CN115321759A - Coating wastewater purification method and purification system - Google Patents
Coating wastewater purification method and purification system Download PDFInfo
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- CN115321759A CN115321759A CN202211039234.8A CN202211039234A CN115321759A CN 115321759 A CN115321759 A CN 115321759A CN 202211039234 A CN202211039234 A CN 202211039234A CN 115321759 A CN115321759 A CN 115321759A
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- 239000002351 wastewater Substances 0.000 title claims abstract description 94
- 239000011248 coating agent Substances 0.000 title claims abstract description 73
- 238000000576 coating method Methods 0.000 title claims abstract description 73
- 238000000746 purification Methods 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 257
- 238000005345 coagulation Methods 0.000 claims abstract description 89
- 230000015271 coagulation Effects 0.000 claims abstract description 89
- 238000005188 flotation Methods 0.000 claims abstract description 44
- 238000000926 separation method Methods 0.000 claims abstract description 40
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 30
- 239000008213 purified water Substances 0.000 claims abstract description 24
- 238000001914 filtration Methods 0.000 claims abstract description 23
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 22
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 22
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 20
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 20
- 238000009287 sand filtration Methods 0.000 claims abstract description 14
- 239000010802 sludge Substances 0.000 claims description 87
- 238000006243 chemical reaction Methods 0.000 claims description 81
- 239000012528 membrane Substances 0.000 claims description 66
- 238000001223 reverse osmosis Methods 0.000 claims description 52
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- 230000001105 regulatory effect Effects 0.000 claims description 42
- 238000005238 degreasing Methods 0.000 claims description 38
- 229920002401 polyacrylamide Polymers 0.000 claims description 32
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 claims description 27
- 239000001110 calcium chloride Substances 0.000 claims description 27
- 229910001628 calcium chloride Inorganic materials 0.000 claims description 27
- 238000004017 vitrification Methods 0.000 claims description 22
- 239000012295 chemical reaction liquid Substances 0.000 claims description 17
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- RUTXIHLAWFEWGM-UHFFFAOYSA-H iron(3+) sulfate Chemical compound [Fe+3].[Fe+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O RUTXIHLAWFEWGM-UHFFFAOYSA-H 0.000 claims description 6
- 229910000360 iron(III) sulfate Inorganic materials 0.000 claims description 6
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- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 description 5
- 229910000831 Steel Inorganic materials 0.000 description 5
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 5
- 229910052731 fluorine Inorganic materials 0.000 description 5
- 239000011737 fluorine Substances 0.000 description 5
- 239000003002 pH adjusting agent Substances 0.000 description 5
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- ZCYVEMRRCGMTRW-UHFFFAOYSA-N 7553-56-2 Chemical compound [I] ZCYVEMRRCGMTRW-UHFFFAOYSA-N 0.000 description 2
- 235000013162 Cocos nucifera Nutrition 0.000 description 2
- 244000060011 Cocos nucifera Species 0.000 description 2
- 239000006004 Quartz sand Substances 0.000 description 2
- 239000005708 Sodium hypochlorite Substances 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
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- 239000003729 cation exchange resin Substances 0.000 description 2
- 150000001768 cations Chemical class 0.000 description 2
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- 229910052740 iodine Inorganic materials 0.000 description 2
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- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical group [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
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- 238000009300 dissolved air flotation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
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- 244000005700 microbiome Species 0.000 description 1
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- 239000000047 product Substances 0.000 description 1
- 238000011403 purification operation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
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- 239000000126 substance Substances 0.000 description 1
- 238000004381 surface treatment Methods 0.000 description 1
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- 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
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
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- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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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
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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
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
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- C—CHEMISTRY; METALLURGY
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
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- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
The invention provides a purification method and a purification system for coating wastewater, and relates to the technical field of wastewater treatment. The invention removes impurities such as grease, COD, grease, heavy metal, fluorinion and the like in the coating wastewater through oil separation regulation treatment and coagulation air flotation treatment, then removes COD through MBR treatment without increasing salt content, provides effective guarantee and support for the water yield of subsequent RO treatment, and the purified water obtained through RO treatment (sand filtration, carbon filtration, ion exchange resin filtration, primary RO treatment and secondary RO treatment) meets the requirement of production water, can save more than 70 percent of the production water, has obvious water-saving effect, and the concentrated water obtained through RO treatment meets the three-level standard of Integrated wastewater discharge Standard (DB 31/199-2018) in Shanghai city. The purification method provided by the invention has the advantages of advanced purification method, stable and reliable purification effect, high automation degree of purification of the coating wastewater, convenience in management and simplicity in operation and maintenance.
Description
Technical Field
The invention relates to the technical field of wastewater treatment, in particular to a method and a system for purifying coating wastewater.
Background
Coating wastewater, mainly degreasing bath solution and vitrification bath solution, is generated in the surface treatment process of the galvanized plate, and is continuously discharged, so that the wastewater treatment difficulty is high. After the wastewater is treated, reclaimed water is recycled, so that water resources are saved, and the method has important environmental, economic and social benefits.
At present, the research and application of coating wastewater treatment mainly focus on oil separation, chemical coagulation, precipitation, coagulation, biochemical treatment, reverse osmosis process and the like, however, the purified water obtained by the treatment method has the conductivity of more than 20 mu S/cm and high conductivity, and does not meet the requirement of production water.
Disclosure of Invention
In view of the above, the present invention aims to provide a purification method and a purification system for coating wastewater, wherein the purified water obtained by the purification method provided by the present invention has an electrical conductivity of less than or equal to 10 μ S/cm and a low electrical conductivity, and meets the requirements of water for production.
In order to achieve the above object, the present invention provides the following technical solutions:
the invention provides a method for purifying coating wastewater, which comprises the following steps:
carrying out oil removal regulation treatment on the coating wastewater to obtain an oil removal regulating solution;
mixing the oil removal regulating solution with an air flotation agent, and performing coagulation air flotation treatment to obtain a coagulation air flotation solution;
performing membrane biological reaction on the mixed coagulation air flotation liquid to obtain membrane biological reaction liquid;
performing reverse osmosis water treatment on the membrane biological reaction liquid to obtain purified water; the reverse osmosis water treatment comprises sand filtration, carbon filtration, ion exchange resin filtration, primary reverse osmosis treatment and secondary reverse osmosis treatment which are sequentially carried out.
Preferably, the coating wastewater comprises at least one of degreasing bath, vitrification bath and coating line overflow wastewater.
Preferably, when the coating wastewater is degreasing bath solution and/or vitrification bath solution, the method further comprises the following steps before the oil removal adjustment treatment: mixing the coating wastewater with a coagulation reaction agent, and carrying out coagulation reaction in batches.
Preferably, when the coating wastewater is degreasing bath solution, the coagulant comprises polymeric ferric sulfate, a pH value regulator and polyacrylamide;
when the coating wastewater is vitrified tank liquor, the coagulating agent comprises polymeric ferric sulfate, calcium chloride, a pH value regulator and polyacrylamide.
Preferably, the air flotation agent comprises polymeric ferric sulfate, calcium chloride, a pH value regulator and polyacrylamide.
The invention provides a coating wastewater purification system which is characterized by comprising an oil separation regulating reservoir 3, wherein the oil separation regulating reservoir 3 is provided with a water inlet, an oil outlet and an overproof wastewater inlet;
the water inlet of the air floatation tank 4 is communicated with the water outlet of the oil separation regulating tank 3; the air floatation tank 4 is also provided with a medicament inlet and a sludge outlet;
the MBR tank 5 is communicated with the water outlet of the air floatation tank 4 at the water inlet, and the MBR tank 5 is provided with a sludge outlet; an aeration anoxic chamber 5-1 and an aerobic reaction chamber 5-2 are arranged in the MBR tank 5;
a reverse osmosis water treatment system 6 with a water inlet communicated with a water outlet of the MBR tank 5, wherein the reverse osmosis water treatment system 6 is sequentially provided with a sand filter 6-1, a carbon filter 6-2, an ion exchange resin filter 6-3, a primary reverse osmosis membrane 6-4, a secondary reverse osmosis membrane 6-5 and a special reverse osmosis membrane 6-9 along the water flow direction; the secondary reverse osmosis membrane 6-5 is provided with a purified water outlet; the special reverse osmosis membrane 6-9 is provided with a concentrated water outlet.
Preferably, the purification system further comprises a coagulation reaction tank 2, and the coagulation reaction tank 2 is provided with a water inlet, a medicament inlet and a sludge outlet; and the water outlet of the coagulation reaction tank 2 is communicated with the water inlet of the oil separation regulating tank 3.
Preferably, the purification system further comprises a coating wastewater collection tank 1, wherein the coating wastewater collection tank 1 comprises a degreasing bath liquid collection tank 1-1 and a vitrification bath liquid collection tank 1-2 which are connected in parallel; the water outlets of the degreasing tank liquid collecting tank 1-1 and the vitrification tank liquid collecting tank 1-2 are communicated with the water inlet of the coagulation reaction tank 2; an oil scraper is arranged in the degreasing tank liquid collecting pool 1-1, and an oil outlet is further formed in the degreasing tank liquid collecting pool 1-1.
Preferably, along the water flow direction, the air floatation tank 4 is provided with an acid-base reaction chamber 4-1, a PFS reaction chamber 4-2, a calcium chloride reaction chamber 4-3, a PAM reaction chamber 4-4, a dissolved air chamber 4-5, a sludge and slag discharge chamber 4-6, a water level adjusting chamber 4-7, a pH adjusting chamber 4-8 and a water outlet chamber 4-9 which are sequentially connected in series;
the air floatation tank 4 is a dissolved air floatation tank.
Preferably, the purification system further comprises a sludge treatment system, wherein the sludge treatment system comprises a sludge concentration tank 13 and a filter press 14, and the inlet of the filter press is communicated with the sludge outlet of the sludge concentration tank 13; and a sludge inlet of the sludge concentration tank 13 is respectively communicated with a sludge outlet of the coagulation reaction tank 2, a sludge outlet of the air flotation tank 4 and a sludge outlet of the MBR tank 5.
The invention provides a method for purifying coating wastewater, which comprises the following steps: carrying out oil removal regulation treatment on the coating wastewater to obtain an oil removal regulating solution; mixing the oil removal regulating solution with an air flotation agent, and performing coagulation air flotation treatment to obtain a coagulation air flotation solution; performing Membrane Biological Reaction (MBR) on the mixed gas suspension to obtain membrane biological reaction liquid; performing reverse osmosis water treatment (RO treatment) on the membrane biological reaction liquid to obtain purified water; the reverse osmosis water treatment comprises sand filtration, carbon filtration, ion exchange resin filtration, primary reverse osmosis treatment (primary RO treatment) and secondary reverse osmosis treatment (secondary RO treatment) which are sequentially carried out. The invention removes grease from the coating wastewater through oil removal and adjustment treatment, removes impurities such as COD, grease, heavy metals, fluoride ions and the like through coagulation air flotation treatment, removes residual COD in the wastewater through MBR treatment without increasing salt content, provides effective guarantee and support for the water yield of subsequent RO treatment, and obviously reduces the conductivity of water through desalination of RO treatment (sand filtration, carbon filtration, ion exchange resin filtration, primary RO treatment and secondary RO treatment), and the obtained purified water meets the requirement of production water, and can save more than 70 percent of the production water and has obvious water-saving effect. The purification method provided by the invention is advanced, and the purification effect is stable and reliable; the water inflow and the water quality change of the coating wastewater have little influence on the purification method provided by the invention, and the impact resistance is good; moreover, the coating wastewater purification automation degree is high, the management is convenient, and the operation and maintenance are simple. The concentrated water obtained by the ROR treatment meets the three-level standard of 'Integrated wastewater discharge Standard' (DB 31/199-2018) in Shanghai city.
The invention also provides a purification system for the coating wastewater. The purification system provided by the invention is practical, advanced, stable and reliable, the water quality of the coating wastewater purified by the purification system can meet the water requirement of a production line, the production water can be saved by more than 70%, and the water-saving effect is obvious. The purification system provided by the invention can be flexibly operated to operate according to the change of water quantity and water quality. Moreover, the purification system provided by the invention adopts PLC control, and can realize the automatic purification operation of the coating wastewater, thereby simplifying operation management and reducing the labor intensity of workers, and the purification system is easy to maintain.
Drawings
FIG. 1 is a view showing the construction of a purification system for coating wastewater;
FIG. 2 is a schematic top view of the air flotation tank;
FIG. 3 is a schematic diagram of the MBR tank structure;
FIG. 4 is a schematic diagram of a RO system;
in the drawings 1-4, 1 is a coating wastewater collecting tank, 1-1 is a degreasing tank liquid collecting tank, 1-2 is a vitrification tank liquid collecting tank 1-2,3 is an oil separation adjusting tank, 4 is an air flotation tank, 4-1 is an acid-base reaction chamber, 4-2 is a PFS reaction chamber, 4-3 is a calcium chloride reaction chamber, 4-4 is a PAM reaction chamber, 4-5 is a dissolved air chamber, 4-5-1 is a dissolved air releaser, 4-5-2 is a dissolved air tank, 4-5-3 is a dissolved air pump, 4-5-4 is a valve, 4-6 is a sludge discharging and scraping chamber, 4-6-1 is a slag scraping machine, 4-6-2 is a first sludge hopper, 4-6-3 is a second sludge hopper, 4-7 is a water level adjusting chamber, 4-7-1 is a water level adjuster, 4-8 is a pH adjusting chamber, 4-9 of a water outlet chamber, 4-10 of a stirrer, 5 of an MBR tank, 5-1 of an aeration anoxic chamber, 5-1-1 of a perforation aeration device, 5-2 of an aerobic reaction chamber, 5-2-2 of a membrane component, 6 of a reverse osmosis water treatment system, 6-1 of a sand filter, 6-2 of a carbon filter, 6-3 of an ion exchange resin filter, 6-4 of a primary reverse osmosis membrane, 6-5 of a secondary reverse osmosis membrane, 6-6 of a primary RO water production reservoir, 6-7 of a purified water reservoir, 6-8 of a primary RO concentrated water reservoir, 6-9 of a special reverse osmosis membrane, 7 of a water collecting tank, 8 of a coagulation medicament reservoir, 9 of a membrane flux restorer reservoir, and 10 of a blower, 11 is an accident pool, 13 is a sludge concentration pool, 12 is an oil collecting pool, 14 is a filter press, 15 is a filter pressing collecting pool, 16 is a cofferdam collecting pool, and 17 is an MBR water producing pool.
Detailed Description
The invention provides a purification method of coating wastewater, which comprises the following steps:
carrying out oil removal regulation treatment on the coating wastewater to obtain an oil removal regulating solution;
mixing the oil removal regulating solution with an air flotation agent, and performing coagulation air flotation treatment to obtain a coagulation air flotation solution;
performing membrane biological reaction on the mixed coagulation air flotation liquid to obtain membrane biological reaction liquid;
performing reverse osmosis water treatment on the membrane biological reaction solution to obtain purified water; the reverse osmosis water treatment comprises sand filtration, carbon filtration, ion exchange resin filtration, primary reverse osmosis treatment and secondary reverse osmosis treatment which are sequentially carried out.
In the present invention, all the raw material components are commercially available products well known to those skilled in the art unless otherwise specified.
The invention carries out oil removal regulation treatment on the coating wastewater to obtain the oil removal regulating solution.
In the present invention, the coating wastewater preferably includes at least one of degreasing bath, vitrification bath, and coating line overflow wastewater. The degreasing bath solution, the vitrification bath solution and the coating line overflow wastewater are not particularly limited, and the degreasing bath solution, the vitrification bath solution and the coating line overflow wastewater which are well known to those skilled in the art can be adopted.
In the present invention, when the coating wastewater is degreasing bath and/or vitrification bath, it is preferable that the coating wastewater further includes, before the oil removal adjustment treatment: and mixing the coating wastewater with a coagulation reaction agent, and carrying out coagulation reaction in batches to obtain a coagulation reaction liquid.
In the invention, when the coating wastewater is a vitrified tank liquor, stirring treatment is also included before the coagulation reaction. In the present invention, the temperature of the stirring treatment is preferably room temperature; the stirring speed and time of the stirring treatment are not particularly limited, and the coating wastewater can be stirred to a uniform system.
In the invention, when the coating wastewater is degreasing bath solution, stirring treatment and oil scraping treatment are also included before the coagulation reaction. In the present invention, the temperature of the stirring treatment is preferably room temperature; the stirring speed and time of the stirring treatment are not particularly limited, and the coating wastewater can be stirred to a uniform system. In the present invention, the temperature of the oil scraping treatment is preferably room temperature; the time for the oil scraping treatment is preferably 1 to 4 hours, and more preferably 1 to 2 hours.
In the present invention, when the coating wastewater is a degreasing bath, the coagulation reagent (denoted as a first coagulation reagent) preferably includes polyferric sulfate (PFS), a pH adjuster, and Polyacrylamide (PAM). In the present invention, the PFS is preferably used in the form of an aqueous PFS solution having a concentration of preferably 5 to 15% by weight, more preferably 5 to 10% by weight; the adding concentration of the PFS (namely the concentration of the PFS in the system) is preferably 200-600 ppm, and more preferably 500-600 ppm; the aqueous PFS solution is preferably added in portions. In the present invention, the pH adjusting agent independently preferably comprises an acid and/or a base, the acid preferably comprising sulfuric acid; the base preferably comprises sodium hydroxide; the acid is preferably used in the form of an aqueous acid solution, preferably at a concentration of 5 to 10% by weight, more preferably 5% by weight; the base is preferably used in the form of an aqueous base solution, preferably in a concentration of 5 to 10wt%, more preferably 10wt%; the amount of the pH regulator used in the present invention is not particularly limited, and the pH of the system may be adjusted to 8 to 9. In the present invention, the PAM is preferably used in the form of an aqueous PAM solution, the concentration of the aqueous PAM solution being preferably 0.1 to 0.5wt%, more preferably 0.1 to 0.3wt%; the adding concentration of the PAM is preferably 10-50 ppm, and more preferably 10-20 ppm.
In the present invention, when the coating wastewater is a vitrified tank liquor, the coagulation reagent (marked as a second coagulation reagent) preferably comprises PFS and calcium chloride (CaCl) 2 ) pH value regulator and polyacrylamide. In the present invention, the use form and concentration of PFS, the use form and optional kind and concentration of pH adjuster, and the use form and concentration of PAM are the same as the first coagulation agent used when the coating wastewater is degreasing bath solution, and are not described herein again. In the present invention, the PFS addition concentration (i.e., the concentration of PFS in the system) is preferably 50About 100ppm, more preferably about 80 to 100ppm. In the present invention, the CaCl is 2 Preferably with CaCl 2 The CaCl is used in the form of an aqueous solution 2 The concentration of the aqueous solution is preferably 0.5 to 1wt%, more preferably 0.5wt%; said CaCl 2 The adding concentration of (A) is preferably 50-100 ppm, and more preferably 50ppm; the CaCl is 2 The aqueous solution is preferably added in portions. The amount of the pH regulator used in the present invention is not particularly limited, and the pH of the system may be adjusted to 8 to 9. In the invention, the addition concentration of PAM is preferably 10-50 ppm, and more preferably 10-20 ppm.
In the invention, the temperature of the coagulation reaction is preferably room temperature, and the time of the coagulation reaction is preferably 5-8 h; the coagulation reaction preferably comprises a first coagulation reaction and a second coagulation reaction which are sequentially carried out, and the time of the first coagulation reaction is preferably 1-2 h; the time of the second coagulation reaction is preferably 4 to 6 hours.
In a specific embodiment of the present invention, the coating wastewater and the coagulation reagent are stirred and mixed to perform a coagulation reaction, and preferably: under the condition of stirring, adding PFS into the coating wastewater, adding a pH value regulator to regulate the pH value to 8-9, carrying out a first coagulation reaction, continuously stirring and mixing for 1-2 min, stopping stirring and mixing, and carrying out a second coagulation reaction under the condition of standing to obtain a coagulation reaction liquid. In the present invention, the speed of the agitation and mixing and the speed of the further agitation and mixing are independently preferably 30 to 60rpm, more preferably 40 to 50rpm. In the present invention, when calcium chloride is further included in the coagulant, the calcium chloride is added after the PFS is added.
After the coagulation reaction is finished, the invention preferably further comprises the step of carrying out mud-water separation on the coagulation reaction system to obtain the coagulated sludge and the coagulation reaction liquid. In the invention, the coagulated sludge is sequentially concentrated and filter-pressed to obtain filter-pressed water and filter-pressed sludge, the filter-pressed water is subjected to oil separation regulation treatment, and the filter-pressed sludge is transported outwards. In the invention, the water content of the concentrated sludge obtained by concentration is 98-98.5 wt%. In the invention, the water content of the filter-pressing sludge is 70-75 wt%.
In the present invention, the oil removal adjustment treatment is preferably performed under a standing condition; the time for the oil removal adjustment treatment is preferably 4 to 6 hours, and more preferably 5 hours.
After the oil removal regulating solution is obtained, the oil removal regulating solution and an air flotation reagent are mixed for coagulation air flotation treatment, and a coagulation air flotation solution is obtained. In the present invention, the air-floating agent preferably comprises PFS, calcium chloride, pH regulator and PAM. In the present invention, the air flotation reagent (optional types of usage form, concentration and acid-base) is the same as the second coagulation reagent, and is not described herein again. In the present invention, the addition concentration of the PFS (i.e., the concentration of PFS in the system) is preferably 100 to 400ppm, more preferably 200 to 300ppm. In the present invention, the CaCl 2 The addition concentration of (B) is preferably 10 to 20ppm, more preferably 10 to 15ppm. The amount of the pH regulator used in the present invention is not particularly limited, and the pH of the system may be adjusted to 7 to 9. In the invention, the PAM is preferably added at a concentration of 4-10 ppm, more preferably 4-6 ppm.
In the present invention, the coagulation air flotation treatment preferably includes sequentially performing a first pH adjustor treatment, a PFS treatment, a calcium chloride treatment, a PAM treatment, and a second pH adjustor treatment. In the present invention, the pH of the system after the treatment with the first pH adjuster is preferably 9 to 10.5. In the present invention, the time for the PFS treatment, the calcium chloride treatment and the PAM treatment is independently preferably 5 to 10min, more preferably 6 to 9min, and still more preferably 7 to 8min. In the present invention, the pH of the system (i.e., the suspension) after the treatment with the second pH adjuster is preferably 7 to 8.
After the coagulation air flotation treatment is completed, the invention preferably further comprises the step of carrying out mud-water separation on the coagulation air flotation treatment system, wherein the mud-water separation is preferably the same as the mud-water separation, and details are not repeated herein.
After the coagulation air flotation liquid is obtained, the invention carries out membrane biological reaction (MBR treatment) on the coagulation air flotation liquid to obtain membrane biological reaction liquid. In the present invention, the MBR treatment preferably includes performing an anoxic treatment and an aerobic treatment in sequence, and the parameters of the anoxic treatment are as follows: the temperature is preferably room temperature, the time is preferably 1.6h, and the sludge concentration is preferably 6000 to 8000ppm; the parameters of the aerobic treatment are as follows: the membrane is preferably a flat membrane, the sludge concentration is preferably 6000 to 8000ppm, and the time is preferably 6.4h. In the invention, the MBR treatment mainly has the function of removing organic matters without increasing salt through the action of microorganisms, and provides effective guarantee and support for the water yield of subsequent RO treatment. In the invention, when the transmembrane pressure difference of the membrane adopted by the MBR treatment is not less than 35kPa, the membrane treatment method preferably further comprises the step of performing membrane flux recovery treatment on the membrane adopted by the MBR treatment, wherein the membrane flux recovery is preferably performed by adopting a membrane flux recovery agent for cleaning, the membrane flux recovery agent is preferably a sodium hypochlorite aqueous solution, and the concentration of the sodium hypochlorite aqueous solution is preferably 0.05-0.1 wt%.
After the MBR treatment is completed, the invention preferably further comprises the step of carrying out mud-water separation on the MBR treatment system, wherein the mud-water separation is preferably the same as the mud-water separation, and the details are not repeated.
After membrane biological reaction liquid is obtained, reverse osmosis water treatment is carried out on the membrane biological reaction liquid to obtain purified water; the reverse osmosis water treatment comprises sand filtration, carbon filtration, ion exchange resin filtration, primary reverse osmosis treatment (primary RO treatment) and secondary reverse osmosis treatment (secondary RO treatment) which are sequentially carried out.
In the present invention, the sand for sand filtration is preferably quartz sand, and the particle size of the sand is preferably 2 to 16mm. In the present invention, the carbon for carbon filtration is preferably activated carbon, more preferably coconut shell activated carbon, and the iodine value of the activated carbon is preferably 800mg/g. In the present invention, the ion exchange resin for ion exchange resin filtration is preferably a strongly acidic cation exchange resin, more preferably a 001 × 7 cation exchange resin; the ion exchange resin preferably has an exchange capacity of 4.3 to 4.5mmol/g, more preferably 4.5mmol/g.
In the invention, the first-stage RO treatment is carried out to obtain first-stage RO concentrated water and first-stage RO produced water; performing secondary RO treatment on the primary RO produced water to obtain purified water and secondary RO concentrated water; preferably, the first-stage RO concentrated water is subjected to high-salt water reverse osmosis treatment (ROR treatment) to obtain ROR concentrated water and ROR produced water; discharging when the ROR concentrated water reaches the standard; when the ROR concentrated water does not reach the standard, the oil removal regulation treatment is continuously carried out, and then the subsequent coagulation air flotation treatment, membrane biological reaction and reverse osmosis water treatment are continuously carried out; the standard reaching the standard is preferably the three-level standard (namely the sewage discharge standard of nano pipes) of 'Integrated wastewater discharge Standard' (DB 31/199-2018) in Shanghai city; and the ROR produced water is subjected to sand filtration treatment continuously. In the invention, the secondary RO concentrated water is repeatedly subjected to secondary RO treatment.
In the present invention, before the sand filtration, it is preferable that: mixing the membrane biological reaction liquid with water; the volume ratio of the membrane biological reaction liquid to water is preferably 1:0.2 to 0.4, more preferably 1:0.3; the water is preferably tap water.
The invention provides a purification system for coating wastewater, which comprises an oil separation regulating reservoir 3, wherein the oil separation regulating reservoir 3 is also provided with a water inlet, an oil outlet and an overproof wastewater inlet;
the water inlet of the air flotation tank 4 is communicated with the water outlet of the oil separation adjusting tank 3; the air floatation tank 4 is also provided with a medicament inlet and a sludge outlet;
the MBR tank 5 is communicated with the water outlet of the air flotation tank 4 through a water inlet, and the MBR tank 5 is provided with a sludge outlet; an aeration anoxic chamber 5-1 and an aerobic reaction chamber 5-2 are arranged in the MBR tank 5;
a reverse osmosis water treatment system 6 with a water inlet communicated with a water outlet of the MBR tank 5, wherein the reverse osmosis water treatment system 6 is sequentially provided with a sand filter 6-1, a carbon filter 6-2, an ion exchange resin filter 6-3, a primary reverse osmosis membrane 6-4, a secondary reverse osmosis membrane 6-5 and a special reverse osmosis membrane 6-9 along the water flow direction; the secondary reverse osmosis membrane 6-5 is provided with a purified water outlet; the special reverse osmosis membrane 6-9 is provided with a concentrated water outlet.
The purification system provided by the invention preferably comprises a coating wastewater collecting tank 1, wherein a stirring device, a water inlet and a water outlet are arranged in the coating wastewater collecting tank 1. In the present invention, the stirring device is preferably an air stirring device. In the present invention, the coating wastewater collection tank 1 preferably includes a degreasing bath liquid collection tank 1-1 and a vitrification bath liquid collection tank 1-2 connected in parallel. In the invention, an oil scraper is preferably further arranged in the degreasing bath liquid collecting tank 1-1, and the oil scraper is preferably a steel belt type oil scraper. In the invention, the degreasing bath liquid collecting tank 1-1 is also provided with an oil outlet. In the invention, the purification system preferably further comprises an oil collecting tank 12 with an oil inlet communicated with an oil outlet of the degreasing tank liquid collecting tank 1-1.
The purification system provided by the invention comprises a coagulation reaction tank 2, wherein a stirring device and a pH meter are arranged in the coagulation reaction tank 2, and the stirring device is preferably an air stirring device; the coagulation reaction tank 2 is provided with a degreasing treatment mode and a vitrification treatment mode, when the coating wastewater is degreasing bath solution, the degreasing treatment mode is adopted for treatment, and when the coating wastewater is vitrification bath solution, the vitrification treatment mode is adopted for treatment; the device is provided with a degreasing water inlet, a vitrification water inlet, a medicament inlet, a water outlet and a sludge outlet, wherein the degreasing water inlet is communicated with the water outlet of the degreasing bath liquid collecting tank 1-1, and the vitrification water inlet is communicated with the water outlet of the vitrification bath liquid collecting tank 1-2.
The purification system provided by the invention comprises an oil separation regulating reservoir 3, wherein the oil separation regulating reservoir 3 is provided with a water inlet, an oil outlet, an overflow wastewater inlet and an overproof wastewater inlet, and the water inlet of the oil separation regulating reservoir 3 is communicated with the water outlet of the coagulation reaction tank 2.
The purification system provided by the invention preferably further comprises a water collecting tank 7, wherein a water inlet of the water collecting tank 7 is communicated with a water outlet of the coagulation reaction tank 2, and a water outlet of the water collecting tank 7 is communicated with a water inlet of the oil separation regulating tank 3.
The purification system provided by the invention comprises an air flotation tank 4, the schematic plan view structure of the air flotation tank 4 is shown in fig. 2, the air flotation tank 4 is provided with a water inlet, a water outlet, a medicament inlet and a sludge outlet, and the water inlet of the air flotation tank 4 is communicated with the water outlet of the oil separation adjusting tank 3. In the invention, the floatation tank 4 is preferably a dissolved air floatation tank; along the water flow direction, the air floatation tank 4 is preferably provided with an acid-base reaction chamber 4-1, a PFS reaction chamber 4-2, a calcium chloride reaction chamber 4-3, a PAM reaction chamber 4-4, a dissolved air chamber 4-5, a sludge discharging and scraping chamber 4-6, a water level adjusting chamber 4-7, a pH adjusting chamber 4-8 and a water outlet chamber 4-9 which are sequentially connected in series; the acid-base reaction chamber 4-1 is provided with a water inlet. In the invention, the dissolved air chamber 4-5 is provided with a dissolved air releaser 4-5-1, a dissolved air tank 4-5-2 and a dissolved air pump 4-5-3 which are communicated in sequence; the air outlet pipe of the dissolved air pump 4-5-3 is divided into two branch pipes, wherein one branch pipe is communicated with the water level adjusting chamber 4-7; and valves 4-5-4 are arranged on a pipeline for communicating the dissolved air pump 4-5-3 with the water level adjusting chamber 4-7, and the number of the valves 4-5-4 is 1 or 2. In the invention, stirrers 4-10 are respectively arranged in the acid-base reaction chamber 4-1, the PFS reaction chamber 4-2, the calcium chloride reaction chamber 4-3, the PAM reaction chamber 4-4, the water level adjusting chamber 4-7 and the pH adjusting chamber 4-8. In the invention, the acid-base reaction chamber 4-1, the PAM reaction chamber 4-4, the dissolved air chamber 4-5, the water level adjusting chamber 4-7 and the pH adjusting chamber 4-8 are all provided with emptying ports. In the invention, a slag scraper 4-6-1, a first mud bucket 4-6-2 and a second mud bucket 4-6-3 are arranged in the sludge discharging and scraping chamber 4-6, and sludge discharging ports are arranged at the bottoms of the first mud bucket 4-6-2 and the second mud bucket 4-6-3; the sludge discharging and scraping chamber 4-6 is also provided with a sludge discharging port. In the invention, a water level regulator 4-7-1 is arranged in the water level regulating chamber 4-7. In the invention, the pH adjusting chamber 4-8 is also provided with a water outlet. In the invention, the air floatation tank 4 is an open device, and air floatation agents are added into each chamber at the opening.
The purification system provided by the invention preferably further comprises a coagulation medicament storage 8, and an outlet of the coagulation medicament storage 7 is respectively communicated with a medicament inlet of the coagulation reaction tank 2 and a medicament inlet of the air flotation tank 4.
The purification system provided by the invention comprises an MBR tank 5, wherein the MBR tank 5 is provided with a water inlet, an air inlet, a water outlet and a sludge outlet; the MBR tank 5 is preferably also provided with a membrane flux restorer inlet; the MBR tank is schematically shown in figure 3, and the MBR tank 5 is provided with an aeration anoxic chamber 5-1 and an aerobic reaction chamber 5-2. In the invention, a perforated aeration device 5-1-1 is arranged in the aeration anoxic chamber 5-1, and a water inlet is arranged in the aeration anoxic chamber 5-1; the volume of the aeration anoxic chamber 5-1 is preferably 1/5 of the volume of the MBR tank 5. In the invention, the aerobic reaction chamber 5-2 is provided with a vent, a sludge outlet and a water outlet; a membrane component 5-2-2 is arranged in the aerobic reaction chamber 5-2, and the form of the membrane component 5-2-2 is preferably a flat membrane component; the cleaning mode of the membrane module is preferably off-line cleaning (namely, the membrane module is taken out from the aerobic reaction chamber 5-2 and then cleaned) and/or on-line cleaning (namely, the membrane module is directly cleaned in the aerobic reaction chamber 5-2); the membrane modules 5-2-2 are preferably arranged in groups, preferably in 1 to 3 groups, more preferably in 3 groups. The invention sets the membrane modules in groups, and when one membrane module cannot be used, the operation of the MBR tank is not influenced. In the invention, the water outlet of the membrane module 5-2-2 is preferably communicated with a water production pump, the operation mode of the MBR tank is preferably that the water production pump operates for 8min to stops for 2min, and the operation is repeated and circulated (recorded as eight-on and two-off).
The purification system provided by the invention preferably further comprises an MBR water production tank 17, and the water inlet of the MBR water production tank 17 is communicated with the water outlet of the MBR tank 5.
The purification system provided by the invention preferably further comprises a membrane flux recovery agent reservoir 9, wherein the outlet of the membrane flux recovery agent reservoir 9 is communicated with the membrane flux recovery agent inlet of the MBR tank 5.
The purification system provided by the invention preferably further comprises a blower 10, and the blower 10 is communicated with an air inlet of the MBR tank 5.
The purification system provided by the invention comprises a reverse osmosis water treatment system (RO system) 6, and the structural schematic diagram of the RO system 6 is shown in FIG. 4. Along the water flow direction, the RO system 6 is sequentially provided with a sand filter 6-1, a carbon filter 6-2, an ion exchange resin filter 6-3, a primary reverse osmosis membrane (primary RO) 6-4, a secondary reverse osmosis membrane (secondary RO) 6-5 and a special reverse osmosis membrane (ROR) 6-9; the first-stage RO6-4 is provided with a water inlet, a water outlet and a concentrated water outlet; the second-stage RO6-5 is provided with a purified water outlet and a second-stage RO concentrated water outlet; the inlet of the sand filter 6-1 is communicated with the water outlet of the MBR water production tank 17. In the present invention, the RO system preferably further comprises a primary RO production water reservoir 6-6, a purified water reservoir 6-7, a primary RO concentrate reservoir 6-8, and an ROR6-9; the water inlet of the primary RO water production reservoir 6-6 is respectively communicated with the water outlet of the primary RO6-4 and the secondary RO concentrated water outlet; the water inlet of the purified water storage 6-7 is communicated with the purified water outlet of the second-stage RO6-5, and the obtained purified water can be reused in a workshop; the inlet of the first-stage RO concentrated water reservoir 6-8 is communicated with the concentrated water outlet of the first-stage RO 6-4; the water inlet of the ROR6-9 is communicated with the outlet of the primary RO concentrated water storage 6-8, and the ROR water production outlet of the ROR6-9 is communicated with the water inlet of the MBR water production tank 17; the ROR6-9 is provided with a concentrated water outlet, and ROR concentrated water obtained through ROR treatment is discharged after reaching the standard.
The purification system provided by the invention preferably further comprises an accident pool 11, wherein an inlet of the accident pool 11 is communicated with an ROR concentrated water outlet of the ROR6-9, and an outlet of the accident pool 11 is communicated with an overproof wastewater inlet of the oil separation regulating pool 3; and returning the excessive wastewater which does not reach the ROR concentrated water standard and is obtained through ROR treatment to the accident pool 11, and then conveying the excessive wastewater to the oil removal regulating pool 3 for continuous treatment.
The purification system provided by the invention preferably further comprises a tap water tank 18, and a water outlet of the tap water tank 18 is communicated with a water inlet of the sand filter 6-1.
The purification system provided by the invention preferably further comprises a sludge treatment system, wherein the sludge treatment system comprises a sludge concentration tank 13 and a filter press 14, and the inlet of the filter press is communicated with the sludge outlet of the sludge concentration tank 13; a sludge inlet of the sludge concentration tank 13 is respectively communicated with a sludge outlet of the coagulation reaction tank 2, a sludge outlet of the air flotation tank 4 and a sludge outlet of the MBR tank 5; the filter press 14 is provided with a pressure filtration water outlet and a sludge outlet; the filter press is preferably a chamber filter press.
The purification system provided by the invention preferably further comprises a filter-pressing water collecting tank 15, wherein the filter-pressing water collecting tank 15 is provided with an inlet and an outlet, the inlet of the filter-pressing water collecting tank 15 is communicated with a filter-pressing water outlet of the filter press 14, and the outlet of the filter-pressing water collecting tank 15 is communicated with an overflow wastewater inlet of the oil separation regulating tank 3.
In the invention, the periphery of the purification system area is preferably provided with a cofferdam to prevent sewage from overflowing. The purification system provided by the invention preferably further comprises a cofferdam water collecting tank 16, the cofferdam water collecting tank 16 is provided with a cofferdam water collecting inlet and an outlet, and the outlet of the cofferdam water collecting tank 16 is communicated with the overflow wastewater inlet of the oil separation regulating tank 3.
The following detailed description of the method for purifying coating wastewater with reference to fig. 1 to 4 includes the following steps: conveying the coating wastewater into a coating wastewater collecting tank 1 for stirring treatment to obtain stirring treatment wastewater; draining the stirred wastewater into a coagulation reaction tank 2, mixing the wastewater with a first coagulation reagent, and carrying out coagulation reaction to obtain a coagulation reaction solution; conveying the coating wastewater to an oil separation regulating reservoir 3 through a water collecting reservoir 7 for oil separation regulating treatment to obtain an oil removal regulating solution; conveying the oil removal regulating solution to an air flotation tank 4 to be mixed with an air flotation agent, and performing coagulation air flotation treatment to obtain a coagulation air flotation solution; conveying the mixed gas flotation liquid to an MBR tank 5 for MBR treatment to obtain MBR treatment liquid; conveying the MBR treatment liquid to an RO system 6, sequentially performing sand filtration through a sand filter 6-1, carbon filtration through a carbon filter 6-2, ion exchange resin filtration through an ion exchange resin filter 6-3, primary RO treatment through a primary RO6-4, and secondary RO treatment through a secondary RO to obtain purified water and ROR concentrated water; wherein, the first-stage RO concentrated water obtained by the first-stage RO treatment is conveyed to ROR6-9 for ROR treatment; ROR concentrated water is discharged after reaching the standard, and if the ROR concentrated water does not reach the standard, the ROR concentrated water is conveyed to the oil removal regulating tank 3 through the accident tank 11 to continue oil removal regulation treatment; and (3) conveying the sludge generated by the coagulation reaction tank 2, the air flotation tank 4 and the MBR tank 5 to a sludge concentration tank 13 for concentration, then conveying the sludge to a filter press 14 for filter pressing to obtain filter pressing water and filter pressing sludge, conveying the filter pressing water to an oil separation adjusting tank 3 for oil separation adjustment treatment, and conveying the filter pressing sludge to the outside.
The technical solution of the present invention will be clearly and completely described below with reference to the embodiments of the present invention. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be obtained by a person skilled in the art without making any creative effort based on the embodiments in the present invention, belong to the protection scope of the present invention.
Example 1
The method for purifying the coating wastewater by adopting the device shown in the figures 1 to 4 comprises the following specific steps:
(1) Conveying degreasing tank liquid to a degreasing tank liquid collecting pool 1-1, stirring under an air stirring device, stopping stirring, and then scraping oil under a steel belt type oil scraper, wherein the starting time of the steel belt type oil scraper every day is 2 hours, so as to obtain degreasing and stirring treatment wastewater; the COD concentration in the degreasing bath solution is 10000mg/L, the zinc concentration is 20ppm, the fluorine concentration is 10ppm, and the conductivity is 2000 mu S/cm.
And/or conveying the vitrified tank liquid to a vitrified tank liquid collecting pool 1-2, and stirring under an air stirring device to obtain vitrified stirring treated wastewater; the COD concentration in the ceramic bath solution is 100mg/L, the zinc concentration is 200ppm, the fluorine concentration is 150ppm, and the conductivity is 3000 mu S/cm.
(2) The degreasing and stirring treatment of the wastewater is carried out in batches (the wastewater treatment amount is 3m each time) 3 ) Conveying the mixture into a coagulation reaction tank 2, starting a stirring device at a high liquid level (the stirring speed is 60 rpm) while stopping water inflow, adding a PFS aqueous solution with the concentration of 5wt% until the PFS is added with the concentration of 600ppm, stirring for 10min, then adding a sulfuric acid aqueous solution with the concentration of 5wt% and/or a sodium hydroxide aqueous solution with the concentration of 10wt% to adjust the pH value to 8-9, stirring for 1h, then adding a PAM aqueous solution with the concentration of 0.1wt% until the PAM is added with the concentration of 10ppm, stirring for 1min, stopping stirring, and standing for 6h to obtain a coagulation reaction solution and sludge slurry; opening a supernatant liquid electromagnetic valve, discharging the coagulation reaction liquid into the water collecting tank 7 under the action of gravity, closing the electromagnetic valve when the liquid level is low, starting a pneumatic diaphragm pump, and discharging sludge slurry into a sludge concentration tank 13;
and/or, the vitrified stirring treatment liquid is divided into batches (the amount of wastewater treated in each time is 3 m) 3 ) Conveying the mixture to a coagulation reaction tank 2, starting a stirring device at a high liquid level, stopping water inflow at the same time, adding a PFS aqueous solution with the concentration of 5wt% until the adding concentration of PFS is 100ppm, stirring for 10min, then adding a calcium chloride aqueous solution with the concentration of 0.5wt% until the adding concentration of calcium chloride is 200ppm, stirring for 5min, then adding a sulfuric acid aqueous solution with the concentration of 5wt% and/or a sodium hydroxide aqueous solution with the concentration of 10wt% to adjust the pH value to be 8-9, stirring for 1h, then adding a PAM aqueous solution with the concentration of 0.1wt% until the adding concentration of PAM is 10ppm, stirring for 1min, stopping stirring, and standing for 6h to obtain a coagulation reaction solution and coagulated sludge slurry; opening the supernatant fluid electromagnetic valve, discharging the coagulation reaction liquid into the water collecting tank 7 under the action of gravity, closing the electromagnetic valve when the liquid level is low, starting the pneumatic diaphragm pump, and discharging the coagulated sludge slurry into the sludge concentration tank 13。
(3) Conveying the coagulation reaction liquid to an oil separation regulating reservoir 3 through a water collecting tank 7, conveying coating line overflow wastewater to the oil separation regulating reservoir 3, performing stirring treatment under an air stirring device, and performing oil separation regulating treatment under a steel belt type oil scraper after stirring is stopped to obtain an oil removal regulating liquid, wherein the air stirring device is always in a starting state when the oil separation regulating reservoir 3 runs, and the steel belt type oil scraper is started for 2 hours every day; wherein, the COD concentration in the coating line overflow wastewater is 400mg/L, the zinc concentration is 10ppm, the fluorine concentration is 10ppm, and the conductivity is 200 MuS/cm. .
(4) Conveying the oil removal regulating solution into an air flotation tank 4, adding a 5wt% sulfuric acid aqueous solution and/or a 10wt% sodium hydroxide aqueous solution into an acid-base reaction chamber 4-1 in a dissolved air flotation mode to adjust the pH value to be 9-10.5, conveying the solution into a PFS reaction chamber, adding a 5wt% PFS aqueous solution until the adding concentration of the PFS is 100ppm, stirring the solution for 10min, then conveying the solution into a calcium chloride reaction chamber 4-3, adding a 0.5wt% calcium chloride aqueous solution until the adding concentration of the calcium chloride is 10ppm, stirring the solution for 10min, then conveying the solution into a PAM reaction chamber 4-4, adding a 0.1wt% PAM aqueous solution until the adding concentration of the PAM is 4ppm, stirring the solution for 10min, then adding a 5wt% sulfuric acid aqueous solution and/or a 10wt% sodium hydroxide aqueous solution to adjust the pH value to be 7-8, and obtaining a coagulation air flotation solution and air flotation sludge slurry; the air-floated sludge slurry is discharged into a sludge concentration tank 13.
(5) Conveying the mixed condensed air flotation liquid into an MBR tank 5, carrying out anoxic treatment for 1.6h under the condition that the sludge concentration is 6000ppm, and then carrying out aerobic treatment for 6.4h under the condition that the sludge concentration is 6000ppm to obtain MBR treatment liquid and MBR sludge slurry; the MBR treatment liquid is conveyed to an MBR water production tank 17, and MBR sludge slurry is discharged into a sludge concentration tank 13; wherein, the MBR tank is provided with 3 groups of flat membrane assemblies, the operation mode of the MBR tank is that a water producing pump operates for 8min to stop for 2min, the operation is repeatedly circulated (recorded as eight times and two times), and the total time of MBR treatment is 8h. The COD concentration in the MBR treatment liquid is 30mg/L, the zinc concentration is less than 0.5ppm, the fluorine concentration is less than 1ppm, and the conductivity is 1000-1300 mu S/cm.
(6) Conveying the MBR treatment solution into a sand filter 6-1 through an MBR water production tank 17, conveying tap water into the sand filter 6-1 through a tap water barrel 18, performing sand filtration, performing carbon filtration on the carbon filter 6-2, performing ion exchange resin filtration on a 001 x 7 cation ion exchange resin (the exchange capacity is 4.5 mmol/g) filter 6-3, and performing primary RO treatment on primary RO6-4 to obtain primary RO water production and primary RO concentrated water; conveying the primary RO produced water to a secondary RO6-5 through a primary RO produced water barrel 6-6 for secondary RO treatment to obtain secondary RO produced water (namely purified water) and secondary RO concentrated water, wherein the purified water is stored in the purified water barrel 6-7 and reused in a workshop; conveying the first-stage RO concentrated water to ROR6-9 for ROR treatment to obtain ROR concentrated water and ROR produced water; the ROR produced water flows back to the MBR water production tank 17 to continue sand filtration; ROR concentrated water is discharged after reaching the standard (DB 31/199-2018 three-level standard), and if not, the ROR concentrated water is conveyed to the oil removal regulating reservoir 3 through the accident reservoir 11 to continue oil removal regulation treatment; and the second-stage RO concentrated water flows back to the first-stage RO water producing barrel 6-6, and then the second-stage RO treatment is continuously carried out. Wherein, the flow ratio of MBR treatment liquid to tap water is 1:0.3. the sand for sand filtration is quartz sand with the particle size of 2-16 mm, the carbon for carbon filtration is preferably coconut shell activated carbon, and the iodine value of the carbon for carbon filtration is 800mg/g; the ion exchange resin filtration was carried out using a strongly acidic cation resin, and the exchange capacity was 4.3mmol/g. The COD concentration in the purified water is less than 1mg/L, and the conductivity is 5-10 mu S/cm; the COD concentration in the ROR concentrated water is 150-200 mg/L, the zinc concentration is 2.5-5 ppm, the fluorine concentration is 5-10 ppm, and the conductivity is 4500-6000 muS/cm.
(7) And (3) concentrating the sludge slurry in the sludge concentration tank 13 until the water content of the obtained concentrated sludge is 98.5wt%, then conveying the concentrated sludge into a filter press 14 for filter pressing to obtain filter pressing water and filter pressing sludge, conveying the filter pressing water into an oil separation regulating tank 3 for oil separation regulation treatment, and transporting the filter pressing sludge outwards, wherein the water content of the filter pressing sludge is 75wt%.
The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A method for purifying coating wastewater comprises the following steps:
carrying out oil removal regulation treatment on the coating wastewater to obtain an oil removal regulating solution;
mixing the oil removal regulating solution with an air flotation agent, and performing coagulation air flotation treatment to obtain a coagulation air flotation solution;
performing membrane biological reaction on the mixed coagulation air flotation liquid to obtain membrane biological reaction liquid;
performing reverse osmosis water treatment on the membrane biological reaction solution to obtain purified water; the reverse osmosis water treatment comprises sand filtration, carbon filtration, ion exchange resin filtration, primary reverse osmosis treatment and secondary reverse osmosis treatment which are sequentially carried out.
2. The purification method according to claim 1, wherein the coating wastewater comprises at least one of degreasing bath, vitrification bath, and coating line overflow wastewater.
3. The purification method according to claim 2, wherein when the coating wastewater is degreasing bath solution and/or vitrification bath solution, the oil removal adjustment treatment further comprises: mixing the coating wastewater with a coagulation reaction agent, and carrying out coagulation reaction in batches.
4. The purification method according to claim 2 or 3, wherein when the coating wastewater is degreasing bath solution, the coagulant comprises polymeric ferric sulfate, a pH regulator and polyacrylamide;
when the coating wastewater is a vitrification tank liquid, the coagulation agent comprises polymeric ferric sulfate, calcium chloride, a pH value regulator and polyacrylamide.
5. The purification method according to claim 1, wherein the air flotation agent comprises polymeric ferric sulfate, calcium chloride, a pH regulator and polyacrylamide.
6. The coating wastewater purification system is characterized by comprising an oil separation regulating reservoir (3), wherein the oil separation regulating reservoir (3) is provided with a water inlet, an oil outlet and an overproof wastewater inlet;
the water inlet of the air floatation tank (4) is communicated with the water outlet of the oil separation adjusting tank (3); the air floatation tank (4) is also provided with a medicament inlet and a sludge outlet;
the water inlet of the MBR tank (5) is communicated with the water outlet of the air floatation tank (4), and the MBR tank (5) is provided with a sludge outlet; an aeration anoxic chamber (5-1) and an aerobic reaction chamber (5-2) are arranged in the MBR tank (5);
a reverse osmosis water treatment system (6) with a water inlet communicated with a water outlet of the MBR tank (5), wherein the reverse osmosis water treatment system (6) is sequentially provided with a sand filter (6-1), a carbon filter (6-2), an ion exchange resin filter (6-3), a first-stage reverse osmosis membrane (6-4), a second-stage reverse osmosis membrane (6-5) and a special reverse osmosis membrane (6-9) along the water flow direction; the second-stage reverse osmosis membrane (6-5) is provided with a purified water outlet, and the special reverse osmosis membrane (6-9) is provided with a concentrated water outlet.
7. The purification system according to claim 7, further comprising a coagulation reaction tank (2), wherein the coagulation reaction tank (2) is provided with a water inlet, a medicament inlet and a sludge outlet; and the water outlet of the coagulation reaction tank (2) is communicated with the water inlet of the oil separation regulating tank (3).
8. The purification system according to claim 8, further comprising a coating wastewater collection tank (1), wherein the coating wastewater collection tank (1) comprises a degreasing bath collection tank (1-1) and a vitrification bath collection tank (1-2) connected in parallel; the water outlets of the degreasing tank liquid collecting tank (1-1) and the vitrification tank liquid collecting tank (1-2) are communicated with the water inlet of the coagulation reaction tank (2); an oil scraper is arranged in the degreasing tank liquid collecting tank (1-1), and an oil outlet is also arranged in the degreasing tank liquid collecting tank (1-1).
9. The purification system according to claim 7, wherein the air flotation tank (4) is provided with an acid-base reaction chamber (4-1), a PFS reaction chamber (4-2), a calcium chloride reaction chamber (4-3), a PAM reaction chamber (4-4), a gas dissolving chamber (4-5), a sludge discharging and scraping chamber (4-6), a water level adjusting chamber (4-7), a pH adjusting chamber (4-8) and a water outlet chamber (4-9) which are connected in series in sequence along the water flow direction;
the air floatation tank (4) is a dissolved air floatation tank.
10. The purification system according to claim 7, 8 or 9, further comprising a sludge treatment system comprising a sludge concentration tank (13) and a filter press (14) having an inlet in communication with a sludge outlet of the sludge concentration tank (13); and a sludge inlet of the sludge concentration tank (13) is respectively communicated with a sludge outlet of the coagulation reaction tank (2), a sludge outlet of the air floatation tank (4) and a sludge outlet of the MBR tank (5).
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