose ether wastewater treatment device, which comprises: a regulating tank, a micro-electrolysis tank, an oxidation tank, a sedimentation tank, a hydrolysis acidification tank, an up-flow anaerobic sludge bed reactor, a sequential intermittent activated sludge tank and an aeration biological filter.
However, the prior art treatment method can not achieve ideal purification effect on wastewater with high salt content and high COD value in cellulose ether production, especially wastewater containing fluorine and silicon, and the treatment cost is too high.
SUMMERY OF THE UTILITY MODEL
Aiming at the defects of the prior art, the utility model provides a treatment system of industrial wastewater, which effectively reduces the content of harmful anions in the wastewater and the hardness of water by adopting a biochemical treatment means combining anaerobic treatment and aerobic treatment in cooperation with chemical advanced treatment, and finally removes impurities in the wastewater by double filtration and double enrichment means, and obtains high-quality crystal salt, thereby achieving the technical effect of changing waste into valuable.
In order to achieve the above purpose, the technical scheme adopted by the utility model is as follows:
the industrial waste water treating system includes water inlet regulating tank, hydrolysis and acidification tank, anaerobic fermentation tank, aerobic aeration tank, chemical advanced treatment unit, filtering unit and concentrating unit. The waste water inlet pipeline is communicated with the water inlet of the water inlet adjusting tank. The water inlet adjusting tank, the hydrolysis acidification tank, the anaerobic fermentation tank, the aerobic aeration tank, the chemical advanced treatment unit, the filtering unit and the concentration unit are sequentially connected in series through a plurality of water pipelines. The purified water discharge pipeline is communicated with the water outlet of the concentration unit.
Wherein: the anaerobic fermentation tank comprises at least one anaerobic fermentation unit. The anaerobic fermentation unit is formed by sequentially connecting a primary anaerobic fermentation tank, a secondary anaerobic fermentation tank and an anaerobic sedimentation tank in series.
The aerobic aeration tank comprises at least one aerobic aeration unit. The aerobic aeration unit is formed by sequentially connecting a first-stage aerobic aeration tank, a first-stage aerobic sedimentation tank, a second-stage aerobic aeration tank and a second-stage aerobic sedimentation tank in series.
The chemical depth treatment unit comprises one or more of the following devices: ozone oxidation treatment equipment, an electrochemical treatment pool, chemical catalytic oxidation treatment equipment, Fenton process treatment equipment and chemical specific reagent treatment equipment.
Preferably, the filtration unit comprises a multi-media filter and an ultrafiltration device connected in series. The multimedia filter is located upstream of the ultrafiltration device, according to the direction of the water flow. The multi-media filter is a multi-media filter comprising a quartz sand filter layer. The ultrafiltration device is a ceramic flat membrane ultrafiltration device. The raw material (or material) of the general ceramic ultrafiltration membrane is generally alumina ceramic, silicon carbide or silicon nitride ceramic.
Preferably, the concentration unit comprises a membrane concentration device and an evaporation desalination device which are connected in series in sequence. The membrane concentration device is located upstream of the evaporative desalination apparatus according to the direction of the water flow. The membrane concentration equipment is reverse osmosis membrane and/or electrodialysis equipment.
Preferably, in the chemical polishing unit comprising the electrochemical treatment cell: the electrochemical treatment cell includes an anode and a cathode. The anode is a combined anode formed by combining a sacrificial anode and an inert anode or a composite anode formed by using an alloy material containing a sacrificial metal and an inert metal, and a direct current voltage is provided between the combined anode and the cathode or between the composite anode and the cathode by a direct current power supply.
Preferably, a plurality of anodes and a plurality of cathodes are provided in the electrochemical treatment cell. A plurality of said anodes and a plurality of said cathodes are alternately arranged or arranged in pairs in the electrochemical treatment cell.
Preferably, between 2 and 150 pairs of anodes are provided in the electrochemical treatment cell.
Preferably, between 2 and 150 pairs of cathodes are provided in the electrochemical treatment cell.
Preferably, a plurality of said anodes and a plurality of said cathodes are arranged alternately or in pairs or consecutively in groups of anodes and cathodes in the electrochemical treatment cell.
Preferably, the anode and the cathode are each independently in the shape of one of a plate, a perforated plate, a grid, a grate, a fence or a wire mesh.
Preferably, a flow guide plate is correspondingly arranged on the same side of each anode and each cathode.
Preferably, the system further comprises a sludge treatment unit. The sludge treatment unit comprises a sludge concentration tank and a filter-pressing dehydration device. The sludge outlets of the anaerobic fermentation tank, the aerobic aeration tank and the chemical advanced treatment unit are all connected with the sludge inlet of the sludge concentration tank through a sludge conveying device, and the concentrated sludge outlet of the sludge concentration tank is connected with the concentrated sludge inlet of the filter-pressing dehydration equipment.
Preferably, the sludge outlet of the anaerobic sedimentation tank is respectively connected with the sludge return inlets of the hydrolysis acidification tank, the primary anaerobic fermentation tank and the secondary anaerobic fermentation tank through a plurality of first sludge return devices.
Preferably, the sludge outlet of the primary aerobic sedimentation tank is connected with the sludge return inlet of the primary aerobic aeration tank through a second sludge return device. The sludge outlet of the second-stage aerobic sedimentation tank is connected with the sludge return inlet of the second-stage aerobic aeration tank through a third sludge return device.
Preferably, a purified water circulation branch pipe is led out from the purified water discharge pipeline and is connected with a water inlet of the water inlet regulating tank.
In the prior art, raw (raw) wastewater (W0) from cellulose ether production contains organic compounds and organic polymers which are difficult to degrade, particularly, the content of sodium chloride in the wastewater (W0) is between 5 and 15 weight percent, and the wastewater is separated by evaporation and desalination, so that firstly, the COD content in condensed water is high, secondly, the content of organic matters in crystallized salt is high, the post-treatment difficulty is high, the generated salt is dangerous waste, the treatment cost is higher, and the ideal purification effect cannot be realized. Meanwhile, because the flow rate of the wastewater containing fluorine and silicon impurities to be treated is large, the fluorine and silicon impurities in the wastewater are very easy to block the pores of various filtering membranes (such as an ultrafiltration membrane, a reverse osmosis membrane and an electrodialysis membrane), so that the purification treatment of the wastewater with high content of the fluorine and silicon impurities is a technical problem which is difficult to solve at present.
In the utility modelIn the novel method, firstly, through the combined use of a double biochemical treatment process combining anaerobic organisms and aerobic organisms and the combined use of a chemical advanced treatment unit comprising an electrochemical treatment tank, most of fluorine and silicon impurities in the wastewater can be removed to reduce the COD of the wastewater; on the other hand, the combined use of these two processes also enables the desired removal of most heavy metals, but also of most other harmful anions (such as phosphate, arsenate and S)2-) At the same time, it is also possible to remove additionally or additionally a portion of other "hardness" cations (e.g. calcium, magnesium ions, etc.).
In the utility model, the wastewater to be treated is firstly collected and homogenized in the inflow regulating reservoir, and meanwhile, dilution and acid-base regulation are carried out in the inflow regulating reservoir so as to improve the efficiency of subsequent biochemical treatment. And performing at least two biochemical treatment processes including anaerobic fermentation and aerobic aeration on the wastewater after the homogenization and the acid-base regulation are completed. Wherein the anaerobic fermentation mainly functions in denitrification by microorganisms (such as heterotrophic bacteria ammoniating protein, fat and other pollutants to free NH)3Or NH4 +(ii) a At the same time, the denitrification of the heterotrophic bacteria converts NO3 -Reduction to molecular nitrogen and hydrolysis of macromolecular organic matter). Aerobic aeration is used for removing organic matters in water, and ammonia nitrogen is removed through nitrification of microorganisms (nitrification of autotrophic bacteria is used for removing NH)3-N or NH4 +Oxidation to NO3 -). The anaerobic treatment and the aerobic treatment can degrade or decompose most COD (organic matter impurities) contained in the wastewater to expose or keep the heavy metal ions or anions in a free state, thereby avoiding the problem that the heavy metal ions and the anions are wrapped or complexed by the organic matter impurities in the wastewater purification method in the prior art.
In the utility model, the chemical advanced treatment unit comprises an electrochemical treatment cell, wherein the electrochemical treatment cell comprises an anode and a cathode, and when the anode is a combined anode or a composite anode of iron and/or aluminum; in the electrochemical impurity removal process of the wastewater, under the action of an electric field, (HF) n, (H) in the form of aggregates or associations4SiO4)n、(H2SiO3) n or) H3PO4) n is dissociated or ionized, with a particular anion (e.g. F)-、SiO3 2-、PO4 3-Or AsO4 3-) Form a precipitate with the corresponding heavy metal cation. The current action between the polar plates can change the molecular aggregation state of silicon dioxide, silicic acid (radical) and fluoride compounds in the waste water to make SiO2Silicic acid radical, F-The plasma is combined with the calcium and magnesium ion precipitates and then coprecipitated, thereby reducing SiO2Silicic acid radical, F-And the indexes of pollutants are equal. When the anode uses a sacrificial anode and an inert anode as a combined anode or uses ferrotitanium alloy, aluminum-titanium alloy or ferroaluminum-titanium alloy as a composite anode, iron ions and/or aluminum ions in the wastewater serve as or form a flocculating agent or a flocculating substance; on the one hand, the flocculant is beneficial to the agglomeration and flocculation of inorganic salt precipitates and small particles of organic matters (COD), and on the other hand, the flocculant promotes the further agglomeration and sedimentation of particulate matters in wastewater. In addition, Fe produced3+Ions or Al3+The ions also facilitate removal of phosphate by forming a precipitate. Also [ FeF ] is formed in the electrochemical treatment cell6]3-And [ AlF6]3-Ions, which settle by flocculation or are adsorbed by activated carbon in the subsequent stages.
In the present invention, the wastewater refers to various wastewaters (including domestic washing water of plant areas) from various links of cellulose ether production enterprises, which are collected in a conditioning tank to form raw wastewater or raw wastewater, and these wastewaters or wastewaters to be treated are referred to as raw wastewater or raw wastewater.
In the present invention, the electrochemical treatment cell typically employs a voltage (V) applied between an inert anode or composite anode and cathode as an electrode pair by a DC power source (preferably a DC pulsed power source, more preferably a pulsed adaptive power source, with power source parameters automatically adjusted based on job response conditions)1) Sufficient to enable the in situ generation of highly active chlorine-containing oxidants (. Cl, Cl) in the wastewater2And/or hypochlorite or salt thereof) and optionally oxygen containing oxygenAgents (. O,. OH and O)2When the content or concentration of chloride ions in the wastewater is low, oxygen with lower activity is generated in the electrolysis process), and a voltage (V) applied between a sacrificial anode or a composite anode as an electrode pair and a cathode by a direct current power supply2) Enough to cause the elemental metal of the sacrificial anode or composite anode to lose electrons as a result of oxidation and enter the wastewater in the form of metal cations, which form or act as flocculants in the wastewater contained within the electrochemical treatment cell. Wherein the voltage (V)1) And voltage (V)2) The same or different. If necessary, a plurality of flow deflectors are provided in the electrochemical treatment cell to guide the wastewater to meander between all the anodes and cathodes.
In the present invention, a plate-shaped anode and a plate-shaped cathode are used in the electrochemical treatment cell. There is no limitation on the material for forming the cathode, and materials commonly used in the art for forming the cathode may be used in the present application, for example, materials for forming the cathode include graphite, iron, titanium, and the like. The inert anode comprises graphite or titanium metal and, therefore, the inert anode plate comprises a graphite plate or a titanium metal plate. In general, the shape of the anode or cathode is generally a flat plate (e.g., an iron plate, an aluminum plate, or an iron-aluminum alloy plate), a perforated plate, a grid, a grate, a fence, a wire mesh, or the like. These anodes or cathodes generally have one or two major faces (i.e., front or back) with a large area. The major face is in the form of a flat or curved surface. For example, when the anode or cathode is in the form of a fence, in the fence-shaped anode or cathode, a plurality of anodes in the shape of rods or bars are arranged upright on a plane or on a curved surface, or a plurality of cathodes in the shape of rods or bars are arranged upright on a plane or on a curved surface. Typically, the major face (or front) of the anode faces the cathode or faces the major face (or front) of the cathode. Preferably, an iron, aluminum or iron-aluminum alloy plate is used as the anode, with the major plane (or face) of the anode facing the cathode or facing the major plane (or face) of the cathode. When using iron or aluminium or an iron-aluminium alloy (e.g. iron or aluminium or iron-aluminium alloy plates) as sacrificial anode, or when using a sacrificial anode comprising a sacrificial metal and an inert metalWhen the alloy material of the metal is used as a composite anode, a flocculating agent (or a substance having a flocculating effect) is formed from iron ions, aluminum ions or iron ions + aluminum ions in the wastewater contained in the electrochemical treatment tank. Such flocculants include, but are not limited to, Fe2+(e.g., [ Fe (H))2O)6]2+)、Fe3+(e.g., [ Fe (H))2O)6]3+)、Al3+(e.g., [ Al (H) ]2O)6]3+) And corresponding inorganic high molecular polymers (such as polymeric ferric chloride, polymeric ferric sulfate, polymeric aluminum chloride) or composite inorganic high molecular polymers (such as polymeric aluminum ferric chloride, polymeric aluminum ferric sulfate, polymeric sulfuric acid (chloride) silicon aluminum ferric), etc.
In the present invention, a plurality of pairs of anodes and cathodes may be used in the electrochemical treatment cell, for example 2 to 150 pairs, preferably 3 to 120 pairs, more preferably 4 to 100 pairs, more preferably 5 to 90 pairs, more preferably 6 to 85 pairs, such as 8, 9, 10, 12, 14, 16, 18, 20, 22, 25, 28, 30, 32, 35, 40, 60, 70 or 80 pairs. For example, when one cathode plate (or anode plate) with a larger surface area is paired with two anode plates (or cathode plates) with a smaller surface area, then 2 pairs of anode and cathode are considered to be present; when one cathode plate (or anode plate) with a larger surface area is paired with three anode plates (or cathode plates) with a smaller surface area, then 3 pairs of anode and cathode are considered to be present. The number of pairs is calculated as an average.
In the present invention, a plurality of anodes and cathodes may be alternately arranged or may be arranged in pairs or in a set of 2 anodes and 1 cathode in an electrochemical treatment cell (or electrolytic cell). Preferably, a plurality of anodes and cathodes (e.g., 8 anodes and 7 cathodes) are alternately disposed, and in addition, two or more anodes may be adjacent to or electrically connected to each other. Likewise, two or more cathodes may be adjacent to or electrically connected to each other. In the present invention, a filler or a three-dimensional filler, generally, a filler or a three-dimensional filler (filler diameter is, for example, 4 to 8 mm) may be placed between the anode and the cathode in the electrochemical treatment cell; for example, a ceramic filler (for example alumina ceramic, silicon carbide ceramic or silicon nitride ceramic), or a wire mesh filler (mesh size of for example 4-8 mm). The filler exerts an adsorption effect and provides a reaction interface and a crystallization point at the same time. Or, adding a coagulant aid or flocculant, such as polyacrylamide, to the wastewater in the electrochemical treatment cell; organic floating slag such as oily matter or floating matter floats on the surface of wastewater due to bubbling caused by hydrogen generated by electrolysis in wastewater and air (aeration) introduced into wastewater, and therefore, the organic floating slag is further aggregated or precipitated by a coagulant aid (or a flocculant or a sedimentation agent), and the floating slag or the precipitate is conveniently fished out or collected.
In the present invention, "electrochemical" and "electrolysis" have the same meaning and may be used interchangeably. The "electrochemical treatment cell" may also be referred to as an "electrolytic cell". "hardness" and "(calcium and magnesium) total hardness" are used interchangeably.
In the present invention, the anaerobic fermentation tank and the aerobic aeration tank are mainly biochemical treatment processes, in which the treatment of anaerobic fermentation and the treatment of aerobic aeration can be performed independently a plurality of times. For example, the anaerobic treatment and the aerobic treatment are each carried out 2 times or 3 times or 4 times or 5 times or 6 times, that is, each may be divided into 2, 3, 4 or 5 or 6 stages, respectively. In addition, anaerobic treatment and aerobic treatment may be alternately performed.
In the utility model, anaerobic and aerobic treatment can greatly reduce the COD value in the wastewater. For the selection of anaerobic bacteria or aerobic bacteria, corresponding bacteria sources are selected according to different specific wastewater for cultivation. Selecting various bacteria to cultivate in the specific wastewater; then, the number and activity of microorganisms suitable for biochemical treatment are observed under a microscope, and water indexes are detected, so that bacteria which can propagate fast in corresponding wastewater are selected.
In the present invention, the wastewater after the chemical advanced treatment is continuously filtered to remove the insoluble substances generated during the electrochemical snow treatment, and the multimedia filter used in the present application is not particularly limited, and a multimedia filter commonly used in the prior art may be used. The present invention preferably uses a multimedia filter including a quartz sand filter layer, for example, a multimedia filter including an activated carbon filter layer, a quartz sand filter layer, and a porous ceramic particle filter layer.
In the present invention, the wastewater after the filtration treatment is subjected to a concentration treatment, i.e., the purified wastewater from the preceding ultrafiltration step is subjected to one or more stages of reverse osmosis treatment (membrane concentration apparatus), thereby obtaining fresh water as reuse water (for diluting the original wastewater in the inlet water adjusting tank) and obtaining concentrated water containing sodium chloride. The concentrated water containing sodium chloride is evaporated and concentrated to recover sodium salt with purity up to 99%, and the condensed water produced in the process may be reused.
Compared with the prior art, the technical scheme provided by the utility model has the following beneficial technical effects:
1. the utility model firstly collects and homogenizes the wastewater to be treated, and simultaneously dilutes and adjusts acid and alkali in the water inlet adjusting tank, thereby improving the efficiency of subsequent biochemical treatment and simultaneously combining deep biochemical treatment with chemical deep treatment.
2. The utility model adopts biochemical treatment and electrochemical treatment to the original wastewater in sequence, wherein the biochemical treatment removes most COD in a low-cost and high-efficiency mode, and avoids the organic matters from treating F-、SiO3 2-Encapsulation and complexation of ions and heavy metal ions, and electrochemical treatment of (HF) n and (H)2SiO3) n, etc. to dissociate from Ca existing in the wastewater2+And Mg2 +The precipitate is formed, so that most of fluorine and silicon impurities are removed, and the phenomenon that the micropores of various filtering membranes (such as an ultrafiltration membrane) are frequently blocked due to the formation of hard scales in the subsequent process is avoided, so that the service life of the filtering equipment is shortened.
3. The sodium chloride salt obtained in the concentration treatment process of the utility model reaches or is superior to the national standard of industrial salt, the obtained reuse water (fresh water generated by membrane concentration and condensed water generated by evaporation desalination) reaches or is superior to the standard of surface three types of water, one part of the reuse water is circulated to the water inlet regulating tank, and the rest can be used as industrial water or civil water for enterprises.
Drawings
FIG. 1 is a schematic view of the overall structure of the treatment system of the present invention.
FIG. 2 is a front (longitudinal) sectional view of the chemical polisher unit of the present invention.
FIG. 3 is a top view of the anode and cathode arrangement in the electrochemical treatment cell of the chemical depth treatment unit of the present invention.
Fig. 4 is a transverse perspective view of the anode and cathode arrangement.
Fig. 5 is a partial top view showing the arrangement of the fluidic plates, anode and cathode in an electrochemical processing cell.
Reference numerals: 1: a water inlet adjusting tank; 2: a hydrolysis acidification pool; 3: an anaerobic fermentation tank; 301: a primary anaerobic fermentation tank; 302: a secondary anaerobic fermentation tank; 303: an anaerobic sedimentation tank; 4: an aerobic aeration tank; 401: a primary aerobic aeration tank; 402: a primary aerobic sedimentation tank; 403: a secondary aerobic aeration tank; 404: a secondary aerobic sedimentation tank; 5: a chemical depth processing unit; 501: an anode; 502: a cathode; 503: a baffle; 6: a filtration unit; 601: a multi-media filter; 602: an ultrafiltration device; 7: a concentration unit; 701: a membrane concentration device; 702: an evaporation desalting device; 8: a sludge treatment unit; 801: a sludge concentration tank; 802: filter pressing dehydration equipment; l1: a wastewater inlet conduit; l2: a water delivery pipeline; l3: a purified water discharge pipeline; l31: a purified water circulation branch pipe; h1: a first sludge recirculation apparatus; h2: a second sludge reflux unit; w: a sludge conveying device.
Detailed Description
The present invention will be described in further detail with reference to the following examples, but the present invention is not limited to these examples.
The apparatuses used in the examples are all apparatuses generally used in the art and commercially available on the market unless otherwise specified. For the commercially available processing apparatus used in each step, when the processing capacity of a single processing apparatus is low, the parallel use of two or more apparatuses may be considered.
The industrial wastewater treatment system comprises a water inlet adjusting tank 1, a hydrolysis acidification tank 2, an anaerobic fermentation tank 3, an aerobic aeration tank 4, a chemical advanced treatment unit 5, a filtering unit 6 and a concentration unit 7. The waste water inlet pipeline L1 is communicated with the water inlet of the water inlet regulating reservoir 1. The water inlet adjusting tank 1, the hydrolysis acidification tank 2, the anaerobic fermentation tank 3, the aerobic aeration tank 4, the chemical advanced treatment unit 5, the filtering unit 6 and the concentration unit 7 are sequentially connected in series through a plurality of water pipelines L2. The clean water discharge line L3 is connected to the water discharge port of the concentration unit 7.
Wherein: the anaerobic fermentation tank 3 comprises at least one anaerobic fermentation unit. The anaerobic fermentation unit is formed by sequentially connecting a first-stage anaerobic fermentation tank 301, a second-stage anaerobic fermentation tank 302 and an anaerobic sedimentation tank 303 in series.
The aerobic aeration tank 4 comprises at least one aerobic aeration unit. The aerobic aeration unit is formed by sequentially connecting a primary aerobic aeration tank 401, a primary aerobic sedimentation tank 402, a secondary aerobic aeration tank 403 and a secondary aerobic sedimentation tank 404 in series.
The chemical depth treatment unit 5 comprises one or more of the following devices: ozone oxidation treatment equipment, an electrochemical treatment pool, chemical catalytic oxidation treatment equipment, Fenton process treatment equipment and chemical specific reagent treatment equipment.
Preferably, the filtration unit 6 comprises a multimedia filter 601 and an ultrafiltration device 602 connected in series. The multimedia filter 601 is located upstream of the ultrafiltration device 602, depending on the direction of the water flow. The multi-media filter 601 is a multi-media filter including a quartz sand filter layer. The ultrafiltration device 602 is a ceramic flat membrane ultrafiltration device.
Preferably, the concentration unit 7 comprises a membrane concentration device 701 and an evaporative desalination device 702 in series. The membrane concentration device 701 is located upstream of the evaporative desalination apparatus 702, depending on the direction of the water flow. The membrane concentration device 701 is a reverse osmosis membrane and/or an electrodialysis device.
Preferably, in the chemical depth treatment unit 5 comprising the electrochemical treatment bath: the electrochemical treatment cell includes an anode 501 and a cathode 502. The anode 501 is a combined anode formed by using a combination of a sacrificial anode and an inert anode or a composite anode formed by using an alloy material containing a sacrificial metal and an inert metal, and a dc voltage is supplied from a dc power source between the combined anode and the cathode 502 or between the composite anode and the cathode 502.
Preferably, a plurality of anodes 501 and a plurality of cathodes 502 are provided in the electrochemical treatment cell. A plurality of said anodes 501 and a plurality of said cathodes 502 are arranged alternately or in pairs in the electrochemical treatment cell.
Preferably, between 2 and 150 pairs of anodes 501 are provided in the electrochemical processing cell.
Preferably, between 2 and 150 pairs of cathodes 502 are provided in the electrochemical treatment cell.
Preferably, a plurality of said anodes 501 and a plurality of said cathodes 502 are arranged alternately or in pairs or consecutively in groups of 2 anodes 501 and 1 cathode 502 in the electrochemical treatment cell.
Preferably, the anode 501 and the cathode 502 are each independently shaped as one of a flat plate, a perforated plate, a grid, a grate, or a wire mesh.
Preferably, a flow guide plate 503 is correspondingly arranged on the same side of each anode 501 and each cathode 502.
Preferably, the system further comprises a sludge treatment unit 8. The sludge treatment unit 8 includes a sludge thickener 801 and a press filtration dewatering device 802. Sludge outlets of the anaerobic fermentation tank 3, the aerobic aeration tank 4 and the chemical advanced treatment unit 5 are connected with a sludge inlet of a sludge concentration tank 801 through a sludge conveying device W, and a concentrated sludge outlet of the sludge concentration tank 801 is connected with a concentrated sludge inlet of a filter-pressing dehydration device 802.
Preferably, the sludge outlet of the anaerobic sedimentation tank 303 is respectively connected with the sludge return inlets of the hydrolytic acidification tank 2, the primary anaerobic fermentation tank 301 and the secondary anaerobic fermentation tank 302 through a plurality of first sludge return devices H1.
Preferably, the sludge outlet of the primary aerobic sedimentation tank 402 is connected with the sludge return inlet of the primary aerobic aeration tank 401 through a second sludge return device H2. The sludge outlet of the secondary aerobic sedimentation tank 404 is connected with the sludge return inlet of the secondary aerobic aeration tank 403 through a third sludge return device H3.
Preferably, a purified water circulation branch pipe L31 is also led out of the purified water discharge pipeline L3 and is connected with a water inlet of the water inlet adjusting tank 1.
Example 1
As shown in fig. 1 to 5, the industrial wastewater treatment system comprises a water inlet adjusting tank 1, a hydrolysis acidification tank 2, an anaerobic fermentation tank 3, an aerobic aeration tank 4, a chemical advanced treatment unit 5, a filtering unit 6 and a concentration unit 7. The waste water inlet pipeline L1 is communicated with the water inlet of the water inlet regulating reservoir 1. The water inlet adjusting tank 1, the hydrolysis acidification tank 2, the anaerobic fermentation tank 3, the aerobic aeration tank 4, the chemical advanced treatment unit 5, the filtering unit 6 and the concentration unit 7 are sequentially connected in series through a plurality of water pipelines L2. The clean water discharge line L3 communicates with the water discharge port of the concentration unit 7.
Wherein: the anaerobic fermentation tank 3 comprises at least one anaerobic fermentation unit. The anaerobic fermentation unit is formed by connecting a first-stage anaerobic fermentation tank 301, a second-stage anaerobic fermentation tank 302 and an anaerobic sedimentation tank 303 in series in sequence.
The aerobic aeration tank 4 comprises at least one aerobic aeration unit. The aerobic aeration unit is formed by sequentially connecting a primary aerobic aeration tank 401, a primary aerobic sedimentation tank 402, a secondary aerobic aeration tank 403 and a secondary aerobic sedimentation tank 404 in series.
The chemical deep treatment unit 5 comprises an electrochemical treatment tank.
Example 2
Example 1 is repeated except that the filtration unit 6 comprises a multimedia filter 601 and an ultrafiltration device 602 connected in series. The multimedia filter 601 is located upstream of the ultrafiltration device 602, depending on the direction of the water flow. The multi-media filter 601 is a multi-media filter including a quartz sand filter layer. The ultrafiltration device 602 is a ceramic flat membrane ultrafiltration device.
Example 3
Example 2 was repeated except that the concentration unit 7 comprised a membrane concentration apparatus 701 and an evaporative desalination device 702 in series in this order. The membrane concentration device 701 is located upstream of the evaporative desalination apparatus 702, depending on the direction of the water flow. The membrane concentration device 701 is a reverse osmosis membrane.
Example 4
Example 3 is repeated except that the membrane concentration apparatus 701 is an electrodialysis apparatus.
Example 5
Example 4 was repeated except that in the chemical depth treatment unit 5 containing the electrochemical treatment cell: the electrochemical processing cell includes an anode 501 and a cathode 502. The anode 501 is a combined anode formed by using a combination of a sacrificial anode and an inert anode or a composite anode formed by using an alloy material containing a sacrificial metal and an inert metal, and a dc voltage is supplied from a dc power source between the combined anode and the cathode 502 or between the composite anode and the cathode 502.
Example 6
Example 5 was repeated except that a plurality of anodes 501 and a plurality of cathodes 502 were provided in the electrochemical treatment cell. A plurality of said anodes 501 and a plurality of said cathodes 502 are arranged alternately or in pairs in the electrochemical treatment cell.
Example 7
Example 6 was repeated except that 100 pairs of anodes 501 were provided in the electrochemical treatment cell.
Example 8
Example 7 was repeated except that 100 pairs of cathodes 502 were provided in the electrochemical treatment cell.
Example 9
Example 8 is repeated except that a plurality of said anodes 501 and a plurality of said cathodes 502 are alternately arranged in the electrochemical treatment cell.
Example 10
Example 8 was repeated except that a plurality of said anodes 501 and a plurality of said cathodes 502 were arranged in pairs in an electrochemical treatment cell.
Example 11
Example 8 was repeated except that a plurality of said anodes 501 and a plurality of said cathodes 502 were successively arranged in the electrochemical treatment cell in a set of 2 anodes 501 and 1 cathode 502.
Example 12
Example 11 was repeated except that the anode 501 and the cathode 502 were each independently shaped as a flat plate structure.
Example 13
Example 12 was repeated except that a baffle 503 was provided on the same side of each anode 501 and each cathode 502.
Example 14
Example 13 is repeated except that the system further comprises a sludge treatment unit 8. The sludge treatment unit 8 includes a sludge thickener 801 and a press filtration dewatering device 802. Sludge outlets of the anaerobic fermentation tank 3, the aerobic aeration tank 4 and the chemical advanced treatment unit 5 are connected with a sludge inlet of a sludge concentration tank 801 through a sludge conveying device W, and a concentrated sludge outlet of the sludge concentration tank 801 is connected with a concentrated sludge inlet of a filter-pressing dehydration device 802.
Example 15
Example 14 is repeated, except that the sludge outlet of the anaerobic sedimentation tank 303 is respectively connected with the sludge return inlets of the hydrolytic acidification tank 2, the primary anaerobic fermentation tank 301 and the secondary anaerobic fermentation tank 302 through a plurality of first sludge return devices H1.
Example 16
Example 15 was repeated except that the sludge outlet of the primary aerobic sedimentation tank 402 was connected to the sludge return inlet of the primary aerobic aeration tank 401 via a second sludge return means H2. The sludge outlet of the secondary aerobic sedimentation tank 404 is connected with the sludge return inlet of the secondary aerobic aeration tank 403 through a third sludge return device H3.
Example 17
The embodiment 16 is repeated, except that a clean water circulating branch pipe L31 is also led out from the clean water discharge pipeline L3 and is connected with the water inlet of the water inlet regulating reservoir 1.
Claims (10)
1. A treatment system for industrial wastewater is characterized in that: the wastewater treatment system comprises a water inlet adjusting tank (1), a hydrolysis acidification tank (2), an anaerobic fermentation tank (3), an aerobic aeration tank (4), a chemical advanced treatment unit (5), a filtering unit (6) and a concentration unit (7); the wastewater inlet pipeline (L1) is communicated with the water inlet of the water inlet regulating tank (1); the water inlet adjusting tank (1), the hydrolysis acidification tank (2), the anaerobic fermentation tank (3), the aerobic aeration tank (4), the chemical advanced treatment unit (5), the filtering unit (6) and the concentration unit (7) are sequentially connected in series through a plurality of water conveying pipelines (L2); the purified water discharge pipeline (L3) is communicated with the water discharge port of the concentration unit (7);
wherein: the anaerobic fermentation tank (3) comprises at least one anaerobic fermentation unit; the anaerobic fermentation unit is formed by sequentially connecting a primary anaerobic fermentation tank (301), a secondary anaerobic fermentation tank (302) and an anaerobic sedimentation tank (303) in series;
the aerobic aeration tank (4) comprises at least one aerobic aeration unit; the aerobic aeration unit is formed by sequentially connecting a primary aerobic aeration tank (401), a primary aerobic sedimentation tank (402), a secondary aerobic aeration tank (403) and a secondary aerobic sedimentation tank (404) in series;
the chemical depth treatment unit (5) comprises one or more of the following devices: ozone oxidation treatment equipment, an electrochemical treatment pool, chemical catalytic oxidation treatment equipment, Fenton process treatment equipment and chemical specific reagent treatment equipment.
2. The processing system of claim 1, wherein: the filtering unit (6) comprises a multi-medium filter (601) and an ultrafiltration device (602) which are sequentially connected in series; the multi-medium filter (601) is positioned upstream of the ultrafiltration device (602) according to the trend of the water flow; the multi-media filter (601) is a multi-media filter comprising a quartz sand filter layer; the ultrafiltration device (602) is a ceramic flat membrane ultrafiltration device.
3. The processing system according to claim 1 or 2, characterized in that: the concentration unit (7) comprises a membrane concentration device (701) and an evaporation desalination device (702) which are connected in series in sequence; the membrane concentration device (701) is positioned at the upstream of the evaporation desalination device (702) according to the trend of the water flow; the membrane concentration device (701) is a reverse osmosis membrane and/or an electrodialysis device.
4. The processing system of claim 3, wherein: in a chemical depth treatment unit (5) containing an electrochemical treatment cell: the electrochemical treatment cell comprises an anode (501) and a cathode (502); the anode (501) is a combined anode formed by combining a sacrificial anode and an inert anode or a composite anode formed by using an alloy material containing a sacrificial metal and an inert metal, and a direct current voltage is provided between the combined anode and the cathode (502) or between the composite anode and the cathode (502) by a direct current power supply.
5. The processing system of claim 4, wherein: a plurality of anodes (501) and a plurality of cathodes (502) are arranged in the electrochemical treatment cell; a plurality of said anodes (501) and a plurality of said cathodes (502) are arranged alternately or in pairs in the electrochemical treatment cell.
6. The processing system of claim 5, wherein: 2-150 pairs of anodes (501) are arranged in the electrochemical treatment cell; and/or
2-150 pairs of cathodes (502) are disposed in the electrochemical treatment cell.
7. The processing system according to claim 5 or 6, wherein: a plurality of said anodes (501) and a plurality of said cathodes (502) are arranged alternately or in pairs or in succession in groups of 2 anodes (501) and 1 cathode (502) in an electrochemical treatment cell.
8. The processing system according to any one of claims 4-6, wherein: the shape of the anode (501) and the cathode (502) are respectively and independently one of a flat plate, a perforated plate, a grid, a grate, a fence or a wire mesh; and/or
And a flow guide plate (503) is correspondingly arranged on the same side of each anode (501) and each cathode (502).
9. The processing system of any of claims 1-2, 4-6, wherein: the system further comprises a sludge treatment unit (8); the sludge treatment unit (8) comprises a sludge concentration tank (801) and a filter-pressing dehydration device (802); the sludge outlets of the anaerobic fermentation tank (3), the aerobic aeration tank (4) and the chemical advanced treatment unit (5) are connected with the sludge inlet of the sludge concentration tank (801) through a sludge conveying device (W), and the concentrated sludge outlet of the sludge concentration tank (801) is connected with the concentrated sludge inlet of the filter-pressing dehydration equipment (802).
10. The processing system according to any one of claims 1-2, 4-6, wherein: a sludge outlet of the anaerobic sedimentation tank (303) is respectively connected with sludge backflow inlets of the hydrolysis acidification tank (2), the primary anaerobic fermentation tank (301) and the secondary anaerobic fermentation tank (302) through a plurality of first sludge backflow devices (H1); and/or
The sludge outlet of the primary aerobic sedimentation tank (402) is connected with the sludge return inlet of the primary aerobic aeration tank (401) through a second sludge return device (H2); a sludge outlet of the secondary aerobic sedimentation tank (404) is connected with a sludge return inlet of the secondary aerobic aeration tank (403) through a third sludge return device (H3); and/or
A purified water circulation branch pipe (L31) is also led out from the purified water discharge pipeline (L3) and is connected with a water inlet of the water inlet adjusting tank (1).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114644425A (en) * | 2020-12-21 | 2022-06-21 | 华岷环保科技(上海)有限公司 | Treatment method of cellulose ether industrial wastewater with high salt content and high COD value |
| CN115521022A (en) * | 2022-09-21 | 2022-12-27 | 陕西尚远水务有限公司 | Pre-concentration separation process for sewage by comprehensive utilization of water resources |
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2022
- 2022-03-11 CN CN202220534690.9U patent/CN216998076U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114644425A (en) * | 2020-12-21 | 2022-06-21 | 华岷环保科技(上海)有限公司 | Treatment method of cellulose ether industrial wastewater with high salt content and high COD value |
| CN115521022A (en) * | 2022-09-21 | 2022-12-27 | 陕西尚远水务有限公司 | Pre-concentration separation process for sewage by comprehensive utilization of water resources |
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