CN111847795A - System and method for recycling and treating PTA reclaimed water - Google Patents
System and method for recycling and treating PTA reclaimed water Download PDFInfo
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- CN111847795A CN111847795A CN202010757326.4A CN202010757326A CN111847795A CN 111847795 A CN111847795 A CN 111847795A CN 202010757326 A CN202010757326 A CN 202010757326A CN 111847795 A CN111847795 A CN 111847795A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 306
- 238000004064 recycling Methods 0.000 title claims abstract description 48
- 238000000034 method Methods 0.000 title claims abstract description 40
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 117
- 230000003647 oxidation Effects 0.000 claims abstract description 92
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 92
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 67
- 238000001914 filtration Methods 0.000 claims abstract description 63
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 55
- 238000004062 sedimentation Methods 0.000 claims abstract description 38
- 238000012544 monitoring process Methods 0.000 claims abstract description 32
- 238000005189 flocculation Methods 0.000 claims abstract description 27
- 230000016615 flocculation Effects 0.000 claims abstract description 27
- 238000004519 manufacturing process Methods 0.000 claims abstract description 25
- 238000001556 precipitation Methods 0.000 claims abstract description 10
- 230000002195 synergetic effect Effects 0.000 claims description 42
- 239000010802 sludge Substances 0.000 claims description 31
- 239000000945 filler Substances 0.000 claims description 25
- 238000004140 cleaning Methods 0.000 claims description 19
- 238000005273 aeration Methods 0.000 claims description 18
- 230000008569 process Effects 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 13
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 239000000701 coagulant Substances 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 239000002245 particle Substances 0.000 claims description 12
- 238000005345 coagulation Methods 0.000 claims description 11
- 230000015271 coagulation Effects 0.000 claims description 11
- 239000010865 sewage Substances 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 11
- 229910021645 metal ion Inorganic materials 0.000 claims description 10
- 241000894006 Bacteria Species 0.000 claims description 9
- 238000011084 recovery Methods 0.000 claims description 9
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims description 8
- 230000009471 action Effects 0.000 claims description 8
- 230000001590 oxidative effect Effects 0.000 claims description 8
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 8
- 239000003054 catalyst Substances 0.000 claims description 7
- 239000003638 chemical reducing agent Substances 0.000 claims description 7
- 239000007800 oxidant agent Substances 0.000 claims description 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 6
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 6
- 239000004571 lime Substances 0.000 claims description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 6
- 239000000084 colloidal system Substances 0.000 claims description 5
- 239000012528 membrane Substances 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- 125000000129 anionic group Chemical group 0.000 claims description 4
- 238000006065 biodegradation reaction Methods 0.000 claims description 4
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 230000033116 oxidation-reduction process Effects 0.000 claims description 4
- 229920002401 polyacrylamide Polymers 0.000 claims description 4
- 235000010265 sodium sulphite Nutrition 0.000 claims description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 3
- 229910021578 Iron(III) chloride Inorganic materials 0.000 claims description 3
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 claims description 3
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 claims description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims description 3
- 229910052748 manganese Inorganic materials 0.000 claims description 3
- 239000011572 manganese Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 239000004576 sand Substances 0.000 claims description 3
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 claims description 2
- 230000000593 degrading effect Effects 0.000 claims description 2
- 238000010612 desalination reaction Methods 0.000 claims description 2
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 claims description 2
- 230000001112 coagulating effect Effects 0.000 abstract 1
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 52
- 239000003344 environmental pollutant Substances 0.000 description 9
- 231100000719 pollutant Toxicity 0.000 description 9
- 238000011001 backwashing Methods 0.000 description 8
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 7
- 238000005406 washing Methods 0.000 description 6
- 238000004065 wastewater treatment Methods 0.000 description 6
- 239000007789 gas Substances 0.000 description 5
- -1 suspended matters Substances 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 239000010941 cobalt Substances 0.000 description 4
- 229910017052 cobalt Inorganic materials 0.000 description 4
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 239000003795 chemical substances by application Substances 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 2
- 229910000329 aluminium sulfate Inorganic materials 0.000 description 2
- 235000011128 aluminium sulphate Nutrition 0.000 description 2
- WPYMKLBDIGXBTP-UHFFFAOYSA-N benzoic acid Chemical compound OC(=O)C1=CC=CC=C1 WPYMKLBDIGXBTP-UHFFFAOYSA-N 0.000 description 2
- 238000011033 desalting Methods 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 239000008394 flocculating agent Substances 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000005711 Benzoic acid Substances 0.000 description 1
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 229940037003 alum Drugs 0.000 description 1
- 235000010233 benzoic acid Nutrition 0.000 description 1
- 229940006460 bromide ion Drugs 0.000 description 1
- 239000012459 cleaning agent Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000265 homogenisation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000006228 supernatant Substances 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
-
- 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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- 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
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
-
- 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
- C02F1/70—Treatment of water, waste water, or sewage by reduction
-
- 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
-
- 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
-
- C—CHEMISTRY; METALLURGY
- 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
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/04—Disinfection
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
- C02F3/105—Characterized by the chemical composition
- C02F3/107—Inorganic materials, e.g. sand, silicates
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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
- C02F7/00—Aeration of stretches of water
Abstract
The invention discloses a system and a method for recycling and treating PTA reclaimed water. The system for recycling and treating PTA reclaimed water comprises a precipitation unit, a filtration unit, an ultrafiltration unit, a reverse osmosis unit and an advanced treatment unit which are connected in sequence; wherein, the precipitation unit is including coagulating basin, flocculation basin and sedimentation tank, filtering unit includes filtering ponds and production pond, the ultrafiltration includes heat exchanger, first filter, ultrafiltration device and second filter, reverse osmosis unit includes reverse osmosis unit, advanced treatment unit includes ozone pre-oxidation pond, homogeneity pond, biological aerated filter, ozone oxidation pond and play water monitoring pond in coordination. The system for recycling and treating PTA reclaimed water provided by the invention has a simple and compact structure, and can realize switching of two treatment lines by changing the opening and closing states of the valve, thereby realizing high-efficiency treatment and resource utilization of the PTA reclaimed water.
Description
Technical Field
The invention relates to an industrial sewage treatment system and process, in particular to a system and a method for recycling and treating PTA reclaimed water, and belongs to the technical field of sewage treatment.
Background
PTA is refined from Terephthalic Acid (TA), and is a main raw material for producing polyester. The wastewater is discharged in the PTA production and maintenance processes, has large water volume, high concentration and complex composition, generally contains pollutants such as terephthalic acid, benzoic acid, p-xylene, acetic acid and the like, and also contains a small amount of metal ions such as cobalt, manganese, iron and the like; at present, the PTA production wastewater is treated by mainly adopting the processes of pretreatment, anaerobic biochemical treatment and aerobic biochemical treatment in China, and the treated wastewater reaches the standard (the national emission standard COD is less than 100mg/L) and is discharged outside.
In recent years, along with the gradual improvement of national requirements for environmental protection, PTA production enterprises are actively trying various reclaimed water recycling technologies to save water and reduce the discharge capacity, wherein PTA reclaimed water refers to effluent which is subjected to anaerobic/aerobic biochemical treatment on PTA production wastewater and meets the national first-level discharge standard, the water quality of the PTA reclaimed water is between that of the wastewater and fresh water, the PTA reclaimed water contains pollutants such as suspended matters, sludge, bacteria, cobalt, manganese, iron metal ions and the like, the salt content of the PTA reclaimed water is usually multiple times of that of the fresh water, and the PTA reclaimed water cannot meet the reclaimed water recycling standard.
Disclosure of Invention
The invention mainly aims to provide a system and a method for recycling and treating PTA reclaimed water, so as to overcome the defects in the prior art.
In order to achieve the purpose, the technical scheme adopted by the invention comprises the following steps:
the embodiment of the invention provides a PTA reclaimed water recycling treatment system, which comprises a precipitation unit, a filtration unit, an ultrafiltration unit, a reverse osmosis unit and an advanced treatment unit, wherein the precipitation unit, the filtration unit, the ultrafiltration unit, the reverse osmosis unit and the advanced treatment unit are used for sequentially treating sewage to be treated; wherein the content of the first and second substances,
the sedimentation unit comprises a coagulation tank, a flocculation tank and a sedimentation tank, the filtering unit comprises a filtering tank and a water producing tank, the ultrafiltration comprises a heat exchanger, a first filter, an ultrafiltration device and a second filter, the reverse osmosis unit comprises a reverse osmosis device, and the advanced treatment unit comprises an ozone pre-oxidation tank, a homogenizing tank, a biological aerated filter, an ozone synergistic oxidation tank and a water outlet monitoring tank; the coagulation tank, the flocculation tank, the sedimentation tank, the filtering tank, the water producing tank, the heat exchanger, the first filter, the ultrafiltration device, the second filter, the reverse osmosis device, the ozone pre-oxidation tank, the homogenizing tank, the biological aerated filter, the ozone synergistic oxidation tank and the water outlet monitoring tank are sequentially connected; and the ozone pre-oxidation tank, the ozone synergistic oxidation tank, the homogenizing tank, the biological aerated filter and the effluent monitoring tank are also sequentially connected to form two advanced treatment process routes.
Furthermore, at least one water outlet of the water generating tank is also connected with the material inlet of the filtering tank, so that part of the outlet water of the filtering tank is used for cleaning the filtering tank.
Furthermore, at least one water outlet of the ultrafiltration device is also connected with a water inlet of the water production pool, so that part of produced water of the ultrafiltration device flows back to the water production pool and is used as cleaning water of the filter pool.
Further, the filtering tank comprises a V-shaped filtering tank.
Further, the first filter comprises a self-cleaning filter and/or a first safety filter, and the second filter comprises a second safety filter.
Further, the filtering precision of the self-cleaning filter is 80-120 μm; the filtration precision of the first safety filter is 10-30 mu m.
Furthermore, the aperture of the filter membrane in the ultrafiltration device is 0.02-0.2 μm.
Furthermore, the filtering precision of the second cartridge filter is 5-10 μm.
Further, the sludge discharge port of the sedimentation tank is also connected with the material inlet of the flocculation tank, so that at least part of sludge discharged by the sedimentation tank flows back to the flocculation tank, and the sedimentation tank is also connected with a sludge treatment system.
Furthermore, the reverse osmosis device is also connected with a produced water recovery system, and the produced water of the reverse osmosis device can be recycled.
Furthermore, the homogenizing tank and the biological aerated filter are also connected with an aeration fan.
Further, an ozone concentration detector is arranged at a water outlet of the homogenizing pool.
The embodiment of the invention also provides a method for recycling and treating PTA reclaimed water, which comprises the following steps:
providing a recycling treatment system of the PTA reclaimed water;
mixing PTA reclaimed water to be treated with coagulant aid, lime solution, flocculant and sodium carbonate solution in sequence, inputting the mixture into a sedimentation tank to realize sludge-water separation, enabling 0-30 wt% of sludge output by the sedimentation tank to flow back into the flocculation tank, and inputting the rest sludge into a sludge treatment system;
adjusting the pH value of the reclaimed water output from the sedimentation tank to 7.5-8.5, and inputting the reclaimed water into a filter tank to remove suspended matters and metal ions in the water;
inputting the filter tank produced water output by the filter tank into a water production tank, and enabling a part of the filter tank produced water in the water production tank to flow back into the filter tank as backwash water, and enabling the other part of the filter tank produced water to be sequentially input into a self-cleaning filter and a security filter after the temperature of the other part of the filter tank produced water is regulated to 15-30 ℃ by a heat exchanger and then enter an ultrafiltration device so as to remove colloids, suspended matters and bacteria in the water;
part of the ultrafiltration produced water of the ultrafiltration device flows back to the water production pool, and the other part of the ultrafiltration produced water enters the reverse osmosis device after being filtered by the second cartridge filter so as to remove TDS and organic matters in the water;
inputting the reverse osmosis produced water output by the reverse osmosis device into a produced water recycling system for recycling, inputting the reverse osmosis concentrated water output by the reverse osmosis device into an ozone pre-oxidation pond, and carrying out pre-oxidation treatment on the reverse osmosis concentrated water by ozone at the temperature of 15-30 ℃, wherein the ozone is continuously aerated;
and (2) sequentially inputting the produced water of the ozone pre-oxidation tank into a homogenizing tank, a biological aerated filter, an ozone synergistic oxidation tank and a water outlet monitoring tank, and/or sequentially inputting the produced water of the ozone pre-oxidation tank into the ozone synergistic oxidation tank, the homogenizing tank, the biological aerated filter and the water outlet monitoring tank, so that COD (chemical oxygen demand) in the discharged water of the water outlet monitoring tank is less than or equal to 100mg/L, and BOD (biochemical oxygen demand) is less than or equal to 20 mg/L.
Furthermore, the usage amount of the ozone in the ozone pre-oxidation pond is 20-40 mg/L.
Further, the method for recycling and treating the PTA reclaimed water specifically comprises the following steps: and inputting the produced water of the ozone pre-oxidation tank into a homogenizing tank, removing ozone in the produced water of the ozone pre-oxidation tank by adopting an aeration treatment mode, then performing biodegradation on the produced water of the homogenizing tank in a biological aerated filter, then enabling the produced water of the biological aerated filter to enter an ozone synergistic oxidation tank, degrading organic matters which are difficult to decompose under the combined action of ozone and a catalyst, and finally enabling the produced water of the ozone synergistic oxidation tank to enter a water outlet monitoring tank and be discharged.
Further, the method for recycling and treating the PTA reclaimed water specifically comprises the following steps: and the produced water of the ozone pre-oxidation tank is input into an ozone synergistic oxidation tank, organic matters which are difficult to decompose are degraded under the combined action of ozone and a catalyst, then the produced water of the synergistic oxidation tank is input into a homogeneous tank, the ozone in the produced water of the synergistic oxidation tank is removed in an aeration treatment mode, then the produced water of the homogeneous tank is subjected to biodegradation in a biological aerated filter, and finally the produced water of the biological aerated filter enters a water outlet monitoring tank and is discharged outside.
Furthermore, the dissolved oxygen content in the aeration biological filter tank is 2-6mg/L, and the adding amount of the ozone in the ozone synergistic oxidation tank is 60-90 mg/L.
Furthermore, the bottom layer filler in the aeration biological filter tank comprises cobblestones with the diameters of 16-32mm and 8-16mm respectively, and the upper layer filler comprises biological ceramsite with the diameter of 2-8 mm.
Further, the bottom layer filler in the ozone synergistic oxidation pond comprises cobbles with the diameters of 16-32mm and 8-16mm respectively, and the upper layer filler comprises an ozone oxidation catalyst with the diameter of 2-8 mm.
Further, the coagulant aid includes any one or a combination of more than two of polyaluminium chloride, ferric chloride and aluminium sulfate, but is not limited thereto.
Further, the flocculant includes, but is not limited to, anionic polyacrylamide.
Furthermore, the addition amount of various agents in the coagulant aid and the flocculant is related to the quality of the incoming water and is adjusted according to the quality of the incoming water; specifically, the coagulant aids such as ferric trichloride are mainly used for enhancing the flocculation effect of impurities such as suspended matters in the sewage, and the dosage is generally controlled to be 10-50 mg/L; the effect of the flocculating agent such as anionic polyacrylamide and the like is mainly to enhance the flocculation effect of impurities such as suspended matters and the like in the sewage, and the dosage is generally controlled to be 0.5-5 mg/L.
Furthermore, the filtering filler in the filtering tank comprises a supporting layer and a filtering material layer, the filtering material layer is arranged above the supporting layer, the particle size of the filtering filler particles of the supporting layer is 2-4mm, and the particle size of the filtering filler particles of the filtering material layer is 0.8-1.5 mm.
Further, the filter filler comprises manganese sand.
Further, the filtering precision of the self-cleaning filter is 80-120 μm; the filtration precision of the first safety filter is 10-30 mu m.
Furthermore, the aperture of a filter membrane in the ultrafiltration device is 0.05 μm, the recovery rate of the ultrafiltration device is more than or equal to 90%, the SDI of produced water is less than or equal to 2, and the turbidity is less than or equal to 0.1 NTU.
Furthermore, the filtering precision of the second cartridge filter is 5-10 μm, the system recovery rate of the reverse osmosis device is more than or equal to 75%, the desalination rate is more than or equal to 95%, the COD of produced water is less than or equal to 5mg/L, and the ammonia nitrogen is less than or equal to 0.1 mg/L.
Further, the method for recycling and treating the PTA reclaimed water further comprises the following steps: and when the ozone content in the produced water of the homogenizing pool is more than 5mg/L, adding a reducing agent into the produced water of the homogenizing pool.
Further, the reducing agent comprises sodium sulfite and/or sodium bisulfite, and the addition amount of the reducing agent is 0-15 mg/L.
Further, the method for recycling and treating the PTA reclaimed water further comprises the following steps: adding an oxidant into the ozone-assisted oxidation pond or the inlet water of the ozone-assisted oxidation pond to adjust the oxidation-reduction potential of the water produced by the ozone-assisted oxidation pond to-150-450 mv.
Further, the oxidant comprises hydrogen peroxide.
Furthermore, the air quantity and the air pressure required in the homogenizing tank, the biological aerated filter and the ozone synergistic oxidation tank are supplied by a fan.
Compared with the prior art, the invention has the advantages that: the recycling treatment system of PTA reclaimed water provided by the embodiment of the invention has a simple and compact structure, and can realize the switching of two treatment lines by changing the opening and closing states of the valve, thereby realizing the high-efficiency treatment and resource utilization of the PTA reclaimed water; the recycling treatment method of PTA reclaimed water provided by the embodiment of the invention effectively removes pollutants such as suspended matters, sludge, bacteria, metal ions and the like in the PTA reclaimed water, and the treated reclaimed water is partially recycled and partially discharged, thereby achieving the purposes of saving water and reducing sewage discharge.
Drawings
Fig. 1 is a schematic flow chart illustrating the structure and processing process of a system for recycling and processing PTA recycled water according to an exemplary embodiment of the present invention.
Detailed Description
In view of the deficiencies in the prior art, the inventors of the present invention have made extensive studies and extensive practices to provide technical solutions of the present invention. The technical solution, its implementation and principles, etc. will be further explained as follows.
The embodiment of the invention provides a PTA reclaimed water recycling treatment system, which comprises a precipitation unit, a filtration unit, an ultrafiltration unit, a reverse osmosis unit and an advanced treatment unit, wherein the precipitation unit, the filtration unit, the ultrafiltration unit, the reverse osmosis unit and the advanced treatment unit are used for sequentially treating sewage to be treated; wherein the content of the first and second substances,
the sedimentation unit comprises a coagulation tank, a flocculation tank and a sedimentation tank, the filtering unit comprises a filtering tank and a water producing tank, the ultrafiltration unit comprises a heat exchanger, a first filter, an ultrafiltration device and a second filter, the reverse osmosis unit comprises a reverse osmosis device, and the advanced treatment unit comprises an ozone pre-oxidation tank, a homogenizing tank, a biological aerated filter, an ozone synergistic oxidation tank and a water outlet monitoring tank; the coagulation tank, the flocculation tank, the sedimentation tank, the filtering tank, the water producing tank, the heat exchanger, the first filter, the ultrafiltration device, the second filter, the reverse osmosis device, the ozone pre-oxidation tank, the homogenizing tank, the biological aerated filter, the ozone synergistic oxidation tank and the water outlet monitoring tank are sequentially connected; and the ozone pre-oxidation tank, the ozone synergistic oxidation tank, the homogenizing tank, the biological aerated filter and the effluent monitoring tank are also sequentially connected to form two advanced treatment process routes.
The embodiment of the invention also provides a method for recycling and treating PTA reclaimed water, which comprises the following steps:
providing a recycling treatment system of the PTA reclaimed water;
mixing PTA reclaimed water to be treated with coagulant aid, lime solution, flocculant and sodium carbonate solution in sequence, inputting the mixture into a sedimentation tank to realize mud-water separation, enabling 0-30 wt% of sludge output by the sedimentation tank to flow back into the flocculation tank, and inputting the rest sludge into a sludge treatment system;
adjusting the pH value of the reclaimed water output from the sedimentation tank to 7.5-8.5, and inputting the reclaimed water into a filter tank to remove suspended matters and metal ions in the water;
inputting the filter tank produced water output by the filter tank into a water production tank, and enabling a part of the filter tank produced water in the water production tank to flow back into the filter tank as backwash water, and enabling the other part of the filter tank produced water to be sequentially input into a self-cleaning filter and a security filter after the temperature of the other part of the filter tank produced water is regulated to 15-30 ℃ by a heat exchanger and then enter an ultrafiltration device so as to remove colloids, suspended matters and bacteria in the water;
part of the ultrafiltration produced water of the ultrafiltration device flows back to the water production pool, and the other part of the ultrafiltration produced water enters the reverse osmosis device after being filtered by the second cartridge filter so as to remove TDS and organic matters in the water;
inputting the reverse osmosis produced water output by the reverse osmosis device into a produced water recycling system for recycling, inputting the reverse osmosis concentrated water output by the reverse osmosis device into an ozone pre-oxidation pond, and pre-oxidizing the reverse osmosis concentrated water by ozone at the temperature of 15-30 ℃, wherein the usage amount of ozone in the ozone pre-oxidation pond is 20-40mg/L, and the ozone is continuously aerated due to the fact that water is continuously fed;
and (2) sequentially inputting the produced water of the ozone pre-oxidation tank into a homogenizing tank, a biological aerated filter, an ozone synergistic oxidation tank and a water outlet monitoring tank, and/or sequentially inputting the produced water of the ozone pre-oxidation tank into the ozone synergistic oxidation tank, the homogenizing tank, the biological aerated filter and the water outlet monitoring tank, so that COD (chemical oxygen demand) in the discharged water of the water outlet monitoring tank is less than or equal to 100mg/L, and BOD (biochemical oxygen demand) is less than or equal to 20 mg/L.
The embodiment of the invention mainly provides a reclaimed water recycling treatment system and a reclaimed water recycling treatment process after PTA wastewater treatment, the system and the process can effectively remove pollutants such as suspended matters, sludge, bacteria, metal ions and the like in PTA reclaimed water, and the treated reclaimed water is partially recycled and partially discharged outside, so that the purposes of saving water and reducing discharge capacity are achieved.
The embodiment of the invention provides a PTA reclaimed water recycling treatment system which mainly comprises a precipitation unit, a filtration unit, an ultrafiltration unit, a reverse osmosis unit and a depth treatment unit which are used for sequentially treating sewage to be treated, and the technical scheme of the invention is explained in detail by combining with the attached drawings.
Referring to fig. 1, fig. 1 is a flow chart of a process for recycling reclaimed water after PTA wastewater treatment according to an embodiment of the present invention, it should be noted that reverse osmosis concentrated water output by a reverse osmosis device can be treated by two process routes after entering an ozone pre-oxidation tank, wherein one process route is marked as "i" and the other process route is marked as "ii".
Specifically, the sedimentation unit comprises a coagulation tank, a flocculation tank and a sedimentation tank (which can be a high-efficiency sedimentation tank), the filtration unit comprises a V-shaped filter tank and a water production tank, the ultrafiltration comprises a heat exchanger, a self-cleaning filter and/or a first safety filter, an ultrafiltration device and a second safety filter, the reverse osmosis unit comprises a reverse osmosis device, and the advanced treatment unit comprises an ozone pre-oxidation tank, a homogenizing tank, an aeration biological filter, an ozone synergistic oxidation tank and a water outlet monitoring tank; the coagulation tank, the flocculation tank, the sedimentation tank, the filtration tank, the water production tank, the heat exchanger, the self-cleaning filter and/or the first safety filter, the ultrafiltration device, the second safety filter, the reverse osmosis device, the ozone pre-oxidation tank, the homogenization tank, the biological aerated filter, the ozone synergistic oxidation tank and the effluent monitoring tank are connected in sequence; the ozone pre-oxidation tank, the ozone synergistic oxidation tank, the homogenizing tank, the biological aerated filter and the effluent monitoring tank are also sequentially connected to form two advanced treatment process routes;
in addition, the sludge discharge port of the sedimentation tank is also connected with the material inlet of the flocculation tank so as to enable at least part of sludge discharged by the sedimentation tank to flow back to the flocculation tank, and the sedimentation tank is also connected with a sludge treatment system; at least one water outlet of the ultrafiltration device is also connected with a water inlet of the water production pool so as to enable part of produced water of the ultrafiltration device to flow back to the water production pool, and at least one water outlet of the water production pool is also connected with a water inlet of the V-shaped filter pool so as to enable part of produced water in the water production pool to flow back to the V-shaped filter pool and serve as cleaning water of the V-shaped filter pool.
The reclaimed water recycling treatment method after PTA wastewater treatment provided by the embodiment of the invention comprises the following steps:
1) the water in the PTA enters a precipitation unit, and pollutants such as suspended matters, sludge and the like in the water in the PTA are converted into precipitable substances under the action of agents (such as coagulant aids, lime solution, flocculating agents and sodium carbonate solution) and sludge-water separation is realized;
2) the produced water of the precipitation unit enters a filtering unit, and suspended matters and metal ions such as cobalt, manganese, iron and the like in the incoming water are removed through a V-shaped filter, so that the influence on the subsequent ultrafiltration and reverse osmosis is avoided;
3) the water produced by the filtering unit sequentially enters the ultrafiltration unit and the reverse osmosis unit, so that the pollutants such as colloid, suspended matters, bacteria, TDS (total dissolved solids), organic matters and the like in the incoming water are further removed, and the water produced by the reverse osmosis unit reaches the recycling standard;
4) the reverse osmosis concentrated water enters an advanced treatment unit and adopts O3And the + BAF' process treatment further reduces COD in the incoming water through the oxidation of ozone and the filtration and biological treatment of BAF, and ensures that the COD in the effluent water is less than or equal to 100 mg/L.
Example 1
A method for recycling and treating reclaimed water after PTA wastewater treatment mainly comprises the following steps:
inputting the reclaimed water after PTA wastewater treatment into a recycling treatment system of the PTA reclaimed water shown in figure 1, wherein the water inlet indexes of the reclaimed water after PTA wastewater treatment are as follows: COD is 100-150mg/L, total phosphorus is 2-3mg/L, ammonia nitrogen is 5-10mg/L, TDS is 4200-4800mg/L, TSS is 50-200mg/L, and bromide ion is 160-250 ppm;
1) the PTA reclaimed water sequentially passes through a coagulation tank, a flocculation tank and a sedimentation tank, pollutants such as suspended matters and sludge in the water are converted into larger-particle precipitable substances under the action of a coagulant, a lime solution, a flocculant in the flocculation tank, a sodium carbonate solution and the like in the coagulation tank (specifically, under the action of stirring, floccules in the water flocculate into precipitable alum flocs under the action of the flocculant), then sludge-water separation is realized in the sedimentation tank, part of the sludge at the bottom of the sedimentation tank flows back into the flocculation tank (the sludge flowing back into the flocculation tank is controlled to be 0-30 wt% of the total amount of the sludge in the sedimentation tank, the sludge is used for enhancing the flocculation effect in the flocculation tank so as to form large-particle flocs), part of the sludge is sent into a sludge treatment system, the pH value of supernatant in the sedimentation tank is adjusted to 5-8, and then the sludge is input into a filtering unit, wherein, the coagulant and the flocculant are conventional agents in the field of sewage treatment, the coagulant can be ferric chloride and/or polyaluminium chloride and/or aluminium sulfate, the flocculant can be anionic polyacrylamide, and the dosage of the coagulant and the flocculant needs to be adjusted according to the state of flocs in a coagulation tank and a flocculation tank; the dosage of the lime solution and the sodium carbonate solution is required to be adjusted according to the water hardness of the incoming water, and the water hardness is controlled below 100mg/L by controlling the dosage;
2) adjusting the pH value of produced water in the sedimentation tank to 7.5-8.5, inputting the water into a V-shaped filter tank, wherein the filler in the V-shaped filter tank can effectively remove suspended matters and metal ions such as cobalt, manganese, iron and the like in the water, part of the produced water in the V-shaped filter tank is input into the produced water tank, part of the produced water in the produced water tank is used for backwashing the V-shaped filter tank, and the produced water in the part of the filter tank sequentially enters an ultrafiltration unit and a reverse osmosis unit; the filler in the V-shaped filter tank comprises a supporting layer positioned at the bottom and a filter material layer positioned at the upper part, the particle size of the filler in the supporting layer is 2-4mm, and the particle size of the filler in the filter material layer is 0.8-1.5 mm; the filler can be manganese sand; the V-shaped filter chamber needs to be backwashed according to the operation condition and the effluent quality, the backwashing adopts a mode of 'gas washing + gas/water simultaneous washing + water washing', the air quantity and the air pressure are provided by a fan, and the backwashing water is the water produced by the V-shaped filter chamber;
3) the filter tank produced water in the water producing tank sequentially passes through a heat exchanger, a self-cleaning filter and/or a first safety filter, an ultrafiltration device, a second safety filter, a reverse osmosis device and other equipment, pollutants such as colloid, suspended matters, bacteria, TDS (total dissolved solids), organic matters and the like in the reclaimed water are further removed, reverse osmosis produced water of the reverse osmosis device is input into a produced water recovery system for recycling, and reverse osmosis concentrated water output by the osmosis device enters an advanced treatment unit; wherein the outlet water temperature of the heat exchanger is 15-30 ℃ (preferably 20-25 ℃); the filtering precision of the self-cleaning filter is 80-120 mu m, the filtering precision of the first security filter is 10-30 mu m, and the filtering precision of the second security filter is 5-10 mu m; the aperture of an ultrafiltration membrane of the ultrafiltration device is 0.02-0.2 mu m, and the unit recovery rate of the ultrafiltration device is more than or equal to 90 percent; the reverse osmosis device adopts a multi-stage continuous desalting mode, the unit recovery rate is more than or equal to 75 percent, and the unit desalting rate is more than or equal to 95 percent; the ultrafiltration device and the reverse osmosis device need to carry out backwashing and chemical cleaning according to the operation of the device and the quality of effluent water, backwashing water of the ultrafiltration device is ultrafiltration produced water, backwashing water of the reverse osmosis device is reverse osmosis produced water, and a chemical cleaning agent is provided by a dosing system;
4) to reduce the risk of failing or unreasonable single process handling, the advanced treatment unit may employ two different process routes: a first circuit: the reverse osmosis concentrated water output by the reverse osmosis device sequentially enters an ozone pre-oxidation tank, a homogenizing tank, an aeration biological filter, an ozone synergistic oxidation tank and an effluent monitoring tank, and the produced water reaches the standard and is discharged; a second circuit: the reverse osmosis concentrated water output by the reverse osmosis device sequentially enters an ozone pre-oxidation tank, an ozone synergistic oxidation tank, a homogenizing tank, an aeration biological filter and a water outlet monitoring tank, and the produced water is discharged after reaching the standard; wherein, the bottom filler in the ozone synergistic oxidation pond is cobblestone with the diameter of 16-32mm and 8-16mm respectively, and the upper filler is an ozone oxidation catalyst with the diameter of 2-8 mm; the bottom layer filler in the aeration biological filter tank is cobblestones with the diameters of 16-32mm and 8-16mm respectively, the upper layer filler is biological ceramsite with the diameter of 2-8mm, the dissolved oxygen amount in water in the aeration biological filter tank is 2-6mg/L, ozone required by the ozone preoxidation tank and the ozone synergistic oxidation tank is supplied by an ozone generating device, the adding amount of the ozone in the ozone preoxidation tank is 20-40mg/L, preferably 30mg/L, the adding amount of the ozone in the ozone synergistic oxidation tank is 60-90mg/L, and tail gas in the tank reaches the standard after being collected and treated; and when detecting that the ozone content in the produced water of the homogenizing tank is more than 5mg/L, adding a reducing agent which can be sodium sulfite into the produced water before the produced water enters the biological aerated filter, wherein the adding amount is 0-15 mg/L; the water inlet of the ozone synergistic oxidation pond needs to be added with an oxidant according to the oxidation-reduction potential of water, the oxidant is hydrogen peroxide, the oxidation-reduction potential is adjusted to-150-450 mv by adding the hydrogen peroxide, and the adding amount of the oxidant is 20-80 mg/L; the air quantity and the air pressure required by the homogenizing tank, the biological aerated filter and the ozone synergistic oxidation tank are supplied by a fan, the biological aerated filter and the ozone synergistic oxidation tank need to be backwashed according to operation and effluent water quality, the backwashing adopts a mode of 'gas washing, gas/water washing and water washing', the air quantity and the air pressure are provided by the fan, and the backwashing water is effluent monitoring tank water production.
Specifically, reverse osmosis concentrated water output by a reverse osmosis device enters an ozone pre-oxidation tank, the ozone adding amount of the ozone pre-oxidation tank is controlled to be 30mg/L, the biodegradability of the reverse osmosis concentrated water is improved after ozone aeration, then the reverse osmosis concentrated water enters a homogenizing tank for fan aeration to remove ozone, finally produced water enters an aeration biological filter tank, and particularly, an ozone concentration detector is arranged on a water outlet pipeline of the homogenizing tank, sodium sulfite (a medicament cannot be directly added into the homogenizing tank) is added into the produced water of the homogenizing tank when the ozone content is higher than 5mg/L, and the adding amount is 0-15 mg/L.
Specifically, the water produced by the homogenizing tank is biodegraded in the biological aerated filter, the dissolved oxygen content in the water in the biological aerated filter is controlled to be 2-6mg/L by a fan, then the water enters an ozone-synergetic oxidation tank to degrade organic matters which are difficult to decompose, the ozone adding amount of the ozone-synergetic oxidation tank is controlled to be about 80mg/L, and finally the produced water enters an effluent monitoring tank to be discharged after reaching the standard.
And finally, detecting the water discharged out of the water outlet monitoring tank, wherein COD (chemical oxygen demand) in the water discharged out of the water outlet monitoring tank is less than or equal to 100mg/L, and BOD (biochemical oxygen demand) is less than or equal to 20 mg/L.
The recycling treatment system of PTA reclaimed water provided by the embodiment of the invention has a simple and compact structure, and can realize the switching of two treatment lines by changing the opening and closing states of the valve, thereby realizing the high-efficiency treatment and resource utilization of the PTA reclaimed water; the recycling treatment method of PTA reclaimed water provided by the embodiment of the invention effectively removes pollutants such as suspended matters, sludge, bacteria, metal ions and the like in the PTA reclaimed water, and the treated reclaimed water is partially recycled and partially discharged, thereby achieving the purposes of saving water and reducing sewage discharge.
It should be understood that the above-mentioned embodiments are merely illustrative of the technical concepts and features of the present invention, which are intended to enable those skilled in the art to understand the contents of the present invention and implement the present invention, and therefore, the protection scope of the present invention is not limited thereby. All equivalent changes and modifications made according to the spirit of the present invention should be covered within the protection scope of the present invention.
Claims (10)
1. A PTA reclaimed water recycling treatment system is characterized by comprising a precipitation unit, a filtering unit, an ultrafiltration unit, a reverse osmosis unit and an advanced treatment unit which are used for sequentially treating sewage to be treated; wherein the content of the first and second substances,
the sedimentation unit comprises a coagulation tank, a flocculation tank and a sedimentation tank, the filtering unit comprises a filtering tank and a water producing tank, the ultrafiltration comprises a heat exchanger, a first filter, an ultrafiltration device and a second filter, the reverse osmosis unit comprises a reverse osmosis device, and the advanced treatment unit comprises an ozone pre-oxidation tank, a homogenizing tank, a biological aerated filter, an ozone synergistic oxidation tank and a water outlet monitoring tank; the coagulation tank, the flocculation tank, the sedimentation tank, the filtering tank, the water producing tank, the heat exchanger, the first filter, the ultrafiltration device, the second filter, the reverse osmosis device, the ozone pre-oxidation tank, the homogenizing tank, the biological aerated filter, the ozone synergistic oxidation tank and the water outlet monitoring tank are sequentially connected; and the ozone pre-oxidation tank, the ozone synergistic oxidation tank, the homogenizing tank, the biological aerated filter and the effluent monitoring tank are also sequentially connected to form two advanced treatment process routes.
2. The system of claim 1, wherein the system comprises: and at least one water outlet of the water producing tank is also connected with the material inlet of the filtering tank, so that part of the outlet water of the filtering tank is used for cleaning the filtering tank.
3. The system of claim 1 or 2, wherein: at least one water outlet of the ultrafiltration device is also connected with a water inlet of the water production pool, so that part of produced water of the ultrafiltration device flows back to the water production pool and is used as cleaning water of the filter pool; preferably, the filtering tank comprises a V-shaped filtering tank; preferably, the first filter comprises a self-cleaning filter and/or a first safety filter, and the second filter comprises a second safety filter; preferably, the filtering precision of the self-cleaning filter is 80-120 μm; the filtering precision of the first safety filter is 10-30 mu m; preferably, the aperture of a filter membrane in the ultrafiltration device is 0.02-0.2 μm; and/or the filtering precision of the second cartridge filter is 5-10 mu m.
4. The system of claim 1, wherein the system comprises: the sludge discharge port of the sedimentation tank is also connected with the material inlet of the flocculation tank so as to enable at least part of sludge discharged by the sedimentation tank to flow back to the flocculation tank, and the sedimentation tank is also connected with a sludge treatment system; and/or the reverse osmosis device is also connected with a produced water recovery system; and/or the homogenizing tank and the biological aerated filter are also connected with an aeration fan; and/or an ozone concentration detector is also arranged at the water outlet of the homogenizing pool.
5. A method for recycling and treating PTA reclaimed water is characterized by comprising the following steps:
providing a reuse treatment system of the PTA water in any of claims 1-4;
mixing PTA reclaimed water to be treated with coagulant aid, lime solution, flocculant and sodium carbonate solution in sequence, inputting the mixture into a sedimentation tank to realize mud-water separation, enabling 0-30 wt% of sludge output by the sedimentation tank to flow back into the flocculation tank, and inputting the rest sludge into a sludge treatment system;
adjusting the pH value of the reclaimed water output from the sedimentation tank to 7.5-8.5, and inputting the reclaimed water into a filter tank to remove suspended matters and metal ions in the water;
inputting the filter tank produced water output by the filter tank into a water production tank, and enabling a part of the filter tank produced water in the water production tank to flow back into the filter tank as backwash water, and enabling the other part of the filter tank produced water to be sequentially input into a self-cleaning filter and a security filter after the temperature of the other part of the filter tank produced water is regulated to 15-30 ℃ by a heat exchanger and then enter an ultrafiltration device so as to remove colloids, suspended matters and bacteria in the water;
part of the ultrafiltration produced water of the ultrafiltration device flows back to the water production pool, and the other part of the ultrafiltration produced water enters the reverse osmosis device after being filtered by the second cartridge filter so as to remove TDS and organic matters in the water;
inputting the reverse osmosis produced water output by the reverse osmosis device into a produced water recycling system for recycling, inputting the reverse osmosis concentrated water output by the reverse osmosis device into an ozone pre-oxidation pond, and carrying out pre-oxidation treatment on the reverse osmosis concentrated water by ozone at the temperature of 15-30 ℃;
the produced water of the ozone pre-oxidation tank is sequentially input into a homogenizing tank, a biological aerated filter, an ozone synergistic oxidation tank and a water outlet monitoring tank, and/or the produced water of the ozone pre-oxidation tank is sequentially input into the ozone synergistic oxidation tank, the homogenizing tank, the biological aerated filter and the water outlet monitoring tank, so that COD (chemical oxygen demand) in the discharged water of the water outlet monitoring tank is less than or equal to 100mg/L, and BOD (biochemical oxygen demand) is less than or equal to 20 mg/L; preferably, the using amount of the ozone in the ozone pre-oxidation pond is 20-40 mg/L.
6. The method for recycling and treating PTA reclaimed water according to claim 5, which is characterized by comprising the following steps: and inputting the produced water of the ozone pre-oxidation tank into a homogenizing tank, removing ozone in the produced water of the ozone pre-oxidation tank by adopting an aeration treatment mode, then performing biodegradation on the produced water of the homogenizing tank in a biological aerated filter, then enabling the produced water of the biological aerated filter to enter an ozone synergistic oxidation tank, degrading organic matters which are difficult to decompose under the combined action of ozone and a catalyst, and finally enabling the produced water of the ozone synergistic oxidation tank to enter a water outlet monitoring tank and be discharged.
7. The method for recycling and treating PTA reclaimed water according to claim 6, which comprises: the method for recycling and treating PTA reclaimed water specifically comprises the following steps: and the produced water of the ozone pre-oxidation tank is input into an ozone synergistic oxidation tank, organic matters which are difficult to decompose are degraded under the combined action of ozone and a catalyst, then the produced water of the synergistic oxidation tank is input into a homogeneous tank, the ozone in the produced water of the synergistic oxidation tank is removed in an aeration treatment mode, then the produced water of the homogeneous tank is subjected to biodegradation in a biological aerated filter, and finally the produced water of the biological aerated filter enters a water outlet monitoring tank and is discharged outside.
8. The method for recycling and treating PTA reclaimed water according to claim 5 or 6, which is characterized in that: the dissolved oxygen content in the aeration biological filter tank is 2-6mg/L, and the adding amount of the ozone in the ozone synergistic oxidation tank is 60-90 mg/L; preferably, the bottom layer filler in the aeration biological filter tank comprises cobblestones with the diameters of 16-32mm and 8-16mm respectively, and the upper layer filler comprises biological ceramsite with the diameter of 2-8 mm; preferably, the bottom layer filler in the ozone synergistic oxidation pond comprises cobbles with the diameters of 16-32mm and 8-16mm respectively, and the upper layer filler comprises an ozone oxidation catalyst with the diameter of 2-8 mm.
9. The method for recycling and treating water in PTA of claim 5, which is characterized in that: the coagulant aid comprises any one or the combination of more than two of polyaluminium chloride, ferric chloride and aluminum sulfate; preferably, the flocculant comprises an anionic polyacrylamide;
and/or the filtering filler in the filtering tank comprises a supporting layer and a filtering material layer, wherein the filtering material layer is arranged above the supporting layer, the particle size of the filtering filler particles of the supporting layer is 2-4mm, and the particle size of the filtering filler particles of the filtering material layer is 0.8-1.5 mm; preferably, the filter filler comprises manganese sand; and/or the filtering precision of the self-cleaning filter is 80-120 μm; the filtering precision of the first safety filter is 10-30 mu m; preferably, the aperture of a filter membrane in the ultrafiltration device is 0.05 mu m, the recovery rate of the ultrafiltration device is more than or equal to 90 percent, the SDI of produced water is less than or equal to 2, and the turbidity is less than or equal to 0.1 NTU; and/or the filtration precision of the second cartridge filter is 5-10 mu m, the system recovery rate of the reverse osmosis device is more than or equal to 75 percent, the desalination rate is more than or equal to 95 percent, the COD of produced water is less than or equal to 5mg/L, and the ammonia nitrogen is less than or equal to 0.1 mg/L.
10. The method for recycling water in PTA according to claim 5, further comprising: when the ozone content in the water produced by the homogenizing tank is more than 5mg/L, adding a reducing agent into the water produced by the homogenizing tank, preferably, the reducing agent comprises sodium sulfite and/or sodium bisulfite, and the adding amount of the reducing agent is 0-15 mg/L;
preferably, the method for recycling and treating the PTA reclaimed water further comprises the following steps: adding an oxidant into the ozone-synergetic oxidation pond to adjust the oxidation-reduction potential of the water produced by the ozone-synergetic oxidation pond to-150-450 mv; preferably, the oxidant comprises hydrogen peroxide;
preferably, the air quantity and the air pressure required in the homogenizing tank, the biological aerated filter and the ozone synergistic oxidation tank are supplied by a fan.
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| CN109851156A (en) * | 2018-12-29 | 2019-06-07 | 中冶赛迪工程技术股份有限公司 | A kind of glass waste water reuse treatment method and system |
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| CN112777882A (en) * | 2021-02-22 | 2021-05-11 | 北京中科康仑环境科技研究院有限公司 | Manganese sand-ozone integrated BAF system and corresponding wastewater treatment method |
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