CN113735333A - Water treatment system and method - Google Patents
Water treatment system and method Download PDFInfo
- Publication number
- CN113735333A CN113735333A CN202111218005.8A CN202111218005A CN113735333A CN 113735333 A CN113735333 A CN 113735333A CN 202111218005 A CN202111218005 A CN 202111218005A CN 113735333 A CN113735333 A CN 113735333A
- Authority
- CN
- China
- Prior art keywords
- reverse osmosis
- treatment
- water
- osmosis concentrated
- concentrated water
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 287
- 238000000034 method Methods 0.000 title claims abstract description 32
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 134
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 106
- 238000006243 chemical reaction Methods 0.000 claims abstract description 87
- 210000002700 urine Anatomy 0.000 claims abstract description 86
- 150000003017 phosphorus Chemical class 0.000 claims abstract description 65
- 229910052567 struvite Inorganic materials 0.000 claims abstract description 55
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 claims abstract description 52
- 230000003647 oxidation Effects 0.000 claims abstract description 50
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 50
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 claims abstract description 43
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 claims abstract description 38
- 229910001425 magnesium ion Inorganic materials 0.000 claims abstract description 38
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 31
- 239000011574 phosphorus Substances 0.000 claims abstract description 31
- 239000002244 precipitate Substances 0.000 claims abstract description 17
- 238000004659 sterilization and disinfection Methods 0.000 claims abstract description 10
- 239000000203 mixture Substances 0.000 claims description 74
- 238000000926 separation method Methods 0.000 claims description 54
- 238000003860 storage Methods 0.000 claims description 43
- 238000001556 precipitation Methods 0.000 claims description 30
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims description 22
- 159000000003 magnesium salts Chemical class 0.000 claims description 21
- 238000002156 mixing Methods 0.000 claims description 18
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 15
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims description 11
- 235000019341 magnesium sulphate Nutrition 0.000 claims description 11
- 239000007788 liquid Substances 0.000 claims description 10
- 239000013589 supplement Substances 0.000 claims description 7
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 claims description 6
- 229910001424 calcium ion Inorganic materials 0.000 claims description 6
- 238000004062 sedimentation Methods 0.000 claims description 6
- 230000001360 synchronised effect Effects 0.000 claims description 6
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 5
- 239000012141 concentrate Substances 0.000 claims description 4
- 239000000126 substance Substances 0.000 abstract description 23
- 231100000331 toxic Toxicity 0.000 abstract description 8
- 230000002588 toxic effect Effects 0.000 abstract description 8
- 230000009286 beneficial effect Effects 0.000 abstract description 5
- 238000005273 aeration Methods 0.000 description 32
- 239000012528 membrane Substances 0.000 description 22
- 230000002572 peristaltic effect Effects 0.000 description 22
- 239000012510 hollow fiber Substances 0.000 description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 20
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 16
- 239000001301 oxygen Substances 0.000 description 16
- 229910052760 oxygen Inorganic materials 0.000 description 16
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 14
- 229910019142 PO4 Inorganic materials 0.000 description 14
- 239000000945 filler Substances 0.000 description 14
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 13
- 239000003344 environmental pollutant Substances 0.000 description 13
- 239000007789 gas Substances 0.000 description 13
- 231100000719 pollutant Toxicity 0.000 description 13
- 239000000178 monomer Substances 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 10
- 238000003756 stirring Methods 0.000 description 10
- 239000003814 drug Substances 0.000 description 9
- 238000010992 reflux Methods 0.000 description 8
- 239000004698 Polyethylene Substances 0.000 description 7
- 229920003023 plastic Polymers 0.000 description 7
- 239000004033 plastic Substances 0.000 description 7
- -1 polyethylene Polymers 0.000 description 7
- 229920000573 polyethylene Polymers 0.000 description 7
- NLKNQRATVPKPDG-UHFFFAOYSA-M potassium iodide Chemical compound [K+].[I-] NLKNQRATVPKPDG-UHFFFAOYSA-M 0.000 description 7
- 238000005086 pumping Methods 0.000 description 6
- 239000002699 waste material Substances 0.000 description 6
- CKMXBZGNNVIXHC-UHFFFAOYSA-L ammonium magnesium phosphate hexahydrate Chemical compound [NH4+].O.O.O.O.O.O.[Mg+2].[O-]P([O-])([O-])=O CKMXBZGNNVIXHC-UHFFFAOYSA-L 0.000 description 5
- 244000005700 microbiome Species 0.000 description 5
- 229920002635 polyurethane Polymers 0.000 description 5
- 239000004814 polyurethane Substances 0.000 description 5
- 239000011777 magnesium Substances 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 230000002195 synergetic effect Effects 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- 238000005192 partition Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- 208000005156 Dehydration Diseases 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 150000004714 phosphonium salts Chemical class 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- AAKBLFQBZDFKMP-UHFFFAOYSA-H trimagnesium azane diphosphate Chemical compound N.[Mg+2].[Mg+2].[Mg+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O AAKBLFQBZDFKMP-UHFFFAOYSA-H 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 239000002033 PVDF binder Substances 0.000 description 1
- 238000012271 agricultural production Methods 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000010000 carbonizing Methods 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 239000000149 chemical water pollutant Substances 0.000 description 1
- 230000008094 contradictory effect Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000000593 degrading effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 229910000397 disodium phosphate Inorganic materials 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011049 filling Methods 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
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 230000007096 poisonous effect Effects 0.000 description 1
- 229920002981 polyvinylidene fluoride Polymers 0.000 description 1
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Inorganic materials [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 1
- 235000010333 potassium nitrate Nutrition 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000028327 secretion Effects 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- AJPJDKMHJJGVTQ-UHFFFAOYSA-M sodium dihydrogen phosphate Chemical compound [Na+].OP(O)([O-])=O AJPJDKMHJJGVTQ-UHFFFAOYSA-M 0.000 description 1
- 229910000162 sodium phosphate Inorganic materials 0.000 description 1
- 229910000406 trisodium phosphate Inorganic materials 0.000 description 1
- 238000000108 ultra-filtration Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B25/00—Phosphorus; Compounds thereof
- C01B25/16—Oxyacids of phosphorus; Salts thereof
- C01B25/26—Phosphates
- C01B25/45—Phosphates containing plural metal, or metal and ammonium
- C01B25/451—Phosphates containing plural metal, or metal and ammonium containing metal and ammonium
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5281—Installations for water purification using chemical agents
-
- 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
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- 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
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
Abstract
The invention discloses a water treatment system and a method, wherein the method comprises the following steps: providing reverse osmosis concentrated water to be treated and source separated urine; carrying out ozone oxidation treatment on the reverse osmosis concentrated water to realize disinfection treatment on the reverse osmosis concentrated water and convert low-valence phosphorus in the reverse osmosis concentrated water into high-valence phosphorus salt; and (3) carrying out mixed reaction on the reverse osmosis concentrated water subjected to ozone oxidation treatment and the source separated urine so as to enable magnesium ions in the reverse osmosis concentrated water, high-valence phosphorus salt and ammonia nitrogen in the source separated urine to react to generate magnesium ammonium phosphate precipitate. The water treatment method solves the problems of high salinity, toxic and harmful substances contained in the reverse osmosis concentrated water and high ammonia nitrogen content in the source separated urine, can effectively reduce the usage and dosage of magnesium ions and/or high-valence phosphorus salt required by the reaction of generating magnesium ammonium phosphate, reduces the cost, can balance the water quality, and is beneficial to the subsequent treatment of the reverse osmosis concentrated water and the source separated urine.
Description
Technical Field
The invention relates to the technical field of water treatment, in particular to a water treatment system and a water treatment method.
Background
The source separated urine is rich in ammonia nitrogen which is an important component of the fertilizer, and the ammonia nitrogen in the source separated urine is recycled, so that the problem of high ammonia nitrogen load of inlet water of a sewage treatment plant can be solved, and the quality of outlet water is improved; on the other hand, the recovered product can be used as a fertilizer for agricultural production, and the cyclic utilization of resources is realized.
Currently, ammonia nitrogen in source separated urine is generally recovered by adopting an ammonia magnesium phosphate precipitation technology, however, when ammonia magnesium phosphate precipitation is adopted, a large amount of magnesium salt and/or high-valence phosphorus salt needs to be added, so that the recovery cost of ammonia nitrogen in source separated urine is high, and the large-scale popularization and application of the method are limited.
Disclosure of Invention
Based on this, it is necessary to provide a water treatment system and method to solve the problems of high salinity of the reverse osmosis concentrated water, toxic and harmful substances contained in the reverse osmosis concentrated water, and high ammonia nitrogen content in the urine separated from the source, and to effectively reduce the usage and addition amount of magnesium ions and/or high valence state phosphorus salt required for the magnesium ammonium phosphate reaction, reduce the cost, and balance the water quality, which is beneficial to the subsequent treatment of the reverse osmosis concentrated water and the urine separated from the source.
A method of water treatment comprising the steps of:
providing reverse osmosis concentrated water to be treated and source separated urine;
carrying out ozone oxidation treatment on the reverse osmosis concentrated water to realize disinfection treatment on the reverse osmosis concentrated water and convert low-valence phosphorus in the reverse osmosis concentrated water into high-valence phosphorus salt, wherein the low-valence phosphorus is phosphorus with the valence less than +5, and the high-valence phosphorus salt is phosphorus with the valence equal to + 5; and
and carrying out mixed reaction on the reverse osmosis concentrated water subjected to ozone oxidation treatment and the source separation urine so as to enable magnesium ions in the reverse osmosis concentrated water, high-valence phosphorus salt and ammonia nitrogen in the source separation urine to react to generate magnesium ammonium phosphate precipitate.
In one embodiment, the step of mixing the reverse osmosis concentrated water after the ozone oxidation treatment and the source separated urine to obtain a first mixture, and the step of mixing and reacting the reverse osmosis concentrated water after the ozone oxidation treatment and the source separated urine comprises:
and adding a magnesium salt and/or the high-valence phosphorus salt into the first mixture to supplement the magnesium ions and/or the high-valence phosphorus salt required for generating the magnesium ammonium phosphate reaction.
In one embodiment, in the step of adding a magnesium salt and/or the high-valence phosphorus salt to the first mixture, the magnesium salt includes magnesium sulfate, so that sulfate ions in the magnesium sulfate react with calcium ions in the reverse osmosis concentrated water to generate calcium sulfate precipitate.
In one embodiment, the reverse osmosis concentrated water after the ozone oxidation treatment and the source separation urine are mixed and reacted to obtain a second mixture containing magnesium ammonium phosphate, and after the step of mixing and reacting the reverse osmosis concentrated water after the ozone oxidation treatment and the source separation urine, the water treatment method further comprises:
and carrying out precipitation treatment on the second mixture to realize solid-liquid separation on the second mixture.
In one embodiment, after the step of subjecting the second mixture to the precipitation treatment, the water treatment method further includes:
and carrying out advanced treatment on the water body obtained after the second mixture is subjected to precipitation treatment.
In one embodiment, the step of performing advanced treatment on the water obtained after the second mixture is subjected to precipitation treatment comprises:
and performing synchronous nitrification and denitrification treatment on the water body obtained after the second mixture is subjected to precipitation treatment.
A water treatment system comprising:
the first storage chamber is used for accommodating reverse osmosis concentrated water to be treated;
a second storage chamber for receiving source separated urine to be treated;
the ozone unit is connected with the first storage chamber and is used for carrying out ozone oxidation treatment on the reverse osmosis concentrated water output by the first storage chamber so as to realize disinfection treatment on the reverse osmosis concentrated water and convert low-valence-state phosphorus in the reverse osmosis concentrated water into high-valence-state phosphorus salt, the low-valence-state phosphorus salt is phosphorus salt with the valence of less than +5, and the high-valence-state phosphorus salt is phosphorus salt with the valence of equal to + 5; and
the first reaction chamber is used for carrying out mixed reaction on the reverse osmosis concentrated water subjected to ozone oxidation treatment and the source separation urine so as to enable magnesium ions in the reverse osmosis concentrated water, high-valence phosphorus salt and ammonia nitrogen in the source separation urine to react to generate magnesium ammonium phosphate precipitate.
In one embodiment, the reverse osmosis concentrated water output by the ozone unit and the source-separated urine output by the second storage chamber are mixed to obtain a first mixture after entering the first reaction chamber, and the water treatment system further comprises:
the dosing unit is connected with the first reaction chamber and used for adding a magnesium salt and/or the high-valence state phosphorus salt into the first mixture in the first reaction chamber so as to supplement and generate the magnesium ions and/or the high-valence state phosphorus salt required by the magnesium ammonium phosphate reaction.
In one embodiment, the reverse osmosis concentrated water after the ozone oxidation treatment in the first reaction chamber is mixed with the source separation urine to react to obtain a second mixture containing magnesium ammonium phosphate, the first reaction chamber is a sedimentation tank, and the first reaction chamber is further used for carrying out sedimentation treatment on the second mixture to realize solid-liquid separation on the second mixture.
In one embodiment, the water treatment system further comprises a deep treatment unit, the deep treatment unit is arranged at the downstream end of the first reaction chamber, and the deep treatment unit is used for performing deep treatment on the water body obtained after the second mixture is subjected to precipitation treatment in the first reaction chamber.
The water treatment method comprises the steps of firstly carrying out ozone oxidation treatment on reverse osmosis concentrated water to realize disinfection treatment on the reverse osmosis concentrated water and convert low-valence-state phosphorus in the reverse osmosis concentrated water into high-valence-state phosphorus salt, then mixing the reverse osmosis concentrated water subjected to the ozone oxidation treatment with source separation urine, wherein magnesium ions in the reverse osmosis concentrated water, the high-valence-state phosphorus salt and ammonia nitrogen in the source separation urine react to generate Magnesium Ammonium Phosphate (MAP) precipitate which can be recycled as struvite, so that effective utilization of the magnesium ions and the phosphorus in the reverse osmosis concentrated water and the ammonia nitrogen in the source separation urine can be realized by carrying out liquid-phase mixing and synergistic treatment on the reverse osmosis concentrated water subjected to the ozone oxidation treatment and the source separation urine, the waste of sewage is changed into the waste conservation, and the problems of high salinity of the reverse osmosis concentrated water, toxic and harmful substances and the high ammonia nitrogen in the source separation urine are solved, and the use dosage of magnesium ions and/or high-valence state phosphorus salt required by the reaction of generating magnesium ammonium phosphate can be effectively reduced, the cost is reduced, and simultaneously the water quality can be balanced, thereby being beneficial to the subsequent treatment of reverse osmosis concentrated water and source separation urine.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the structures shown in the drawings without creative efforts.
Fig. 1 is a schematic structural diagram of a water treatment system in an embodiment.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
It should be noted that all directional indicators (such as up, down, left, right, front, and back) in the embodiments of the present invention are only used to explain the relative position relationship between the components, the motion situation, and the like in a specific posture (as shown in the drawings), and if the specific posture is changed, the directional indicator is changed accordingly.
In addition, the descriptions related to "first", "second", etc. in the present invention are for descriptive purposes only and are not to be construed as indicating or implying relative importance or implicitly indicating the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one such feature. In addition, "and/or" in the whole text includes three schemes, taking a and/or B as an example, including a technical scheme, and a technical scheme that a and B meet simultaneously; in addition, technical solutions between various embodiments may be combined with each other, but must be realized by a person skilled in the art, and when the technical solutions are contradictory or cannot be realized, such a combination should not be considered to exist, and is not within the protection scope of the present invention.
The application provides a water treatment method, which comprises the following steps:
s100, providing reverse osmosis concentrated water to be treated and source separation urine.
In particular, reverse osmosis concentrate is an extremely difficult organic wastewater to treat that occurs in RO processes, often with high concentrations, high salinity and presenceA large amount of toxic and harmful substances, wherein the reverse osmosis concentrated water is rich in magnesium ions (Mg)2+) And low-valence phosphorus-containing substances, wherein the source separated urine is rich in ammonia Nitrogen (NH)4 +) In one embodiment, the reverse osmosis concentrate may be a reverse osmosis concentrate of landfill leachate.
S200, carrying out ozone oxidation treatment on the reverse osmosis concentrated water to realize disinfection treatment on the reverse osmosis concentrated water and convert low-valence phosphorus in the reverse osmosis concentrated water into high-valence phosphorus salt, wherein the low-valence phosphorus is phosphorus with the valence less than +5, and the high-valence phosphorus salt is phosphorus with the valence equal to + 5.
Specifically, the ozone oxidation treatment is carried out on the reverse osmosis concentrated water, so that the reverse osmosis concentrated water is primarily purified, the disinfection treatment on the reverse osmosis concentrated water can be realized, toxic and harmful substances in the reverse osmosis concentrated water are removed, the biodegradability of the reverse osmosis concentrated water is improved, and meanwhile, low-valence phosphorus-containing substances in the reverse osmosis concentrated water are converted into high-valence phosphorus salts.
The low-valence-state phosphorus-containing substances in the reverse osmosis concentrated water comprise inorganic phosphorus-containing substances and organic phosphorus-containing substances, so that the reverse osmosis concentrated water can be subjected to ozone oxidation treatment to further achieve the effect of degrading organic substances in the reverse osmosis concentrated water. Further, the higher valent phosphorus salt includes H2PO4-Salt, HPO4 2-Salt and PO4 3-At least one of salts.
Preferably, the initial pH of the reverse osmosis concentrated water is controlled to be 7-8, the contact time of the reverse osmosis concentrated water and ozone is 10min, and thus, the COD removal rate of the reverse osmosis concentrated water can reach 20% -30%.
S300, carrying out mixing reaction on the reverse osmosis concentrated water subjected to ozone oxidation treatment and the source separation urine so as to enable magnesium ions in the reverse osmosis concentrated water, high-valence phosphorus salt and ammonia nitrogen in the source separation urine to react to generate magnesium ammonium phosphate precipitate.
Specifically, after the reverse osmosis concentrated water subjected to ozone oxidation treatment and the source separation urine are mixed, magnesium ions in the reverse osmosis concentrated water, high-valence phosphorus salt and ammonia nitrogen in the source separation urine react to generate Magnesium Ammonium Phosphate (MAP) precipitate which can be recycled as struvite, so that the magnesium ions and phosphorus in the reverse osmosis concentrated water and ammonia nitrogen in the source separation urine are mixed and subjected to synergistic treatment, the effective utilization of the magnesium ions and phosphorus in the reverse osmosis concentrated water and the ammonia nitrogen in the source separation urine can be realized, the waste is changed into the conservation, the problems of high salinity of the reverse osmosis concentrated water, toxic and harmful substances and high ammonia nitrogen in the source separation urine are solved, the use dosage of the magnesium ions and/or the high-valence phosphorus salt required by the reaction for generating the magnesium ammonium phosphate can be effectively reduced, the cost is reduced, and the water quality can be balanced at the same time, is beneficial to the subsequent treatment of reverse osmosis concentrated water and source separated urine.
The water treatment method comprises the steps of firstly carrying out ozone oxidation treatment on reverse osmosis concentrated water to realize disinfection treatment on the reverse osmosis concentrated water and convert low-valence-state phosphorus in the reverse osmosis concentrated water into high-valence-state phosphorus salt, then mixing the reverse osmosis concentrated water subjected to the ozone oxidation treatment with source separation urine, wherein magnesium ions in the reverse osmosis concentrated water, the high-valence-state phosphorus salt and ammonia nitrogen in the source separation urine react to generate Magnesium Ammonium Phosphate (MAP) precipitate which can be recycled as struvite, so that effective utilization of the magnesium ions and the phosphorus in the reverse osmosis concentrated water and the ammonia nitrogen in the source separation urine can be realized by carrying out liquid-phase mixing and synergistic treatment on the reverse osmosis concentrated water subjected to the ozone oxidation treatment and the source separation urine, the waste of sewage is changed into the waste conservation, and the problems of high salinity of the reverse osmosis concentrated water, toxic and harmful substances and the high ammonia nitrogen in the source separation urine are solved, and the use dosage of magnesium ions and/or high-valence state phosphorus salt required by the reaction of generating magnesium ammonium phosphate can be effectively reduced, the cost is reduced, and simultaneously the water quality can be balanced, thereby being beneficial to the subsequent treatment of reverse osmosis concentrated water and source separation urine.
As can be seen from the foregoing, the higher valent phosphorus salts include H2PO4 -Salt, HPO4 2-Salt and PO4 3-At least one of the salts, whereby the resulting struvite precipitate comprises MgNH4PO4·6H2O、MgNH4PO4·6H2O and MgNH4PO4·6H2At least one of O.
Wherein, the chemical formation principle of the corresponding magnesium ammonium phosphate sediment is respectively as follows:
NH4 ++H2PO4 -+Mg2++6H2O＝MgNH4PO4·6H2O+2H+
NH4 ++HPO4 2-+Mg2++6H2O＝MgNH4PO4·6H2O+H+
NH4 ++PO4 3-+Mg2++6H2O＝MgNH4PO4·6H2O
in one embodiment, the volume of the reverse osmosis concentrated water after the ozone oxidation treatment and the urine separated by the source is 1: 1-1.5: 1, and preferably, the volume of the reverse osmosis concentrated water after the ozone oxidation treatment and the urine separated by the source is 1: 1. Further, the pH value of the reaction of the reverse osmosis concentrated water subjected to ozone oxidation and the source separation urine is 7-9. Mg (magnesium)2+And PO4 3-The concentration of (1: 1) - (1.5: 1) and Mg2+And NH4 +The concentration of (A) is 1: 1 to 1: 6, preferably Mg2+And NH4 +The concentration of the catalyst is 1: 3, so that the TP removal rate can reach more than 99 percent, the ammonia nitrogen removal rate reaches 60 to 90 percent, and the COD removal rate reaches 30 to 40 percent.
Specifically, the step S300 of mixing the reverse osmosis concentrated water subjected to the ozone oxidation treatment with the source-separated urine to obtain a first mixture, and performing a mixing reaction on the reverse osmosis concentrated water subjected to the ozone oxidation treatment with the source-separated urine includes:
step S310, adding magnesium salt and/or phosphorus salt with high valence state into the first mixture to supplement magnesium ions and/or phosphorus salt with high valence state required for generating magnesium ammonium phosphate reaction, specifically, when magnesium ions and/or phosphorus salt with high valence state in the reverse osmosis concentrated water after ozone oxidation treatment are insufficient, adding magnesium salt and/or phosphorus salt with high valence state into the first mixture obtained by mixing the reverse osmosis concentrated water after ozone oxidation treatment with source separation urine to ensure supply of magnesium ions and/or phosphorus salt with high valence state required for generating magnesium ammonium phosphate reaction, thereby ensuring complete recovery of ammonia nitrogen in the source separation urine.
In step S310 of adding magnesium salt and/or high valence state phosphorus salt to the first mixture, the added magnesium salt may be replaced by magnesium oxide, and further, the added high valence state phosphorus salt includes H2PO4 -Salt, HPO4 2-Salt and PO4 3-At least one of salts. Specifically, the added high-valence state phosphorus salt comprises NaH2PO4、Na2HPO4And Na3PO4At least one of (1).
In step S310 of adding magnesium salt and/or high valence state phosphorus salt to the first mixture, the magnesium salt includes magnesium sulfate, so as to generate calcium sulfate precipitate by using the reaction of sulfate ions in the magnesium sulfate and calcium ions in the reverse osmosis concentrated water.
Specifically, the magnesium salt to be added includes magnesium sulfate (MgSO)4) Magnesium sulfate (MgSO)4) Sulfate ion (SO) of (2)4 2-) Can react with calcium ion (Ca) in reverse osmosis concentrated water2+) Reaction to produce calcium sulfate (CaSO)4) Precipitation, the chemical formation principle of calcium sulfate precipitation is:
SO4 2-+Ca2+＝CaSO4
therefore, by adopting magnesium sulfate as the added magnesium source, the problem of high calcium ion concentration in reverse osmosis concentrated water can be solved, and the generated calcium sulfate can be recycled as an inorganic fertilizer.
After the step S300 of performing a mixing reaction on the reverse osmosis concentrated water after the ozone oxidation treatment and the source separated urine, the water treatment method further includes:
and step S400, carrying out precipitation treatment on the second mixture to realize solid-liquid separation of the second mixture.
Specifically, a second mixture containing magnesium ammonium phosphate is obtained after a mixed reaction of the reverse osmosis concentrated water and the source separation urine after ozone oxidation treatment is carried out precipitation treatment, so that solid-liquid separation of the second mixture is realized, and the magnesium ammonium phosphate in the second mixture is convenient to recycle.
In one embodiment, when magnesium salt and high-valence state phosphorus salt are added into the first mixture, the reverse osmosis concentrated water after ozone oxidation treatment, the source separated urine solution, the added magnesium salt and high-valence state phosphorus salt are mixed together for reaction to obtain a second mixture containing magnesium ammonium phosphate.
Further, when magnesium sulfate and high-valence phosphorus salt are added into the first mixture, the reverse osmosis concentrated water after ozone oxidation treatment, the source separation urine, the added magnesium sulfate and the high-valence phosphorus salt are mixed together for reaction to obtain a second mixture containing magnesium ammonium phosphate and calcium sulfate.
After the step S400 of performing the precipitation treatment on the second mixture, the water treatment method further includes:
and S500, carrying out advanced treatment on the water body obtained after the second mixture is subjected to precipitation treatment. Because certain pollutants (the pollutants can comprise at least one of COD, ammonia nitrogen, nitrate nitrogen and nitrite nitrogen) can not be directly discharged in the water body obtained after the second mixture is subjected to precipitation treatment, the water body obtained after the second mixture is subjected to precipitation treatment is subjected to advanced treatment so as to further purify the water quality of the water body and ensure that the treated water body can reach the water quality standard of standard discharge.
Further, the step S500 of performing advanced treatment on the water body obtained after performing precipitation treatment on the second mixture includes:
and step S510, performing synchronous nitrification and denitrification treatment on the water body obtained after the second mixture is subjected to precipitation treatment. Specifically, nitrate Nitrogen (NO) in the water body is removed by performing denitrification treatment on the water body3 -) And/or nitrite Nitrogen (NO)2 -) Conversion to nitrogen (N)2) And realizes the removal of organic matters in the water body, and simultaneously carries out saltpeter treatment on the water bodyChemical treatment to remove ammonia Nitrogen (NH) in water4 +) And the nitrogen is converted into nitrate nitrogen and/or nitrite nitrogen, so that organic matters, ammonia nitrogen and total nitrogen in the water body can be effectively removed by realizing synchronous nitrification and denitrification treatment on the water body, and the water body can be discharged up to the standard.
Further, after the step S400 of performing the precipitation treatment on the second mixture, the water treatment method further includes:
in step S520, the magnesium ammonium phosphate aqueous mixture obtained after the second mixture is precipitated is dehydrated to remove water mixed in the magnesium ammonium phosphate, so as to obtain dehydrated magnesium ammonium phosphate crystals, thereby facilitating later recycling of magnesium ammonium phosphate.
Further, after the step S520 of performing the dehydration process on the magnesium ammonium phosphate aqueous mixture obtained after the precipitation process is performed on the second mixture, the water treatment method further includes:
step S530, carrying out advanced treatment on the water body obtained by carrying out dehydration treatment on the magnesium ammonium phosphate aqueous mixture. Because certain pollutants (the pollutants can comprise at least one of COD, ammonia nitrogen, nitrate nitrogen and nitrite nitrogen) still exist in the water body obtained by dehydrating the magnesium ammonium phosphate aqueous mixture and cannot be directly discharged, the water body obtained by dehydrating the magnesium ammonium phosphate aqueous mixture is subjected to advanced treatment so as to further purify the water quality of the water body and ensure that the treated water body can reach the water quality standard of standard discharge.
As shown in fig. 1, the present application further provides a water treatment system 10, wherein the water treatment system 10 includes a first storage chamber 110, a second storage chamber 120, an ozone unit 130, and a first reaction chamber 140, the first storage chamber 110 is used for accommodating reverse osmosis concentrated water to be treated; second reservoir 120 is for holding source separated urine to be treated; the ozone unit 130 is connected to the first storage chamber 110, and the ozone unit 130 is configured to perform ozone oxidation treatment on the reverse osmosis concentrated water output by the first storage chamber 110, so as to realize disinfection treatment on the reverse osmosis concentrated water and convert low-valence phosphorus in the reverse osmosis concentrated water into high-valence phosphorus salt, where the low-valence phosphorus salt is phosphorus salt whose valence is less than +5, and the high-valence phosphorus salt is phosphorus salt whose valence is equal to + 5.
The first reaction chamber 140 is connected to the ozone unit 130 and the second storage chamber 120, and the first reaction chamber 140 is used for mixing the reverse osmosis concentrated water subjected to ozone oxidation treatment by the ozone unit 130 with the source separated urine output by the second storage chamber 120 to react, so that magnesium ions in the reverse osmosis concentrated water, high-valence phosphorus salt and ammonia nitrogen in the source separated urine react to generate magnesium ammonium phosphate precipitate.
In the water treatment system 10, the ozone unit 130 is used to perform ozone oxidation treatment on the reverse osmosis concentrated water output from the first storage chamber 110 to sterilize the reverse osmosis concentrated water and convert low-valence phosphorus in the reverse osmosis concentrated water into high-valence phosphorus, and then the reverse osmosis concentrated water output from the ozone unit 130 and the source separation urine output from the second storage chamber 120 are input into the first reaction chamber 140 to be mixed, and at this time, magnesium ions, high-valence phosphorus and ammonia nitrogen in the source separation urine in the reverse osmosis concentrated water in the first reaction chamber 140 react to generate Magnesium Ammonium Phosphate (MAP) precipitate which can be recycled as struvite, so that the reverse osmosis concentrated water and the source separation urine after the ozone oxidation treatment by the ozone unit 130 are mixed for synergistic treatment, and effective utilization of magnesium ions, phosphorus and ammonia nitrogen in the source separation urine can be realized, the waste changing of the sewage is realized, so that the problems of high salinity of the reverse osmosis concentrated water, toxic and harmful substances and high ammonia nitrogen content of the source separated urine are solved, the use and addition amount of magnesium ions and/or high-valence phosphorus salt required by the reaction of generating magnesium ammonium phosphate can be effectively reduced, the cost is reduced, the water quality can be balanced, and the subsequent treatment of the reverse osmosis concentrated water and the source separated urine is facilitated.
The ozone unit 130 includes an oxygen tank 131, an ozone generator 132, and an ozone contact chamber 133 connected in sequence, the ozone contact chamber 133 is connected to the first storage chamber 110, the oxygen tank 131 is used to contain oxygen, the ozone generator 132 is used to convert oxygen output from the oxygen tank 131 into ozone under the condition of power supply, and the ozone generator 132 forms ozone according to the chemical principle:
3O2＝2O3wherein the reaction conditions are electrical discharge;
specifically, the ozone generator 132 is an area for generating ozone, and the voltage of the ozone generator 132 is 6-8V to ensure the smooth proceeding of the process of converting oxygen into ozone.
The ozone contact chamber 133 is used for receiving and coming from the ozone output by the ozone generator 132 to perform contact oxidation on the reverse osmosis concentrated water output by the first storage chamber 110 so as to realize ozone oxidation treatment on the reverse osmosis concentrated water.
The ozone unit 130 further includes an oxygen flow meter 134, the oxygen flow meter 134 is disposed between the oxygen tank 131 and the ozone generator 132, and the oxygen flow meter 134 is configured to detect a flow rate of oxygen output from the oxygen tank 131. Further, the ozone unit 130 further includes an ozone control valve 135, the ozone control valve 135 is disposed between the ozone generator 132 and the ozone contact chamber 133, and the ozone control valve 135 is used for controlling the flow and the cutoff of the ozone output by the ozone generator 132 with respect to the ozone contact chamber 133.
The tail gas treatment unit 136 comprises a tail gas collection chamber 137 and ozone absorption liquid filled in the tail gas collection chamber 137, the tail gas collection chamber 137 is connected with the ozone contact chamber 133, the tail gas collection chamber 137 is used for receiving the tail gas containing ozone discharged from the ozone contact chamber 133, and the ozone absorption liquid is used for absorbing the ozone in the tail gas collection chamber 137, so as to treat the tail gas containing ozone discharged from the ozone contact chamber 133.
In one embodiment, the ozone absorption liquid may be a potassium iodide (KI) solution, and the chemical principle of the potassium iodide solution for absorbing ozone is as follows:
O3+2KI+H2O＝2KOH+I2+O2
the water treatment system 10 further comprises a reverse osmosis concentrated water inlet peristaltic pump 140, the reverse osmosis concentrated water inlet peristaltic pump 140 is disposed between the first storage chamber 110 and the ozone contact chamber 133, and the reverse osmosis concentrated water inlet peristaltic pump 140 is configured to pressurize and transmit the reverse osmosis concentrated water output from the first storage chamber 110 to the ozone contact chamber 133.
The water treatment system 10 further includes a source-separated urine inlet peristaltic pump 150, the source-separated urine inlet peristaltic pump 150 is disposed between the second storage chamber 120 and the first reaction chamber 140, and the source-separated urine inlet peristaltic pump 150 is configured to pressurize and transmit the source-separated urine output from the second storage chamber 120 to the first reaction chamber 140.
The reverse osmosis concentrated water output by the ozone unit 130 and the source separation urine output by the second storage chamber 120 enter the first reaction chamber 140 and are mixed to obtain a first mixture, the water treatment system 10 further comprises a dosing unit 160, the dosing unit 160 is connected with the first reaction chamber 140, and the dosing unit 160 is used for adding magnesium salt and/or phosphorus salt with high valence into the first mixture in the first reaction chamber 140 to supplement magnesium ions and/or phosphorus salt with high valence required by the reaction of generating magnesium ammonium phosphate, so as to ensure the supply of magnesium ions and/or phosphorus salt with high valence required by the reaction of generating magnesium ammonium phosphate, and thus ensure the complete recovery of ammonia nitrogen in the source separation urine.
The water treatment system 10 further includes a first stirrer 170, the first stirrer 170 is disposed in the first reaction chamber 140, the first stirrer 170 is configured to achieve stirring and mixing of the substances input into the first reaction chamber 140 to accelerate a reaction rate between the substances in the first reaction chamber 140, and specifically, the first stirrer 170 is configured to achieve stirring and mixing of the reverse osmosis concentrated water subjected to ozone oxidation treatment and the source separated urine input into the first reaction chamber 140 to accelerate a reaction rate at which magnesium ions and high-valence phosphorus salts in the reverse osmosis concentrated water in the first reaction chamber 140 and ammonia nitrogen in the source separated urine precipitate to form magnesium ammonium phosphate precipitate.
The first stirrer 170 includes a main shaft 172 and a stirring blade 174, the main shaft 172 partially extends into the first reaction chamber 140, the stirring blade 174 is disposed at one end of the main shaft 172 extending into the first reaction chamber 140, and the main shaft 172 can drive the stirring blade 174 to synchronously rotate around the axial direction of the main shaft 172, so that the stirring blade 174 can stir and mix the substances input into the first reaction chamber 140.
In one embodiment, the stirring speed of the first stirrer 170 is 200r/min, and the stirring time of the first stirrer 170 is 10-20 min.
Further, the reverse osmosis concentrated water after the ozone oxidation treatment and the source separation urine in the first reaction chamber 140 are mixed and reacted to obtain a second mixture containing magnesium ammonium phosphate, and the first reaction chamber 140 is a sedimentation tank, that is, the first reaction chamber 140 can also be used for carrying out sedimentation treatment on the second mixture to realize solid-liquid separation on the second mixture.
The water treatment system 10 further comprises a centrifugal separator 180, the centrifugal separator 180 is connected with the first reaction chamber 140, and the centrifugal separator 180 is used for dehydrating the magnesium ammonium phosphate aqueous mixture obtained after the second mixture is subjected to precipitation treatment in the first reaction chamber 140 so as to remove water mixed in the magnesium ammonium phosphate, so that dehydrated magnesium ammonium phosphate crystals are obtained, and the magnesium ammonium phosphate can be recycled at a later stage.
The water treatment system 10 further includes a deep treatment unit 190, the deep treatment unit 190 is disposed at a downstream end of the first reaction chamber 140, and the deep treatment unit 190 is configured to perform deep treatment on the water body obtained after the second mixture is subjected to precipitation treatment in the first reaction chamber 140. Because certain pollutants (the pollutants can comprise at least one of COD, ammonia nitrogen, nitrate nitrogen and nitrite nitrogen) can not be directly discharged in the water body obtained after the second mixture is subjected to precipitation treatment, the water body obtained after the second mixture is subjected to precipitation treatment is subjected to advanced treatment by the advanced treatment unit 190 so as to further purify the water quality of the water body and ensure that the treated water body can reach the water quality standard of standard discharge.
Further, the advanced treatment unit 190 is connected to the centrifugal separator 180, and the advanced treatment unit 190 is further configured to perform advanced treatment on the water separated by the centrifugal separator 180. Because certain pollutants (the pollutants can comprise at least one of COD, ammonia nitrogen, nitrate nitrogen and nitrite nitrogen) which cannot be directly discharged exist in the water body obtained by the separation of the centrifugal separator 180, the water body obtained by the separation of the centrifugal separator 180 is subjected to advanced treatment by the advanced treatment unit 190 so as to further purify the water quality of the water body and ensure that the treated water body can reach the water quality standard of standard discharge.
The advanced treatment unit 190 comprises an anoxic unit 191 and an aerobic unit 192 which are sequentially communicated along the water inlet direction, the anoxic unit 191 is connected with the first reaction chamber 140, and the anoxic unit 191 is used for performing denitrification treatment on the water body output by the first reaction chamber 140 so as to remove nitrate Nitrogen (NO) in the water body3 -) And/or nitrite Nitrogen (NO)2 -) Conversion to nitrogen (N)2) And the aerobic unit 192 is used for carbonizing and nitrifying the water body output by the anoxic unit 191 to remove the organic matters in the water body and remove ammonia Nitrogen (NH) in the water body4 +) And the nitrogen is converted into nitrate nitrogen and/or nitrite nitrogen, so that the synchronous nitrification and denitrification treatment of the water body can be realized through the arrangement of the anoxic unit 191 and the aerobic unit 192 which are sequentially communicated, so that the organic matter, ammonia nitrogen and total nitrogen in the water body can be effectively removed by the advanced treatment unit 190, and the water body can be discharged after reaching the standard.
The advanced treatment unit 190 further comprises a second reaction chamber 193 and a partition 194, the partition 194 is disposed in the second reaction chamber 193 and partitions the interior of the second reaction chamber 193 into an anoxic unit 191 and an aerobic unit 192 which are communicated with each other, and the volume of the anoxic unit 191 and the aerobic unit 192 is 1: 3.
In one embodiment, the Dissolved Oxygen (DO) content within the anoxic unit 191 is less than 0.5mg/L to remove a portion of the COD and a majority of the nitrate and/or nitrite nitrogen in the water body. The Dissolved Oxygen (DO) content of the aerobic unit 192 is 2mg/L, the hydraulic retention time is 4h, and the effluent meets the third-level standard of Integrated wastewater discharge Standard (GB 8978-1996).
The advanced treatment unit 190 further comprises a backflow unit 195, the backflow unit 195 is connected with the anoxic unit 191 and the aerobic unit 192, and the backflow unit 195 is used for returning the water body containing nitrate nitrogen and/or nitrite nitrogen obtained after the treatment of the aerobic unit 192 to the anoxic unit 191 so as to supplement the nitrate nitrogen and/or nitrite nitrogen required by the water body in the anoxic unit 191 in the denitrification process.
The reflux unit 195 comprises a reflux pipe 1952 and a reflux peristaltic pump 1954, the reflux pipe 1952 is connected with the anoxic unit 191 and the aerobic unit 192, the reflux peristaltic pump 1954 is arranged on the reflux pipe 1952, and the reflux pipe 1952 is used for pressurizing and feeding back the water body containing nitrate nitrogen and/or nitrite nitrogen obtained after the treatment of the aerobic unit 192 to the anoxic unit 191 by means of the reflux peristaltic pump 1954.
The advanced treatment unit 190 further comprises an aeration unit 196, the aeration unit 196 is connected with the aerobic unit 192, and the aeration unit 196 is used for filling air into the water body in the aerobic unit 192 so as to meet the content requirement of dissolved oxygen in the aerobic unit 192.
The aeration unit 196 comprises an aeration pump 1961, an aeration pipe 1962 and an aeration head 1963, wherein the aeration pump 1961 is arranged outside the aerobic unit 192, one end of the aeration pipe 1962 is connected with the aeration pump 1961, the other end of the aeration pipe 1962 extends to the inner side of the bottom of the aerobic unit 192 through the outer side of the bottom of the aerobic unit 192, the aeration pump 1961 is used for outputting air, the aeration head 1963 is arranged at one end of the aeration pipe 1962 extending to the aerobic unit 192, the aeration pipe 1962 is used for transmitting the air output by the aeration pump 1961 to the aeration head 1963, and the aeration head 1963 is used for charging the received air into the water body in the aerobic unit 192. Specifically, the number of the aeration heads 1963 is plural, and the plurality of aeration heads 1963 are disposed at intervals on the aeration tube 1962.
Further, the aeration unit 196 further includes an aeration valve 1964, the aeration valve 1964 is disposed on the aeration pipe 1962, and the aeration valve 1964 is used for controlling the on/off of the aeration pipe 1962. The aeration unit 196 further includes an air flow meter 1965, the air flow meter 1965 being provided on the aeration tube 1962, the air flow meter 1965 being used to detect the flow rate of air delivered by the aeration tube 1962.
The advanced treatment unit 190 further comprises a hollow fiber membrane 197, the hollow fiber membrane 197 is disposed in the aerobic unit 192, and the hollow fiber membrane 197 is used for physically trapping pollutants in the water body in the aerobic unit 192, so as to further remove the pollutants in the water body.
Specifically, the hollow fiber membrane 197 is provided with a plurality of micron-level filter holes, water molecules and some inorganic substances in the water body can permeate through the filter holes, and organic substances and some bacteria in the water body cannot permeate through the filter holes and are trapped in the filter holes of the hollow fiber membrane 197, so that physical trapping of pollutants in the water body by the hollow fiber membrane 197 is realized.
In one embodiment, the hollow fiber membrane 197 is made of polyvinylidene fluoride with a pore size of 0.1 μm and an effective area of 0.42m2。
Further, the hollow fiber membrane 197 is an ultrafiltration membrane to realize effective interception of organic matters, ammonia nitrogen, nitrate nitrogen and nitrite nitrogen in the water body.
The advanced treatment unit 190 further comprises a suction unit 198, the suction unit 198 is disposed on the water outlet side of the hollow fiber membrane 197, and the suction unit 198 is configured to form a negative pressure on the water outlet side of the hollow fiber membrane 197, so that the water body flows through the hollow fiber membrane 197 under the action of the negative pressure and flows out from the water outlet side of the hollow fiber membrane 197, thereby ensuring effective realization of physical entrapment of the pollutants in the water body by the hollow fiber membrane 197.
The pumping unit 198 comprises a pumping peristaltic pump 1982 and a conveying pipeline 1984, the pumping peristaltic pump 1982 is arranged outside the aerobic unit 192, one end of the conveying pipeline 1984 is connected with the pumping peristaltic pump 1982, the other end of the conveying pipeline 1984 extends into the aerobic unit 192 and extends to the water outlet side of the hollow fiber membrane 197, and the conveying pipeline 1984 is used for conveying negative pressure generated by the pumping peristaltic pump 1982 to the water outlet side of the hollow fiber membrane 197 so as to enable the water outlet side of the hollow fiber membrane 197 to form negative pressure. The pumping unit 198 further includes a vacuum gauge 1986, the vacuum gauge 1986 being disposed on the transfer pipe 1984, the vacuum gauge 1986 being used to detect the magnitude of the negative pressure formed in the transfer pipe 1984.
The advanced treatment unit 190 further comprises a filler 199, the filler 199 is arranged in the aerobic unit 192, the filler 199 is used for attachment and growth of aerobic microorganisms, and the aerobic microorganisms are used for carrying out carbonization treatment and nitrification treatment on the water body in the aerobic unit 192 so as to remove organic matters in the water body and remove ammonia Nitrogen (NH) in the water body4 +) Converted to nitrate nitrogen and/or nitrite nitrogen. Further, the number of the packing 199 is plural, and the plural packing 199 are arranged at intervals in the aerobic unit 192.
Further, the filler 199 is formed by a combination of polyurethane sponge monomer and polyethylene plastic monomer, the filler 199 is suspended in the water body in the aerobic unit 192 and is located near the hollow fiber membranes 197, the filler 199 can move along with the water flow under the action of aeration, and the filler 199 can collide with the hollow fiber membranes 197.
Specifically, since the filler 199 is formed by combining a polyurethane sponge monomer and a polyethylene plastic monomer, the filler 199 has the mechanical hardness of polyethylene plastic, the filler 199 can move together with water flow under the action of aeration, and when the filler 199 continuously collides with the hollow fiber membranes 197 in the process of moving together with the water flow, the generation and distribution of solubility products (SMP) and extracellular secretions (EPS) of aerobic microorganisms in the whole aerobic unit 192 can be changed, so that the adhesion of pollutants on the hollow fiber membranes 197 can be relieved, and the effect of relieving the pollution of the hollow fiber membranes 197 is achieved; meanwhile, the polyurethane sponge in the filler 199 has the advantage of loose structure, so that aerobic microorganisms are conveniently attached to the inside of the filler 199, the number of the aerobic microorganisms attached to the filler 199 can be increased, dissolved oxygen gradient is formed, and the synchronous nitrification and denitrification treatment effect of the water body is more favorably realized.
In one embodiment, the polyurethane sponge monomer isCube, the polyurethane sponge monomer has the size of 0.5cm multiplied by 1cm and the density of 30kg/m3Pore size is 60 PPI; the polyethylene plastic monomer is a cylinder, the diameter of the bottom circle of the polyethylene plastic monomer is 10mm, the height of the bottom circle of the polyethylene plastic monomer is 10mm, and the density of the polyethylene plastic monomer is more than 0.96g/cm3Specific surface area of more than 500m2/m3。
The advanced treatment unit 190 further comprises a second stirrer 200, the first stirrer 170 is disposed in the anoxic unit 191, and the second stirrer 200 is used for stirring and mixing the water body input into the anoxic unit 191 to accelerate the denitrification process of the water body in the anoxic unit 191. In the present embodiment, the second stirrer 200 and the first stirrer 170 have similar structures, and the description thereof will not be repeated.
The water treatment system 10 further includes a water storage tank 210, the water storage tank 210 is disposed between the first reaction chamber 140 and the advanced treatment unit 190, the water storage tank 210 is configured to accommodate a water body obtained after the second mixture is precipitated by the first reaction chamber 140, so as to realize water volume adjustment of the water body, and the advanced treatment unit 190 is configured to perform advanced treatment on the water body output by the water storage tank 210.
Specifically, in this embodiment, the anoxic unit 191 is connected to the water storage tank 210 and the centrifugal separator 180, and the anoxic unit 191 is configured to perform denitrification on the water output from the water storage tank 210 and the water separated by the centrifugal separator 180.
The water treatment system 10 further comprises a first peristaltic pump 220 and a second peristaltic pump 230, the first peristaltic pump 220 is arranged between the anoxic unit 191 and the water storage tank 210, the first peristaltic pump 220 is used for pressurizing and conveying the water body output by the water storage tank 210 to the anoxic unit 191, the second peristaltic pump 230 is arranged between the anoxic unit 191 and the centrifugal separator 180, and the second peristaltic pump 230 is used for pressurizing and conveying the water body obtained by separation of the centrifugal separator 180 to the anoxic unit 191.
The above description is only a preferred embodiment of the present invention, and not intended to limit the scope of the present invention, and all modifications and equivalents of the present invention, which are made by the contents of the present specification and the accompanying drawings, or directly/indirectly applied to other related technical fields, are included in the scope of the present invention.
Claims (10)
1. A method of water treatment comprising the steps of:
providing reverse osmosis concentrated water to be treated and source separated urine;
carrying out ozone oxidation treatment on the reverse osmosis concentrated water to realize disinfection treatment on the reverse osmosis concentrated water and convert low-valence phosphorus in the reverse osmosis concentrated water into high-valence phosphorus salt, wherein the low-valence phosphorus is phosphorus with the valence less than +5, and the high-valence phosphorus salt is phosphorus with the valence equal to + 5; and
and carrying out mixed reaction on the reverse osmosis concentrated water subjected to ozone oxidation treatment and the source separation urine so as to enable magnesium ions in the reverse osmosis concentrated water, high-valence phosphorus salt and ammonia nitrogen in the source separation urine to react to generate magnesium ammonium phosphate precipitate.
2. The water treatment method according to claim 1, wherein the reverse osmosis concentrated water subjected to the ozone oxidation treatment and the source-separated urine are mixed to obtain a first mixture, and the step of performing a mixing reaction on the reverse osmosis concentrated water subjected to the ozone oxidation treatment and the source-separated urine comprises:
and adding a magnesium salt and/or the high-valence phosphorus salt into the first mixture to supplement the magnesium ions and/or the high-valence phosphorus salt required for generating the magnesium ammonium phosphate reaction.
3. The water treatment method according to claim 2, wherein in the step of adding a magnesium salt and/or the high-valence phosphorus salt to the first mixture, the magnesium salt comprises magnesium sulfate, so that sulfate ions in the magnesium sulfate and calcium ions in the reverse osmosis concentrated water react to generate calcium sulfate precipitate.
4. The water treatment method according to claim 1, wherein the reverse osmosis concentrated water after the ozone oxidation treatment and the source-separated urine are mixed and reacted to obtain a second mixture containing the magnesium ammonium phosphate, and after the step of mixing and reacting the reverse osmosis concentrated water after the ozone oxidation treatment and the source-separated urine, the water treatment method further comprises:
and carrying out precipitation treatment on the second mixture to realize solid-liquid separation on the second mixture.
5. The water treatment method according to claim 4, further comprising, after the step of subjecting the second mixture to a precipitation treatment:
and carrying out advanced treatment on the water body obtained after the second mixture is subjected to precipitation treatment.
6. The water treatment method according to claim 5, wherein the step of performing advanced treatment on the water body obtained after the second mixture is subjected to precipitation treatment comprises the following steps:
and performing synchronous nitrification and denitrification treatment on the water body obtained after the second mixture is subjected to precipitation treatment.
7. A water treatment system, comprising:
the first storage chamber is used for accommodating reverse osmosis concentrated water to be treated;
a second storage chamber for receiving source separated urine to be treated;
the ozone unit is connected with the first storage chamber and is used for carrying out ozone oxidation treatment on the reverse osmosis concentrated water output by the first storage chamber so as to realize disinfection treatment on the reverse osmosis concentrated water and convert low-valence-state phosphorus in the reverse osmosis concentrated water into high-valence-state phosphorus salt, the low-valence-state phosphorus salt is phosphorus salt with the valence of less than +5, and the high-valence-state phosphorus salt is phosphorus salt with the valence of equal to + 5; and
the first reaction chamber is used for carrying out mixed reaction on the reverse osmosis concentrated water subjected to ozone oxidation treatment and the source separation urine so as to enable magnesium ions in the reverse osmosis concentrated water, high-valence phosphorus salt and ammonia nitrogen in the source separation urine to react to generate magnesium ammonium phosphate precipitate.
8. The water treatment system of claim 7, wherein the reverse osmosis concentrate output by the ozone unit and the source-separated urine output by the second storage chamber are mixed to obtain a first mixture after entering the first reaction chamber, the water treatment system further comprising:
the dosing unit is connected with the first reaction chamber and used for adding a magnesium salt and/or the high-valence state phosphorus salt into the first mixture in the first reaction chamber so as to supplement and generate the magnesium ions and/or the high-valence state phosphorus salt required by the magnesium ammonium phosphate reaction.
9. The water treatment system according to claim 7, wherein the reverse osmosis concentrated water after ozone oxidation treatment in the first reaction chamber is mixed with the source separation urine to react to obtain a second mixture containing the magnesium ammonium phosphate, the first reaction chamber is a sedimentation tank, and the first reaction chamber is further used for performing sedimentation treatment on the second mixture to realize solid-liquid separation of the second mixture.
10. The water treatment system of claim 9, further comprising a depth treatment unit disposed at a downstream end of the first reaction chamber, wherein the depth treatment unit is configured to perform depth treatment on the water obtained after the second mixture is subjected to precipitation treatment in the first reaction chamber.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111218005.8A CN113735333A (en) | 2021-10-19 | 2021-10-19 | Water treatment system and method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111218005.8A CN113735333A (en) | 2021-10-19 | 2021-10-19 | Water treatment system and method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN113735333A true CN113735333A (en) | 2021-12-03 |
Family
ID=78726918
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111218005.8A Pending CN113735333A (en) | 2021-10-19 | 2021-10-19 | Water treatment system and method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113735333A (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62289298A (en) * | 1986-06-10 | 1987-12-16 | Kiyoshi Aoshima | Treatment of excrement, urine, organic sludge and sewage or the like |
| WO2006005733A1 (en) * | 2004-07-08 | 2006-01-19 | Hans Huber Ag Maschinen- Und Anlagenbau | Method and device for separating magnesium-ammonium-phosphate (map) from waste water |
| CN102344209A (en) * | 2010-08-06 | 2012-02-08 | 同济大学 | Method for treating glyphosate wastewater and recovering nitrogen and phosphor in wastewater |
| CN109896613A (en) * | 2019-04-18 | 2019-06-18 | 曹式芳 | The super oxidation water tackling method of a kind of nanometer of free radical and its device |
| CN112979352A (en) * | 2021-03-08 | 2021-06-18 | 亚太建设科技信息研究院有限公司 | Method for recovering phosphate in urine |
-
2021
- 2021-10-19 CN CN202111218005.8A patent/CN113735333A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62289298A (en) * | 1986-06-10 | 1987-12-16 | Kiyoshi Aoshima | Treatment of excrement, urine, organic sludge and sewage or the like |
| WO2006005733A1 (en) * | 2004-07-08 | 2006-01-19 | Hans Huber Ag Maschinen- Und Anlagenbau | Method and device for separating magnesium-ammonium-phosphate (map) from waste water |
| CN102344209A (en) * | 2010-08-06 | 2012-02-08 | 同济大学 | Method for treating glyphosate wastewater and recovering nitrogen and phosphor in wastewater |
| CN109896613A (en) * | 2019-04-18 | 2019-06-18 | 曹式芳 | The super oxidation water tackling method of a kind of nanometer of free radical and its device |
| CN112979352A (en) * | 2021-03-08 | 2021-06-18 | 亚太建设科技信息研究院有限公司 | Method for recovering phosphate in urine |
Non-Patent Citations (5)
| Title |
|---|
| 冯皓迪等: ""MAP法沉淀回收尿液中氮磷的研究"" * |
| 冯皓迪等: "MAP法沉淀回收尿液中氮磷的研究", 《环境工程》 * |
| 杨期勇: "中国环境科学学会技术年会优秀论文集（2007）", 中国环境科学学会技术年会优秀论文集（2007） * |
| 陈丽萍: ""源分离尿液的短程硝化反硝化生物脱氮技术研究"", 《中国优秀硕士学位论文全文数据库工程科技I辑》 * |
| 陈观文等: "《膜技术新进展与工程应用》", 31 August 2013, 国防工业出版社 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106242163B (en) | A kind of processing method of percolate embrane method concentrate | |
| CN104591473B (en) | Advanced nitrogen and phosphorus removal technology | |
| CN108314269A (en) | A kind of system and method for macropore denitrogenation acid-basic regenerated waste liquids in water processing and reuse | |
| CN104085987A (en) | Method and device for synchronously realizing sewage nitrogen and phosphorus removal, residual sludge reduction and phosphorus resource recovery | |
| CN102718371B (en) | Treatment method and treatment equipment for coal chemical industry wastewater | |
| CN107840537A (en) | Method for treating garbage percolation liquid and system | |
| CN100591632C (en) | Advanced treatment method and device for dyeing waste water by ozone iron zinc catalysis | |
| CN102372391A (en) | Method and system for removing phosphorous in high-calcium content sewage through combination of biological method and chemical method | |
| CN207904106U (en) | A kind of cyanide-containing waste water treatment system | |
| CN207062081U (en) | A kind of pharmaceutical wastewater processing system | |
| Chen et al. | Donnan dialysis-osmotic distillation (DD-OD) hybrid process for selective ammonium recovery driven by waste alkali | |
| CN110217932A (en) | A kind of processing unit and processing method of landfill leachate discharge | |
| CN110526504A (en) | A kind of system and method for targeting denitrogenation dephosphorizing acid-basic regenerated waste liquids in water processing | |
| CN105152330B (en) | A kind of processing method for percolate | |
| CN205974184U (en) | Processing system of landfill leachate embrane method concentrate | |
| CN109704514A (en) | A kind of system and method for advanced treatment of wastewater and concentrated water disposition | |
| CN110156270A (en) | Source-separated urine recovery of nitrogen and phosphorus and water reclaiming system and its operation method | |
| CN207142990U (en) | A kind of low concentration wastewater carries mark transformation device | |
| CN216005468U (en) | Water treatment system | |
| CN108675568A (en) | A kind of Lithium Battery Industry waste water purification system | |
| CN113735333A (en) | Water treatment system and method | |
| CN209685515U (en) | A kind of system of advanced treatment of wastewater and concentrated water disposition | |
| CN205035215U (en) | Landfill leachate treatment device | |
| CN207877521U (en) | A kind of garbage leachate treatment device | |
| CN207483528U (en) | Garbage percolation liquid treating system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20211203 |
|
| RJ01 | Rejection of invention patent application after publication |