CN115536186A - Method and device for treating wastewater containing phosphorus and chlorobenzene - Google Patents
Method and device for treating wastewater containing phosphorus and chlorobenzene Download PDFInfo
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- CN115536186A CN115536186A CN202110741483.0A CN202110741483A CN115536186A CN 115536186 A CN115536186 A CN 115536186A CN 202110741483 A CN202110741483 A CN 202110741483A CN 115536186 A CN115536186 A CN 115536186A
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- chlorobenzene
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- MVPPADPHJFYWMZ-UHFFFAOYSA-N chlorobenzene Chemical compound ClC1=CC=CC=C1 MVPPADPHJFYWMZ-UHFFFAOYSA-N 0.000 title claims abstract description 162
- 239000002351 wastewater Substances 0.000 title claims abstract description 95
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 37
- 239000011574 phosphorus Substances 0.000 title claims abstract description 37
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 37
- 238000000034 method Methods 0.000 title claims abstract description 34
- 230000003647 oxidation Effects 0.000 claims abstract description 91
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 91
- 239000002912 waste gas Substances 0.000 claims abstract description 52
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 42
- 238000004062 sedimentation Methods 0.000 claims abstract description 38
- 239000003054 catalyst Substances 0.000 claims abstract description 29
- 239000007800 oxidant agent Substances 0.000 claims abstract description 24
- 230000001590 oxidative effect Effects 0.000 claims abstract description 22
- 238000000265 homogenisation Methods 0.000 claims abstract description 18
- 239000010802 sludge Substances 0.000 claims abstract description 18
- 239000007789 gas Substances 0.000 claims abstract description 16
- 238000003825 pressing Methods 0.000 claims abstract description 8
- 238000007599 discharging Methods 0.000 claims abstract description 7
- 230000003139 buffering effect Effects 0.000 claims abstract description 6
- 230000014759 maintenance of location Effects 0.000 claims description 22
- 238000002156 mixing Methods 0.000 claims description 20
- 239000008394 flocculating agent Substances 0.000 claims description 16
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical group OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 13
- 239000002253 acid Substances 0.000 claims description 12
- 239000003513 alkali Substances 0.000 claims description 10
- 238000001556 precipitation Methods 0.000 claims description 8
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 7
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 6
- 230000007935 neutral effect Effects 0.000 claims description 6
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 5
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 5
- 239000000203 mixture Substances 0.000 claims description 5
- 229910052742 iron Inorganic materials 0.000 claims description 4
- 238000004065 wastewater treatment Methods 0.000 claims description 4
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 3
- 229910001448 ferrous ion Inorganic materials 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 2
- VTLYFUHAOXGGBS-UHFFFAOYSA-N Fe3+ Chemical compound [Fe+3] VTLYFUHAOXGGBS-UHFFFAOYSA-N 0.000 claims 1
- 229910001447 ferric ion Inorganic materials 0.000 claims 1
- 239000012530 fluid Substances 0.000 claims 1
- 230000001376 precipitating effect Effects 0.000 claims 1
- 230000001105 regulatory effect Effects 0.000 claims 1
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 abstract description 62
- 229910000073 phosphorus hydride Inorganic materials 0.000 abstract description 31
- 239000010865 sewage Substances 0.000 abstract description 15
- 238000006243 chemical reaction Methods 0.000 abstract description 14
- 230000003197 catalytic effect Effects 0.000 abstract description 10
- 229910019142 PO4 Inorganic materials 0.000 abstract description 6
- 239000010452 phosphate Substances 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 abstract description 5
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- 231100000719 pollutant Toxicity 0.000 abstract description 4
- 238000005189 flocculation Methods 0.000 abstract description 3
- 230000016615 flocculation Effects 0.000 abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 15
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 10
- 239000011575 calcium Substances 0.000 description 10
- 229910052791 calcium Inorganic materials 0.000 description 10
- 239000000701 coagulant Substances 0.000 description 9
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 7
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 5
- 229920002401 polyacrylamide Polymers 0.000 description 5
- -1 polytetrafluoroethylene Polymers 0.000 description 5
- 235000012239 silicon dioxide Nutrition 0.000 description 5
- 235000011121 sodium hydroxide Nutrition 0.000 description 5
- 239000003814 drug Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000010453 quartz Substances 0.000 description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 3
- 239000004912 1,5-cyclooctadiene Substances 0.000 description 2
- HGUFODBRKLSHSI-UHFFFAOYSA-N 2,3,7,8-tetrachloro-dibenzo-p-dioxin Chemical compound O1C2=CC(Cl)=C(Cl)C=C2OC2=C1C=C(Cl)C(Cl)=C2 HGUFODBRKLSHSI-UHFFFAOYSA-N 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 2
- 239000004698 Polyethylene Substances 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000008139 complexing agent Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 2
- 244000005700 microbiome Species 0.000 description 2
- 150000007524 organic acids Chemical class 0.000 description 2
- 229920000573 polyethylene Polymers 0.000 description 2
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000001988 toxicity Effects 0.000 description 2
- 231100000419 toxicity Toxicity 0.000 description 2
- 206010033799 Paralysis Diseases 0.000 description 1
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000009303 advanced oxidation process reaction Methods 0.000 description 1
- 239000012298 atmosphere Substances 0.000 description 1
- 238000011001 backwashing Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000002306 biochemical method Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 238000009841 combustion method Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000005108 dry cleaning Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000011790 ferrous sulphate Substances 0.000 description 1
- 235000003891 ferrous sulphate Nutrition 0.000 description 1
- 231100000086 high toxicity Toxicity 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 239000000976 ink Substances 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- 235000012245 magnesium oxide Nutrition 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 239000013335 mesoporous material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 235000005985 organic acids Nutrition 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 230000001699 photocatalysis Effects 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 238000000053 physical method Methods 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 239000002455 scale inhibitor Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000011949 solid catalyst Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000009279 wet oxidation reaction Methods 0.000 description 1
Images
Classifications
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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
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
-
- 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
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved 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
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
-
- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
-
- 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
-
- 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
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- 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
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F2101/36—Organic compounds containing halogen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/043—Treatment of partial or bypass streams
Abstract
The invention belongs to the field of advanced oxidation sewage treatment, and particularly relates to a method and a device for treating phosphorus-containing chlorobenzene-containing wastewater, wherein the wastewater firstly enters a homogenization tank for buffering, then is mixed with water at the lower outlet of an oxidation tank, is added with a liquid catalyst and an oxidant, is mixed with chlorobenzene waste gas at the top of the homogenization tank, and then enters a UV generator for oxidation cycle treatment; controlling the adding amount of the catalyst to ensure the treatment efficiency of organic phosphine and chlorobenzene, adjusting the pH value of effluent from the upper part of the oxidation tank by flocculation, feeding the effluent into a sedimentation tank, discharging the effluent of the sedimentation tank after reaching the standard, and treating sludge after filter pressing; and tail gas is discharged from the top of the oxidation tank after reaching the standard. The invention utilizes the same device to treat the waste water and the waste gas, thereby saving the investment and the occupied area of the subsequent waste gas; homogeneous catalytic oxidation is adopted, reaction conditions are controlled, and the influence of catalyst blockage caused by phosphate radical scaling is prevented; the same device is adopted to solve the problem of removing two characteristic pollutants of organic phosphine and chlorobenzene.
Description
Technical Field
The invention belongs to the field of advanced oxidation sewage treatment, and particularly relates to a method and a device for treating phosphorus-containing chlorobenzene-containing wastewater.
Background
Along with the development of the industry in China, the application of organic phosphine in the fields of pesticides, catalysts, scale inhibitors, mesoporous materials, luminescent materials and the like is more and more extensive, and the treatment of wastewater containing organic phosphine is a difficult problem in the field of domestic and foreign water treatment. Along with the increasingly stricter and stricter requirements of China on the external wastewater discharge, the control on the total phosphorus concentration of the wastewater is increasingly strict, the wastewater has high toxicity, more difficultly-degradable substances and poor biodegradability, other wastewater with better biodegradability needs to be mixed or diluted by adopting a biochemical method for treatment, and the problems of insufficient oxidation capacity and high operation cost sometimes exist by adopting an advanced oxidation technology for treatment. The biochemical or advanced oxidation process adopted for treating the organic phosphine wastewater basically comprises the steps of oxidizing the organic phosphine wastewater into inorganic phosphorus wastewater, and then removing inorganic phosphorus to reach the discharge standard.
Chlorobenzene is a common chemical raw material, can be used for preparing solvents, rubber auxiliaries, paints, quick-drying inks, dry cleaning agents and the like, and also can be used for organic synthesis, raw material inspection and the like. The chlorobenzene-containing wastewater has serious harm to the environment and can cause pollution to water, soil and atmosphere. Therefore, the chlorobenzene waste water treatment necessarily involves waste water and waste gas treatment.
According to the physical properties of chlorobenzene, high-concentration chlorobenzene in water can be treated by physical methods, namely an adsorption method, a rectification method and a gas stripping method, and if low-concentration chlorobenzene wastewater is directly discharged to a sewage farm for treatment, the low-concentration chlorobenzene wastewater inevitably affects activated sludge of the sewage farm, so that the treatment efficiency of the sewage farm is reduced and even paralysis is caused. Although activated sludge for degrading chlorobenzene can be acclimated for a long time, sewage farm sludge is impacted again when the concentration of the incoming chlorobenzene fluctuates. Therefore, the chlorobenzene-containing wastewater must be treated separately, and enters a sewage field for treatment after the toxicity to microorganisms is removed or is directly and separately treated to reach the discharge standard. When chlorobenzene waste gas is treated, the conventional combustion method treatment facilities of a factory are not suitable to be adopted, or dioxin is generated to cause secondary pollution, and a set of treatment system is required to be independently arranged for treating waste gas by an oxidation method, so that the operation is complex.
When the wastewater contains organic phosphine and chlorobenzene, the treatment difficulty is greatly increased. Advanced oxidation technology is widely applied to the treatment of sewage difficult to be biochemically degraded, such as Fenton oxidation, photocatalytic oxidation, high-temperature wet catalytic oxidation and the like. Although the Fenton oxidation can decompose the organic matters in the sewage into small molecules or open rings, the complete oxidation is difficult even if an excessive amount of oxidant is added; the high-temperature wet oxidation has strong oxidation capacity, organic matters are removed more thoroughly, but harsh conditions of high temperature, high pressure and corrosion resistance are required, the equipment investment is large, the operation cost is high, and potential safety hazards exist. The ozone catalytic oxidation greatly improves the ozone oxidation capability and simultaneously reduces the operation cost, and has the problems that phosphate radicals are easy to precipitate with calcium, iron and other ions in water to block catalyst pore channels.
Patent CN106865825A discloses a method for treating wastewater containing benzene and chlorobenzene, which comprises the steps of adjusting the pH value of wastewater to be treated, adding a flocculant, mixing uniformly, filtering to remove precipitate, and finally performing efficient catalytic oxidation on the wastewater without precipitate to remove benzene and chlorobenzene. The wastewater after the precipitation is removed is firstly treated by microwave, the reaction time is 1.5 to 2 hours, then the high-efficiency catalytic oxidation is carried out, and the ozone enters the tower from the bottom of the tower; the adding amount of the ozone is 50-1000 mg/L, the adding amount of the hydrogen peroxide is 0.1-1 per mill, the pH is adjusted to 6.5-8, and the retention time is 0.1-5 h, and then the treatment is finished. The invention has long process, adopts microwave, and also adds two oxidants of ozone and hydrogen peroxide, has high operation cost, and simultaneously requires the SS of inlet water to be less than 20mg/L by a catalytic oxidation device, thereby setting a multi-media filter, leading to further increase of the operation cost, and inevitably causing the chlorobenzene waste gas to diffuse to the environment during the treatment process, particularly during the backwashing of the multi-media filter.
Patent CN 106745613B discloses a method for treating organophosphine precipitant and high-concentration organophosphine-containing wastewater, wherein anhydrous ferrous sulfate, magnesium oxide, silicon dioxide, and manganese oxide are uniformly mixed according to a predetermined mass portion, and then under the auxiliary action of hydrogen peroxide, by adjusting the pH value of the organophosphine wastewater, the organophosphine precipitant can directly react with organophosphonate to generate insoluble organophosphonate for homogeneous precipitation, so as to more thoroughly remove total phosphorus; in addition, a small amount of ferrous ions contained in the organic phosphine precipitator can catalyze hydrogen peroxide to generate hydroxyl free radicals with strong oxidizability, so that organic acids and organic amine complexing agents in water are damaged, and phosphine in wastewater can be directly removed by precipitation after the organic acid and the organic amine complexing agents are adjusted to be alkaline. The method adopts the medicament to precipitate the organic phosphine, has selectivity to the organic phosphine, and has large medicament adding amount and high operation cost.
In summary, the following technical problems exist in the current advanced treatment process of the waste water containing phosphine and chlorobenzene:
1. the wastewater has toxicity to microorganisms, and is not suitable for being directly treated by activated sludge in a sewage farm.
2. The wastewater treatment process is long, the types of the added medicaments are large, the adding amount of multiple medicaments is large, and the operation cost is high.
3. After the organic phosphine is converted into inorganic phosphorus, the organic phosphine is easy to scale and block the pore channels on the surface of the catalyst.
4. The chlorobenzene waste water has large peculiar smell, the sewage treatment facility and the waste gas treatment facility are separately arranged, the treatment cost is high, and the occupied area is large.
5. Chlorobenzene waste gas is not easy to burn, and dioxin is easily generated by high-temperature incineration treatment and is harmful to the environment.
Disclosure of Invention
The technical problem to be solved by the invention is as follows: the method overcomes the defects of the prior art, and solves the problems of multiple types of oxidants, long flow, high operation cost and independent treatment of waste gas in the prior treatment process of the phosphorus-containing chlorobenzene-containing wastewater; the method and the device for treating the chlorobenzene-containing wastewater with high oxidation efficiency, high organic matter degradation efficiency, short flow, small occupied area, waste gas treatment and stable operation are provided.
The invention relates to a method for treating wastewater containing phosphorus and chlorobenzene, which comprises the steps of firstly carrying out buffer treatment on the wastewater, naturally volatilizing chlorobenzene waste gas into an air layer in a tank, then adding a catalyst and an oxidant into the buffered wastewater, mixing the wastewater with the chlorobenzene waste gas, then feeding the mixture into a UV generator for oxidation cycle treatment, adding a flocculating agent into the wastewater after the oxidation cycle treatment, adjusting the pH value to be neutral, carrying out precipitation treatment, and discharging the effluent which reaches the standard.
The method for treating the wastewater containing phosphorus and chlorobenzene comprises the following steps:
(1) Homogenizing: the wastewater enters a homogenizing tank filled with air for buffering treatment, and chlorobenzene waste gas naturally volatilizes into the air in the tank; aims to homogenize the waste water;
(2) And (3) oxidation: mixing the buffered wastewater with outlet water at the lower part of an oxidation tank, adding a catalyst and an oxidant, mixing with chlorobenzene waste gas, entering a UV generator, and returning outlet water to the oxidation tank added with acid liquor for oxidation cycle treatment; aims to efficiently degrade organic phosphine, chlorobenzene and other organic matters in waste water and waste gas under the multiple actions of an oxidant, a catalyst and a UV generator lamp tube under an acidic condition and prevent phosphate from scaling; the tail gas after the step is discharged from the top of the oxidation tank after reaching the standard;
(3) And (3) precipitation: adding a flocculating agent into the wastewater subjected to oxidation cycle treatment, adjusting the pH value to be neutral, and then allowing the wastewater to enter a sedimentation tank for sedimentation treatment; the catalyst and phosphate added in the sedimentation tank are settled along with flocculation;
(4) Draining and deslagging: the effluent of the sedimentation tank is discharged out after reaching the standard, and the sludge is sent to a sludge filter pressing system.
The treatment device comprises a waste water pipeline, a homogenizing tank and an oxidation tank, wherein a one-way air inlet and a waste gas pipeline are arranged at the upper part of the homogenizing tank, the oxidation tank is connected with an acid liquor tank, a lower outlet circulating pipeline is arranged at the bottom of the oxidation tank, the lower outlet circulating pipeline is respectively connected with a catalyst feeding line and an oxidant feeding line, the waste water pipeline is connected with the homogenizing tank, a water outlet of the homogenizing tank is connected with the lower outlet circulating pipeline through a lift pump, the waste gas pipeline and the lower outlet circulating pipeline are both connected with a UV generator through a mixing circulating pump, the UV generator is connected with the oxidation tank, the upper part of the oxidation tank is connected with a sedimentation tank, and the sedimentation tank is respectively connected with a flocculating agent tank and an alkali liquor tank.
The upper part of the oxidation tank is provided with an exhaust gas discharge port.
The bottom of the sedimentation tank is connected with a sludge filter pressing system.
The homogenization tank is a conventional homogenization tank, and the hydraulic retention time of buffer treatment in the homogenization tank is preferably 1-8 h.
The material of the oxidation tank is preferably but not limited to polytetrafluoroethylene, polyethylene and lining anti-corrosion material; the hydraulic retention time is preferably 1-4 h calculated by water inflow; the oxidizing agent is preferably, but not limited to, hydrogen peroxide solution; preferably, the ratio of the dry-basis addition amount to the inlet water COD is 2.
The reaction temperature of the oxidation tank is preferably controlled to be 45-50 ℃, the control mode can be circulating water heat exchange cooling, and the ultraviolet lamp power control is preferably adopted.
Acid liquor is added into the oxidation tank, and the pH value in the oxidation tank is controlled to be 2.0-2.5
The water outlet flow of the oxidation tank is 1-3 times of the flow of the lift pump.
The air-water mixing circulating pump is preferably selected as the mixing circulating pump, the effluent flow of the oxidation tank and the flow of the lift pump are designed, and the air-water ratio of the waste gas to the waste water is preferably 1. The air inflow is controlled by the homogeneous tank to the air port.
The ultraviolet light generator consists of a power supply, an ultraviolet lamp tube and a reaction tube.
The ultraviolet lamp tube is a lamp tube capable of generating ultraviolet light with the wavelength of 200-400 nm, preferably a high-pressure ultraviolet lamp tube, and preferably the installation power is 1000-3000 w/m 3 。
The reaction tube is divided into a quartz sleeve region and a sewage region, and the quartz sleeve is preferably made of quartz and used for isolating the ultraviolet lamp tube from a wastewater medium; the material of the waste water and waste gas reaction area is preferably, but not limited to quartz, polytetrafluoroethylene and polyethylene. The effective volume is preferably 10 to 20s in terms of the hydraulic retention time of the influent water.
The flocculant is conventional polyaluminium chloride or polyaluminium ferric chloride, the adding concentration is 0-100 mg/L, and a polyacrylamide coagulant aid is further preferably added for assisting flocculation, wherein the adding concentration is 1-5 mg/L.
The sedimentation tank calculates the hydraulic retention time by water inflow and preferably selects 30-60 min, and the pH value of the sedimentation tank is preferably controlled to be 7-8 by the adding amount of liquid caustic soda.
The catalyst is preferably but not limited to soluble salts of iron ions and ferrous ions. The adding amount is preferably controlled to be 50-100 mg/L of the total iron concentration in the oxidation tank.
The acid solution is preferably, but not limited to, sulfuric acid and hydrochloric acid; the alkali solution is preferably, but not limited to, sodium hydroxide solution and potassium hydroxide solution.
The sludge filter pressing system is a conventional filter pressing system, and sludge filter pressing liquid returns to the inlet of the sedimentation tank.
The wastewater enters the homogenization tank for buffering, and then enters the lower outlet circulation pipeline of the oxidation tank through the lift pump; the top of the homogenizing tank is provided with a one-way air inlet, and the chlorobenzene-containing waste gas also escapes from a top pipeline. And (3) mixing the effluent of the homogenizing tank with the water at the lower outlet of the oxidation tank, adding a catalyst and an oxidant, mixing with the waste gas of the homogenizing tank through a gas-water mixing circulating pump, and then feeding the mixed gas into a UV generator, wherein the effluent of the UV generator returns to the middle lower part of the oxidation tank for circular treatment. Acid is added into the oxidation tank to control the pH value of the reaction, the waste water and waste gas mixture is oxidized in the UV generator to remove chlorobenzene, and the residual organic phosphine and other organic matters are gradually and efficiently degraded in the circulation process. Adding a flocculating agent into the wastewater with degraded organic matters on the upper part of the oxidation tank, adjusting the pH value to be neutral by using liquid alkali, then, feeding the wastewater into a sedimentation tank, discharging the effluent of the sedimentation tank after reaching the standard, conveying sludge at the bottom of the sedimentation tank to a filter pressing system, and discharging tail gas from the top of the oxidation tank after reaching the standard.
The waste gas is introduced into the waste water treatment pipeline, and the waste water and the waste gas are treated by using the same device, so that the subsequent waste gas investment and the occupied area are saved; homogeneous catalytic oxidation is adopted, reaction conditions are controlled, and the influence of catalyst blockage caused by phosphate radical scaling is prevented; the same device is adopted to solve the problem of removing two characteristic pollutants of organic phosphine and chlorobenzene.
Compared with the prior art, the invention has the following beneficial effects:
1. the invention has short flow and small floor area; when the waste water is treated, a new device is not needed to treat the waste gas, so that the investment and the occupied area of subsequent waste gas treatment are saved.
2. The invention has high advanced oxidation efficiency, and completely removes organic matters, especially organic phosphine and chlorobenzene characteristic pollutants.
3. The pH value range controlled by the invention not only can effectively ensure the oxidation efficiency, but also can prevent the phosphate from scaling.
4. The invention does not adopt solid catalyst, thus avoiding the problem of scaling.
5. The method has the advantages of low addition amount of the oxidant, conventional and easily-obtained catalyst, low operation cost, increased environmental capacity of enterprises, and good application prospect and environmental benefit.
Drawings
FIG. 1 is a schematic view of the structure of the present invention;
in the figure: 1. a waste water line; 2. homogenizing tank; 3. a one-way air inlet; 4. an exhaust gas line; 5. a lift pump; 6. a lower outlet recycle line; 7. a catalyst feed line; 8. an oxidant feed line; 9. a mixing and circulating pump; 10. a UV generator; 11. an oxidation tank; 12. an acid liquor tank; 13. an exhaust gas discharge port; 14. a sedimentation tank; 15. a flocculant tank; 16. an alkali liquor tank; 17. a sludge press filtration system; 18. and a water outlet.
Detailed Description
The invention is further described with reference to the following figures and examples.
As shown in fig. 1, the treatment device for the method for treating the phosphorus-containing chlorobenzene-containing wastewater comprises a wastewater pipeline 1, a homogenization tank 2 and an oxidation tank 11, wherein a one-way air inlet 3 and a waste gas pipeline 4 are arranged at the upper part of the homogenization tank 2, the oxidation tank 11 is connected with an acid liquor tank 12, a lower outlet circulation pipeline 6 is arranged at the bottom of the oxidation tank 11, a waste gas discharge port 13 is arranged at the upper part of the oxidation tank 11, the lower outlet circulation pipeline 6 is respectively connected with a catalyst feeding line 7 and an oxidant feeding line 8, the wastewater pipeline 1 is connected with the homogenization tank 2, a water outlet of the homogenization tank 2 is connected with the lower outlet circulation pipeline 6 through a lift pump 5, the waste gas pipeline 4 and the lower outlet circulation pipeline 6 are both connected with a UV generator 10 through a mixing and circulating pump 9, the UV generator 10 is connected with the oxidation tank 11, the upper part of the oxidation tank 11 is connected with a sedimentation tank 14, and the sedimentation tank 14 is respectively connected with a flocculant tank 15 and an alkali liquor tank 16; the bottom of the sedimentation tank 14 is connected with a sludge press filtration system 17, and a water outlet 18 is arranged on the sedimentation tank 14.
The method for treating the phosphorus-containing chlorobenzene-containing wastewater comprises the following steps: by adopting the device shown in FIG. 1, wastewater firstly enters the homogenization tank 2 through the wastewater pipeline 1 for buffering and then enters the lower outlet circulation pipeline 6 of the oxidation tank 11 through the lift pump 5; a unidirectional air inlet 3 is arranged at the top of the homogenization tank 2, and chlorobenzene-containing waste gas also escapes from a top waste gas pipeline 4. The effluent of the homogenization tank 2 is mixed with the lower outlet water of the oxidation tank 11, then catalyst and oxidant are added, the mixture is mixed with the exhaust gas of the homogenization tank 2 through a gas-water mixing and circulating pump 9 and then enters a UV generator 10, and the effluent of the UV generator 10 returns to the middle lower part of the oxidation tank 11 for circular treatment. Acid is added into an oxidation tank 11 to control the pH value of the reaction, the waste water and waste gas mixture is oxidized in a UV generator 10 to remove chlorobenzene, and the residual organic phosphine and other organic matters are gradually and efficiently degraded in the circulation process. Adding a flocculating agent into the wastewater with degraded organic matters on the upper part of the oxidation tank 11, adjusting the pH value to be neutral by using liquid alkali, then feeding the wastewater into a sedimentation tank 14, discharging the effluent of the sedimentation tank 14 to reach the standard, conveying sludge at the bottom of the sedimentation tank to a sludge press filtration system 17, and discharging the tail gas from a waste gas discharge port 13 at the top of the oxidation tank 11 to reach the standard.
The embodiment adopts the device and the treatment method to treat the wastewater.
Example 1
The concentration of chlorobenzene in waste water of a special rubber device is 200-350 mg/L, the concentration of organic phosphine is 100-120 mg/L, COD is 800-900 mg/L, total phosphorus is 8.6-9.2 mg/L, and calcium hardness is 100-120 mg/L. The operating parameters are as follows.
Homogenizing the tank: the hydraulic retention time is preferably 8h.
An oxidation tank: the proportion of oxidant dry basis addition and influent COD is 6, the hydraulic retention time is preferably 4h, the reaction temperature is 50 ℃, the pH value is 2.0-2.3, the effluent flow is 3 times of the lift pump flow, the gas-water ratio of the waste gas and the wastewater in the gas-water mixing pump is preferably 1.
UV reactor: the ultraviolet wavelength is 200-400 nm, and the power is 3000w/m 3 And the sewage area of the reaction pipe has hydraulic retention time of 10s.
A sedimentation tank: the adding concentration of the flocculating agent is 50mg/L, the adding concentration of the coagulant aid is 3mg/L, the hydraulic retention time is 60min, and the pH value is 7-8.
The acid solution is 98% concentrated sulfuric acid, the alkali solution is 30% sodium hydroxide solution, the catalyst is 30% ferric chloride solution, the oxidant is 27.5% industrial grade hydrogen peroxide solution, the flocculating agent is 10% polyaluminium chloride solution, and the coagulant aid is 1% polyacrylamide solution.
Run 1 month results: the concentration of chlorobenzene at the waste gas outlet of the homogeneous tank is 100-150 mg/m 3 The concentration of chlorobenzene at the top of the oxidation tank is 1-2 mg/m 3 ；
The concentration of chlorobenzene in the effluent of the sedimentation tank is less than 0.1mg/L, COD is 30-35 mg/L, organic phosphine is not detected, total phosphorus is 0.2-0.3 mg/L, and calcium hardness is 90-110 mg/L. Chlorobenzene waste gas, chlorobenzene, COD, organic phosphine and total phosphorus in water are efficiently removed, and the emission requirement of GB31571-2015 is met.
Example 2
The concentration of chlorobenzene in waste water of a certain gas stripping device is 60-100 mg/L, the concentration of organic phosphine is 50-60 mg/L, COD is 300-350 mg/L, total phosphorus is 5.6-6.2 mg/L, and calcium hardness is 50-60 mg/L. The operating parameters are as follows.
Homogenizing the tank: the hydraulic retention time is preferably 1h.
An oxidation tank: the proportion of oxidant dry basis addition and influent COD is 2, the hydraulic retention time is preferably 1h, the reaction temperature is 45 ℃, the pH value is 2.3-2.5, the effluent flow is 1 time of the lift pump flow, the gas-water ratio of the waste gas and the wastewater in the gas-water mixing pump is preferably 1.
UV reactor: the ultraviolet wavelength is 200-400 nm, and the power is 1000w/m 3 The sewage area of the reaction pipe has hydraulic retention time of 20s.
A sedimentation tank: the adding concentration of the flocculating agent is 0mg/L, the adding concentration of the coagulant aid is 1mg/L, the hydraulic retention time is 30min, and the pH value is 7-8.
The acid solution is 98% concentrated sulfuric acid, the alkali solution is 30% sodium hydroxide solution, the catalyst is 30% ferric chloride solution, the oxidant is 27.5% industrial grade hydrogen peroxide solution, the flocculating agent is 10% polyaluminium chloride solution, and the coagulant aid is 1% polyacrylamide solution.
Run 2 weeks results: the concentration of chlorobenzene at the waste gas outlet of the homogeneous tank is 50-100 mg/m 3 The chlorobenzene concentration at the top of the oxidation tank is 0.3-0.8 mg/m 3 ；
The concentration of chlorobenzene in the effluent of the sedimentation tank is less than 0.1mg/L, COD is 40-45 mg/L, organic phosphine is not detected, total phosphorus is 0.3-0.4 mg/L, and calcium hardness is 50-60 mg/L. Chlorobenzene waste gas, chlorobenzene, COD, organic phosphine and total phosphorus in water are efficiently removed, and the emission requirement of GB31571-2015 is met.
Example 3
The concentration of chlorobenzene in chemical wastewater is 100-200 mg/L, the concentration of organic phosphine is 250-300 mg/L, COD is 500-650 mg/L, total phosphorus is 16.0-20.0 mg/L, and calcium hardness is 100-110 mg/L. The operating parameters are as follows.
Homogenizing the tank: the hydraulic retention time is preferably 4h.
An oxidation tank: the proportion of oxidant dry basis addition and water inflow COD is 4, the hydraulic retention time is preferably 3h, the reaction temperature is 52 ℃, the pH value is 2.2-2.4, the water outflow is 2 times of the lift pump flow, the ratio of waste gas to waste water in the gas-water mixing pump is preferably 1.
UV reactor: the ultraviolet wavelength is 200-400 nm, and the power is 2000w/m 3 And the sewage area of the reaction pipe has the hydraulic retention time of 20s.
A sedimentation tank: the adding concentration of the flocculating agent is 100mg/L, the adding concentration of the coagulant aid is 3mg/L, the hydraulic retention time is 50min, and the pH value is 7-8.
The acid solution is 98% concentrated sulfuric acid, the alkali solution is 30% sodium hydroxide solution, the catalyst is 30% ferric chloride solution, the oxidant is 27.5% industrial grade hydrogen peroxide solution, the flocculating agent is 10% polyaluminium chloride solution, and the coagulant aid is 1 ‰ polyacrylamide solution.
Run 1 month results: the concentration of chlorobenzene at the waste gas outlet of the homogeneous tank is 80-100 mg/m 3 The chlorobenzene concentration at the top of the oxidation tank is 0.8-1.2 mg/m 3 ；
The effluent of the sedimentation tank has the chlorobenzene concentration less than 0.1mg/L, COD 38-47 mg/L, undetected organic phosphine, total phosphorus 0.1-0.3 mg/L and calcium hardness 80-100 mg/L. Chlorobenzene waste gas, water chlorobenzene, COD, organic phosphine and total phosphorus are efficiently removed, and the emission requirement of GB31571-2015 is met.
Comparative example 1
In the wastewater in the example 1, an ozone catalytic unit is used for replacing the UV reactor and the oxidation tank in the example 1 for oxidation treatment, the catalyst is a solid spherical catalyst, the ratio of the ozone addition concentration to the water inflow COD is 20, the pH value is 7-8, the hydraulic retention time is 4h, the exhaust gas of the homogeneous tank also enters the catalytic oxidation unit for treatment, and the gas-water ratio of the exhaust gas to the wastewater is preferably 1.
A sedimentation tank: the adding concentration of flocculant polyaluminium chloride is 500mg/L, the adding concentration of coagulant aid polyacrylamide is 30mg/L, the hydraulic retention time is 60min, and the pH value is 7-8.
The effluent of the sedimentation tank at the initial stage of operation has the chlorobenzene concentration less than 0.1mg/L, COD 50-80 mg/L, undetected organic phosphine, total phosphorus 0.4-0.5 mg/L and calcium hardness 50-80 mg/L. Chlorobenzene waste gas, water chlorobenzene, COD, organic phosphine and total phosphorus are efficiently removed, and the emission requirement of GB31571-2015 is met. The chlorobenzene content in the catalytic oxidation tail gas is 40-70 mg/m 3 And the emission requirement of GB31571-2015 cannot be met.
After running for 1 week, the effluent of the sedimentation tank has the chlorobenzene concentration of 10-20 mg/L, COD of 300-500 mg/L, organic phosphine of 30-50 mg/L, total phosphorus of 0.4-0.5 mg/L and calcium hardness of 40-50 mg/L. Comparative example 1 the pollutant removal effect is reduced, and the fouling on the surface of the catalyst is serious; the tail gas chlorobenzene is 100 to 120mg/m 3 。
Compared with example 1, the operation is unstable, especially the existence of calcium hard causes severe scale formation on the surface of the catalyst, and the dosage of the flocculating agent and the coagulant aid is far higher than that of example 1 in order to reach the total phosphorus.
Of course, the foregoing is merely exemplary of the invention and is not to be construed as limiting the scope of the embodiments of the invention. The present invention is not limited to the above examples, and equivalent changes and modifications made by those skilled in the art within the spirit and scope of the present invention should be construed as being included in the scope of the present invention.
Claims (10)
1. A method for treating phosphorus-containing chlorobenzene-containing wastewater is characterized by comprising the following steps: firstly, buffering the wastewater, naturally volatilizing chlorobenzene waste gas into an air layer in a tank, then adding a catalyst and an oxidant into the buffered wastewater, mixing the wastewater with the chlorobenzene waste gas, then feeding the mixture into a UV (ultraviolet) generator for oxidation cycle treatment, adding a flocculating agent into the wastewater after the oxidation cycle treatment, regulating the pH value of the wastewater to be neutral, precipitating, and discharging the effluent which reaches the standard after the precipitation treatment.
2. The method for treating the phosphorus-containing chlorobenzene-containing wastewater according to claim 1, wherein: the method comprises the following steps:
(1) Homogenizing: the wastewater enters a homogenizing tank filled with air for buffering treatment, and chlorobenzene waste gas naturally volatilizes into the air in the tank;
(2) And (3) oxidation: mixing the buffered wastewater with outlet water at the lower part of an oxidation tank, adding a catalyst and an oxidant, mixing with chlorobenzene waste gas, entering a UV generator, and returning outlet water to the oxidation tank added with acid liquor for oxidation cycle treatment;
(3) And (3) precipitation: adding a flocculating agent into the wastewater subjected to oxidation cycle treatment, adjusting the pH value to be neutral, and then allowing the wastewater to enter a sedimentation tank for sedimentation treatment;
(4) Draining and deslagging: the effluent of the sedimentation tank is discharged out after reaching the standard, and the sludge is sent to a sludge filter pressing system.
3. The method for treating phosphorus-containing chlorobenzene-containing wastewater according to claim 1, wherein: the hydraulic retention time of the buffer treatment is 1-8 h, and the hydraulic retention time of the oxidation circulation treatment is 1-4 h.
4. The method for treating the phosphorus-containing chlorobenzene-containing wastewater according to claim 1, wherein: the catalyst is soluble salt of ferric ion or ferrous ion, and the dosage is 50-100 mg/L of total iron concentration; the oxidant is hydrogen peroxide solution, and the ratio of dry basis addition to inlet water COD is (2) - (6).
5. The method for treating phosphorus-containing chlorobenzene-containing wastewater according to claim 1, wherein: the temperature of the oxidation circulation treatment is 45-50 ℃, and the pH value is 2.0-2.5.
6. The method for treating phosphorus-containing chlorobenzene-containing wastewater according to claim 1, wherein: the gas-water ratio of the chlorobenzene waste gas and the wastewater entering the UV generator is 1.
7. The method for treating phosphorus-containing chlorobenzene-containing wastewater according to claim 1, wherein: the flocculating agent is polyaluminium chloride or polyaluminium ferric chloride, the adding concentration is 0-100 mg/L, and the hydraulic retention time of the precipitation treatment is 30-60 min.
8. A treatment apparatus for the phosphorus-containing chlorobenzene-containing wastewater treatment method according to any one of claims 1 to 7, characterized in that: including waste water pipeline (1), homogenization jar (2) and oxidation tank (11), the upper portion of homogenization jar (2) is equipped with one-way air inlet (3) and waste gas pipeline (4), and oxidation tank (11) are connected with acidizing fluid jar (12), and the bottom of oxidation tank (11) is equipped with down export circulation pipeline (6), export circulation pipeline (6) are connected with catalyst feeding line (7) and oxidant feeding line (8) respectively down, and waste water pipeline (1) is connected with homogenization jar (2), and the delivery port of homogenization jar (2) is connected with export circulation pipeline (6) down through elevator pump (5), and waste gas pipeline (4) are connected with UV generator (10) through mixing cycle pump (9) with export circulation pipeline (6) down, and UV generator (10) are connected with oxidation tank (11), and the upper portion of oxidation tank (11) is connected with sedimentation tank (14), and sedimentation tank (14) are connected with flocculating agent jar (15) and alkali liquor jar (16) respectively.
9. The apparatus for treating the phosphorus-containing chlorobenzene-containing wastewater according to claim 8, wherein: an exhaust gas discharge port (13) is arranged at the upper part of the oxidation tank (11).
10. The apparatus for treating the phosphorus-containing chlorobenzene-containing wastewater according to claim 8, wherein: the bottom of the sedimentation tank (14) is connected with a sludge press filtration system (17).
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