CN116854296A - Method and system for recovering purified water from high-salt sewage by reinforced coagulation and membrane separation - Google Patents
Method and system for recovering purified water from high-salt sewage by reinforced coagulation and membrane separation Download PDFInfo
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- CN116854296A CN116854296A CN202310877608.1A CN202310877608A CN116854296A CN 116854296 A CN116854296 A CN 116854296A CN 202310877608 A CN202310877608 A CN 202310877608A CN 116854296 A CN116854296 A CN 116854296A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 165
- 239000012528 membrane Substances 0.000 title claims abstract description 134
- 238000005345 coagulation Methods 0.000 title claims abstract description 45
- 230000015271 coagulation Effects 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 41
- 239000010865 sewage Substances 0.000 title claims abstract description 41
- 238000000926 separation method Methods 0.000 title claims abstract description 26
- 239000008213 purified water Substances 0.000 title claims abstract description 24
- 239000000701 coagulant Substances 0.000 claims abstract description 74
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims abstract description 68
- 239000005708 Sodium hypochlorite Substances 0.000 claims abstract description 56
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims abstract description 56
- 238000006243 chemical reaction Methods 0.000 claims abstract description 48
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 48
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 48
- 238000005189 flocculation Methods 0.000 claims abstract description 46
- 230000016615 flocculation Effects 0.000 claims abstract description 46
- 238000002156 mixing Methods 0.000 claims abstract description 42
- 239000007790 solid phase Substances 0.000 claims abstract description 37
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 31
- 230000003647 oxidation Effects 0.000 claims abstract description 30
- 239000000126 substance Substances 0.000 claims abstract description 23
- 238000003756 stirring Methods 0.000 claims abstract description 20
- 239000011259 mixed solution Substances 0.000 claims abstract description 18
- 238000001556 precipitation Methods 0.000 claims abstract description 15
- 150000003839 salts Chemical class 0.000 claims abstract description 11
- 239000000203 mixture Substances 0.000 claims abstract description 5
- 238000005374 membrane filtration Methods 0.000 claims abstract description 4
- 230000001376 precipitating effect Effects 0.000 claims abstract description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 30
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical class O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 26
- 238000003860 storage Methods 0.000 claims description 21
- 239000000243 solution Substances 0.000 claims description 19
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 13
- 238000001914 filtration Methods 0.000 claims description 12
- 150000004676 glycans Chemical class 0.000 claims description 11
- 229920001282 polysaccharide Polymers 0.000 claims description 11
- 239000005017 polysaccharide Substances 0.000 claims description 11
- 102000004169 proteins and genes Human genes 0.000 claims description 11
- 108090000623 proteins and genes Proteins 0.000 claims description 11
- 239000007787 solid Substances 0.000 claims description 11
- 238000007599 discharging Methods 0.000 claims description 10
- 230000004907 flux Effects 0.000 claims description 8
- 238000004062 sedimentation Methods 0.000 claims description 6
- 230000001590 oxidative effect Effects 0.000 claims description 5
- 238000000746 purification Methods 0.000 claims description 5
- 239000006228 supernatant Substances 0.000 claims description 5
- BZSXEZOLBIJVQK-UHFFFAOYSA-N 2-methylsulfonylbenzoic acid Chemical compound CS(=O)(=O)C1=CC=CC=C1C(O)=O BZSXEZOLBIJVQK-UHFFFAOYSA-N 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 4
- 230000035484 reaction time Effects 0.000 claims description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 3
- 230000007935 neutral effect Effects 0.000 claims description 3
- 238000002360 preparation method Methods 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 2
- 238000003825 pressing Methods 0.000 claims description 2
- 239000002351 wastewater Substances 0.000 claims 8
- 238000005516 engineering process Methods 0.000 abstract description 24
- 238000012423 maintenance Methods 0.000 abstract description 2
- 239000008399 tap water Substances 0.000 abstract description 2
- 235000020679 tap water Nutrition 0.000 abstract description 2
- 239000007788 liquid Substances 0.000 description 13
- 230000000694 effects Effects 0.000 description 10
- 239000003344 environmental pollutant Substances 0.000 description 6
- 231100000719 pollutant Toxicity 0.000 description 6
- 239000012466 permeate Substances 0.000 description 5
- 239000010802 sludge Substances 0.000 description 5
- 239000002245 particle Substances 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 239000000084 colloidal system Substances 0.000 description 3
- 238000010612 desalination reaction Methods 0.000 description 3
- 239000003814 drug Substances 0.000 description 3
- 244000005700 microbiome Species 0.000 description 3
- 230000003014 reinforcing effect Effects 0.000 description 3
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 2
- 238000011109 contamination Methods 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000000813 microbial effect Effects 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- -1 salt ions Chemical class 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000000844 anti-bacterial effect Effects 0.000 description 1
- 239000003899 bactericide agent Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000010485 coping Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 229910001410 inorganic ion Inorganic materials 0.000 description 1
- 230000009545 invasion Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000009285 membrane fouling Methods 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- 230000010349 pulsation Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 238000002791 soaking Methods 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
-
- 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
- C02F1/44—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
- 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
-
- 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
- C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Abstract
A method for recovering purified water from high-salt sewage by reinforced coagulation and membrane separation comprises the following steps: (1) sodium hypochlorite pre-oxidation; (2) mixing polyaluminium chloride; adding polyaluminium chloride into the pretreated sewage, and uniformly stirring and mixing to form polyaluminium chloride mixed solution; (3) flocculation reaction: adding a solid phase coagulant aid into the polyaluminium chloride mixed solution, stirring and mixing the mixture, and removing granular substances and most of turbidity substances contained in water to obtain flocculation mixed solution; (4) precipitation: precipitating the flocculation mixed solution; (5) ultrafiltration membrane filtration; (6) reverse osmosis separation. The invention combines the reinforced coagulation technology and the ultrafiltration/reverse osmosis membrane technology to form a set of high-efficiency method for obtaining purified water from secondary effluent of sewage treatment plants containing higher salt. Compared with other methods, the method can obtain purified water similar to the water quality of tap water, and meanwhile, the system is more stable, the maintenance is simpler and more convenient, and the service time is longer.
Description
Technical Field
The invention relates to a method and a device for recovering purified water from sewage by a membrane separation technology, belonging to the technical field of sewage treatment.
Background
The purified water extracted from the water treated by the sewage treatment plant is used for meeting the water demands of municipal administration, industry, agriculture and the like, has important significance for relieving the crisis of water resource shortage, and is also an important measure for coping with the water crisis. However, for some sewage treatment plants with higher salt content of the inlet water, such as those in coastal areas affected by seawater invasion and those receiving industrial wastewater containing salt, the salt content of the outlet water is higher, and when extracting purified water from the water, not only organic pollutants but also salt in the water need to be removed.
The existing reverse osmosis technology can realize the efficient removal of salt and organic matters in water, is a very promising technology for extracting purified water from sewage, but the pollution problem of the reverse osmosis membrane is always a key for restricting the operation of the reverse osmosis technology. In a reverse osmosis membrane treatment system for extracting purified water from effluent of a sewage treatment plant, a coagulation technology is widely used at present as a pretreatment technology for membrane separation.
The coagulation treatment technology mainly removes insoluble substances such as colloid, particulate matters and the like contained in water, and has very limited removal capacity for dissolved pollutants contained in water. However, since the effluent of the sewage treatment plant generally still contains higher substances which are easy to cause membrane pollution, such as protein, polysaccharide and the like, the subsequent membrane pollution problem becomes more serious, and meanwhile, if the coagulant is added excessively in the coagulation process, the residual coagulant can also aggravate the membrane pollution.
The existing coagulation technology can only reduce the pollution of granular pollutants and turbidity matters contained in water to the subsequent membrane components, and hardly has the removal effect on dissolved proteins, polysaccharides and other organic matters contained in water, so that the pollution of the two pollutants to the subsequent membrane components cannot be reduced; meanwhile, when the secondary effluent of a sewage treatment plant with low turbidity is treated, the existing coagulation technology needs to achieve better coagulation efficiency in a mode of adding a large amount of coagulant, so that pollution to a subsequent membrane assembly caused by coagulant residues can be caused; meanwhile, the existing coagulation technology cannot solve the problems of subsequent ultrafiltration and microbial contamination of reverse osmosis membranes.
Therefore, how to combine the high-efficiency pretreatment technology with the membrane separation technology, the influence of protein, polysaccharide organic matters and residual coagulant in water on the subsequent separation membrane is reduced while the recovery of purified water from the salt-containing sewage is achieved, and the method plays an important role in large-scale popularization and application of the technology for recovering the purified water from the treated sewage by adopting the reverse osmosis membrane technology.
Chinese patent document CN1807268 discloses a double-membrane water treatment system and a water treatment method, comprising a pretreatment unit and a desalination unit, wherein a pressure liquid storage tank is arranged in front of the desalination unit after the pretreatment unit, the pretreatment unit provides liquid to the pressure liquid storage tank, the pressure liquid storage tank provides liquid to the desalination unit, and the pressure liquid storage tank also provides backflushing liquid to the pretreatment unit. The method uses the pressure difference generated by the pressure storage of the pressure liquid storage tank and the pressure drop of the pretreatment device of the closed liquid inlet valve branch caused by the opening of the blow-down valve to implement instantaneous pulsation backwashing. CN102942265a discloses an integrated device for whole membrane water treatment, which is sequentially connected with a raw water pump, an ultrafiltration security filter, an ultrafiltration device formed by an ultrafiltration membrane component, an ultrafiltration water tank, a first-stage reverse osmosis high-pressure pump, a reverse osmosis membrane component, a second-stage reverse osmosis high-pressure pump, a second-stage reverse osmosis membrane component, a fresh water tank, an EDI water supply pump and an EDI device to desalted water outlet through pipelines; an ultrafiltration backwash water pump is arranged to be connected with an ultrafiltration membrane component for backwash, and an acid dosing device, an alkali dosing device and a bactericide device are all connected to the ultrafiltration device.
The key point of the method is that the membrane pollution problem cannot be effectively solved in the aspect of backwashing of an ultrafiltration device and a reverse osmosis membrane component.
The sewage treatment method and system adopting the composite pretreatment of ultraviolet, sodium hypochlorite and active carbon to reduce membrane pollution are disclosed in CN 114772814A. This approach can address membrane fouling by organics. But can not solve the problem of pollution of residual coagulant to the subsequent membrane modules caused by too high coagulant addition in order to reduce the influence of turbidity substances on the subsequent membrane modules in the coagulation treatment process.
The existing coagulation technology can only reduce the pollution of granular pollutants and turbidity matters contained in water to the subsequent membrane components, and hardly has the removal effect on dissolved proteins, polysaccharides and other organic matters contained in water, so that the pollution of the two pollutants to the subsequent membrane components cannot be reduced; meanwhile, when the secondary effluent of a sewage treatment plant with low turbidity is treated, the existing coagulation technology needs to achieve better coagulation efficiency in a mode of adding a large amount of coagulant, so that pollution to a subsequent membrane assembly caused by coagulant residues can be caused; meanwhile, the existing coagulation technology cannot solve the problems of subsequent ultrafiltration and microbial contamination of reverse osmosis membranes.
Disclosure of Invention
The invention aims at the problem that a membrane component is easy to be polluted when water is extracted from high-salt sewage by adopting a membrane technology, and provides a method for recycling water from the high-salt sewage by combining reinforced coagulation with membrane separation, which can reduce pollution caused by coagulant residues to the membrane component and improve the removal rate of organic matters in water. A system for implementing the method is also provided.
The invention relates to a method for recovering purified water from high-salt sewage by reinforced coagulation and membrane separation, which comprises the following steps:
(1) Pre-oxidizing with sodium hypochlorite:
adding sodium hypochlorite into the high-salt sewage, and carrying out mixed reaction to obtain pretreated sewage; oxidizing part of soluble organic matters in the sewage into insoluble matters, and reducing the content of protein and polysaccharide matters in the water;
(2) Mixing polyaluminium chloride:
adding polyaluminium chloride into the pretreated sewage, and stirring and mixing uniformly to form polyaluminium chloride mixed solution (solution for uniformly mixing the polyaluminium chloride and water);
(3) Flocculation reaction:
adding a solid phase coagulant aid into the polyaluminium chloride mixed solution, stirring and mixing the mixture, and removing granular substances and most of turbidity substances contained in water to obtain flocculation mixed solution;
(4) Precipitation: precipitating the flocculation mixed solution;
(5) Ultrafiltration membrane filtration:
pressing the supernatant after precipitation into an ultrafiltration membrane, and removing residual turbidity substances and particulate matters in water through filtration interception of the ultrafiltration membrane;
(6) Reverse osmosis separation:
the ultrafiltration effluent after passing through the ultrafiltration membrane is pressurized to enter a reverse osmosis membrane assembly to remove salt.
The adding amount of sodium hypochlorite in the step (1) in the high-salt sewage is 20-30 mg/L, and the reaction time is 5-15 min.
The adding amount of the polyaluminium chloride in the step (2) is 10-20 mg/L, the stirring speed in the step (2) is 400-500 r/min, and the stirring time is 30-60 s.
The adding amount of the solid coagulant aid in the step (3) is 5-10 mg/L, the stirring speed in the step (3) is 40-50 r/min, and the stirring time is 10-15 min.
The solid coagulant aid in the step (3) is MnO 2 The weight ratio of the modified diatomite to the powdered activated carbon is 3:1.MnO (MnO) 2 The preparation process of the modified diatomite comprises the following steps:
(1) adding sodium hydroxide into water according to the proportion of 20-25 g of sodium hydroxide, 100m of water and 10-20 g of diatomite to prepare sodium hydroxide solution (the concentration is 5-6.25 mol/L), adding diatomite, and placing the mixture in a water bath at 80 ℃ to react for 2-3 hours to prepare diatomite mixed solution;
(2) according to 49.5 g MnCl 2 ·4H 2 Ratio of O to 100mL Water MnCl 2 ·4H 2 O is dissolved in water, and the pH of the solution is adjusted to 1-2 by dilute HCl to prepare MnCl 2 A solution;
(3) then MnCl is added 2 Adding the solution into diatomite mixed solution, and stirring at room temperature for reaction for 10-15 hours;
(4) filtering to remove water in the reaction system, adding diatomite obtained by filtering into the sodium hydroxide solution prepared according to the step (1) to soak for 12-18 hours, and filtering alkali liquor;
(5) after 24 hours of standing in air, the kieselguhr was washed with water until the pH became neutral, and dried in a drying oven at 105 ℃.
The precipitation time in the step (4) is 20-30 min.
The ultrafiltration membrane in the step (5) has a membrane aperture of 0.01-0.1 mu m and a membrane flux of 50-80L/m 2 H; and (3) pressurizing in the step (5) to 100-500 kPa.
The membrane flux of reverse osmosis in the step (6) is 15-25L/m 2 H; and (3) pressurizing in the step (6) to a pressure of 800-1200 kPa.
The method strengthens coagulation by pre-oxidizing and adding the reinforcing phase coagulant aid to reduce the adding amount of the coagulant, thereby achieving the purposes of reducing pollution of the coagulant residue to the membrane assembly and improving the removal rate of organic matters in water.
The reinforced coagulation combined membrane separation realizing the method is used for recovering the water purification system from the high-salt sewage, and the following technical scheme is adopted:
the system comprises a sodium hypochlorite feeding device, a pre-oxidation tank, a polyaluminium chloride feeding device, a mixing tank, a solid-phase coagulant aid feeding device, a flocculation reaction tank, a settling tank, an intermediate water tank, an ultrafiltration membrane component and a reverse osmosis membrane component; the pre-oxidation tank, the mixing tank, the flocculation reaction tank, the sedimentation tank and the middle water tank are sequentially connected through pipelines, the middle water tank is connected with the ultrafiltration membrane component through a primary booster pump, and a water outlet of the ultrafiltration membrane component is connected with a water inlet of the reverse osmosis membrane component through a secondary booster pump; the sodium hypochlorite feeding device is connected with the pre-oxidation tank, the polyaluminum chloride feeding device is connected with the mixing tank, and the solid-phase coagulant aid feeding device is connected with the flocculation reaction tank; the mixing tank and the flocculation reaction tank are both internally provided with stirrers.
The sodium hypochlorite adding device comprises a sodium hypochlorite adding tank, a sodium hypochlorite adding pipe and a sodium chlorate adding pump, wherein the sodium chlorate adding tank is connected with the lower part of the pre-oxidation pond through the sodium hypochlorite adding pipe, and the sodium hypochlorite adding pump is arranged on the sodium hypochlorite adding pipe.
The polyaluminum chloride feeding device comprises a polyaluminum chloride feeding tank, a feeding pipe and a feeding pump, wherein the polyaluminum chloride feeding tank is connected with the lower part of the mixing tank through the feeding pipe, and the feeding pump is arranged on the feeding pipe.
The solid-phase coagulant aid adding device comprises a solid-phase coagulant aid storage tank, a vibration doser and an adding pipe, wherein the solid-phase coagulant aid storage tank is connected with the flocculation reaction tank through the adding pipe, and the vibration doser is arranged at the lower part of the solid-phase coagulant aid storage tank.
A folded plate is arranged in the pre-oxidation tank.
The bottom of flocculation reaction pond is provided with the blow-down pipe, sets up the blow-down valve on the blow-down pipe.
The bottom of the precipitation tank is provided with a mud discharging pipe, and the mud discharging pipe is provided with a mud discharging valve.
The secondary effluent of the sewage treatment plant is conveyed into a pre-oxidation tank through a water inlet pump, and sodium hypochlorite is pumped from a sodium hypochlorite feeding tank by a sodium hypochlorite feeding pump and is conveyed into the pre-oxidation tank for a first reaction. And (3) fully mixing and reacting the secondary effluent entering the pre-oxidation tank and sodium hypochlorite in the flowing process of gaps among the folded plates, decomposing protein and polysaccharide substances contained in the secondary effluent, and simultaneously converting part of soluble organic matters into insoluble matters. The secondary effluent flows into a mixing tank after sodium hypochlorite pre-oxidation treatment, meanwhile, polyaluminum chloride solution is quantitatively extracted from a polyaluminum chloride adding tank through a polyaluminum chloride adding pump and added into the mixing tank, the polyaluminum chloride is fully dissolved into the secondary effluent under the stirring action in the mixing tank, and the residence time of water in the mixing tank is 30-60 s, so that uniform solution (polyaluminum chloride mixed solution) is formed. Then flows into a flocculation reaction tank, the solid-phase coagulant aid compounded by modified diatomite and powdered activated carbon according to the proportion of 3:1 is quantitatively added into the flocculation reaction tank by a solid-phase coagulant aid adding device, the residence time of water in the flocculation reaction tank is 10-15 min, and secondary effluent, polyaluminium chloride and the solid-phase coagulant aid are uniformly mixed under the stirring action and gradually form large flocs, so that flocculation mixed liquid is obtained. The flocculation mixed liquor with large flocs flows into the settling tank, the flocs are deposited at the bottom of the settling tank, the supernatant flows into the middle water tank, and the sludge deposited at the bottom of the settling tank is periodically discharged out of the settling tank through the bottom sludge discharge valve. And pumping water from the middle water tank by adopting a first-stage booster pump and pressurizing the water into the ultrafiltration membrane component. The ultrafiltration produced water enters a reverse osmosis membrane assembly after being pressurized by a secondary booster pump, water molecules in the reverse osmosis membrane assembly can permeate the membrane to form fresh water, most pollutants and salt ions contained in the water are difficult to permeate the membrane and are still trapped at the water inlet end of the membrane, and the produced water permeated through the membrane is the purified water recovered from sewage by the technology of the invention.
The invention combines the reinforced coagulation technology and the ultrafiltration/reverse osmosis membrane technology to form a set of high-efficiency method for obtaining purified water from secondary effluent of sewage treatment plants containing higher salt. Compared with other methods, the method can obtain purified water similar to the water quality of tap water, and meanwhile, the system is more stable, the maintenance is simpler and more convenient, and the service time is longer.
The invention has the following characteristics:
1. the pre-oxidation process adopts sodium hypochlorite as an oxidant, so that the operation is simpler and more convenient, and the following effects are generated: (1) The protein and polysaccharide substances in the water can be oxidized into small molecular substances which are not easy to cause membrane pollution, and the content of the protein and polysaccharide substances in the water is reduced, so that the pollution of a subsequent reverse osmosis membrane caused by the protein and polysaccharide substances is reduced; (2) The method has the advantages that part of macromolecular substances in the water are converted into small molecular substances, so that the pollution of the ultrafiltration membrane can be reduced, the small molecular substances are not easy to deposit on the reverse osmosis membrane, and the pollution of the reverse osmosis membrane can be reduced; (3) Bacteria in water can be killed, and subsequent biological pollution of the ultrafiltration membrane and the reverse osmosis membrane is avoided; (4) Can convert part of soluble substances in water into insoluble substances to be separated out, improves the effect of subsequent coagulation treatment, and is beneficial to the subsequent coagulation sedimentation process.
2. The solid-phase coagulant aid is adopted to strengthen the coagulation, so that the probability of particle collision in the coagulation process can be improved, and the solid-phase coagulant aid is adopted to strengthen the coagulation for the secondary effluent with lower turbidity, so that the coagulation efficiency can be improved.
3. The solid coagulant aid is prepared from MnO 2 The modified diatomite and the powdered activated carbon are compounded to obtain the two-phase coagulant aid, the solid coagulant aid can strengthen the coagulation effect, and meanwhile, the adsorption capacity can be exerted to adsorb and remove part of organic substances contained in water, so that the pollution influence of the organic substances on a subsequent membrane module is reduced.
4. The coagulation effect of the polyaluminum chloride is enhanced by adding the solid-phase coagulant aid into the flocculation reaction tank, and the addition amount of the coagulant can be reduced by the enhanced coagulation effect of the solid-phase coagulant aid, so that the residue of aluminum salt is reduced, and the pollution of a subsequent reverse osmosis membrane caused by the residue of the aluminum salt is reduced.
Drawings
FIG. 1 is a schematic diagram of the structural principle of the water purification system for recovering high-salt sewage from the high-salt sewage by combining reinforced coagulation with membrane separation.
In the figure: 1. sodium hypochlorite feeding tank, sodium hypochlorite feeding pump, 3, pre-oxidation tank, 4, mixing tank, 5, flocculation reaction tank, 6, polyaluminum chloride feeding tank, 7, polyaluminum chloride feeding pump, 8, solid-phase coagulant aid storage tank, 9, vibration medicine feeder, 10, settling tank, 11, intermediate water tank, 12, primary pressure pump, 13, ultrafiltration membrane component, 14, secondary pressure pump, 15, reverse osmosis membrane component, 16, blow-down valve, 17, mud discharging valve, 18, folded plate, 19, stirrer, 20, stirrer, 21, stirrer, 22, sodium hypochlorite feeding pipe, 23, water inlet pipe, 24, water outlet pipe, 25, polyaluminum chloride feeding pipe, 26, pipeline, 27.
Detailed Description
In order to solve the problem that the existing pre-membrane coagulation pretreatment technology cannot effectively reduce the pollution of residual coagulant to a subsequent membrane and the problem that the coagulation pretreatment cannot effectively reduce the pollution of organic matters and microorganisms in water to the subsequent membrane, the invention improves the efficiency of the coagulation treatment by adding an oxidant before the coagulation treatment and adding a reinforcing phase coagulant aid in the coagulation process, so that the same coagulation effect is achieved, the amount of the coagulant added in the coagulation process is reduced, the residual amount of the coagulant is further reduced, and the pollution influence of excessive coagulant residues to the subsequent membrane is avoided. Meanwhile, the invention can also reduce membrane pollution caused by organic matters and microorganisms in water.
As shown in fig. 1, the reinforced coagulation combined membrane separation water purification system used in the invention comprises a sodium hypochlorite feeding tank 1, a sodium hypochlorite feeding pump 2, a pre-oxidation tank 3, a mixing tank 4, a flocculation reaction tank 5, a polyaluminum chloride feeding tank 6, a polyaluminum chloride feeding pump 7, a solid-phase coagulant aid storage tank 8, a vibration doser 9, a precipitation tank 10, an intermediate water tank 11, a primary booster pump 12, an ultrafiltration membrane component 13, a secondary booster pump 14 and a reverse osmosis membrane component 15. The pre-oxidation tank 3, the mixing tank 4, the flocculation reaction tank 5, the sedimentation tank 10, the middle water tank 11, the primary booster pump 12, the ultrafiltration membrane component 13, the secondary booster pump 14 and the reverse osmosis membrane component 15 are connected through pipelines in sequence.
The lower part of the pre-oxidation tank 3 is provided with a water inlet pipe 23 and a sodium hypochlorite adding pipe 22, the upper part is provided with a water outlet pipe 24, the water outlet pipe 24 is connected with the water inlet of the mixing tank 4, and a folded plate 18 which is vertically arranged is arranged in the pre-oxidation tank 3. The sodium hypochlorite adding pipe 22 is connected with the sodium hypochlorite adding tank 1 through the sodium hypochlorite adding pump 2, and the sodium hypochlorite adding pipe 22, the sodium hypochlorite adding pump 2 and the sodium hypochlorite adding tank 1 form a sodium hypochlorite adding device. Sodium hypochlorite liquid is contained in the sodium hypochlorite adding tank 1, and sodium hypochlorite is conveyed into the pre-oxidation tank 3 through the sodium hypochlorite adding pump 2.
The upper outlet of the mixing tank 4 is connected with the inlet of the flocculation reaction tank 5 through a pipeline, and a stirrer 20 is arranged in the mixing tank 4. The upper part of the mixing tank 4 is connected with a polyaluminum chloride feeding device. The polyaluminum chloride feeding device comprises a polyaluminum chloride feeding tank 6, a polyaluminum chloride feeding pipe 25 and a polyaluminum chloride feeding pump 7, wherein the polyaluminum chloride feeding tank 6 is connected with the mixing tank 4 through the polyaluminum chloride feeding pipe 25, and the polyaluminum chloride feeding pump 7 is arranged on the polyaluminum chloride feeding pipe 25. The polyaluminum chloride adding tank 6 is internally provided with a stirrer 19, and the polyaluminum chloride is uniformly stirred with water in the adding tank 6 through the stirrer 19 to form polyaluminum chloride water liquid (the concentration of the polyaluminum chloride is 1% -3%). Is conveyed into the mixing tank 4 by a polyaluminum chloride feeding pipe 25 through a polyaluminum chloride feeding pump 7.
The outlet of the upper part of the flocculation reaction tank 5 is connected with the inlet of the sedimentation tank 10 through a pipeline 26, a stirrer 21 is arranged in the flocculation reaction tank 5, a blow-down pipe is arranged at the bottom of the flocculation reaction tank 5, and a blow-down valve 16 is arranged on the blow-down pipe. The upper part of the flocculation reaction tank 5 is connected with a solid-phase coagulant aid adding device. The solid-phase coagulant aid adding device comprises a solid-phase coagulant aid storage tank 8 and a solid-phase coagulant aid adding pipe 27, wherein a vibration medicine feeder 9 is arranged at the lower part of the solid-phase coagulant aid storage tank 8, the solid-phase coagulant aid storage tank 8 is connected with the flocculation reaction tank 5 through the solid-phase coagulant aid adding pipe 27, and the solid-phase coagulant aid storage tank 8 and the vibration medicine feeder 9 are positioned above the flocculation reaction tank 5. MnO is contained in a solid-phase coagulant aid storage tank 8 2 The modified diatomite and the powdered activated carbon are compounded according to a ratio of 3:1 to form the compound coagulant aid. The solid coagulant aid stored in the solid coagulant aid storage tank 8 is added into the flocculation reaction tank 5 through the vibration doser 9.
MnO 2 The preparation process of the modified diatomite comprises the following steps:
adding 20-25 g of hydrogen oxide into a 1L beakerAdding sodium, adding water to 100mL to prepare 5-6.25 mol/L sodium hydroxide solution, adding 10-20 g of diatomite into the solution, and placing the solution in a water bath at 80 ℃ to react for 2-3 h. 49.5 g of MnCl is taken 2 ·4H 2 O was dissolved in 100mL of water and the pH of the solution was adjusted to between 1 and 2 with dilute HCl. Then MnCl is added 2 The solution is added into the diatomite mixed solution and stirred at room temperature for reaction for 10 to 15 hours. Filtering to remove water in the reaction system, adding the diatomite obtained by filtering into 100mL of 5-6.25 mol/L sodium hydroxide solution, soaking for 12-18 h, filtering alkali liquor, standing in air for 24h, washing the diatomite with water until the pH is neutral, drying in a drying oven at 105 ℃, and storing for later use.
MnO 2 The dosage of the modified diatomite is prepared according to the above process and proportion.
The bottom of the precipitation tank 10 is provided with a mud discharging pipe, and the mud discharging pipe is provided with a mud discharging valve 17. The water outlet of the precipitation tank 10 is connected with the water inlet of the middle water tank 11 through a pipeline. The water outlet of the middle water tank 11 is connected with the inlet of the ultrafiltration membrane component 13 through the primary booster pump 12. The outlet of the ultrafiltration membrane component 13 is connected with the water inlet of the reverse osmosis membrane component 15 through a pipeline by a secondary booster pump 14.
The operation of the above system is as follows.
1. Pre-oxidation
Secondary effluent of the sewage treatment plant enters the pre-oxidation tank 3 through a water inlet pipe 23 arranged at the bottom of the pre-oxidation tank 3. Simultaneously, sodium hypochlorite liquid stored in the sodium hypochlorite adding tank 1 is added into the pre-oxidation tank 3 through the sodium hypochlorite adding pump 2, and the adding amount of sodium hypochlorite is 20-30 mg/L. The secondary effluent of the sewage treatment plant and sodium hypochlorite are mixed and then flow in a turbulent flow state in gaps among folded plates 18 in the pre-oxidation tank 3, so that the reaction of the sodium hypochlorite and organic matters in the inflow water is promoted. The retention time of the water flow in the pre-oxidation tank 3 is 5-15 min.
2. Mixing
The secondary effluent after pre-oxidation enters the mixing tank 4 through the water outlet pipe 24, and meanwhile, the polyaluminum chloride stored in the polyaluminum chloride feeding tank 6 is quantitatively fed into the mixing tank 4 through the polyaluminum chloride feeding pump 7. The polyaluminum chloride is added in the form of aqueous solution, the polyaluminum chloride and water are mixed into the polyaluminum chloride aqueous solution in a polyaluminum chloride adding tank 6 through a stirrer 19, and the concentration of the polyaluminum chloride is 1% -3%. The concentration of the polyaluminum chloride added into the mixing tank 4 is 10-20 mg/L. The water is stirred in the mixing tank 4 by the stirrer 20 at a rotating speed of 400-500 r/min, and the residence time of the water in the mixing tank 4 is 30-60 s.
3. Flocculation reaction
The mixed water enters the flocculation reaction tank 5 through a connecting pipeline. Meanwhile, the modified diatomite and the powdered activated carbon compound coagulant aid in the solid coagulant aid storage tank 8 are added into the flocculation reaction tank 5 through the vibration doser 9. In the flocculation reaction tank 5, the added solid coagulant aid is mixed with water by stirring by the stirrer 21 to react with the water to form large flocs. In this step, the amount of the solid coagulant aid added to the flocculation reaction tank 5 is 5 to 10mg/L, the stirring speed of the stirrer 21 is 40 to 50r/min, and the residence time of water in the reaction tank 5 is 10 to 15min.
4. Precipitation
The flocs formed during the flocculation reaction stage flow together with the water through conduit 26 into settling tank 10 where they settle to form sludge at the bottom. The sludge settled at the bottom is periodically discharged from the settling tank 10 through the sludge discharge valve 17. The residence time of the water in the precipitation tank is 20-30 min. The supernatant after precipitation enters the intermediate water tank 11.
5. Ultrafiltration membrane filtration process
The effluent (supernatant) of the settling tank 10 flows into the intermediate tank 11 through a connecting pipe. The primary booster pump 12 pumps water from the intermediate water tank 11 and pressurizes the water, and then sends the water to the ultrafiltration membrane module 13. The outlet pressure of the primary booster pump 11 is 100 to 500kPa. In the ultrafiltration membrane separation process, water molecules and dissolved substances contained in the water can permeate the membrane and enter the other side of the membrane to form produced water, particles and colloid contained in the water can not permeate the membrane, and the membrane is trapped on one side of the inlet water and is subjected to filtration trapping effect of the ultrafiltration membrane component 13, so that the particles in the water are trapped and removed. The ultrafiltration membrane adopts a hollow fiber membrane, the pore diameter of the membrane is 0.01-0.1 mu m, and the flux of the membrane is 50-80L/m 2 H, return of ultrafiltration membraneThe yield is 90-95%.
6. Reverse osmosis separation process
The ultrafiltration effluent enters a reverse osmosis membrane assembly 15 after being pressurized by a secondary pressurizing pump 14. Under the action of pressure, water molecules can penetrate through the reverse osmosis membrane to enter the other side of the reverse osmosis membrane, and colloid, particles, microorganisms and most organic matters and inorganic salts contained in the water cannot penetrate through the membrane and are trapped on the water inlet side of the reverse osmosis membrane. Under the interception effect of the reverse osmosis membrane component 15, most organic matters and inorganic ions in the secondary effluent are intercepted, and water molecules permeate the membrane to become purified water. The outlet pressure of the secondary booster pump 14 is 800 kPa-1200 kPa, and the membrane flux of the reverse osmosis membrane is 15-25L/m 2 H, the recovery rate is 70-75%.
Specific examples are given below.
The secondary effluent of an actual municipal sewage treatment plant with the conductivity of 8200 mu m/cm is taken as a treatment target, and the relevant parameters are as follows:
the adding amount of sodium hypochlorite is 20mg/L in the preoxidation process, and the reaction time is 5min.
The adding amount of the polyaluminium chloride is 10mg/L during mixing, the rotating speed of the stirrer is 400r/min, and the mixing time is 30s.
The addition amount of the solid-phase coagulant aid is 5mg/L during flocculation reaction, the rotating speed of the stirrer is 50r/min, and the flocculation reaction time is 10min.
The sedimentation time was 20min.
The outlet pressure of the primary pressurizing pump before ultrafiltration is 200kPa, and the membrane flux is 50L/m 2 ·h。
The outlet pressure of the second-stage pressurizing pump before reverse osmosis is 1000kPa, and the membrane flux of the reverse osmosis membrane is 20L/m 2 ·h。
Treatment results:
when sodium hypochlorite is added for pre-oxidation to strengthen coagulation, compared with the pure coagulation treatment without sodium hypochlorite for pre-oxidation, turbidity, protein, polysaccharide and UV 254 And DOC removal rates may be increased by 30%, 43%, 35%, 40% and 40%, respectively.
After the solid phase coagulant aid is added, the turbidity removal rate can reach 80.3 percent, which is improved by 32.7 percent compared with the turbidity removal rate when only the polyaluminium chloride coagulant is added; when only polyaluminium chloride is added, but not the reinforcing phase coagulant aid, the polyaluminium chloride with the turbidity removal rate of more than 80% is required to be added. Therefore, the addition of the solid phase coagulant aid can reduce the addition amount of the polyaluminium chloride and reduce the concentration of residual aluminum ions in water by more than 40 percent. And after the solid phase coagulant aid is added, the TOC removal rate can be improved by more than 40%.
Compared with the coagulation by using the polyaluminium chloride as the coagulant, the method of the invention has the advantages that the decrease of the water production rate of the reverse osmosis membrane is smaller along with the extension of the operation time after the pretreatment, and the water production rate of the reverse osmosis membrane can be more than one time when the polyaluminium chloride coagulant is only added after the pretreatment method of the invention is adopted after the operation for 35 hours, thus the method of the invention effectively relieves the pollution of the reverse osmosis membrane.
Claims (10)
1. A method for recovering purified water from high-salt sewage by reinforced coagulation combined with membrane separation, which is characterized by comprising the following steps:
(1) Pre-oxidizing with sodium hypochlorite:
adding sodium hypochlorite into the high-salt sewage, and carrying out mixed reaction to obtain pretreated sewage; oxidizing part of soluble organic matters in the sewage into insoluble matters, and reducing the content of protein and polysaccharide matters in the water;
(2) Mixing polyaluminium chloride:
adding polyaluminium chloride into the pretreated sewage, and uniformly stirring and mixing to form polyaluminium chloride mixed solution;
(3) Flocculation reaction:
adding a solid phase coagulant aid into the polyaluminium chloride mixed solution, stirring and mixing the mixture, and removing granular substances and most of turbidity substances contained in water to obtain flocculation mixed solution;
(4) Precipitation: precipitating the flocculation mixed solution;
(5) Ultrafiltration membrane filtration:
pressing the supernatant after precipitation into an ultrafiltration membrane, and removing residual turbidity substances and particulate matters in water through filtration interception of the ultrafiltration membrane;
(6) Reverse osmosis separation:
the ultrafiltration effluent after passing through the ultrafiltration membrane is pressurized to enter a reverse osmosis membrane assembly to remove salt.
2. The method for recovering purified water from high-salt wastewater by reinforced coagulation-membrane separation according to claim 1, wherein the adding amount of sodium hypochlorite in the step (1) in the high-salt wastewater is 20-30 mg/L, and the reaction time is 5-15 min.
3. The method for recovering purified water from high-salt wastewater by reinforced coagulation-membrane separation according to claim 1, wherein the adding amount of polyaluminum chloride in the step (2) is 10-20 mg/L, the stirring speed in the step (2) is 400-500 r/min, and the stirring time is 30-60 s.
4. The method for recovering purified water from high-salt wastewater by reinforced coagulation-membrane separation according to claim 1, wherein the solid coagulant aid in the step (3) is added in an amount of 5-10 mg/L, the stirring speed in the step (3) is 40-50 r/min, and the stirring time is 10-15 min.
5. The method for recovering purified water from high-salt wastewater by reinforced coagulation-membrane separation according to claim 1, wherein the solid coagulant aid in the step (3) is MnO 2 The weight ratio of the modified diatomite to the powdered activated carbon is 3:1;
the MnO 2 The preparation process of the modified diatomite comprises the following steps:
(1) adding sodium hydroxide into water according to the proportion of 20-25 g of sodium hydroxide, 100m of water and 10-20 g of diatomite to prepare sodium hydroxide solution, adding diatomite, and placing the mixture in a water bath at 80 ℃ to react for 2-3 hours to prepare diatomite mixed solution;
(2) according to 49.5 g MnCl 2 ·4H 2 Ratio of O to 100mL Water MnCl 2 ·4H 2 O is dissolved in water, and the pH of the solution is adjusted to 1-2 by dilute HCl to prepare MnCl 2 A solution;
(3) then MnCl is added 2 Adding the solution into diatomite mixed solution, and stirring at room temperature for reaction for 10-15 hours;
(4) filtering to remove water in the reaction system, adding diatomite obtained by filtering into the sodium hydroxide solution prepared according to the step (1) to soak for 12-18 hours, and filtering alkali liquor;
(5) after 24 hours of standing in air, the kieselguhr was washed with water until the pH became neutral, and dried in a drying oven at 105 ℃.
6. The method for recovering purified water from high-salt wastewater by reinforced coagulation-combined membrane separation according to claim 1, wherein the ultrafiltration membrane in the step (5) has a membrane pore size of 0.01 to 0.1 μm and a membrane flux of 50 to 80L/m 2 H; and (3) pressurizing in the step (5) to 100-500 kPa.
7. The method for recovering purified water from high-salt wastewater by reinforced coagulation-combined membrane separation according to claim 1, wherein the membrane flux of reverse osmosis in the step (6) is 15 to 25L/m 2 H; and (3) pressurizing in the step (6) to a pressure of 800-1200 kPa.
8. The water purification system is characterized by comprising a sodium hypochlorite feeding device, a pre-oxidation tank, a polyaluminium chloride feeding device, a mixing tank, a solid-phase coagulant aid feeding device, a flocculation reaction tank, a precipitation tank, an intermediate water tank, an ultrafiltration membrane component and a reverse osmosis membrane component; the pre-oxidation tank, the mixing tank, the flocculation reaction tank, the sedimentation tank and the middle water tank are sequentially connected through pipelines, the middle water tank is connected with the ultrafiltration membrane component through a primary booster pump, and a water outlet of the ultrafiltration membrane component is connected with a water inlet of the reverse osmosis membrane component through a secondary booster pump; the sodium hypochlorite feeding device is connected with the pre-oxidation tank, the polyaluminum chloride feeding device is connected with the mixing tank, and the solid-phase coagulant aid feeding device is connected with the flocculation reaction tank; the mixing tank and the flocculation reaction tank are both internally provided with stirrers.
9. The reinforced coagulation combined membrane separation water purification system for recovering high-salt sewage from high-salt sewage according to claim 8, wherein the sodium hypochlorite adding device comprises a sodium hypochlorite adding tank, a sodium hypochlorite adding pipe and a sodium chlorate adding pump, wherein the sodium chlorate adding tank is connected with the lower part of the pre-oxidation tank through the sodium hypochlorite adding pipe, and the sodium hypochlorite adding pump is arranged on the sodium hypochlorite adding pipe;
the polyaluminum chloride feeding device comprises a polyaluminum chloride feeding tank, a feeding pipe and a feeding pump, wherein the polyaluminum chloride feeding tank is connected with the lower part of the mixing tank through the feeding pipe, and the feeding pump is arranged on the feeding pipe;
the solid-phase coagulant aid adding device comprises a solid-phase coagulant aid storage tank, a vibration doser and an adding pipe, wherein the solid-phase coagulant aid storage tank is connected with the flocculation reaction tank through the adding pipe, and the vibration doser is arranged at the lower part of the solid-phase coagulant aid storage tank.
10. The reinforced coagulation-based membrane separation system for recovering water from high-salt wastewater as recited in claim 8, wherein flaps are provided in the pre-oxidation tank;
the bottom of the flocculation reaction tank is provided with a blow-down pipe, and a blow-down valve is arranged on the blow-down pipe; the bottom of the precipitation tank is provided with a mud discharging pipe, and the mud discharging pipe is provided with a mud discharging valve.
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