CN221071273U - Advanced treatment system for high-salt wastewater - Google Patents
Advanced treatment system for high-salt wastewater Download PDFInfo
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- CN221071273U CN221071273U CN202322862318.8U CN202322862318U CN221071273U CN 221071273 U CN221071273 U CN 221071273U CN 202322862318 U CN202322862318 U CN 202322862318U CN 221071273 U CN221071273 U CN 221071273U
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- reverse osmosis
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- 239000002351 wastewater Substances 0.000 title claims abstract description 60
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 88
- 238000001704 evaporation Methods 0.000 claims abstract description 58
- 230000008020 evaporation Effects 0.000 claims abstract description 56
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 48
- 238000001728 nano-filtration Methods 0.000 claims abstract description 47
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 46
- 238000006243 chemical reaction Methods 0.000 claims abstract description 45
- 229920005989 resin Polymers 0.000 claims abstract description 33
- 239000011347 resin Substances 0.000 claims abstract description 33
- 230000003647 oxidation Effects 0.000 claims abstract description 31
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 31
- 238000001471 micro-filtration Methods 0.000 claims abstract description 26
- 239000011737 fluorine Substances 0.000 claims abstract description 25
- 229910052731 fluorine Inorganic materials 0.000 claims abstract description 25
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 24
- 239000011780 sodium chloride Substances 0.000 claims abstract description 22
- 229910052938 sodium sulfate Inorganic materials 0.000 claims abstract description 22
- 235000011152 sodium sulphate Nutrition 0.000 claims abstract description 22
- 238000001914 filtration Methods 0.000 claims abstract description 19
- 230000001105 regulatory effect Effects 0.000 claims abstract description 12
- 238000005352 clarification Methods 0.000 claims abstract description 11
- 239000012528 membrane Substances 0.000 claims description 21
- 150000003839 salts Chemical class 0.000 claims description 21
- 239000010703 silicon Substances 0.000 claims description 21
- 229910052710 silicon Inorganic materials 0.000 claims description 21
- 238000002425 crystallisation Methods 0.000 claims description 12
- 230000008025 crystallization Effects 0.000 claims description 12
- 238000004062 sedimentation Methods 0.000 claims description 7
- 238000006386 neutralization reaction Methods 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 4
- 229920001429 chelating resin Polymers 0.000 claims description 4
- 238000004140 cleaning Methods 0.000 claims description 4
- 238000005189 flocculation Methods 0.000 claims description 4
- 230000016615 flocculation Effects 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 claims description 4
- 239000000835 fiber Substances 0.000 claims description 3
- 238000000108 ultra-filtration Methods 0.000 claims description 3
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 claims 2
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 abstract description 15
- 238000000034 method Methods 0.000 abstract description 14
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 239000010802 sludge Substances 0.000 abstract description 3
- 238000004065 wastewater treatment Methods 0.000 abstract description 3
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 19
- 239000000047 product Substances 0.000 description 16
- -1 printing and dyeing Substances 0.000 description 12
- 238000001035 drying Methods 0.000 description 10
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 9
- 229910001424 calcium ion Inorganic materials 0.000 description 8
- 239000013078 crystal Substances 0.000 description 8
- 229910001385 heavy metal Inorganic materials 0.000 description 8
- 150000002500 ions Chemical class 0.000 description 8
- 239000007788 liquid Substances 0.000 description 8
- 229910001425 magnesium ion Inorganic materials 0.000 description 8
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 7
- 239000011575 calcium Substances 0.000 description 7
- 239000002244 precipitate Substances 0.000 description 7
- 230000018044 dehydration Effects 0.000 description 6
- 238000006297 dehydration reaction Methods 0.000 description 6
- 238000004806 packaging method and process Methods 0.000 description 6
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 229910052791 calcium Inorganic materials 0.000 description 3
- 229940043430 calcium compound Drugs 0.000 description 3
- 150000001674 calcium compounds Chemical class 0.000 description 3
- 239000012141 concentrate Substances 0.000 description 3
- 239000011777 magnesium Substances 0.000 description 3
- 229910052749 magnesium Inorganic materials 0.000 description 3
- 159000000003 magnesium salts Chemical class 0.000 description 3
- 238000000926 separation method 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
- 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 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 239000003513 alkali Substances 0.000 description 2
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 2
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 2
- 239000000920 calcium hydroxide Substances 0.000 description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000006115 defluorination reaction Methods 0.000 description 2
- 239000011552 falling film Substances 0.000 description 2
- 125000000524 functional group Chemical group 0.000 description 2
- 238000000265 homogenisation Methods 0.000 description 2
- 239000008235 industrial water Substances 0.000 description 2
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 125000001741 organic sulfur group Chemical group 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 239000006200 vaporizer Substances 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- UXVMQQNJUSDDNG-UHFFFAOYSA-L Calcium chloride Chemical compound [Cl-].[Cl-].[Ca+2] UXVMQQNJUSDDNG-UHFFFAOYSA-L 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 1
- 239000002033 PVDF binder Substances 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 239000004115 Sodium Silicate Substances 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 229910000323 aluminium silicate Inorganic materials 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
- WUKWITHWXAAZEY-UHFFFAOYSA-L calcium difluoride Chemical compound [F-].[F-].[Ca+2] WUKWITHWXAAZEY-UHFFFAOYSA-L 0.000 description 1
- 229910001634 calcium fluoride Inorganic materials 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000009295 crossflow filtration Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 208000028659 discharge Diseases 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003657 drainage water Substances 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 1
- 229910001635 magnesium fluoride Inorganic materials 0.000 description 1
- 239000000347 magnesium hydroxide Substances 0.000 description 1
- 239000000395 magnesium oxide Substances 0.000 description 1
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 description 1
- 239000000391 magnesium silicate Substances 0.000 description 1
- 229910052919 magnesium silicate Inorganic materials 0.000 description 1
- 235000019792 magnesium silicate Nutrition 0.000 description 1
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- ZADYMNAVLSWLEQ-UHFFFAOYSA-N magnesium;oxygen(2-);silicon(4+) Chemical compound [O-2].[O-2].[O-2].[Mg+2].[Si+4] ZADYMNAVLSWLEQ-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 229910001415 sodium ion Inorganic materials 0.000 description 1
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 description 1
- 229910052911 sodium silicate Inorganic materials 0.000 description 1
- 229910052979 sodium sulfide Inorganic materials 0.000 description 1
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 230000001360 synchronised effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Classifications
-
- 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
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Removal Of Specific Substances (AREA)
Abstract
The utility model discloses a high-salt wastewater advanced treatment system which comprises an adjusting tank, a high-density tank, a filtering device, a resin device, a nanofiltration device, a reverse osmosis device, a reaction clarification tank, a microfiltration device, a sodium chloride evaporation device, a high-grade oxidation device and a sodium sulfate evaporation device, wherein the adjusting tank is connected with the resin device; the device comprises a regulating tank, a high-density tank, a filtering device, a resin device and a nanofiltration device, wherein the regulating tank, the high-density tank, the filtering device, the resin device and the nanofiltration device are sequentially connected, the reverse osmosis device, the reaction clarification tank, the microfiltration device and the sodium chloride evaporation device are sequentially connected, the reverse osmosis device is connected with a water outlet of the nanofiltration device, the advanced oxidation device is connected with a concentrated water outlet of the nanofiltration device, and the sodium sulfate evaporation device is connected with the advanced oxidation device. The utility model has the characteristics of short process route, small dosage, small sludge production amount, strong operability and the like through multistage hardness and fluorine removal, and can greatly reduce the investment and operation cost of high-salt wastewater treatment.
Description
Technical Field
The utility model relates to the technical field of wastewater treatment, in particular to a high-salt wastewater advanced treatment system.
Background
Along with the increasing strictness of national environmental protection policies, high-salt-content wastewater generated by enterprises is required to be subjected to strict treatment, and various high-consumption water enterprises such as steel, printing and dyeing, chemical industry, electric power and the like begin to carry out advanced treatment on the wastewater for reuse, especially for industrial parks such as new material parks, chemical industry parks, pharmaceutical industry parks and the like with large water consumption and complex drainage water quality, and zero discharge treatment and resource utilization of the park wastewater are comprehensively required.
The current industrial wastewater zero-emission and resource utilization engineering generally adopts a pretreatment, membrane concentration and evaporation crystallization process, and scaling factors such as calcium, magnesium, fluorine, silicon and the like in the wastewater are mostly removed after the pretreatment process section, and the scaling factors such as calcium, magnesium, fluorine, silicon and the like in the wastewater are concentrated again along with the concentration of salt after the multistage membrane concentration, so that serious scaling and corrosion risks are generated for a subsequent treatment system, and the operation stability of the whole set of zero-emission system is greatly influenced.
Aiming at the problems of long process flow, multiple dosing types, large dosing amount, large sludge production amount, unsatisfactory removal effect and the like of the scale factors in the high-salt-content wastewater, if the scale factors are removed by adopting the traditional synchronous removal process for treatment, the system investment and the operation cost are high. Therefore, aiming at the requirements of different process stages, innovative researches on the treatment process of deep hardness removal, silicon removal and fluorine removal of the high-salt wastewater are greatly necessary and urgent.
Disclosure of utility model
The utility model aims to solve the technical problem of providing a high-salt wastewater advanced treatment system and a high-salt wastewater advanced treatment system which are suitable for the requirements of different process stages and optimize the reagent adding scheme.
The technical scheme adopted for solving the technical problems is as follows: the high-salinity wastewater advanced treatment system comprises an adjusting tank, a high-density tank for primarily removing hard silicon and fluorine from high-salinity wastewater, a filtering device for removing suspended matters, a resin device for deeply removing hard matters, a nanofiltration device for separating salt treatment, a reverse osmosis device for concentration and decrement, a reaction clarification tank for deeply removing silicon and fluorine, a microfiltration device for removing suspended matters, a sodium chloride evaporation device for evaporation concentration and crystallization treatment, an advanced oxidation device for removing organic matters, and a sodium sulfate evaporation device for evaporation concentration and crystallization treatment;
The device comprises a regulating tank, a high-density tank, a filtering device, a resin device and a nanofiltration device, wherein the regulating tank, the high-density tank, the filtering device, the resin device and the nanofiltration device are sequentially connected, the reverse osmosis device, the reaction clarification tank, the microfiltration device and the sodium chloride evaporation device are sequentially connected, the reverse osmosis device is connected with a water outlet of the nanofiltration device, the advanced oxidation device is connected with a concentrated water outlet of the nanofiltration device, and the sodium sulfate evaporation device is connected with the advanced oxidation device.
Preferably, the regulating tank comprises a tank body and a stirrer arranged in the tank body; the stirrer adopts a hyperboloid stirrer.
Preferably, the high-density tank comprises a first reaction tank, a second reaction tank, a flocculation tank, a first sedimentation tank and a neutralization tank which are sequentially communicated.
Preferably, the filtering device comprises a fiber bundle filter, a self-cleaning filter and an ultrafiltration membrane group which are connected in sequence.
Preferably, the resin device is a weak acid resin tank or a chelating resin tank.
Preferably, the nanofiltration device is a primary nanofiltration or a secondary nanofiltration membrane group.
Preferably, the reverse osmosis device is a primary reverse osmosis or a secondary reverse osmosis membrane group.
Preferably, the reaction clarifying tank comprises a third reaction tank, a fourth reaction tank and a second sedimentation tank which are sequentially communicated.
Preferably, the microfiltration device comprises a concentration tank and a microfiltration membrane group which are connected in sequence.
Preferably, the advanced oxidation device comprises an AOP water inlet tank, an AOP reaction tower, a BAC water inlet tank and a BAC adsorption tower which are connected in sequence.
Preferably, the sodium chloride evaporation device and the sodium sulfate evaporation device are respectively MVR evaporators or multi-effect evaporators.
Preferably, the high-salt wastewater advanced treatment system further comprises a reuse water tank, wherein the reverse osmosis device, the sodium chloride evaporation device and the sodium sulfate evaporation device are respectively connected with the reuse water tank through reuse pipelines, and reverse osmosis produced water and evaporation condensate water are conveyed to the reuse water tank through the reuse pipelines.
The utility model has the beneficial effects that: the method ensures that the treated high-salt wastewater cannot generate scaling and corrosion risks to a subsequent treatment system through multistage hardness and silicon removal and fluorine removal, and has the characteristics of short process route, small dosage, small sludge production, strong operability and the like, and the investment and the running cost of high-salt wastewater treatment can be greatly reduced.
The high-salt wastewater is subjected to quality separation and purification, and the qualified sodium chloride crystal salt and sodium sulfate crystal salt are produced through evaporation and crystallization, so that the advanced treatment and resource recovery of the high-salt wastewater are realized.
Drawings
The utility model will be further described with reference to the accompanying drawings and examples, in which:
FIG. 1 is a schematic diagram of a connection structure of a high-salinity wastewater advanced treatment system according to an embodiment of the utility model.
Detailed Description
For a clearer understanding of technical features, objects and effects of the present utility model, a detailed description of embodiments of the present utility model will be made with reference to the accompanying drawings.
As shown in fig. 1, the advanced treatment system for high-salt wastewater according to an embodiment of the present utility model includes a regulating tank 10, a high-density tank 20, a filtering device 30, a resin device 40, a nanofiltration device 50, a reverse osmosis device 60, a reaction clarifier 70, a microfiltration device 80, and a sodium chloride evaporation device 90, which are sequentially connected through pipes and sequentially treat high-salt wastewater, and further includes an advanced oxidation device 100 connected to the receiving device 50, and a sodium sulfate evaporation device 110 connected to the advanced oxidation device 100.
Wherein the regulating tank 10 is used for receiving and homogenizing high-salt wastewater discharged from industry. The high-density tank 20 receives the high-salt wastewater from the regulating tank 10, and performs preliminary hardness removal, silicon removal and fluorine removal on the high-salt wastewater to remove most of calcium ions, magnesium ions, fluorine ions, silicon and heavy metal ions, thereby obtaining softened effluent. The filtering device 30 receives the softened water from the high density tank 20, and clarifies and filters the softened water to remove suspended substances and obtain clarified liquid. The resin device 40 receives the clarified liquid from the filter device 30, and removes residual calcium and magnesium ions by deep hardening of the clarified liquid to obtain resin produced water. The nanofiltration device 50 receives the resin produced water from the resin device 40, and performs salt separation treatment on the resin produced water to separate mono-and divalent ions, thereby obtaining nanofiltration produced water and nanofiltration concentrate.
The reverse osmosis unit 60 receives nanofiltration produced water from the nanofiltration unit 50, and performs concentration reduction on the nanofiltration produced water to obtain reverse osmosis produced water and reverse osmosis concentrated water. The reaction clarification tank 70 receives the reverse osmosis concentrated water from the reverse osmosis device 60, and carries out deep silicon and fluorine removal treatment on the reverse osmosis concentrated water, so as to remove fluorine ions and silicon in a targeted manner, and obtain clarified effluent meeting the requirements of the subsequent process. The micro-filtration device 80 receives clarified effluent from the reaction clarifier 70, clarifies and filters the clarified effluent to remove suspended substances and obtain micro-filtration produced water. The sodium chloride evaporation device 90 receives the microfiltration product water from the microfiltration device 80, and performs evaporation concentration crystallization drying treatment on the microfiltration product water to obtain a sodium chloride crystal salt product and evaporation condensate water.
The advanced oxidation unit 100 receives the nanofiltration concentrate from the nanofiltration unit 50, and performs catalytic oxidation on the nanofiltration concentrate to remove organic matters, thereby obtaining advanced oxidation product water. The sodium sulfate evaporation device 110 receives the advanced oxidation product water from the advanced oxidation device 100, and performs evaporation concentration crystallization drying treatment on the advanced oxidation product water to obtain a sodium sulfate crystal salt product and evaporation condensate water.
The reuse water tank 120 receives reverse osmosis produced water from the reverse osmosis unit 60, evaporation condensate from the sodium chloride evaporation unit 90, and evaporation condensate from the sodium sulfate evaporation unit 110.
In particular, the conditioning tank 10 may include a tank body and a stirrer disposed within the tank body; after the high-salt wastewater enters the tank body, the high-salt wastewater is subjected to homogenization treatment through the stirring work of the stirrer. The stirrer is preferably a hyperboloid stirrer, and the hyperboloid stirrer can enable the high-salt wastewater to be continuously turned over, inclined and staggered in three directions during stirring, so that solid and liquid in the high-salt wastewater are rapidly and uniformly mixed, and the purpose of homogenization is achieved.
The inlet of the high-density tank 20 is connected with the outlet of the regulating tank 10 through a pipeline, and the homogenized high-salt wastewater enters the high-density tank 20 through the pipeline. The high-density tank 20 may further include a first reaction tank 21, a second reaction tank 22, a flocculation tank 23, a first sedimentation tank 24, and a neutralization tank 25, which are sequentially communicated; the inlet of the high density tank 20 is provided on the first reaction tank 21. The high-salt wastewater enters the first reaction tank 21 and can enter the second reaction tank 22 through overflow. In the first reaction tank 21, the high-salt wastewater reacts with calcium compounds and magnesium salts added thereto; in the second reaction tank 22, the high-salt wastewater reacts with carbonate and heavy metal remover added thereto.
Wherein the calcium compound is selected from one or more of calcium hydroxide and calcium chloride, and the main purpose is to remove magnesium ions and fluoride ions; the magnesium salt is selected from one or more of magnesium chloride and magnesium oxide, and is mainly used for removing silicon; the carbonate is selected from one or more of sodium carbonate and potassium carbonate, and is mainly used for removing calcium ions; the heavy metal remover is one or more selected from sodium sulfide, organic sulfur TMT and organic phosphorus, and is mainly used for removing other heavy metal ions.
The reacted high-salt wastewater sequentially enters a flocculation tank 23, a first sedimentation tank 24 and a neutralization tank 25. The high-salt wastewater can remove most of calcium ions, magnesium ions, fluorine ions, silicon and heavy metal ions in the high-salt wastewater by reacting with calcium compounds, magnesium salts, carbonates and heavy metal removing agents, so as to obtain softened effluent.
In some embodiments, the total hardness of the softened effluent is less than or equal to 100mg/L, fluoride is less than or equal to 10mg/L, and silica is less than or equal to 15mg/L.
When the high-density tank 20 performs preliminary hardness removal and silicon removal and fluorine removal, the pH value of the high-salt wastewater is adjusted to be 10.5-11.5 by adding calcium hydroxide or sodium hydroxide in the first reaction tank 21, and the reaction is more facilitated under alkaline conditions, and the method comprises the following steps: magnesium ions and hydroxide ions in the high-salt wastewater form magnesium hydroxide precipitates, fluoride ions and calcium ions form calcium fluoride precipitates, silicon and magnesium ions form magnesium silicate precipitates, most heavy metals are centrifuged to form hydroxide precipitates, and bicarbonate ions are converted into carbonate ions. In the second reaction tank 22, calcium ions and carbonate ions form calcium carbonate precipitates, and the remaining heavy metal ions are sequestered with organic sulfur or the like to form precipitates.
The pH of the high-salt wastewater in the neutralization tank 25 is adjusted to 7.5-8.5 by adding hydrochloric acid or sulfuric acid, and the weak alkaline water quality is favorable for the subsequent deep removal of calcium and magnesium by the resin device 40.
The filtering device 30 is connected with the outlet of the high-density tank 20 through a pipeline and receives softened effluent discharged from the high-density tank 20. The filtering device 30 can comprise a fiber bundle filter 31, a self-cleaning filter 32 and an ultrafiltration membrane group 33 which are sequentially connected, and sequentially carries out clarification and filtration treatment on softened water after preliminary hardness removal and defluorination to remove suspended matters of the softened water, so as to obtain clarified liquid with turbidity less than or equal to 0.5NTU.
The clarified liquid obtained by the filtration device 30 is transported to the resin device 40 through a pipe so that the clarified liquid is subjected to deep hardening by the resin device 40 to remove the remaining calcium and magnesium ions. The total hardness of the produced water of the resin device 40 is less than or equal to 10mg/l.
The resin device 40 may employ a weak acid resin tank or a chelating resin tank. In this embodiment, the resin device 40 adopts chelating resin suitable for high salt water, and adopts a series operation mode to fully ensure the hardness removal effect.
In the embodiment, calcium and magnesium ions in the high-salt wastewater are adsorbed by a large number of functional groups on the resin, and are exchanged with sodium ions on the functional groups of the resin, so that the deep removal of the calcium and magnesium ions is realized.
The nanofiltration device 50 is connected with the resin device 40 through a pipeline, receives resin produced water from the resin device 40, carries out salt separation treatment on the resin produced water to separate mono-valent ions and divalent ions, obtains nanofiltration produced water and nanofiltration concentrated water, the nanofiltration produced water enters the reverse osmosis device 60 for further concentration, and the nanofiltration concentrated water enters the advanced oxidation device 100 for removing organic matters.
Nanofiltration device 50 may be a primary nanofiltration membrane group or a secondary nanofiltration membrane group. In the embodiment, the initial retention rate of the nanofiltration membrane on divalent ions is not lower than 98%, and the nanofiltration membrane has a certain negative retention rate on chloride ions.
The reverse osmosis device 60 is connected with the water outlet of the receiving and filtering device 50 through a pipeline, receives nanofiltration water from the nanofiltration device 50, and performs concentration decrement on the nanofiltration water to obtain reverse osmosis water and reverse osmosis concentrated water. The reverse osmosis unit 60 may be a primary reverse osmosis or a secondary reverse osmosis membrane module.
In this embodiment, the reverse osmosis device 60 employs a two-stage reverse osmosis membrane module. Wherein the first-stage reverse osmosis produced water is recycled, and the first-stage reverse osmosis concentrated water enters the second-stage reverse osmosis; wherein the secondary reverse osmosis produced water is recycled, and the secondary reverse osmosis concentrated water enters a reaction clarification tank to remove impurities.
The reaction clarifier 70 is connected with and receives the reverse osmosis concentrated water from the reverse osmosis device 60 through a pipeline, and carries out deep desilication and defluorination treatment on the reverse osmosis concentrated water, and the fluorine ions and the silicon are removed in a targeted manner, so that clarified water meeting the requirements of the subsequent process is obtained.
In this example, the fluoride ion content of the clarified effluent from the reaction clarifier 70 was controlled to 5mg/L to 10mg/L, and the silica content was controlled to 5mg/L to 10mg/L.
The reaction clarification tank 70 comprises a third reaction tank 71, a fourth reaction tank 72 and a second sedimentation tank 73 which are sequentially communicated; in the third reaction tank 71, the high-salt wastewater reacts with the fluorine removing agent added therein to remove fluorine ions; in the fourth reaction tank 72, the high-salt wastewater reacts with aluminum salt added thereto to remove silicon. The fluorine removing agent is selected from one or more of deep fluorine removing agent, PFS and PAC to remove fluorine ions. The aluminum salt is selected from one or more of aluminum oxide and sodium metaaluminate to remove silicon.
When the reaction clarifying tank 70 is used for deep silicon removal and fluorine removal, the pH value of the high-salt wastewater is adjusted to 6-8 by adding hydrochloric acid or sulfuric acid in the third reaction tank 71, and fluorine ions are more easily reacted with a fluorine removing agent under the weak acidic condition to generate insoluble fluoride, so that the removal of the fluorine ions is realized. In the fourth reaction tank 72, the pH of the high-salt wastewater is adjusted to 8-9 by adding liquid alkali, and under the pH condition, sodium silicate reacts with sodium metaaluminate to generate aluminosilicate precipitate, so that silicon is removed.
The clarified effluent of the reaction clarifier 70 is conveyed to a microfiltration device 80 through a pipeline to carry out clarification and filtration treatment, and suspended matters are removed, so that the microfiltration produced water with turbidity less than or equal to 1NTU is obtained.
The microfiltration device 80 includes a concentration tank 81 and a microfiltration membrane group 82 connected in this order. In this embodiment, the microfiltration membrane set 82 adopts a large-flux cross-flow filtration operation mode, and the microfiltration membrane is made of PVDF, which can resist strong acid, strong alkali and oxidant cleaning.
The sodium chloride evaporation device 90 receives the microfiltration product water from the microfiltration device 80, and performs evaporation concentration crystallization drying treatment on the microfiltration product water to obtain a sodium chloride crystal salt product and evaporation condensate water. The sodium chloride vaporization apparatus 90 may be a MVR vaporizer or a multiple effect vaporizer.
In this embodiment, the sodium chloride evaporation device 90 adopts two-stage MVR evaporation crystallization, and specifically includes a first-stage MVR falling film evaporator 91, a second-stage MVR forced circulation evaporator 92, and a dehydration drying packaging device 93 which are sequentially connected. The microfiltration product water is concentrated to TDS200000mg/L in a first-stage MVR falling film evaporator 91, enters a second-stage MVR forced circulation evaporator 92 for further evaporation to obtain sodium chloride salt slurry, and the sodium chloride salt slurry is discharged into a dehydration drying packaging device 93 for sequentially carrying out centrifugal dehydration, vibration bed drying and quantitative packaging, thus obtaining sodium chloride crystal salt meeting the industrial dry salt second-stage standard (purity is more than or equal to 97.5%) in industrial salt (GB 5462-2015).
The advanced oxidation device 100 receives the nanofiltration concentrated water from the nanofiltration device 50, and performs catalytic oxidation on the nanofiltration concentrated water to remove organic matters, thereby obtaining advanced oxidation produced water; the advanced oxidation unit 100 has an organic matter removal rate of not less than 40%. Advanced oxidation unit 100 may be implemented using advanced oxidation treatment equipment of the prior art.
Advanced oxidation unit 100 further may include an AOP intake tank 101, an AOP reaction tower 102, a BAC intake tank 103, and a BAC adsorption tower 104 connected in this order. In the AOP reaction tower 102, the high-salt wastewater reacts with ozone and a catalyst added into the high-salt wastewater to remove organic matters; in the BAC adsorption tower 104, the adsorbent adsorbs and removes pollutants in the high-salt wastewater.
The sodium sulfate evaporation device 110 receives the advanced oxidation product water from the advanced oxidation device 100, and performs evaporation concentration crystallization drying treatment on the advanced oxidation product water to obtain a sodium sulfate crystal salt product and evaporation condensate water. The sodium sulfate evaporation device 110 may be selected from an MVR evaporator or a multiple effect evaporator.
In this embodiment, the sodium sulfate evaporating device 110 adopts two-effect evaporation crystallization, and specifically includes a first-effect evaporator 111, a second-effect evaporator 112, and a dehydration drying packaging device 113, which are sequentially connected. Concentrating the high-grade oxidation product water to TDS200000mg/L in a first-effect evaporator 111, further evaporating in a second-effect evaporator 112 to obtain sodium sulfate salt slurry, discharging the salt slurry into a dehydration drying and packaging device 113, and sequentially carrying out centrifugal dehydration, vibration bed drying and quantitative packaging to obtain sodium sulfate crystal salt meeting the class II qualified product standard (purity is more than or equal to 97%) in industrial anhydrous sodium sulfate (GB 6009-2014).
The high-salinity wastewater advanced treatment system further comprises a reuse water tank 120, wherein the reverse osmosis device 60, the sodium chloride evaporation device 90 and the sodium sulfate evaporation device 110 are respectively connected with the reuse water tank 120 through reuse pipelines, and reverse osmosis produced water of the reverse osmosis device 60, evaporation condensate water of the sodium chloride evaporation device 90 and evaporation condensate water of the sodium sulfate evaporation device 110 are conveyed to the reuse water tank 120 through corresponding reuse pipelines for reuse, and the quality of the reuse water meets the water quality standard of the open type circulating cooling water system with reclaimed water used as an industrial water source in urban wastewater recycling industrial water quality (GB/T19923-2005).
The foregoing description is only illustrative of the present utility model and is not intended to limit the scope of the utility model, and all equivalent structures or equivalent processes or direct or indirect application in other related technical fields are included in the scope of the present utility model.
Claims (10)
1. The advanced treatment system for the high-salt wastewater is characterized by comprising an adjusting tank, a high-density tank for primarily removing hard silicon and fluorine from the high-salt wastewater, a filtering device for removing suspended matters, a resin device for deeply removing hard matters, a nanofiltration device for separating salt treatment, a reverse osmosis device for concentration and decrement, a reaction clarification tank for deeply removing silicon and fluorine, a microfiltration device for removing suspended matters, a sodium chloride evaporation device for evaporation concentration and crystallization treatment, an advanced oxidation device for removing organic matters, and a sodium sulfate evaporation device for evaporation concentration and crystallization treatment;
The device comprises a regulating tank, a high-density tank, a filtering device, a resin device and a nanofiltration device, wherein the regulating tank, the high-density tank, the filtering device, the resin device and the nanofiltration device are sequentially connected, the reverse osmosis device, the reaction clarification tank, the microfiltration device and the sodium chloride evaporation device are sequentially connected, the reverse osmosis device is connected with a water outlet of the nanofiltration device, the advanced oxidation device is connected with a concentrated water outlet of the nanofiltration device, and the sodium sulfate evaporation device is connected with the advanced oxidation device.
2. The high salt wastewater advanced treatment system according to claim 1, wherein the regulating tank comprises a tank body and a stirrer arranged in the tank body; the stirrer adopts a hyperboloid stirrer.
3. The high salt wastewater advanced treatment system of claim 1, wherein the high density tank comprises a first reaction tank, a second reaction tank, a flocculation tank, a first sedimentation tank and a neutralization tank which are communicated in sequence.
4. The high salt wastewater advanced treatment system of claim 1, wherein the filtration device comprises a fiber bundle filter, a self-cleaning filter and an ultrafiltration membrane module connected in sequence.
5. The high-salinity wastewater advanced treatment system according to claim 1, wherein the resin device is a weak acid resin tank or a chelating resin tank;
the nanofiltration device is a primary nanofiltration membrane or a secondary nanofiltration membrane group.
6. The high salt wastewater advanced treatment system of claim 1, wherein the reverse osmosis device is a primary reverse osmosis or a secondary reverse osmosis membrane set.
7. The high-salt wastewater advanced treatment system according to claim 1, wherein the reaction clarifier comprises a third reaction tank, a fourth reaction tank and a second sedimentation tank which are communicated in sequence;
The microfiltration device comprises a concentration tank and a microfiltration membrane group which are sequentially connected.
8. The advanced treatment system for high-salinity wastewater according to claim 1, wherein the advanced oxidation device comprises an AOP water inlet tank, an AOP reaction tower, a BAC water inlet tank and a BAC adsorption tower which are connected in sequence.
9. The advanced treatment system for high-salinity wastewater according to claim 1, wherein the sodium chloride evaporation device and the sodium sulfate evaporation device are respectively an MVR evaporator or a multi-effect evaporator.
10. The high-salinity wastewater advanced treatment system according to any one of claims 1 to 9, further comprising a reuse water tank, wherein the reverse osmosis device, the sodium chloride evaporation device and the sodium sulfate evaporation device are respectively connected with the reuse water tank through reuse pipelines, and reverse osmosis produced water and evaporated condensate water are conveyed to the reuse water tank through the reuse pipelines.
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