CN217459127U - Strong brine waste water high-efficient nitrogen and phosphorus removal processing system - Google Patents
Strong brine waste water high-efficient nitrogen and phosphorus removal processing system Download PDFInfo
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- CN217459127U CN217459127U CN202121660489.7U CN202121660489U CN217459127U CN 217459127 U CN217459127 U CN 217459127U CN 202121660489 U CN202121660489 U CN 202121660489U CN 217459127 U CN217459127 U CN 217459127U
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 46
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 42
- 239000011574 phosphorus Substances 0.000 title claims abstract description 42
- 239000002351 wastewater Substances 0.000 title claims abstract description 36
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 23
- 238000012545 processing Methods 0.000 title claims description 5
- 239000012267 brine Substances 0.000 title abstract description 13
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 138
- 239000010802 sludge Substances 0.000 claims abstract description 55
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 48
- 238000005189 flocculation Methods 0.000 claims abstract description 38
- 230000016615 flocculation Effects 0.000 claims abstract description 38
- 238000005345 coagulation Methods 0.000 claims abstract description 37
- 230000015271 coagulation Effects 0.000 claims abstract description 37
- 230000003647 oxidation Effects 0.000 claims abstract description 28
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 28
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 238000012544 monitoring process Methods 0.000 claims abstract description 23
- 230000003197 catalytic effect Effects 0.000 claims abstract description 12
- 238000004519 manufacturing process Methods 0.000 claims abstract description 10
- 238000006243 chemical reaction Methods 0.000 claims description 35
- 238000004062 sedimentation Methods 0.000 claims description 30
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 22
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 20
- 150000003839 salts Chemical class 0.000 claims description 16
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 15
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 15
- 239000003814 drug Substances 0.000 claims description 13
- 238000007872 degassing Methods 0.000 claims description 12
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 claims description 8
- 239000004571 lime Substances 0.000 claims description 8
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 8
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 7
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 claims description 7
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 7
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 claims description 7
- 238000005273 aeration Methods 0.000 claims description 3
- 229920000642 polymer Polymers 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 239000008233 hard water Substances 0.000 claims description 2
- 238000001556 precipitation Methods 0.000 abstract description 2
- 229920002401 polyacrylamide Polymers 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 239000000126 substance Substances 0.000 description 7
- 239000002244 precipitate Substances 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229940037003 alum Drugs 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- 241000282414 Homo sapiens Species 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- -1 and meanwhile Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000012851 eutrophication Methods 0.000 description 2
- 239000008394 flocculating agent Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- RYQHXWDFNMMYSD-UHFFFAOYSA-O (1-methylpyridin-4-ylidene)methyl-oxoazanium Chemical compound CN1C=CC(=C[NH+]=O)C=C1 RYQHXWDFNMMYSD-UHFFFAOYSA-O 0.000 description 1
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000008235 industrial water Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 239000008239 natural water Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
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- 238000003911 water pollution Methods 0.000 description 1
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- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
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Abstract
The utility model discloses a strong brine wastewater high-efficiency nitrogen and phosphorus removal treatment system, which comprises a hardness removal multi-effect separation system, an ozone catalytic oxidation system, a biological aerated filter system, a phosphorus removal multi-effect separation system, a sludge concentration system, a water production monitoring system and a dosing system which are connected in sequence; the hardness removal multi-effect separation tank integrates coagulation, flocculation, precipitation separation and sludge concentration, and can effectively remove hardness, alkalinity and suspended matters in water; the multiple groups of ozone oxidation tanks are connected in series for operation, and meanwhile, a circulating water pump is also arranged, so that sufficient contact time between ozone and wastewater is ensured, and the high ozone utilization efficiency can be remarkably improved; NP in the waste water is treated in a targeted manner by the multi-effect dephosphorization separation tank, so that the dephosphorization efficiency of the strong brine waste water can be obviously improved.
Description
Technical Field
The utility model belongs to the technical field of the high-efficient nitrogen and phosphorus removal of strong brine waste water is handled, concretely relates to high-efficient nitrogen and phosphorus removal processing system of strong brine waste water.
Background
With the continuous development of industry in recent years, the phenomenon of water resource shortage is becoming more severe, and improving the water reuse rate becomes a key way for solving the industrial development and water resource shortage. The coal chemical industry enterprises are water consumers, follow the principle of improving the water reuse rate and saving fresh water, and rapidly develop technologies such as concentrated water reverse osmosis, circulating water high-concentration multiple operation, reclaimed water reuse and the like, so that on one hand, a large amount of process wastewater can be converted into high-quality water required by industrial water, but a considerable part of concentrated salt wastewater with high salt content, high COD (chemical oxygen demand), high total nitrogen and high total phosphorus can be generated.
If the concentrated salt wastewater is not treated or is not treated properly, the concentrated salt wastewater is directly discharged into a natural water body, so that the water resource is seriously polluted. The problem of water pollution caused by nitrogen and phosphorus is increasingly prominent, nitrogen substances have great harm to water body environment and human beings, ammonia nitrogen consumes dissolved oxygen in water body, and nitrogen-containing compounds have toxic action on human beings and other organisms; the phosphorus substance can accelerate the eutrophication process of the water body, and the eutrophication is a water quality pollution phenomenon caused by excessive content of plant nutrient substances (mainly phosphorus), such as nitrogen, phosphorus and the like. Therefore, how to remove nitrogen and phosphorus substances in water becomes an unavoidable problem in the field of high-salt wastewater treatment, and the exploration of a high-efficiency nitrogen and phosphorus removal treatment system for strong-salt wastewater is particularly important.
The existing technology for removing nitrogen and phosphorus from concentrated salt wastewater mainly adopts an A2/O technology, but is limited by factors such as carbon source competition, sludge age contradiction and the like, and the A2/O technology has many defects in the actual treatment process, such as relatively low treatment efficiency, incomplete treatment, large occupied area of treatment equipment, high investment in one-time construction cost and the like, and in addition, when the quality of incoming water of high-concentration brine fluctuates greatly, the A2/O technology has poor stability of the effect of removing nitrogen and phosphorus.
In order to compensate the deficiency of the current strong brine wastewater nitrogen and phosphorus removal treatment technology, the utility model provides a high-efficient nitrogen and phosphorus removal system of strong brine wastewater.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a strong brine waste water high efficiency nitrogen and phosphorus removal processing system to solve the problem that proposes in the above-mentioned background art.
In order to achieve the above object, the utility model provides a following technical scheme: a strong brine wastewater high-efficiency nitrogen and phosphorus removal treatment system comprises a hardness removal multiple-effect separation system, an ozone catalytic oxidation system, an aeration biological filter system, a phosphorus removal multiple-effect separation system, a sludge concentration system, a produced water monitoring system and a dosing system which are sequentially connected; the hardness-removing multi-effect separation system comprises a hardness-removing reaction tank, a hardness-removing coagulation tank, a hardness-removing flocculation tank, a hardness-removing sedimentation tank and a hardness-removing drainage tank; the water outlet of the hardness removing reaction tank is connected with the water inlet of a hardness removing coagulation tank, the water outlet of the hardness removing coagulation tank is connected with the water inlet of a hardness removing flocculation tank, the water outlet of the hardness removing flocculation tank is connected with the water inlet of a hardness removing sedimentation tank, and the water outlet of the hardness removing sedimentation tank is connected with the water inlet of a hardness removing drainage tank;
the ozone catalytic oxidation system comprises an ozone oxidation tank and an ozone degassing tank; the water outlet of the hard water removal and drainage pool is connected with the water inlet of the ozone oxidation pool, and the water outlet of the ozone oxidation pool is connected with the water inlet of the ozone degassing pool;
the biological aerated filter system comprises a BAF-CN pool, a BAF-DN pool and a BAF water production pool; the water outlet of the ozone degassing pool is connected with the water inlet of the BAF-CN pool through a BAF lifting pump, the water outlet of the BAF-CN pool is connected with the water inlet of the BAF-DN pool, and the water outlet of the BAF-DN pool is connected with the water inlet of the BAF water producing pool;
the multi-effect dephosphorization separation system comprises a dephosphorization reaction tank, a dephosphorization coagulation tank, a dephosphorization flocculation tank, a dephosphorization sedimentation tank and a dephosphorization drainage tank; a water outlet of the BAF water producing tank is connected with a water inlet of the dephosphorization reaction tank through a lift pump; the water outlet of the dephosphorization reaction tank is connected with the water inlet of the dephosphorization coagulation tank, the water outlet of the dephosphorization coagulation tank is connected with the water inlet of the dephosphorization flocculation tank, the water outlet of the dephosphorization flocculation tank is connected with the water inlet of the dephosphorization sedimentation tank, and the water outlet of the dephosphorization sedimentation tank is connected with the water inlet of the dephosphorization drainage tank;
the sludge concentration system comprises a sludge concentration tank and a plate-and-frame filter press; the sludge outlets of the hard removal sedimentation tank and the phosphorus removal sedimentation tank are connected with the sludge inlet of the sludge concentration tank through a sludge discharge pump, and the sludge outlet of the sludge concentration tank is connected with the plate-and-frame filter press through a sludge delivery pump;
the water production monitoring system comprises a monitoring pool and an accident pool; the water outlet of the dephosphorization drainage pool is connected with the water inlet of the monitoring pool through a lift pump, one water outlet of the monitoring pool is communicated with the outside, and the other water outlet of the monitoring pool is connected with the accident pool;
the dosing system comprises a sodium carbonate dosing system, a lime dosing system, a ferric trichloride dosing system, a PAM dosing system, a sodium hydroxide dosing system, a sulfuric acid dosing system, a sodium bisulfite dosing system and a methanol dosing system; the sodium carbonate dosing system is connected with the hardness removal reaction tank through a pipeline; the lime dosing system is connected with the hardness removal reaction tank through a pipeline; the ferric trichloride dosing system is respectively connected with the hard removing coagulation tank and the phosphorus removing coagulation tank through pipelines; the PAM dosing system is respectively connected with the hard-removing flocculation tank, the dephosphorization flocculation tank and the pipeline; the sodium hydroxide dosing system is connected with the hard flocculation removal tank through a pipeline; the sulfuric acid dosing system is connected with the hard removal drainage pool through a pipeline; the sodium bisulfite dosing system and the methanol dosing system are respectively connected with the water inlet of the BAF-DN pool through pipelines.
Preferably, a stirrer is arranged in the hard removing coagulation tank, and a sludge densimeter is arranged in the sludge concentration tank.
Preferably, a polymer feeding system is arranged inside the hard flocculation removal tank.
Preferably, the water inlet of the hardness removal reaction tank is connected with a strong salt wastewater conveying pipe, and the water outlet of the BAF-DN tank is provided with a reflux device.
Preferably, the ozone catalytic oxidation system further comprises a circulating water pump.
Compared with the prior art, the beneficial effects of the utility model are that: the hardness removal multi-effect separation tank integrates coagulation, flocculation, precipitation separation and sludge concentration, and can effectively remove hardness, alkalinity and suspended matters in water; the multiple groups of ozone oxidation tanks are connected in series for operation, and meanwhile, a circulating water pump is also arranged, so that sufficient contact time between ozone and wastewater is ensured, and the high ozone utilization efficiency can be obviously improved; the biological aerated filter system can realize biological denitrification and carbon removal of sewage; NP in the waste water is treated in the multiple-effect dephosphorization separation tank in a targeted manner, and the dephosphorization efficiency of the strong brine waste water can be obviously improved.
Drawings
FIG. 1 is a schematic view of the system of the present invention;
in the figure: 1-a hardness-removing multi-effect separation system; 1.1-a hardness removing reaction tank, 1.2-a hardness removing coagulation tank, 1.3-a hardness removing flocculation tank, 1.4-a hardness removing sedimentation tank and 1.5-a hardness removing drainage tank; 2-an ozone catalytic oxidation system; 2.1-ozone oxidation tank, 2.2 ozone degassing tank; 3-a biological aerated filter system; 3.1-BAF-CN pool, 3.2-BAF-DN pool, 3.3-BAF water producing pool; 4-a multiple-effect phosphorus removal separation system; 4.1-a phosphorus removal reaction tank, 4.2-a phosphorus removal coagulation tank, 4.3-a phosphorus removal flocculation tank, 4.4-a phosphorus removal sedimentation tank and 4.5-a phosphorus removal drainage tank; 5-a sludge concentration system; 5.1-sludge concentration tank, 5.2-plate and frame filter press; 6-a water production monitoring system; 6.1-monitoring pool, 6.2-accident pool; 7-a dosing system; a 7.1-sodium carbonate dosing system, a 7.2-lime dosing system, a 7.3-ferric trichloride dosing system, a 7.4-PAM dosing system, a 7.5-sodium hydroxide dosing system, a 7.6-sulfuric acid dosing system, a 7.7-sodium bisulfite dosing system, and a 7.8-methanol dosing system.
Detailed Description
The technical solutions in the embodiments of the present invention will be described clearly and completely with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only some embodiments of the present invention, not all embodiments. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative work belong to the protection scope of the present invention.
Example 1
As shown in figure 1, the concentrated salt wastewater high-efficiency nitrogen and phosphorus removal treatment system comprises a hardness removal multiple-effect separation system 1, an ozone catalytic oxidation system 2, a biological aerated filter system 3, a phosphorus removal multiple-effect separation system 4, a sludge concentration system 5, a water production monitoring system 6 and a dosing system 7 which are sequentially connected.
Further, the hardness-removing multi-effect separation system 1 comprises a hardness-removing reaction tank 1.1, a hardness-removing coagulation tank 1.2, a hardness-removing flocculation tank 1.3, a hardness-removing sedimentation tank 1.4 and a hardness-removing drainage tank 1.5; the strong brine wastewater automatically flows into a hardness removal reaction tank 1.1 through a distribution channel; the effluent of the reaction tank for removing hardness 1.1 automatically flows into a coagulation tank for removing hardness 1.2, the effluent of the coagulation tank for removing hardness 1.2 automatically flows into a flocculation tank for removing hardness 1.3, the effluent of the flocculation tank for removing hardness 1.3 automatically flows into a sedimentation tank for removing hardness 1.4, and the effluent of the sedimentation tank for removing hardness 1.4 automatically flows into a drainage tank for removing hardness 1.5.
Further, the ozone catalytic oxidation system 2 comprises an ozone oxidation tank 2.1 and an ozone degassing tank 2.2; the effluent of the hard removing drainage pool 1.5 enters an ozone oxidation pool 2.1 through a hard removing lift pump, and the effluent of the ozone oxidation pool 2.1 enters an ozone degassing pool 2.2.
Further, the biological aerated filter system 3 comprises a BAF-CN pool 3.1, a BAF-DN pool 3.2 and a BAF water production pool 3.3; the effluent of the ozone degassing pool 2.2 enters a BAF-CN pool 3.1 through a BAF lifting pump, the effluent of the BAF-CN pool 3.1 automatically flows into the BAF-DN pool 3.2, and the effluent of the BAF-DN pool 3.2 automatically flows into the BAF water production pool 3.3.
Further, the multiple-effect dephosphorization separation system 4 comprises a dephosphorization reaction tank 4.1, a dephosphorization coagulation tank 4.2, a dephosphorization flocculation tank 4.3, a dephosphorization sedimentation tank 4.4 and a dephosphorization drainage tank 4.5; the effluent of the BAF water producing tank 3.3 enters a dephosphorization reaction tank 4.1 through a lift pump. The effluent of the dephosphorization reaction tank 4.1 automatically flows into a dephosphorization coagulation tank 4.2, the effluent of the dephosphorization coagulation tank 4.2 automatically flows into a dephosphorization flocculation tank 4.3, the effluent of the dephosphorization flocculation tank 4.3 automatically flows into a dephosphorization sedimentation tank 4.4, and the effluent of the dephosphorization sedimentation tank 4.4 automatically flows into a dephosphorization drainage tank 4.5.
Further, the sludge concentration system 5 comprises a sludge concentration tank 5.1 and a plate-and-frame filter press 5.2; the sludge discharged from the hard removal sedimentation tank 1.4 and the phosphorus removal sedimentation tank 4.4 is conveyed to a sludge concentration tank 5.1 by a sludge discharge pump, and the sludge discharged from the sludge concentration tank 5.1 enters a plate-and-frame filter press 5.2 by a sludge conveying pump.
Further, the water production monitoring system 6 comprises a monitoring pool 6.1 and an accident pool 6.2; and 4.5, the effluent of the dephosphorization drainage pool enters a monitoring pool 6.1 through a lift pump for water quality monitoring, and is discharged or used for other purposes if the water quality is qualified, and is discharged into an accident pool 6.2 if the water quality is unqualified.
Further, the dosing system comprises a sodium carbonate dosing system 7.1, a lime dosing system 7.2, an iron trichloride dosing system 7.3, a PAM dosing system 7.4, a sodium hydroxide dosing system 7.5, a sulfuric acid dosing system 7.6, a sodium bisulfite dosing system 7.7 and a methanol dosing system 7.8; the sodium carbonate dosing system 7.1 is connected with the hardness removal reaction tank 1.1 through a pipeline; the lime dosing system 7.2 is connected with the hardness removal reaction tank 1.1 through a pipeline; the ferric trichloride dosing system 7.3 is respectively connected with the hard removing coagulation tank 1.2 and the phosphorus removing coagulation tank 4.2 through pipelines; a PAM dosing system 7.4 is respectively connected with the hard removal flocculation tank 1.3 and the dephosphorization flocculation tank 4.3 through pipelines; the sodium hydroxide dosing system 7.5 is connected with the hard flocculation removal tank 1.3 through a pipeline; the sulfuric acid dosing system 7.6 is connected with the hard removal drainage pool 1.5 through a pipeline; and a sodium bisulfite dosing system 7.7 and a methanol dosing system 7.8 are respectively connected with a water inlet of the-DN pool 3.2 through pipelines.
Further, a stirrer is arranged in the hard removing coagulation tank 1.2, the front floc can be formed by controlling the rotating speed of the stirrer and the hydraulic retention time, and a sludge densimeter is arranged in the sludge concentration tank.
Further, a polymer adding system is arranged in the hard flocculation removal tank 1.3, so that a good forming environment can be provided for alum floc in a flocculation area.
Furthermore, the water inlet of the hardness removal reaction tank 1.1 is connected with a strong brine wastewater conveying pipe, and the water outlet of the BAF-DN tank 3.2 is provided with a reflux device, so that the reactions such as denitrification and the like can be flexibly adjusted according to the quality condition of the incoming water, and the TN of the outgoing water can be controlled below 10 mg/L.
Further, ozone catalytic oxidation system 2 still includes circulating water pump, guarantees that ozone and waste water have sufficient contact time to improve ozone utilization efficiency.
The utility model discloses a theory of operation and use flow: the concentrated salt wastewater automatically flows through a distribution channel and firstly enters a hardness removal reaction tank 1.1, and then a sodium carbonate dosing system 7.1 and a lime dosing system 7.2 respectively dose corresponding agents into the concentrated salt wastewater to react with alkalinity and calcium and magnesium hardness ions in water to form micro-precipitates;
after water produced by the hardness removing reaction tank 1.1 enters a hardness removing coagulation tank 1.2, a ferric trichloride dosing system 7.3 adds corresponding agents to carry out coagulation reaction, and fine alum floc is formed;
the effluent of the hard removing coagulation tank 1.2 enters a hard removing flocculation tank 1.3, a flocculating agent is added by a PAM (polyacrylamide) dosing system 7.4, so that alumen ustum collision adsorption bridging grows up to form large precipitates, and meanwhile, sludge reflowing from the rear hard removing sedimentation tank 1.4 is mixed with the inlet water, so that the contact area is increased, and the adhesion of the precipitates is facilitated;
the effluent of the hardness-removing flocculation tank 1.3 enters a hardness-removing sedimentation tank 1.4 for separation and removal, the upper clear liquid is collected by a water collecting tank and enters a hardness-removing drainage tank 1.5, and a sulfuric acid dosing system 7.6 is lifted by a pump to enter a lower ozone catalytic oxidation system 2 for continuous treatment after the pH value is adjusted by adding a medicament; a sludge densimeter is arranged to detect the sludge concentration of the sludge concentration tank 5.1, and the redundant sludge is discharged into a sludge disposal tank 5.1 through a lifting pump at regular time;
the effluent of the hard removal drainage pool 1.5 enters an ozone oxidation pool 2.1, a plurality of groups of ozone oxidation pools 2.1 run in a series connection mode, and meanwhile, a circulating water pump is arranged to ensure that the ozone and the wastewater have sufficient contact time so as to improve the utilization efficiency of the ozone; the ozone and the wastewater are mixed by adopting the ejector, so that the defects that the microporous aeration disc is easy to scale and block, difficult to overhaul underwater and the like can be avoided;
the effluent of the ozone oxidation tank 2.1 automatically flows into an ozone degassing tank 2.2, and after stably releasing residual ozone, the effluent is lifted by a pump to enter a subordinate biological aerated filter system 3 for continuous treatment;
the effluent of the ozone degassing pool 2.2 enters a BAF-CN pool 3.1, and BOD, COD, NH4-N, SS and other harmful substances are effectively removed through technologies such as biological membrane oxidation, filter material adsorption, filtration and the like, and the main purpose is to remove carbon sources and ammonia nitrogen;
before the effluent of the BAF-CN pool 3.1 automatically flows into the BAF-DN pool 3.2, a sodium bisulfite dosing system 7.7 and a methanol dosing system 7.8 are respectively added with corresponding medicaments and mixed with the corresponding medicaments to create favorable conditions for the subsequent denitrification reaction; the effluent of the BAF-DN pool 3.2 enters a BAF water producing pool 3.3 and then is treated continuously by a subordinate phosphorus removal multi-effect separation system 4;
the BAF water producing pool 3.3 automatically flows into a dephosphorization reaction pool 4.1 through a distribution channel, and micro sol is formed by stirring suspended matters in water and the like;
the water discharged from the phosphorus removal reaction tank 4.1 enters a phosphorus removal coagulation tank 4.2, and a ferric trichloride dosing system 7.3 adds corresponding reagents to carry out coagulation reaction to form fine alum floc;
the water discharged from the dephosphorization coagulation tank 4.2 enters a dephosphorization flocculation zone tank 4.3, a flocculating agent is added by a PAM (polyacrylamide) dosing system 7.4, so that alumen ustum collision adsorption bridges grow to form large precipitates, and meanwhile, sludge reflowing from the rear dephosphorization sedimentation tank 4.4 is mixed with the water inlet, so that the contact area is increased, and the adhesion of the precipitates is facilitated;
the effluent of the dephosphorization flocculation tank 4.3 enters a dephosphorization sedimentation tank 4.4 for separation and removal, and the supernatant is collected by a water collecting tank and enters a dephosphorization drainage tank 1.5 and is lifted by a pump and drained into a monitoring water tank 6.1; the monomer has less mud amount, controls the mud amount in a mud concentration area according to a mud level meter, and discharges the mud into a mud tank 5.1 through a lifting pump at regular time;
the sludge concentration tank 5.1 reduces the water content and the volume of the sludge concentration tank through sludge thickening, so that the subsequent treatment cost is reduced; concentrated sludge produced by the sludge concentration tank 5.1 enters a plate-and-frame filter press 5.2 through a sludge feed pump so as to realize the sludge-water separation process of the sludge;
the monitoring pool 6.1 is provided with an online monitoring instrument, if the water quality is qualified, the water is discharged or used for other purposes, and if the water quality is not qualified, the water is discharged to the accident pool 6.2.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (5)
1. The utility model provides a strong salt waste water high efficiency nitrogen and phosphorus removal processing system which characterized in that: comprises a hardness-removing multi-effect separation system (1), an ozone catalytic oxidation system (2), an aeration biological filter tank system (3), a phosphorus-removing multi-effect separation system (4), a sludge concentration system (5), a water production monitoring system (6) and a medicine adding system (7) which are connected in sequence; the multi-effect hardness-removing separation system (1) comprises a hardness-removing reaction tank (1.1), a hardness-removing coagulation tank (1.2), a hardness-removing flocculation tank (1.3), a hardness-removing sedimentation tank (1.4) and a hardness-removing drainage tank (1.5); the water outlet of the hardness removing reaction tank (1.1) is connected with the water inlet of a hardness removing coagulation tank (1.2), the water outlet of the hardness removing coagulation tank (1.2) is connected with the water inlet of a hardness removing flocculation tank (1.3), the water outlet of the hardness removing flocculation tank (1.3) is connected with the water inlet of a hardness removing sedimentation tank (1.4), and the water outlet of the hardness removing sedimentation tank (1.4) is connected with the water inlet of a hardness removing drainage tank (1.5);
the ozone catalytic oxidation system (2) comprises an ozone oxidation tank (2.1) and an ozone degassing tank (2.2); the water outlet of the hard water discharge tank (1.5) is connected with the water inlet of the ozone oxidation tank (2.1), and the water outlet of the ozone oxidation tank (2.1) is connected with the water inlet of the ozone degassing tank (2.2);
the biological aerated filter system (3) comprises a BAF-CN pool (3.1), a BAF-DN pool (3.2) and a BAF water producing pool (3.3); the water outlet of the ozone degassing pool (2.2) is connected with the water inlet of a BAF-CN pool (3.1) through a BAF lift pump, the water outlet of the BAF-CN pool (3.1) is connected with the water inlet of the BAF-DN pool (3.2), and the water outlet of the BAF-DN pool (3.2) is connected with the water inlet of the BAF water producing pool (3.3);
the multiple-effect dephosphorization separation system (4) comprises a dephosphorization reaction tank (4.1), a dephosphorization coagulation tank (4.2), a dephosphorization flocculation tank (4.3), a dephosphorization sedimentation tank (4.4) and a dephosphorization drainage tank (4.5); the water outlet of the BAF water producing tank (3.3) is connected with the water inlet of the dephosphorization reaction tank (4.1) through a lift pump; the water outlet of the dephosphorization reaction tank (4.1) is connected with the water inlet of the dephosphorization coagulation tank (4.2), the water outlet of the dephosphorization coagulation tank (4.2) is connected with the water inlet of the dephosphorization flocculation tank (4.3), the water outlet of the dephosphorization flocculation tank (4.3) is connected with the water inlet of the dephosphorization sedimentation tank (4.4), and the water outlet of the dephosphorization sedimentation tank (4.4) is connected with the water inlet of the dephosphorization drainage tank (4.5);
the sludge concentration system (5) comprises a sludge concentration tank (5.1) and a plate-and-frame filter press (5.2); the sludge outlets of the hard removal sedimentation tank (1.4) and the phosphorus removal sedimentation tank (4.4) are connected with the sludge inlet of the sludge concentration tank (5.1) through a sludge discharge pump, and the sludge outlet of the sludge concentration tank (5.1) is connected with the plate-and-frame filter press (5.2) through a sludge delivery pump;
the water production monitoring system (6) comprises a monitoring pool (6.1) and an accident pool (6.2); a water outlet of the dephosphorization drainage pool (4.5) is connected with a water inlet of the monitoring pool (6.1) through a lift pump, one water outlet of the monitoring pool (6.1) is communicated with the outside, and the other water outlet of the monitoring pool (6.1) is connected with the accident pool (6.2);
the medicine adding system (7) comprises a sodium carbonate medicine adding system (7.1), a lime medicine adding system (7.2), an iron trichloride medicine adding system (7.3), a PAM medicine adding system (7.4), a sodium hydroxide medicine adding system (7.5), a sulfuric acid medicine adding system (7.6), a sodium bisulfite medicine adding system (7.7) and a methanol medicine adding system (7.8); the sodium carbonate dosing system (7.1) is connected with the hardness removal reaction tank (1.1) through a pipeline; the lime dosing system (7.2) is connected with the hardness removal reaction tank (1.1) through a pipeline; the ferric trichloride dosing system (7.3) is respectively connected with the hard removing coagulation tank (1.2) and the phosphorus removing coagulation tank (4.2) through pipelines; a PAM dosing system (7.4) is respectively connected with the deflocculating pool (1.3) and the dephosphorizing flocculation pool (4.3) through pipelines; the sodium hydroxide dosing system (7.5) is connected with the hard flocculation removal tank (1.3) through a pipeline; the sulfuric acid dosing system (7.6) is connected with the hard removal drainage pool (1.5) through a pipeline; the sodium bisulfite dosing system (7.7) and the methanol dosing system (7.8) are respectively connected with the water inlet of the BAF-DN pool (3.2) through pipelines.
2. The system for efficiently removing nitrogen and phosphorus from concentrated salt wastewater according to claim 1, which is characterized in that: a stirrer is arranged in the hard removing coagulation tank (1.2), and a sludge densimeter is arranged in the sludge concentration tank.
3. The system for efficiently removing nitrogen and phosphorus from concentrated salt wastewater according to claim 1, which is characterized in that: and a polymer adding system is arranged in the hard flocculation removal tank (1.3).
4. The system for efficiently removing nitrogen and phosphorus from concentrated salt wastewater according to claim 1, which is characterized in that: the water inlet of the hardness removal reaction tank (1.1) is connected with a concentrated salt wastewater conveying pipe, and the water outlet of the BAF-DN tank (3.2) is provided with a reflux device.
5. The system for efficiently removing nitrogen and phosphorus from concentrated salt wastewater according to claim 1, which is characterized in that: the ozone catalytic oxidation system (2) also comprises a circulating water pump.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116217001A (en) * | 2023-03-22 | 2023-06-06 | 华自格兰特环保科技(北京)有限公司 | A high-salt wastewater treatment device and method |
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