CN111792796A - Reverse osmosis strong brine processing system - Google Patents
Reverse osmosis strong brine processing system Download PDFInfo
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- CN111792796A CN111792796A CN202010745113.XA CN202010745113A CN111792796A CN 111792796 A CN111792796 A CN 111792796A CN 202010745113 A CN202010745113 A CN 202010745113A CN 111792796 A CN111792796 A CN 111792796A
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- 239000012267 brine Substances 0.000 title claims abstract description 95
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 94
- 238000001223 reverse osmosis Methods 0.000 title claims abstract description 39
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 156
- 239000007788 liquid Substances 0.000 claims abstract description 91
- 238000002425 crystallisation Methods 0.000 claims abstract description 57
- 230000008025 crystallization Effects 0.000 claims abstract description 55
- 230000003647 oxidation Effects 0.000 claims abstract description 45
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 45
- 230000003197 catalytic effect Effects 0.000 claims abstract description 36
- 239000003054 catalyst Substances 0.000 claims abstract description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 35
- 239000001301 oxygen Substances 0.000 claims description 35
- 229910052760 oxygen Inorganic materials 0.000 claims description 35
- 239000002562 thickening agent Substances 0.000 claims description 24
- 239000013078 crystal Substances 0.000 claims description 14
- 238000011084 recovery Methods 0.000 claims description 13
- 238000005273 aeration Methods 0.000 claims description 9
- 230000006378 damage Effects 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 239000000945 filler Substances 0.000 claims description 5
- 230000001939 inductive effect Effects 0.000 claims description 3
- 239000003795 chemical substances by application Substances 0.000 claims description 2
- 239000003814 drug Substances 0.000 claims description 2
- 239000005416 organic matter Substances 0.000 abstract description 14
- 238000000746 purification Methods 0.000 abstract description 3
- 238000006243 chemical reaction Methods 0.000 description 13
- 150000003839 salts Chemical group 0.000 description 11
- 238000000034 method Methods 0.000 description 9
- 230000008569 process Effects 0.000 description 6
- 239000002455 scale inhibitor Substances 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- 244000005700 microbiome Species 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 238000000354 decomposition reaction Methods 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- 239000002351 wastewater Substances 0.000 description 4
- 239000012141 concentrate Substances 0.000 description 3
- -1 hydroxyl free radical Chemical class 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000011574 phosphorus Substances 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 241000894007 species Species 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000009423 ventilation Methods 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000004071 biological effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000005672 electromagnetic field Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 229910052747 lanthanoid Inorganic materials 0.000 description 1
- 150000002602 lanthanoids Chemical class 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/725—Treatment of water, waste water, or sewage by oxidation by catalytic oxidation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/72—Treatment of water, waste water, or sewage by oxidation
- C02F1/78—Treatment of water, waste water, or sewage by oxidation with ozone
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F5/00—Softening water; Preventing scale; Adding scale preventatives or scale removers to water, e.g. adding sequestering agents
Abstract
The utility model relates to a strong brine processing technology field provides a reverse osmosis strong brine processing system. The system comprises a crystallization device, an ozone-biochemical treatment device and a homogeneous catalytic oxidation device which are used for treating the strong brine in sequence; the crystallization device is provided with a liquid inlet end for feeding strong brine, and is used for carrying out crystallization treatment on the strong brine; the liquid inlet end of the ozone-biochemical treatment device is communicated with the liquid outlet end of the crystallization device, and the ozone-biochemical treatment device is used for carrying out ozone oxidation and aerobic biochemical treatment on the strong brine treated by the crystallization device; the liquid inlet end of the homogeneous catalytic oxidation device is communicated with the liquid outlet end of the ozone-biochemical treatment device, and a catalyst and ozone are introduced into the homogeneous catalytic oxidation device and are used for carrying out catalytic oxidation treatment on the strong brine treated by the ozone-biochemical treatment device; realize the purification treatment of reverse osmosis strong brine, realize that salinity and organic matter high efficiency are got rid of.
Description
Technical Field
The utility model relates to the technical field of wastewater treatment, in particular to a reverse osmosis strong brine treatment system.
Background
The reverse osmosis strong brine is salt-containing wastewater concentrated by a reverse osmosis membrane when wastewater is discharged from enterprises of petrochemical engineering and the like.
The reverse osmosis strong brine has high content of organic matters and salt, and can cause great pollution when being directly discharged. At present, most enterprises at home and abroad usually adopt an evaporative crystallization method to treat reverse osmosis strong brine, namely, the reverse osmosis strong brine is concentrated by an evaporator and then is conveyed to an evaporation pond for natural evaporation, and is recrystallized to form salt for safe landfill, but the reverse osmosis strong brine is difficult to avoid pollution caused by sewage leakage in the treatment process and cannot be effectively treated to remove organic matters and salt.
Therefore, how to efficiently remove organic matters and salts in the reverse osmosis concentrated brine becomes a problem to be solved urgently.
Disclosure of Invention
The utility model aims at providing a reverse osmosis strong brine processing system can high-efficiently get rid of salt and the organic matter in the reverse osmosis strong brine.
The reverse osmosis strong brine treatment system comprises a crystallization device, an ozone-biochemical treatment device and a homogeneous catalytic oxidation device, wherein the crystallization device, the ozone-biochemical treatment device and the homogeneous catalytic oxidation device are used for sequentially treating strong brine; the crystallization device is provided with a liquid inlet end for feeding strong brine, and is used for carrying out crystallization treatment on the strong brine; the liquid inlet end of the ozone-biochemical treatment device is communicated with the liquid outlet end of the crystallization device, and the ozone-biochemical treatment device is used for carrying out ozone oxidation and aerobic biochemical treatment on the strong brine treated by the crystallization device; the liquid inlet end of the homogeneous catalytic oxidation device is communicated with the liquid outlet end of the ozone-biochemical treatment device, and a catalyst and ozone are introduced into the homogeneous catalytic oxidation device and used for carrying out catalytic oxidation treatment on the strong brine treated by the ozone-biochemical treatment device.
Optionally, the crystallization device comprises a crystallizer, the crystallizer is provided with a containing cavity, the crystallizer is provided with a liquid inlet end and a first clear liquid outlet end which are respectively communicated with the containing cavity, and the liquid inlet end of the crystallizer is formed as the liquid inlet end of the crystallization device;
a stirrer is arranged in the accommodating cavity, and seed crystals for inducing crystallization of the strong brine are introduced into the accommodating cavity;
the first clear liquid outlet end is formed into at least part of the liquid outlet end of the crystallization device and is communicated with the liquid inlet end of the ozone-biochemical treatment device.
Optionally, the crystallization device further comprises a thickener and a centrifuge, wherein a liquid inlet end of the thickener is communicated with a concentrated solution outlet end of the crystallizer, and the thickener is used for concentrating the strong brine treated by the crystallizer; the thickener is provided with a second clear liquid outlet end communicated with the ozone-biochemical treatment device;
the liquid inlet end of the centrifuge is communicated with the concentrated liquid outlet end of the thickener, and the centrifuge is provided with a third clear liquid outlet end communicated with the ozone-biochemical treatment device.
Optionally, the crystallization device further comprises a dosing tank and a dosing pump;
the descaling agent remover is communicated with the dosing tank, the inlet end of the dosing pump is communicated with the medicine outlet of the dosing tank, and the outlet end of the dosing pump is communicated with the accommodating cavity.
Optionally, the ozone-biochemical treatment device comprises at least one ozone contact tank and at least one biochemical aerobic tank; the liquid inlet end of the ozone contact tank is communicated with the liquid outlet end of the crystallization device, and ozone is introduced into the ozone contact tank; the liquid outlet end of the ozone contact tank is communicated with the liquid inlet end of the biochemical aerobic tank, and oxygen is introduced into the biochemical aerobic tank; and the liquid outlet end of the biochemical aerobic tank is communicated with the liquid inlet end of the homogeneous catalytic oxidation device.
Optionally, the number of the ozone contact tanks is two, and the two ozone contact tanks are respectively a primary ozone contact tank and a secondary ozone contact tank, and the ozone concentration in the secondary ozone contact tank is lower than that in the primary ozone contact tank;
the two biochemical aerobic tanks are respectively a primary biochemical aerobic tank and a secondary biochemical aerobic tank, and the concentration of dissolved oxygen in the secondary biochemical aerobic tank is lower than that in the primary biochemical aerobic tank;
the liquid inlet end of the first-level ozone contact tank is communicated with the liquid outlet end of the crystallization device, the first-level ozone contact tank, the first-level biochemical aerobic tank, the second-level ozone contact tank and the second-level biochemical aerobic tank are communicated, and the liquid outlet end of the second-level biochemical aerobic tank is communicated with the liquid inlet end of the homogeneous catalytic oxidation device.
Optionally, a biological filler is arranged in the biochemical aerobic tank;
and/or the reverse osmosis concentrated brine treatment system further comprises an air blower, and the biochemical aerobic tank is provided with an oxygen inlet communicated with the air blower.
Optionally, the ozone generator further comprises an ozone generating device, wherein the ozone generating device comprises an air separation device, an ozone generator and an ozone aeration disc which are sequentially communicated;
the ozone aeration discs are arranged in the ozone contact tank and the homogeneous catalytic oxidation device.
Optionally, the ozone generator further comprises an ozone recovery device, wherein the inlet end of the ozone recovery device is communicated with the ozone contact tank and the homogeneous catalytic oxidation device, and the outlet end of the ozone recovery device is communicated with the ozone generator.
Optionally, the ozone generator further comprises an ozone destruction device, and the outlet end of the ozone recovery device is communicated with the ozone destruction device.
Compared with the prior art, the technical scheme provided by the embodiment of the disclosure has the following advantages: this disclose get rid of the salinity in the strong brine through the crystallizer earlier, the crystallization gets into ozone-biochemical treatment device after getting rid of, the ozone that lets in carries out ozone oxidation treatment to the organic matter of strong brine, the oxygen solution that ozone and organic matter reaction produced is in the strong brine and can be utilized, after the supplementary oxygen, the microorganism carries out aerobic biological treatment to the organic matter of strong brine, subsequently the strong brine gets into homogeneous catalytic oxidation device, the ozone that dissolves in the strong brine under the catalyst effect generates the hydroxyl free radical, make difficult degradation organic matter that is treated by ozone oxidation and aerobic biological treatment of remaining further by catalytic oxidation decomposition, finally realize the purification treatment of reverse osmosis strong brine, realize that salinity and organic matter are high-efficient to get rid of.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present disclosure and together with the description, serve to explain the principles of the disclosure.
In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present disclosure, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.
FIG. 1 is a block flow diagram of a reverse osmosis concentrated brine treatment system provided by an embodiment of the present disclosure;
fig. 2 is a schematic layout of a reverse osmosis concentrated brine treatment system provided in an embodiment of the present disclosure.
100, a crystallization device; 200. an ozone-biochemical treatment device; 300. a homogeneous catalytic oxidation unit; 1. a concentrated brine tank; 2. a lift pump; 3. a crystallizer; 4. a stirrer; 5. a thickener; 6. a centrifuge; 7. a dosing box; 8. a dosing pump; 9. a primary ozone contact tank; 10. a primary biochemical aerobic tank; 11. a secondary ozone contact tank; 12. a secondary biochemical aerobic tank; 13. a homogeneous reaction tank; 14. biological fillers; 15. a blower; 16. an air separation plant; 17. an ozone generator; 18. an ozone concentration detector; 19. an ozone aeration disc; 20. an ozone recovery device; 21. an ozone destruction device; 22. a clean water tank.
Detailed Description
In order that the above objects, features and advantages of the present disclosure may be more clearly understood, aspects of the present disclosure will be further described below. It should be noted that the embodiments and features of the embodiments of the present disclosure may be combined with each other without conflict.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present disclosure, but the present disclosure may be practiced in other ways than those described herein; it is to be understood that the embodiments disclosed in the specification are only a few embodiments of the present disclosure, and not all embodiments.
As shown in fig. 1, the present disclosure provides a reverse osmosis concentrated brine treatment system, comprising a crystallization device 100, an ozone-biochemical treatment device 200, and a homogeneous catalytic oxidation device 300, which sequentially treat concentrated brine; the crystallization device 100 is provided with a liquid inlet end for feeding strong brine, and the crystallization device 100 is used for carrying out crystallization treatment on the strong brine; the liquid inlet end of the ozone-biochemical treatment device 200 is communicated with the liquid outlet end of the crystallization device 100, and the ozone-biochemical treatment device 200 is used for carrying out ozone oxidation and aerobic biochemical treatment on the strong brine treated by the crystallization device 100; the liquid inlet end of the homogeneous catalytic oxidation device 300 is communicated with the liquid outlet end of the ozone-biochemical treatment device 200, and a catalyst and ozone are introduced into the homogeneous catalytic oxidation device 300 and are used for carrying out catalytic oxidation treatment on the concentrated brine treated by the ozone-biochemical treatment device 200.
Compared with the prior art, this is disclosed to get rid of the salinity in the strong brine through crystallizer 100 earlier, the crystallization gets rid of back strong brine and gets into ozone-biochemical treatment device 200, the ozone that lets in carries out ozone oxidation treatment to the organic matter of strong brine, the oxygen that ozone and organic matter reaction generated dissolves in the strong brine can be utilized, after the supplementary oxygen, the microorganism carries out aerobic biological treatment to the organic matter of strong brine, subsequently the strong brine gets into homogeneous catalytic oxidation device 300, the ozone that dissolves in the strong brine under the catalytic action generates the hydroxyl free radical, make difficult by ozone oxidation treatment and aerobic biological treatment's the difficult degradation organic matter of residue further by catalytic oxidation decomposition, finally realize the purification treatment of reverse osmosis strong brine, realize the high-efficient removal of salinity and organic matter.
In some embodiments, as shown in fig. 2, a preferred embodiment of the present disclosure is to employ an agitation crystallization apparatus, the crystallization apparatus 100 includes a crystallizer 3, the crystallizer 3 has a holding cavity for holding brine, the crystallizer 3 has a liquid inlet end and a first clear liquid outlet end respectively communicated with the holding cavity, and the liquid inlet end of the crystallizer 3 is formed as a liquid inlet end of the crystallization apparatus 100; a stirrer 4 is arranged in the accommodating cavity, and seed crystals for inducing crystallization of the strong brine are introduced into the accommodating cavity; the first clear liquid outlet end is formed as at least part of the liquid outlet end of the crystallization device 100, and the first clear liquid outlet end is communicated with the liquid inlet end of the ozone-biochemical treatment device 200.
Among the above-mentioned technical scheme, the upper portion of crystallizer 3 is cylindricly, and the lower part is the back taper tube-shape, and first clear solution outlet port sets up in the upper portion of crystallizer 3, and the concentrate outlet port sets up in the lower part of crystallizer 3, and agitator 4 arranges in upper portion, and strong brine gets into crystallizer 3 after, can let in CaSO to crystallizer 34.2H20 seed crystal and other seed crystals, and removing Ca by induced crystallization2+Other ions, the stirrer 4 starts to work, Ca in the strong brine2+And other ions contact with the crystal seeds, crystals grow and gather downwards, the concentrated brine is correspondingly divided into clear liquid and concentrated liquid at the upper part and the lower part of the crystallizer 3, the clear liquid flows out from a first clear liquid outlet end to a liquid inlet end of the ozone-biochemical treatment device 200, and the concentrated liquid flows out from a concentrated liquid outlet end.
In some embodiments, as shown in fig. 2, in order to further separate salt, a thickener 5 and a centrifuge 6 are sequentially disposed downstream of the concentrate outlet end of the crystallizer 3, the liquid inlet end of the thickener 5 is communicated with the concentrate outlet end of the crystallizer 3, and the thickener 5 is used for concentrating the concentrated brine treated by the crystallizer 3; the thickener 5 has a second clear liquid outlet end communicated with the ozone-biochemical treatment device 200; the liquid inlet end of the centrifuge 6 is communicated with the concentrated liquid outlet end of the thickener 5, and the centrifuge 6 is provided with a third clear liquid outlet end communicated with the ozone-biochemical treatment device 200.
In the above technical solution, the crystallizer 3, the stirrer 4, the thickener 5 and the centrifuge 6 integrally form the crystallization apparatus 100, the crystal mixture is gradually concentrated by the crystallizer 3 and the thickener 5, the thickener 5 is usually a liquid-spinning type, the crystal mixture tangentially enters the upper part of the cylindrical section of the thickener 5 from the lower part of the crystallizer 3, the concentrated solution is discharged from the conical bottom of the thickener 5, and is dehydrated by the centrifuge 6 to obtain a salt with extremely low water content, such as calcium sulfate or other crystals, wherein the clear liquids of the crystallizer 3, the thickener 5 and the centrifuge 6 are correspondingly introduced into the ozone-biochemical treatment apparatus 200 through the first clear liquid outlet end, the second clear liquid outlet end and the third clear liquid outlet end to perform subsequent organic decomposition treatment.
In some embodiments, as shown in fig. 2, the reverse osmosis concentrated brine is usually mixed with a scale remover, the scale remover is generally added when the wastewater is treated by a reverse osmosis membrane, and the crystallization of salt may be affected by the presence of the scale remover, so the crystallization apparatus 100 is further provided with a dosing tank 7 and a dosing pump 8, the dosing tank 7 is communicated with the scale remover, the inlet end and the outlet end of the dosing pump 8 are correspondingly communicated with the dosing tank 7 and the crystallizer 3, and the dosing pump 8 is used for adding the scale remover in the dosing tank 7 into the concentrated brine in the accommodating cavity.
In the technical scheme, the scale inhibitor remover is firstly dissolved in the dosing tank 7, the flow is controlled by the dosing pump 8 to feed the scale inhibitor remover into the crystallizer 3, the scale inhibitor in the concentrated brine is usually a reverse osmosis scale inhibitor and can prevent the membrane surface from scaling, and the corresponding scale inhibitor remover can adopt a phosphorus removal flocculant, polyaluminium chloride and the like.
In some embodiments, as shown in fig. 2, to ensure effective treatment of organic matter, the ozone-biochemical treatment apparatus 200 comprises at least one ozone contact tank and at least one biochemical aerobic tank; the liquid inlet end of the ozone contact tank is communicated with the liquid outlet end of the crystallization device 100, and ozone is introduced into the ozone contact tank; the liquid outlet end of the ozone contact tank is communicated with the liquid inlet end of the biochemical aerobic tank, and oxygen is introduced into the biochemical aerobic tank; the liquid outlet end of the biochemical aerobic tank is communicated with the liquid inlet end of the homogeneous catalytic oxidation device 300.
Among the above-mentioned technical scheme, the ozone contact tank can comprise one-level ozone contact tank 9 and second grade ozone contact tank 11, biochemical good oxygen pond can comprise one-level biochemical good oxygen pond 10 and second grade biochemical good oxygen pond 12, one-level ozone contact tank 9, one-level biochemical good oxygen pond 10, second grade ozone contact tank 11 and second grade biochemical good oxygen pond 12 communicate in order and arrange, one-level biochemical good oxygen pond 10 corresponds with second grade biochemical good oxygen pond 12 and carries out effectual utilization with the oxygen that one-level ozone contact tank 9 and second grade ozone contact tank 11 produced, carry out ozone oxidation treatment and good oxygen biological treatment to the strong brine in succession, decompose the organic matter as far as possible.
Most organic matters are decomposed by the first-stage ozone contact tank 9 with high ozone concentration and the first-stage biochemical aerobic tank 10 with high dissolved oxygen concentration, so that the ozone concentration and the dissolved oxygen concentration of the second-stage ozone contact tank 11 and the second-stage biochemical aerobic tank 12 of the next stage do not need to be too high, and unnecessary cost waste is avoided; and the different oxygen concentrations of the first-stage biochemical aerobic tank 10 and the second-stage biochemical aerobic tank 12 are respectively beneficial to the growth of different species of microorganisms, so that the different species of microorganisms cooperate with each other to further decompose the organic matters.
In some embodiments, as shown in fig. 2, the blower 15 is arranged to supply oxygen to the biochemical aerobic tank, and the biological filler 14 is arranged in the biochemical aerobic tank, so that the microbial biomass of the biochemical aerobic tank is further increased, and the processing capacity of the system is improved.
In the technical scheme, the biological filler has strong adsorption capacity, is easy to attach microorganisms, is suitable for enriching the growth of biological communities, forms an ecosystem with longer food chains such as bacteria, algae, protozoa, metazoans and the like, and can efficiently degrade organic pollutants, remove nitrogen and phosphorus; the biological membrane is high, and is high in biological activity and mass transfer efficiency.
In some embodiments, as shown in fig. 2, the air separation device further comprises an ozone generating device, wherein the ozone generating device comprises an air separation device 16, an ozone generator 17 and an ozone aeration disc 19 which are sequentially communicated; the ozone aeration disc 19 is arranged in the ozone contact tank and the homogeneous catalytic oxidation device 300, and the homogeneous catalytic oxidation device 300 comprises a homogeneous phase reaction tank 13.
In the technical scheme, the air separation device 16 is used for separating each component gas in the air to produce oxygen, the oxygen enters the ozone generator 17 to react to generate ozone, and the ozone is conveyed to the primary ozone contact tank 9, the secondary ozone contact tank 11 and the ozone aeration disc 19 at the lower part of the homogeneous phase reaction tank 13 through the ozone concentration detector 18; in other embodiments, a dissolved air pump may be provided, which replaces the ozone aeration disk 19, and the dissolved air pump may mix ozone with the concentrated brine, and then the mixed solution is introduced into the primary ozone contact tank 9, the secondary ozone contact tank 11, and the homogeneous reaction tank 13.
In some embodiments, as shown in fig. 2, the ozone recovery device 20 is further included, the ozone recovery device 20 can adopt a negative pressure absorption device, the first-stage ozone contact tank 9, the second-stage ozone contact tank 11 and the homogeneous reaction tank 13 all adopt sealed tank bodies, the inlet end of the ozone recovery device 20 is communicated with the ozone outlet end of the upper parts of the first-stage ozone contact tank 9, the second-stage ozone contact tank 11 and the homogeneous reaction tank 13, and the outlet end of the ozone recovery device 20 is communicated with the ozone generator 17.
In the technical scheme, a part of ozone does not react in the primary ozone contact tank 9, the secondary ozone contact tank 11 and the homogeneous reaction tank 13, and oxygen generated by the reaction of the ozone and the ozone can be collected by a negative pressure absorption device and then is introduced into the ozone generator 17 again for recycling; ozone destruction can also be vented to the atmosphere again by ozone destruction device 21.
The specific working process of one embodiment of the present disclosure is as follows:
discharging reverse osmosis strong brine to a strong brine tank 1, lifting the strong brine to a crystallizer 3 through a lifting pump 2, adding a scale remover in a dosing tank 7 to the crystallizer 3 through a dosing pump 8, controlling the concentration of the scale remover to be 100 plus 200mg/L, adding seed crystals to the crystallizer 3, starting a stirrer 4 to work, and separating salt crystals from the strong brine through the crystallizer 3, a thickener 5 and a centrifuge 6;
then the concentrated brine sequentially enters a first-stage ozone contact tank 9, a first-stage biochemical aerobic tank 10, a second-stage ozone contact tank 11 and a second-stage biochemical aerobic tank 12, ozone is provided for the first-stage ozone contact tank 9 and the second-stage ozone contact tank 11 through an ozone generating device, the ozone concentration is respectively 10-20mg/L and 5-10mg/L, oxygen is provided for the first-stage biochemical aerobic tank 10 and the second-stage biochemical aerobic tank 12 through an air blower 15, and the dissolved oxygen concentration is respectively 3-5mg/L and 1-3 mg/L;
then the strong brine enters a homogeneous reaction tank 13, ozone is introduced into the homogeneous reaction tank 13, the ozone generates hydroxyl radicals under the action of lanthanide metal catalyst and electromagnetic field, the residual refractory organic matters which are not easily subjected to ozone oxidation treatment and aerobic biological treatment are subjected to high-efficiency catalytic oxidation decomposition, and finally the strong brine with salt and organic matters removed enters a clean water tank 22.
One specific application example of the present disclosure is as follows:
in a sewage treatment plant in an industrial park, the wastewater regeneration is realized by adopting the ultrafiltration and reverse osmosis process, the reverse osmosis strong brine is generated, the hardness fluctuates at 1400-1800mg/L, and the highest hardness reaches 2200 mg/L.
The reverse osmosis strong brine firstly enters a crystallizer 3, the crystallization retention time is 90min, and 1.5-2.5g/LCaSO is added4.2H20 seed crystal induced crystallization, the chemical adding concentration of the scale inhibitor remover is 100-200ppm, the hardness of the effluent is influenced by multiple factors such as the quality of inlet water, temperature, concentration of crystal slurry and the like, the fluctuation is 700mg/L at 600-200 ppm, and the hardness removal rate is stabilized at 55-65%; after being treated by a thickener 5 and dewatered by a centrifuge 6, the CaSO is realized4And (4) recycling.
After being treated by the crystallization device 100, the strong brine sequentially enters a first-stage ozone contact tank 9, a first-stage biochemical aerobic tank 10, a second-stage ozone contact tank 11 and a second-stage biochemical aerobic tank 12. The concentration of ozone in the primary ozone contact tank 9 is 15mg/L, the ventilation volume is 1.5L/min, and the retention time is 3 h; the first-stage biochemical aerobic tank 10 stays for 3 hours, and the dissolved oxygen concentration is controlled to be 3.5 g/L; the concentration of ozone in the secondary ozone contact tank 11 is 5mg/L, the ventilation volume is 1.5L/min, and the retention time is 1 h; the residence time of the secondary biochemical aerobic tank 12 is 3 hours, and the dissolved oxygen concentration is controlled to be 2 mg/L. Along with the change of upstream water quality, the concentrated brine (chemical oxygen Demand, COD for short) after crystallization treatment fluctuates within the range of 140-200mg/L, and after the concentrated brine is treated by an ozone contact tank and a biochemical aerobic tank, the COD of the concentrated brine is stabilized between 40-50mg/L, thereby reaching the first grade A standard of pollutant discharge Standard of urban sewage treatment plant (GB 18918-2002).
Then the concentrated brine enters a homogeneous reaction tank 13, after 1h of catalytic oxidation by a catalyst and ozone, the final COD of the treated effluent is within the range of 20-30mg/L, and the ozone addition removal ratio is O3Δ COD was approximately 1.2: 1.
it is noted that, in this document, relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.
The foregoing are merely exemplary embodiments of the present disclosure, which enable those skilled in the art to understand or practice the present disclosure. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the disclosure. Thus, the present disclosure is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (10)
1. A reverse osmosis strong brine treatment system is characterized by comprising a crystallization device (100), an ozone-biochemical treatment device (200) and a homogeneous catalytic oxidation device (300) which are used for treating strong brine in sequence;
the crystallization device (100) is provided with a liquid inlet end for feeding strong brine, and the crystallization device (100) is used for carrying out crystallization treatment on the strong brine; the liquid inlet end of the ozone-biochemical treatment device (200) is communicated with the liquid outlet end of the crystallization device (100), and the ozone-biochemical treatment device (200) is used for carrying out ozone oxidation and aerobic biochemical treatment on the concentrated brine treated by the crystallization device (100); the liquid inlet end of the homogeneous catalytic oxidation device (300) is communicated with the liquid outlet end of the ozone-biochemical treatment device (200), and a catalyst and ozone are introduced into the homogeneous catalytic oxidation device (300) and are used for carrying out catalytic oxidation treatment on the concentrated brine treated by the ozone-biochemical treatment device (200).
2. A reverse osmosis concentrated brine treatment system according to claim 1, wherein said crystallization device (100) comprises a crystallizer (3), said crystallizer (3) having a receiving cavity, said crystallizer (3) having a feed end and a first clear liquid outlet end respectively communicating with said receiving cavity, said feed end of said crystallizer (3) being formed as the feed end of said crystallization device (100);
a stirrer (4) is arranged in the accommodating cavity, and seed crystals for inducing crystallization of the concentrated brine are introduced into the accommodating cavity;
the first clear liquid outlet end is formed into at least a part of the liquid outlet end of the crystallization device (100), and the first clear liquid outlet end is communicated with the liquid inlet end of the ozone-biochemical treatment device (200).
3. A reverse osmosis concentrated brine treatment system according to claim 2, wherein the crystallization device (100) further comprises a thickener (5) and a centrifuge (6), the liquid inlet end of the thickener (5) is communicated with the concentrated liquid outlet end of the crystallizer (3), and the thickener (5) is used for concentrating the concentrated brine treated by the crystallizer (3); the thickener (5) is provided with a second clear liquid outlet end communicated with the ozone-biochemical treatment device (200);
the liquid inlet end of the centrifuge (6) is communicated with the concentrated liquid outlet end of the thickener (5), and the centrifuge (6) is provided with a third clear liquid outlet end communicated with the ozone-biochemical treatment device (200).
4. A reverse osmosis concentrated brine treatment system according to claim 2, wherein said crystallization device (100) further comprises a dosing tank (7) and a dosing pump (8);
the descaling agent remover is communicated with the dosing tank (7), the inlet end of the dosing pump (8) is communicated with the medicine outlet of the dosing tank (7), and the outlet end of the dosing pump (8) is communicated with the accommodating cavity.
5. A reverse osmosis concentrated brine treatment system according to any one of claims 1 to 4, wherein said ozone-biochemical treatment unit (200) comprises at least one ozone contact tank and at least one biochemical aerobic tank; the liquid inlet end of the ozone contact tank is communicated with the liquid outlet end of the crystallization device (100), and ozone is introduced into the ozone contact tank; the liquid outlet end of the ozone contact tank is communicated with the liquid inlet end of the biochemical aerobic tank, and oxygen is introduced into the biochemical aerobic tank; the liquid outlet end of the biochemical aerobic tank is communicated with the liquid inlet end of the homogeneous catalytic oxidation device (300).
6. A reverse osmosis concentrated brine treatment system according to claim 5, wherein the number of ozone contact tanks is two, namely a primary ozone contact tank (9) and a secondary ozone contact tank (11), and the concentration of ozone in the secondary ozone contact tank (11) is lower than that in the primary ozone contact tank (9);
the two biochemical aerobic tanks are respectively a primary biochemical aerobic tank (10) and a secondary biochemical aerobic tank (12), and the concentration of dissolved oxygen in the secondary biochemical aerobic tank (12) is lower than that in the primary biochemical aerobic tank (10);
the feed liquor end of one-level ozone contact tank (9) with the play liquid end intercommunication of crystallization device (100), one-level ozone contact tank (9) biochemical good oxygen pond (10) of one-level second grade ozone contact tank (11) and biochemical good oxygen pond (12) of second grade, the play liquid end of biochemical good oxygen pond of second grade (12) with the feed liquor end intercommunication of homogeneous phase catalytic oxidation device (300).
7. A reverse osmosis concentrated brine treatment system according to claim 5, wherein a biological filler (14) is arranged in the biochemical aerobic tank;
and/or the reverse osmosis concentrated brine treatment system further comprises a blower (15), and the biochemical aerobic tank is provided with an oxygen inlet communicated with the blower (15).
8. A reverse osmosis concentrated brine treatment system according to claim 5, further comprising an ozone generation device, wherein the ozone generation device comprises an air separation device (16), an ozone generator (17) and an ozone aeration disc (19) which are sequentially communicated;
the ozone aeration disc (19) is arranged in both the ozone contact tank and the homogeneous catalytic oxidation device (300).
9. A reverse osmosis concentrated brine treatment system according to claim 8, further comprising an ozone recovery unit (20), wherein the inlet end of said ozone recovery unit (20) is in communication with said ozone contact tank and said homogeneous catalytic oxidation unit (300), and the outlet end of said ozone recovery unit (20) is in communication with said ozone generator (17).
10. A reverse osmosis concentrated brine treatment system according to claim 9 further comprising an ozone destruction device (21), the outlet end of the ozone recovery device (20) being in communication with the ozone destruction device (21).
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