CN108373237B - Pesticide waste water's processing apparatus - Google Patents
Pesticide waste water's processing apparatus Download PDFInfo
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- CN108373237B CN108373237B CN201810247136.0A CN201810247136A CN108373237B CN 108373237 B CN108373237 B CN 108373237B CN 201810247136 A CN201810247136 A CN 201810247136A CN 108373237 B CN108373237 B CN 108373237B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 239000010914 pesticide waste Substances 0.000 title description 2
- 238000012545 processing Methods 0.000 title description 2
- 239000002351 wastewater Substances 0.000 claims abstract description 79
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 74
- 230000003197 catalytic effect Effects 0.000 claims abstract description 68
- 230000003647 oxidation Effects 0.000 claims abstract description 65
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 58
- 239000000575 pesticide Substances 0.000 claims abstract description 20
- 238000001179 sorption measurement Methods 0.000 claims abstract description 20
- 238000004519 manufacturing process Methods 0.000 claims abstract description 18
- 239000012528 membrane Substances 0.000 claims abstract description 16
- 238000000926 separation method Methods 0.000 claims abstract description 16
- 238000004069 wastewater sedimentation Methods 0.000 claims abstract description 13
- 239000004576 sand Substances 0.000 claims abstract description 12
- 238000001914 filtration Methods 0.000 claims abstract description 9
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 239000007789 gas Substances 0.000 claims description 34
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 27
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 20
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 14
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 14
- 239000011790 ferrous sulphate Substances 0.000 claims description 14
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 14
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 14
- 239000000243 solution Substances 0.000 claims description 13
- 239000003054 catalyst Substances 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 6
- 239000010802 sludge Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 4
- 239000006004 Quartz sand Substances 0.000 claims description 3
- 239000003463 adsorbent Substances 0.000 claims description 3
- 244000005700 microbiome Species 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 239000000835 fiber Substances 0.000 claims description 2
- 239000011259 mixed solution Substances 0.000 claims description 2
- 150000002894 organic compounds Chemical class 0.000 claims description 2
- 238000012856 packing Methods 0.000 claims 2
- 238000000034 method Methods 0.000 abstract description 20
- 238000000746 purification Methods 0.000 abstract description 4
- 238000007599 discharging Methods 0.000 abstract description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 6
- 230000001105 regulatory effect Effects 0.000 description 5
- 238000004065 wastewater treatment Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000010842 industrial wastewater Substances 0.000 description 3
- 229920002521 macromolecule Polymers 0.000 description 3
- 238000006385 ozonation reaction Methods 0.000 description 3
- 239000008213 purified water Substances 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000006065 biodegradation reaction Methods 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- WCXDHFDTOYPNIE-RIYZIHGNSA-N (E)-acetamiprid Chemical compound N#C/N=C(\C)N(C)CC1=CC=C(Cl)N=C1 WCXDHFDTOYPNIE-RIYZIHGNSA-N 0.000 description 1
- PXMNMQRDXWABCY-UHFFFAOYSA-N 1-(4-chlorophenyl)-4,4-dimethyl-3-(1H-1,2,4-triazol-1-ylmethyl)pentan-3-ol Chemical compound C1=NC=NN1CC(O)(C(C)(C)C)CCC1=CC=C(Cl)C=C1 PXMNMQRDXWABCY-UHFFFAOYSA-N 0.000 description 1
- 239000005875 Acetamiprid Substances 0.000 description 1
- 239000005839 Tebuconazole Substances 0.000 description 1
- 239000003905 agrochemical Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 231100000086 high toxicity Toxicity 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 239000011541 reaction mixture Substances 0.000 description 1
- 238000009287 sand filtration Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000004083 survival effect Effects 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8671—Removing components of defined structure not provided for in B01D53/8603 - B01D53/8668
- B01D53/8675—Ozone
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/722—Oxidation by peroxides
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/306—Pesticides
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
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- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/78—Details relating to ozone treatment devices
- C02F2201/784—Diffusers or nozzles for ozonation
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- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/02—Odour removal or prevention of malodour
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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Abstract
The invention relates to a device for treating pesticide production wastewater. The device is by raw materials waste water entry, waste water grid well, the waste water equalizing basin, fenton oxidation pond, the buffer pool, ozone catalytic oxidation reactor connects gradually, it is connected with tail gas catalytic adsorption integral type reactor to be equipped with the export at ozone catalytic oxidation reactor middle part, tail gas catalytic adsorption integral type reactor is equipped with exhaust port, ozone catalytic oxidation reactor is connected with the waste water sedimentation tank, the waste water sedimentation tank is connected with modular biological treatment pond, the membrane separation filtering ponds, the active sand filtering pond, the water purification collecting pit in proper order. The device can achieve the aim of efficiently treating the pesticide production wastewater. In addition, the invention can detect the concentration of ozone entering and discharging the whole process flow on line, and the tail gas catalytic adsorption integrated reactor is utilized to strictly ensure the tail gas to reach the standard by combining the means of catalytic oxidation reaction and physical adsorption, thereby avoiding the problem of secondary pollution in the treatment process.
Description
Technical Field
The invention belongs to the technical field of environment-friendly sewage treatment, and particularly relates to a treatment device for treating pesticide production wastewater.
Background
Statistics show that the discharge amount of industrial wastewater in 2015 of China is 199.5 million tons accounting for 27.1 percent of the total discharge amount of the wastewater, the discharge amount of chemical oxygen demand in the industrial wastewater is 293.5 million tons accounting for 13.2 percent of the total discharge amount of the chemical oxygen demand, and the discharge amount of ammonia nitrogen in the industrial wastewater is 21.7 million tons accounting for 9.4 percent of the total discharge amount of the ammonia nitrogen. But also with the rapid development and application of various new materials or processes, large amounts of more complex, more difficult to biochemically degrade waste water are formed. Especially, as a pesticide in a large country, the situation of pesticide production wastewater is more complicated. The pesticide production wastewater has the biggest characteristics of small wastewater amount, high toxicity and salinity, and the pesticide production wastewater causes no survival of microorganisms, thereby providing a serious challenge for the traditional treatment process mainly based on biodegradation, and the pesticide production wastewater reaching the standard is treated very little at present.
In order to overcome the limitation of a biodegradation method in the aspect of treating pesticide production wastewater, the generation amount and the generation rate of hydroxyl radicals can be greatly improved by considering the ozone catalytic oxidation, organic matters which are difficult to degrade or have low degradation efficiency are high in removal rate, and the ozone catalytic oxidation and related processes with relatively low cost and high treatment efficiency are more and more widely accepted and applied. Meanwhile, the catalysis and adsorption characteristics of the catalyst are combined with the strong oxidation performance of ozone, so that the organic matters are degraded more completely and the reaction is quicker and more thorough.
Although catalytic ozonation can oxidize most pollutants into carbon dioxide and water through catalytic oxidation reaction of macromolecules, organic matters which are difficult to biodegrade and ozone, the complex pesticide wastewater can hardly reach the standard by a single catalytic ozonation process.
Disclosure of Invention
The invention provides a pesticide production wastewater treatment device for making up the defects of the prior art, and the device can efficiently solve the problem of pesticide production wastewater.
The invention adopts the following technical scheme: raw materials waste water entry, waste water grid well, the waste water equalizing basin, fenton oxidation pond, the buffer pool, ozone catalytic oxidation reactor connects gradually, be equipped with the ozone entry on buffer pool and ozone catalytic oxidation reactor connecting pipe way, be equipped with the gas-liquid distributor at ozone catalytic oxidation reactor top, it is connected with tail gas catalytic adsorption integral type reactor bottom to be equipped with the export at ozone catalytic oxidation reactor middle part, tail gas catalytic adsorption integral type reactor top is equipped with tail gas discharge port, ozone catalytic oxidation reactor bottom is equipped with the export and is connected with the waste water sedimentation tank, the waste water sedimentation tank in proper order with modular biological treatment pond, the membrane separation filtering ponds, the active sand filter, the water purification collecting ponds are connected, be equipped with row mud mouth bottom modular biological treatment pond.
Further, a circulating water pump IA is arranged on a connecting pipeline between the Fenton oxidation pond and the buffer pond; a circulating water pump IIB is arranged on a connecting pipeline between the buffer tank and the ozone catalytic oxidation reactor; a circulating water pump IIIC is arranged on a connecting pipeline between the wastewater sedimentation tank and the modular biological treatment tank; and a circulating water pump IV D is arranged on a connecting pipeline of the modular biological treatment tank and the membrane separation filtering tank.
Furthermore, an air first-stage inlet is arranged at the bottom of the wastewater regulating tank.
Furthermore, an air second-section inlet is arranged at the bottom of the modular biological treatment pool.
Further, an air three-section inlet is arranged at the bottom of the membrane separation and filtration tank.
Furthermore, a hydrogen peroxide inlet, a ferrous sulfate solution inlet and a sulfuric acid inlet are arranged at the top of the Fenton oxidation pond.
Furthermore, a gas sample collection port a is arranged on one side of the upper part of the ozone catalytic oxidation reactor.
Furthermore, a gas sample collecting port b is arranged on one side of the upper part of the tail gas catalytic adsorption integrated reactor.
The invention makes full use of the catalytic oxidation technology to greatly improve the oxidation capacity of the ozone. Aiming at high-degradation-resistant macromolecules, firstly, the macromolecules are converted into easily-treated micromolecular substances through catalytic oxidation of ozone, the micromolecular substances are decomposed into a plurality of organic matter structures which are not biodegradable in raw material wastewater through the catalytic oxidation characteristic, and the purpose of efficiently treating the pesticide production wastewater is achieved by combining subsequent treatment processes of biochemical treatment of a modular biological treatment tank, membrane treatment of a membrane separation filter tank, sand filtration of an active sand filter tank and the like. In addition, the invention also fully considers the detection and treatment of the surplus ozone and the newly generated gas introduced into the process, can detect the concentration of the ozone entering and discharging the whole process flow on line, and utilizes the tail gas catalysis and adsorption integrated reactor to strictly ensure the tail gas to reach the standard by combining the means of catalytic oxidation reaction and physical adsorption, thereby well avoiding the problem of secondary pollution in the treatment process.
Drawings
FIG. 1 is a schematic view of the structure of a wastewater treatment apparatus for agricultural chemical production.
The system comprises a raw material wastewater inlet, a gas first-stage inlet, a hydrogen peroxide solution inlet, a ferrous sulfate solution inlet, a sulfuric acid inlet, a 6 ozone inlet, a 7 tail gas discharge outlet, a 8 air second-stage inlet, a 9 sludge discharge port, a 10 air third-stage inlet, a 101 wastewater grid well, a 102 wastewater adjusting tank, a 103 wastewater adjusting tank, a Fenton oxidation tank, a 104 buffer tank, a 105 ozone catalytic oxidation reactor, a 106 wastewater settling tank, a 107 exhaust gas catalytic adsorption integrated reactor, a 108 modular biological treatment tank, a 109 membrane separation filter tank, a 110 active sand, a 111, a collection water purification tank, a A, a circulating water pump I, B, a circulating water pump II, C, a circulating water pump III, D, a circulating water pump IV, a gas sample collection port I, and B gas sample collection port II.
Detailed Description
The invention is described in more detail below with reference to specific examples, without limiting the scope of the invention. Unless otherwise specified, the experimental methods adopted by the invention are all conventional methods, and experimental equipment, materials, reagents and the like used in the experimental method can be obtained from commercial sources.
As shown in fig. 1, a device for treating pesticide production wastewater comprises a raw material wastewater inlet 1, a wastewater grid well 101, a wastewater adjusting tank 102, a fenton oxidation tank 103, a buffer tank 104 and an ozone catalytic oxidation reactor 105 which are connected in sequence; the bottom of the wastewater regulating tank 102 is provided with an air first-stage inlet 2; a circulating water pump IA is arranged on a connecting pipeline between the Fenton oxidation pond 103 and the buffer pond 104; a hydrogen peroxide inlet 3, a ferrous sulfate solution inlet 4 and a sulfuric acid inlet 5 are arranged at the top of the Fenton oxidation pond 103; a circulating water pump IIB is arranged on a connecting pipeline between the buffer tank 104 and the ozone catalytic oxidation reactor 105; be equipped with ozone entry 6 on buffer pool 104 and ozone catalytic oxidation reactor 105 connecting pipeline, be equipped with gas sample collection mouth a on ozone catalytic oxidation reactor 105 upper portion one side, be equipped with the gas-liquid distributor at ozone catalytic oxidation reactor 105 top, it passes through the pipeline to be connected with tail gas catalytic adsorption integral type reactor 107 bottom to be equipped with the export in ozone catalytic oxidation reactor 105 middle part, tail gas catalytic adsorption integral type reactor 107 top is equipped with exhaust outlet 7, upper portion one side is equipped with gas sample collection mouth b. An outlet arranged at the bottom of the ozone catalytic oxidation reactor 105 is connected with a wastewater sedimentation tank 106, and the wastewater sedimentation tank 106 is sequentially connected with a modular biological treatment tank 108, a membrane separation filtering tank 109, an active sand filter 110 and a purified water collection tank 111; a circulating water pump IIIC is arranged on a connecting pipeline between the wastewater sedimentation tank 106 and the modular biological treatment tank 108; the bottom of the modular biological treatment pool 108 is provided with a sludge discharge port 9 and an air second-stage inlet 8. A circulating water pump IVD is arranged on a connecting pipeline of the modular biological treatment tank 108 and the membrane separation filtering tank 109, and an air three-section inlet 10 is arranged at the bottom of the membrane separation filtering tank 109.
The pesticide production wastewater treatment process comprises the following steps:
(1) pesticide production wastewater enters the wastewater grid well 101 through the raw material wastewater inlet 1, and part of pollutants are intercepted through grid channels of the wastewater grid well, and meanwhile, a circulating water pump and pipelines in the subsequent process are prevented from being blocked. Wastewater enters a wastewater adjusting tank 102 from a bottom channel between a wastewater grid well 101 and the wastewater adjusting tank 102; meanwhile, air from the air first-stage inlet 2 at the bottom of the wastewater regulating tank 102 tangentially enters the wastewater regulating tank 102 to strongly disturb wastewater, so that the wastewater quality is uniform.
(2) The waste water after air disturbance mixing enters a Fenton oxidation tank 103 through a waste water regulating tank 102, and in the Fenton oxidation tank 103, the mixed solution of hydrogen peroxide and ferrous sulfate and the waste water undergo a Fenton oxidation reaction to oxidize part of organic compounds into inorganic states. The concentration of the hydrogen peroxide added into the hydrogen peroxide inlet 3 is 20-30%, and the concentration of the ferrous sulfate solution added into the ferrous sulfate solution inlet 4 is 15-35%; controlling the molar ratio of the hydrogen peroxide to the ferrous sulfate to be between 2 and 5, simultaneously detecting the pH value of the wastewater in the Fenton oxidation pond 103, injecting a sulfuric acid solution with the concentration of 40 to 98 percent from a sulfuric acid inlet 5, and controlling the pH value of the wastewater in the Fenton oxidation pond 103 to be between 3 and 6.
(3) The wastewater subjected to preliminary oxidation treatment and adjusted in pH value is input into the buffer tank 104 from the Fenton oxidation tank 103 through the circulating water pump IA, and stays in the buffer tank 104 to further homogenize the water quality, the water temperature and the like of the wastewater subjected to preliminary treatment.
(4) The homogenized wastewater is mixed with 5-30mg/L ozone input by an ozone inlet 6 in a pipeline through a circulating water pump IIB, and uniformly enters the inside of the ozone catalytic oxidation reactor 105 through a gas-liquid distributor at the top of the ozone catalytic oxidation reactor 105, so that the wastewater is fully contacted with a catalyst in the ozone catalytic oxidation reactor 105, the catalytic oxidation reaction of the wastewater and the ozone is carried out on the surface of the catalyst, and most of organic pollutants which are large in molecular and difficult to biodegrade are oxidized into carbon dioxide and water through the catalytic oxidation reaction. The upper part of the ozone catalytic oxidation reactor 105 is filled with a catalyst, and a gas-liquid separation member is arranged below the catalyst. The top of the catalytic ozonation reactor 105 is provided with a gas sample collection port Ia.
(5) Unreacted ozone and a gas product generated by catalytic oxidation reaction flow into the tail gas catalytic adsorption integrated reactor 107 from an outlet in the middle of the ozone catalytic oxidation reactor 105, the tail gas catalytic adsorption integrated reactor 107 is divided into an upper section and a lower section, and the upper section is provided with a particle adsorbent which can adsorb the unreacted ozone; the lower section is provided with the same catalyst as the ozone catalytic oxidation reactor 105; ozone and part of gas products generated in the ozone catalytic oxidation reactor 105 are subjected to catalytic oxidation reaction, the reaction mixture after the reaction is physically adsorbed by a particle adsorbent, and tail gas reaching the emission standard is discharged from a tail gas discharge port 7; the wastewater after catalytic oxidation flows into a wastewater sedimentation tank 106 from the outlet at the bottom of the ozone catalytic oxidation reactor 105. And a gas sample collection port IIb is arranged at the top of the tail gas catalytic adsorption integrated reactor 107.
(6) Injecting the wastewater after the catalytic oxidation of the ozone in the wastewater sedimentation tank 106 into the modular biological treatment tank 108 through a circulating water pump IIIC; fiber type fixed fillers are filled in the modular biological treatment tank 108, and microorganisms are adsorbed and grown on the fillers; an air second-stage inlet 8 is arranged at the bottom of the modular biological treatment pool 108 to keep the aerobic environment of the water body. The wastewater is further purified by a biochemical treatment mode, and sludge produced in the treatment process is discharged from a sludge outlet 9 at the bottom of the modular biological treatment pool 108.
(7) The wastewater in the modular biological treatment pool 108 is injected into the membrane separation filter pool 109 through a circulating water pump IVD; and part of air is introduced into the air three-section inlet 10 to ensure constant pressure and stir the wastewater, and the wastewater is further separated and purified under the action of the membrane.
(8) The wastewater in the membrane separation filter tank 109 flows into an active sand filter tank 110, and the active sand filter tank 110 adopts granular quartz sand as a filter material, and the diameter range of the granular quartz sand is between 1 and 8 mm. The water flow reversely flows through the filter bed from bottom to top, the water filtered by the active sand filter 110 is gathered at the top of the active sand filter 110 and flows into the clean water collecting tank 111 through the overflow port, and finally the purification treatment of the pesticide production wastewater is completed.
Application example 1
Treating tebuconazole waste water by 20m3H, CODcr18000mg/L, ammonia nitrogen 500 mg/L. The treatment process of the pesticide production wastewater of the invention is used for completing a wastewater treatment process in a mode of continuously running for 10 hours on line and staying for 1 hour. The pH value of the Fenton oxidation pond is adjusted and controlled to be about 4 through a sulfuric acid solution, the feeding amount of 30% hydrogen peroxide is 120Kg/h, and the feeding amount of 30% ferrous sulfate is 100 Kg/h; the ozone concentration is 15mg/L, the flow rate is 150m3H is used as the reference value. After completing a batch operation according to the above process, the purified water indexes are measured as follows: CODcr is less than or equal to 200mg/L, and ammonia nitrogen is less than or equal to 50 mg/L.
Application example 2
Treatment of acetamiprid wastewater with a volume of 10m3H, CODcr25000mg/L and ammonia nitrogen 800 mg/L. The treatment process of the pesticide production wastewater of the invention is used for completing a wastewater treatment process in a mode of continuously running for 10 hours on line and staying for 1 hour. The pH value of the Fenton oxidation pond is adjusted and controlled to be about 5 by a sulfuric acid solution, the feeding amount of 30% hydrogen peroxide is 60Kg/h, and the feeding amount of 30% ferrous sulfate is 50 Kg/h; the ozone concentration is 15mg/L, and the flow rate is 100m3H is used as the reference value. After completing a batch operation according to the above process, the purified water indexes are measured as follows: CODcr is less than or equal to 180mg/L, and ammonia nitrogen is less than or equal to 60 mg/L.
The above description is only for the purpose of creating a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can substitute or change the technical solution and the inventive concept of the present invention within the technical scope of the present invention.
Claims (1)
1. A treatment device for pesticide production wastewater is characterized in that a raw material wastewater inlet (1), a wastewater grid well (101), a wastewater adjusting tank (102), a Fenton oxidation tank (103), a buffer tank (104) and an ozone catalytic oxidation reactor (105) are sequentially connected, wastewater enters the wastewater adjusting tank (102) through a bottom channel between the wastewater grid well (101) and the wastewater adjusting tank (102), an air first-section inlet (2) is arranged at the bottom of the wastewater adjusting tank (102), air from the air first-section inlet (2) tangentially enters the wastewater adjusting tank (102), and strong disturbance is carried out on the wastewater; a circulating water pump I (A) is arranged on a connecting pipeline of the Fenton oxidation pond (103) and the buffer pond (104); the top of the Fenton oxidation pond (103) is provided with a hydrogen peroxide inlet (3), a ferrous sulfate solution inlet (4) and a sulfuric acid inlet (5), in the Fenton oxidation pond (103), a mixed solution of hydrogen peroxide and ferrous sulfate and wastewater generate a Fenton oxidation reaction to oxidize part of organic compounds into inorganic state, the concentration of hydrogen peroxide added into the hydrogen peroxide inlet (3) is 20-30%, and the concentration of ferrous sulfate solution added into the ferrous sulfate solution inlet (4) is 15-35%; the mol ratio of the hydrogen peroxide to the ferrous sulfate is controlled between 2 and 5, a sulfuric acid solution with the concentration of 40 to 98 percent is injected from a sulfuric acid inlet (5), and the pH value of the wastewater in the Fenton oxidation pond (103) is controlled between 3 and 6; a circulating water pump II (B) is arranged on a connecting pipeline between the buffer pool (104) and the ozone catalytic oxidation reactor (105); an ozone inlet (6) is arranged on a connecting pipeline between the buffer pool (104) and the ozone catalytic oxidation reactor (105), a gas sample collecting port (a) is arranged on one side of the upper part of the ozone catalytic oxidation reactor (105), a catalyst is filled in the upper part of the ozone catalytic oxidation reactor (105), and a gas-liquid separation part is arranged below the catalyst; the top of the ozone catalytic oxidation reactor (105) is provided with a gas-liquid distributor, the middle of the ozone catalytic oxidation reactor (105) is provided with an outlet which is connected with the bottom of the tail gas catalytic adsorption integrated reactor (107) through a pipeline, the top of the tail gas catalytic adsorption integrated reactor (107) is provided with a tail gas discharge port (7), the tail gas catalytic adsorption integrated reactor (107) is divided into an upper section and a lower section, and the upper section is provided with a particle adsorbent which can adsorb unreacted ozone; the lower section is provided with the same catalyst as the catalyst in the ozone catalytic oxidation reactor (105); a gas sample collection port (b) is arranged on one side of the upper part of the tail gas catalytic adsorption integrated reactor (107); an outlet arranged at the bottom of the ozone catalytic oxidation reactor (105) is connected with a wastewater sedimentation tank (106), the wastewater sedimentation tank (106) is sequentially connected with a modular biological treatment tank (108), a membrane separation filter tank (109), an active sand filter tank (110) and a clean water collection tank (111), fiber type fixed packing is arranged in the modular biological treatment tank (108), and microorganisms are adsorbed and grown on the packing; a sludge discharge port (9) is arranged at the bottom of the modular biological treatment pool (108), and a circulating water pump III (C) is arranged on a connecting pipeline between the wastewater sedimentation pool (106) and the modular biological treatment pool (108); an air second-stage inlet (8) is arranged at the bottom of the modular biological treatment pool (108) to keep the aerobic environment of the water body; a circulating water pump IV (D) is arranged on a connecting pipeline of the modular biological treatment tank (108) and the membrane separation filtering tank (109); the bottom of the membrane separation filter tank (109) is provided with an air three-section inlet (10), and the active sand filter tank (110) adopts granular quartz sand as a filter material, and the diameter range of the active sand filter tank is 1-8 mm.
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| CN102951755A (en) * | 2012-11-23 | 2013-03-06 | 南京格洛特环境工程有限公司 | Processing method and processing equipment of rear earth wastewater |
| CN106396270A (en) * | 2016-10-26 | 2017-02-15 | 云南炳森环境工程有限公司 | High-concentration pharmaceutical wastewater treatment system and treatment method |
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| CN102951755A (en) * | 2012-11-23 | 2013-03-06 | 南京格洛特环境工程有限公司 | Processing method and processing equipment of rear earth wastewater |
| CN106396270A (en) * | 2016-10-26 | 2017-02-15 | 云南炳森环境工程有限公司 | High-concentration pharmaceutical wastewater treatment system and treatment method |
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Application publication date: 20180807 Assignee: Dalian Kaichang Environmental Engineering Co.,Ltd. Assignor: DALIAN University Contract record no.: X2023210000247 Denomination of invention: A treatment device for pesticide production wastewater Granted publication date: 20200922 License type: Common License Record date: 20231129 |
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