CN221440540U - Fluoride industry effluent disposal system - Google Patents
Fluoride industry effluent disposal system Download PDFInfo
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- CN221440540U CN221440540U CN202323243003.1U CN202323243003U CN221440540U CN 221440540 U CN221440540 U CN 221440540U CN 202323243003 U CN202323243003 U CN 202323243003U CN 221440540 U CN221440540 U CN 221440540U
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- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 title claims abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 179
- 238000006115 defluorination reaction Methods 0.000 claims abstract description 37
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 37
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 34
- 239000011347 resin Substances 0.000 claims abstract description 27
- 229920005989 resin Polymers 0.000 claims abstract description 27
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 22
- 238000001728 nano-filtration Methods 0.000 claims abstract description 21
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 18
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- 238000005352 clarification Methods 0.000 claims abstract description 11
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 15
- 238000000034 method Methods 0.000 claims description 13
- 238000004064 recycling Methods 0.000 claims description 13
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 8
- 239000010842 industrial wastewater Substances 0.000 claims description 8
- -1 caCl 2 Chemical compound 0.000 claims description 5
- WDIHJSXYQDMJHN-UHFFFAOYSA-L barium chloride Chemical compound [Cl-].[Cl-].[Ba+2] WDIHJSXYQDMJHN-UHFFFAOYSA-L 0.000 claims description 4
- 229910001626 barium chloride Inorganic materials 0.000 claims description 4
- 230000008569 process Effects 0.000 claims description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 4
- 239000002351 wastewater Substances 0.000 abstract description 27
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 abstract description 4
- 239000006227 byproduct Substances 0.000 abstract description 3
- 239000003344 environmental pollutant Substances 0.000 abstract description 2
- 231100000719 pollutant Toxicity 0.000 abstract description 2
- 239000011780 sodium chloride Substances 0.000 abstract 1
- 239000012528 membrane Substances 0.000 description 20
- 150000003839 salts Chemical class 0.000 description 15
- 150000002500 ions Chemical class 0.000 description 14
- 239000011575 calcium Substances 0.000 description 9
- 239000011777 magnesium Substances 0.000 description 9
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 7
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 7
- 229910052791 calcium Inorganic materials 0.000 description 7
- 229910052749 magnesium Inorganic materials 0.000 description 7
- 238000000926 separation method Methods 0.000 description 7
- 239000003153 chemical reaction reagent Substances 0.000 description 6
- 238000004140 cleaning Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 5
- 238000001704 evaporation Methods 0.000 description 5
- 230000008020 evaporation Effects 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 239000010703 silicon Substances 0.000 description 5
- 229910052710 silicon Inorganic materials 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 238000005342 ion exchange Methods 0.000 description 4
- 239000010802 sludge Substances 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 238000005189 flocculation Methods 0.000 description 3
- 230000016615 flocculation Effects 0.000 description 3
- 229910052731 fluorine Inorganic materials 0.000 description 3
- 239000011737 fluorine Substances 0.000 description 3
- 229910017053 inorganic salt Inorganic materials 0.000 description 3
- 239000012466 permeate Substances 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 238000004062 sedimentation Methods 0.000 description 3
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- 238000011001 backwashing Methods 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000012459 cleaning agent Substances 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 239000013049 sediment Substances 0.000 description 2
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 239000006004 Quartz sand Substances 0.000 description 1
- 238000005411 Van der Waals force Methods 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 229940037003 alum Drugs 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000001110 calcium chloride Substances 0.000 description 1
- 229910001628 calcium chloride Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000012510 hollow fiber Substances 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000000053 physical method Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011268 retreatment Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model discloses a fluoride waste water treatment system, which comprises a water inlet tank, a defluorination and hardness removal reaction tank, a clarification tank, a lifting tank, a multi-medium filter, an activated carbon filter, a resin softener, an ultrafiltration filter, a reverse osmosis filter, a defluorination and hardness removal-MCR tank, a nanofiltration filter, a DTRO filter, an evaporator and a condenser, wherein the fluoride waste water is treated by the system, so that the fluoride waste water is effectively treated, the waste water is reused in a workshop, and meanwhile, sodium chloride is a byproduct, so that no pollutant is discharged.
Description
Technical Field
The utility model relates to the technical field of chemical wastewater treatment, in particular to a fluoride wastewater treatment system.
Background
In the field of fluoride industry, industrial wastewater contains fluorine, chlorine, sulfate radical and other ions, and the TDS concentration of the wastewater is high. The wastewater discharge standard has definite limit requirements on fluoride ion indexes, and the current defluorination method comprises a physical method and a chemical method, wherein inorganic salt can be introduced in the chemical defluorination method, so that the TDS concentration of the wastewater is increased. Physical defluorination methods include membrane separation and exchange resin methods, which have the problems of concentrated water and reclaimed water treatment. In order to ensure that indexes such as fluoride ions and TDS meet emission requirements, the utility model provides a fluoride wastewater treatment system, which has practical significance.
Disclosure of utility model
In view of the problems existing in the prior art, the utility model aims to provide a fluoride wastewater treatment system, which effectively solves the problem of fluoride wastewater treatment.
The technical scheme of the utility model is as follows:
A fluoride industrial wastewater treatment system comprises a water inlet tank, a defluorination and hardness removal reaction tank, a clarification tank, a lifting tank, a multi-medium filter, an active carbon filter, a resin softener, an ultrafiltration filter, a reverse osmosis filter, a defluorination and hardness removal-MCR tank, a nanofiltration filter, a DTRO filter, an evaporator and a condenser;
the water outlet of the water inlet tank is connected with the water inlet of the defluorination and hardness removal reaction tank through a pipeline, the defluorination and hardness removal reaction tank is communicated with the clarification tank and the lifting tank, the water outlet of the lifting tank is connected with the water inlet of the multi-medium filter through a pipeline, the water outlet of the multi-medium filter is connected with the water inlet of the activated carbon filter, the water outlet of the activated carbon filter is connected with the resin softener through a pipeline, and the water outlet of the resin softener is divided into two paths, wherein one path is: the water outlet of the resin softener is connected with the water inlet of the ultrafiltration filter through a pipeline, the water outlet of the side part of the ultrafiltration filter is divided into two paths, one path is connected with the water inlet of the side part of the reverse osmosis filter, the water outlet of the top of the reverse osmosis filter is connected with the water inlet of the defluorination and hardness removal-MCR pool through a pipeline, the water outlet of the defluorination and hardness removal-MCR pool is connected with the water inlet of the nanofiltration filter through a pipeline, the water outlet of the side part of the nanofiltration filter is connected with the water inlet of the DTRO filter, the water outlet of the side part of the DTRO filter is divided into two paths, one path is connected with the water inlet of the evaporator through a pipeline, and the water outlet of the top of the evaporator is connected with the water inlet of the condenser through a pipeline.
Further, the other path of the water outlet of the resin softener is connected with the water inlet of the water inlet tank through a pipeline.
Further, the other path of the water outlet at the side part of the ultrafiltration filter is connected with the water inlet of the water inlet tank through a pipeline.
Further, the water outlet at the bottom of the ultrafiltration filter is divided into two paths: one path is connected with a water inlet at the top of the reverse osmosis filter through a pipeline.
Further, the water outlet at the side part of the reverse osmosis filter is divided into two paths, one path is connected with the reuse pool through a pipeline, and the other path of the water outlet at the side part of the reverse osmosis filter is connected with the water inlet pool through a pipeline.
Further, the water outlet at the side part of the evaporator and the water outlet at the bottom of the condenser are connected with the recycling pool through pipelines.
Further, a water outlet at the top of the multi-medium filter is connected with a water inlet pool through a pipeline; the water outlet at the bottom of the nanofiltration filter and the water outlet at the bottom of the DTRO filter are respectively connected with the water inlet at the side part of the reverse osmosis filter through pipelines.
Further, the other path of the water outlet at the side part of the DTRO filter is connected with the water inlet tank through a pipeline.
Further, the defluorination and hardness removal reaction tank is provided with a NaOH, caCl 2、Na2CO3、BaCl2, PAC and PAM dosing device.
Compared with the prior art, the utility model has the following beneficial effects:
1) By adopting the technical scheme, fluoride industrial wastewater passes through a defluorination and hardness removal reaction tank and a clarification tank of the system to remove ions such as calcium, magnesium, silicon and sulfate, the wastewater after hardness removal is filtered by adopting a multi-medium filter to remove particulate matters such as SS, the wastewater after filtration of the multi-medium filter is adsorbed by utilizing an activated carbon filter to remove a small amount of organic matters such as COD, the wastewater after adsorption of the activated carbon filter is softened by utilizing a special resin softener, the adsorption and ion exchange of multivalent ions such as calcium and magnesium are realized by an ion exchange technology, the hardness in the wastewater is deeply removed, the effluent after resin softening is subjected to ultrafiltration and reverse osmosis to realize the separation of water and salt, the reverse osmosis concentrated water is treated in a defluorination and hardness removal-MCR tank to remove fluorine, silicon and sulfate, the defluorination and hardness removal-MCR effluent is subjected to salt separation by adopting a nanofiltration filter, the concentration of the nanofiltration produced water is subjected to a concentration of a DTRO filter, so that the ion concentration is increased, the concentrated water is reduced, the produced water returns to reverse osmosis by adopting an evaporator to carry out evaporation crystallization, and sodium chloride salt, and the byproduct fluoride industrial wastewater is effectively treated, and the problems of the conventional method are avoided;
2) The novel resin softener is added before the ultrafiltration filter and the reverse osmosis filter, and the hardness of calcium and magnesium in the wastewater is reduced to below 10ppm through the adsorption selectivity of the resin, so that the fouling and blocking risk of a reverse osmosis membrane system is reduced, the service life of the membrane is prolonged, the cleaning frequency and the usage amount of medicaments are reduced, and the running stability of the system is ensured;
3) According to the utility model, the defluorination and hardness removal-MCR pool is coupled through the process, the defluorination and hardness removal are performed by the traditional chemical method, and simultaneously, small floc particles which cannot be removed by adopting a sedimentation method are intercepted by utilizing the filtering effect of MCR, so that the defluorination and hardness removal effect is greatly improved;
4) According to the utility model, the DTRO filter is adopted to re-concentrate the salt before evaporation, so that the evaporation water quantity can be reduced by more than 65%, and the construction scale of the desalting unit and the ton water disposal cost are greatly reduced.
Drawings
FIG. 1 is a schematic diagram of the overall structure of the present utility model.
In the figure: 1. a water inlet tank; 2. a defluorination and hardness removal reaction tank; 3. a clarification tank; 4. a lifting pool; 5. a multi-media filter; 6. an activated carbon filter; 7. a resin softener; 8. an ultrafiltration filter; 9. a reverse osmosis filter; 10. a defluorination and hardness removal-MCR pool; 11. nanofiltration filters; 12. a DTRO filter; 13. an evaporator; 14. a condenser; 15. and (5) recycling the water in a pool.
Detailed Description
The utility model will be further described with reference to the accompanying drawings, but the scope of protection of the utility model is not limited to the described scope.
Because the fluoride wastewater contains suspended matters, calcium, magnesium, silicon, sulfate radical, chloride radical and the like, the components are complex, and the wastewater can not be discharged up to the standard by adopting a single wastewater treatment mode, the fluoride wastewater treatment system provided by the utility model can ensure that the treated wastewater meets the recycling requirement and the salt is recovered by adopting a process coupling mode.
As shown in FIG. 1, the system of the present utility model comprises a water inlet tank 1, a defluorination and hardness removal reaction tank 2, a clarification tank 3, a lifting tank 4, a multi-media filter 5, an activated carbon filter 6, a resin softener 7, an ultrafiltration filter 8, a reverse osmosis filter 9, a defluorination and hardness removal-MCR tank 10, a nanofiltration filter 11, a DTRO filter 12, an evaporator 13 and a condenser 14.
The water outlet of the water inlet tank 1 is connected with the water inlet of the defluorination and hardness removal reaction tank 2 through a pipeline, the defluorination and hardness removal reaction tank 2 is communicated with the clarification tank 3 and the lifting tank 4, the water outlet of the lifting tank 4 is connected with the water inlet of the multi-medium filter 5 through a pipeline, the water outlet of the multi-medium filter 5 is connected with the water inlet of the activated carbon filter 6, the water outlet of the activated carbon filter 6 is connected with the resin softener 7 through a pipeline, and the water outlet of the resin softener 7 is divided into two paths, wherein one path is: the water outlet of the resin softener 7 is connected with the water inlet of the ultrafiltration filter 8 through a pipeline, the water outlet at the side part of the ultrafiltration filter 8 is divided into two paths, one path is connected with the water inlet at the side part of the reverse osmosis filter 9, the water outlet at the top of the reverse osmosis filter 9 is connected with the water inlet of the defluorination and hardness removal-MCR pool 10 through a pipeline, the water outlet of the defluorination and hardness removal-MCR pool 10 is connected with the water inlet of the nanofiltration filter 11 through a pipeline, the water outlet at the side part of the nanofiltration filter 11 is connected with the water inlet of the DTRO filter 12, the water outlet at the side part of the DTRO filter 12 is divided into two paths, one path is connected with the water inlet of the evaporator 13 through a pipeline, and the water outlet at the top of the evaporator 13 is connected with the water inlet of the condenser 14 through a pipeline.
In the embodiment, the other path of the water outlet of the resin softener 7 is connected with the water inlet of the water inlet tank 1 through a pipeline. The other path of the water outlet at the side part of the ultrafiltration filter 8 is connected with the water inlet of the water inlet tank 1 through a pipeline.
The water outlet at the bottom of the ultrafiltration filter 8 is divided into two paths: one is connected with a water inlet at the top of the reverse osmosis filter 9 through a pipeline, and the other is used for cleaning the membrane system periodically.
The system of the embodiment also comprises a recycling pool 15, wherein the water outlet at the side part of the reverse osmosis filter 9 is divided into two paths, one path is connected with the recycling pool 15 through a pipeline, and the other path of the water outlet at the side part of the reverse osmosis filter 9 is connected with the water inlet pool 1 through a pipeline.
The water outlet at the side of the evaporator 13 and the water outlet at the bottom of the condenser 14 are connected with the recycling pool 15 through pipelines.
The water outlet at the top of the multi-medium filter 5 is connected with the water inlet pool 1 through a pipeline; the water outlet at the bottom of the nanofiltration filter 11 and the water outlet at the bottom of the DTRO filter 12 are respectively connected with the water inlet at the side part of the reverse osmosis filter 9 through pipelines.
The other path of the water outlet on the side part of the DTRO filter 12 is connected with the water inlet tank 1 through a pipeline.
After the wastewater enters the system, removing calcium, magnesium, silicon and sulfate radical plasma by a defluorination and hardness removal reaction tank 2 and a clarification tank 3; removing hardness by adopting a chemical softening method, adding sodium carbonate, calcium chloride, barium chloride, sodium hydroxide and other medicaments, reacting to form calcium carbonate and magnesium hydroxide precipitate for removing calcium and magnesium, and forming BaSO 4 precipitate for removing sulfate radical; adding flocculation reagent to form large alum blossom, and discharging in a sedimentation tank in a sludge form. The suspended matters can be removed simultaneously when the hardness is removed, and the hardness removal rate can reach more than 90 percent.
The defluorination and hardness removal reaction tank 2 is provided with a NaOH, caCl 2、Na2CO3、BaCl2, PAC and PAM dosing device.
Firstly, adding NaOH and CaCl 2 reagent to remove Ca (HCO 3)2 and Mg (HCO 3)2 hardness and F-, then adding Na 2CO3 reagent to form CaCO 3 and MgCO 3 sediment, removing Ca 2- and Mg 2- hardness to make total hardness of waste water less than 200Mg/L, finally adding BaCl 2 reagent to form BaSO 4 sediment, removing SO 4 2- ion, adding PAC and PAM to implement flocculation precipitation, discharging sludge, making effluent of a clarification tank enter a lifting tank 4, and lifting the effluent into a multi-medium filter 5 by a pump.
The wastewater after the hardness removal is filtered by a multi-medium filter 5 to remove particulate matters such as SS, the filtered particulate matters are discharged into a water inlet tank 01 through backwashing, and the filtered wastewater is discharged into an activated carbon filter 6.
Suspended impurities in water are trapped by using a filter material layer such as quartz sand, anthracite and the like in the multi-medium filter 5. The filtering function is mainly to remove suspended impurities in water, in particular to effectively remove suspended flocs which cannot be removed by a precipitation technology.
The wastewater filtered by the multi-medium filter 5 is adsorbed by the activated carbon filter 6 to remove a small amount of organic matters such as COD, and the like, so that the COD of the system is ensured to be less than 60mg/L, and the adsorbed wastewater is discharged into the resin softener 7.
The active carbon with high porosity and large specific surface area is mainly used for physically adsorbing organic impurities in water, and when water flows through the pores of the active carbon, various suspended particles, organic matters and the like are adsorbed in the pores of the active carbon under the action of Van der Waals force, so that the organic matters are effectively removed, and the running condition of the membrane is met.
The wastewater adsorbed by the activated carbon filter 6 is softened by a special resin softener 7, and the adsorption and ion exchange of multivalent ions such as calcium and magnesium are realized by an ion exchange technology, so that the hardness in the wastewater is deeply removed, and the fouling and blocking of a membrane are reduced. Meanwhile, the resin softener 7 is provided with a regeneration agent adding device, acid and alkali are added to the resin softener at regular intervals to regenerate the agent, the regenerated wastewater is discharged into the water inlet tank 1, and softened effluent is discharged into the ultrafiltration filter 8.
The water and salt are separated from the water which is softened by the resin softener 7 by adopting an ultrafiltration filter 8 and a reverse osmosis filter 9, so that the concentration of inorganic salt and the preparation of recycled pure water are achieved, the salt is trapped on the concentrated water side, and the produced clean water is discharged into a recycling pool 15 for recycling.
The ultrafiltration filter 8 is adopted for pretreatment to reduce COD and SS entering reverse osmosis, the reverse osmosis filter 9 is utilized for separating water and inorganic salt, so that the TDS concentration of the concentrated water side of the reverse osmosis membrane reaches more than 3%, and a reverse osmosis membrane combination mode is set according to the water quality requirement of the reuse water.
The reverse osmosis concentrate is treated in the defluorination and hardness removal-MCR tank 10 to remove fluorine, silicon, sulfate, and the like. The membrane system is periodically cleaned by a cleaning agent to ensure the water yield and salt removal rate of the membrane, and the cleaning wastewater is discharged into the water inlet tank 1.
The method comprises the steps of synchronously adding a reagent, enabling sulfate radicals, fluoride ions and silicon dioxide to react with the reagent respectively to form double salts, removing the double salts through flocculation precipitation, clarifying in a sedimentation tank, discharging sludge, enabling clear liquid to pass through MCR, namely, directly placing a membrane in a clear liquid tank, pumping the clear liquid through a self-priming pump under negative pressure, enabling water to permeate the surface of the membrane, pumping the clear liquid from the inner side of a hollow fiber membrane, intercepting pollutants on the surface of the membrane, and removing membrane pollution through periodical air washing, backwashing, pollution discharge, online dosing cleaning and offline chemical enhancement cleaning, so that membrane pollution is eliminated, membrane flux is effectively recovered, normal operation of a system is guaranteed, and the intercepted impurities are discharged through sludge.
The effluent of the defluorination and hardness removal-MCR pool 10 is subjected to salt separation by adopting a nanofiltration filter 11, monovalent ions and divalent ions in the wastewater are separated, and concentrated water is returned to the water inlet pool 1 for retreatment.
Mainly intercepts the remained bivalent sulfate ions in the wastewater on the concentrated water side, and the monovalent ions permeate the membrane, thereby realizing the separation and purification of inorganic salts in the process. The concentrated water containing divalent ions is returned to reverse osmosis.
The nanofiltration filter 11 mainly uses the selective function of a semipermeable membrane to allow only solvent molecules or some low molecular mass solutes or low valence ions to permeate therethrough, and the present project mainly separates monovalent ions and divalent ions. After nanofiltration and salt separation, concentrated water of the nanofiltration filter 11 flows back to the water inlet end of the reverse osmosis filter 9, and nanofiltration product water enters the DTRO filter 12.
The ion concentration is realized by adopting the DTRO filter 12, and the membrane of the DTRO filter 12 has the advantages of pollution resistance, high pressure resistance, high COD resistance, TDS resistance, pollution resistance and scaling resistance, and the TDS concentration can reach more than 10 percent so as to reduce the evaporated water quantity. The water produced by the DTRO filter 12 is discharged into the water inlet end of the reverse osmosis filter 09, and the concentrated water of the DTRO filter 12 enters the evaporator 13 for desalination.
The DTRO filter 12 is periodically cleaned by a cleaning agent to ensure its water production rate and salt removal rate, and the cleaning wastewater is discharged into the water intake tank 1.
Ion concentration is achieved using DTRO filter 12, which aims to increase the concentration of inorganic salts while reducing the amount of water evaporated to reduce operating costs. The concentration of the TDS in the obtained concentrated solution can be increased to more than 10%, and the evaporation water quantity is reduced by more than 65%.
And (3) regulating the pH value of the concentrated water of the DTRO filter 12 to 7-9, carrying out crystallization separation of salt in the evaporator 13, and condensing by-product sodium chloride salt, wherein the evaporation liquid is condensed by circulating water of the condenser 14, and discharging the condensate into the recycling pool 15 for recycling.
Claims (9)
1. The fluoride industrial wastewater treatment system is characterized by comprising a water inlet tank (1), a defluorination and hardness removal reaction tank (2), a clarification tank (3), a lifting tank (4), a multi-medium filter (5), an activated carbon filter (6), a resin softener (7), an ultrafiltration filter (8), a reverse osmosis filter (9), a defluorination and hardness removal-MCR tank (10), a nanofiltration filter (11), a DTRO filter (12), an evaporator (13) and a condenser (14);
The water outlet of the water inlet tank (1) is connected with the water inlet of the defluorination and hardness removal reaction tank (2) through a pipeline, the defluorination and hardness removal reaction tank (2) is communicated with the clarification tank (3) and the lifting tank (4), the water outlet of the lifting tank (4) is connected with the water inlet of the multi-medium filter (5) through a pipeline, the water outlet of the multi-medium filter (5) is connected with the water inlet of the activated carbon filter (6), the water outlet of the activated carbon filter (6) is connected with the resin softener (7) through a pipeline, and the water outlet of the resin softener (7) is divided into two paths, wherein one path is: the water outlet of the resin softener (7) is connected with the water inlet of the ultrafiltration filter (8) through a pipeline, the water outlet of the side part of the ultrafiltration filter (8) is divided into two paths, one path is connected with the water inlet of the side part of the reverse osmosis filter (9), the water outlet of the top of the reverse osmosis filter (9) is connected with the water inlet of the defluorination and hardness removal-MCR pool (10) through a pipeline, the water outlet of the defluorination and hardness removal-MCR pool (10) is connected with the water inlet of the nanofiltration filter (11) through a pipeline, the water outlet of the side part of the nanofiltration filter (11) is connected with the water inlet of the DTRO filter (12), the water outlet of the side part of the DTRO filter (12) is divided into two paths, one path is connected with the water inlet of the evaporator (13) through a pipeline, and the water outlet of the top of the evaporator (13) is connected with the water inlet of the condenser (14) through a pipeline.
2. The fluoride industrial wastewater treatment system according to claim 1, wherein the other path of the water outlet of the resin softener (7) is connected with the water inlet of the water inlet tank (1) through a pipeline.
3. The fluoride wastewater treatment system according to claim 1, wherein the other path of the water outlet at the side part of the ultrafiltration filter (8) is connected with the water inlet of the water inlet tank (1) through a pipeline.
4. A fluorochemical wastewater treatment system according to claim 1 wherein the water outlet at the bottom of said ultrafiltration filter (8) is divided into two paths: one path is connected with a water inlet at the top of the reverse osmosis filter (9) through a pipeline.
5. The fluoride industrial wastewater treatment system according to claim 1, comprising a recycling tank (15), wherein the water outlet at the side part of the reverse osmosis filter (9) is divided into two paths, one path is connected with the recycling tank (15) through a pipeline, and the other path of the water outlet at the side part of the reverse osmosis filter (9) is connected with the water inlet tank (1) through a pipeline.
6. The fluoride process wastewater treatment system of claim 5, wherein the water outlet at the side of the evaporator (13) and the water outlet at the bottom of the condenser (14) are connected with the recycling pool (15) through pipelines.
7. The fluoride industrial wastewater treatment system according to claim 1, wherein the water outlet at the top of the multi-medium filter (5) is connected with the water inlet tank (1) through a pipeline; the water outlet at the bottom of the nanofiltration filter (11) and the water outlet at the bottom of the DTRO filter (12) are respectively connected with the water inlet at the side part of the reverse osmosis filter (9) through pipelines.
8. The fluoride engineering wastewater treatment system according to claim 1, wherein the other path of the water outlet at the side part of the DTRO filter (12) is connected with the water inlet tank (1) through a pipeline.
9. The fluoride wastewater treatment system according to claim 1, wherein the defluorination and hardness removal reaction tank (2) is provided with a NaOH, caCl 2、Na2CO3、BaCl2, PAC and PAM dosing device.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202323243003.1U CN221440540U (en) | 2023-11-30 | 2023-11-30 | Fluoride industry effluent disposal system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202323243003.1U CN221440540U (en) | 2023-11-30 | 2023-11-30 | Fluoride industry effluent disposal system |
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| CN221440540U true CN221440540U (en) | 2024-07-30 |
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| CN202323243003.1U Active CN221440540U (en) | 2023-11-30 | 2023-11-30 | Fluoride industry effluent disposal system |
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