CN114853246A - Iron phosphate wastewater treatment device and treatment method - Google Patents
Iron phosphate wastewater treatment device and treatment method Download PDFInfo
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- CN114853246A CN114853246A CN202210588771.1A CN202210588771A CN114853246A CN 114853246 A CN114853246 A CN 114853246A CN 202210588771 A CN202210588771 A CN 202210588771A CN 114853246 A CN114853246 A CN 114853246A
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- 238000000034 method Methods 0.000 title claims abstract description 79
- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 title claims abstract description 47
- 229910000398 iron phosphate Inorganic materials 0.000 title claims abstract description 40
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 324
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 153
- 150000003839 salts Chemical class 0.000 claims abstract description 55
- 239000007788 liquid Substances 0.000 claims abstract description 49
- 239000002351 wastewater Substances 0.000 claims abstract description 45
- 239000013505 freshwater Substances 0.000 claims abstract description 29
- 239000000243 solution Substances 0.000 claims abstract description 27
- 238000002156 mixing Methods 0.000 claims abstract description 26
- 238000011033 desalting Methods 0.000 claims abstract description 24
- 239000012452 mother liquor Substances 0.000 claims abstract description 22
- 238000002425 crystallisation Methods 0.000 claims abstract description 21
- 230000008025 crystallization Effects 0.000 claims abstract description 21
- 229910001385 heavy metal Inorganic materials 0.000 claims abstract description 21
- 238000001914 filtration Methods 0.000 claims abstract description 20
- 150000002500 ions Chemical class 0.000 claims abstract description 20
- 239000011259 mixed solution Substances 0.000 claims abstract description 18
- 238000000746 purification Methods 0.000 claims abstract description 17
- 239000008237 rinsing water Substances 0.000 claims abstract description 17
- 238000009776 industrial production Methods 0.000 claims abstract description 10
- 238000011084 recovery Methods 0.000 claims description 33
- 239000011347 resin Substances 0.000 claims description 11
- 229920005989 resin Polymers 0.000 claims description 11
- 239000012141 concentrate Substances 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 4
- 239000005955 Ferric phosphate Substances 0.000 abstract description 7
- 229940032958 ferric phosphate Drugs 0.000 abstract description 7
- 229910000399 iron(III) phosphate Inorganic materials 0.000 abstract description 7
- 238000010612 desalination reaction Methods 0.000 description 12
- 239000012528 membrane Substances 0.000 description 12
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 238000004064 recycling Methods 0.000 description 6
- 238000013461 design Methods 0.000 description 5
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 238000005406 washing Methods 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 4
- 238000003825 pressing Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 3
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 3
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- -1 ammonium ions Chemical class 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000012153 distilled water Substances 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 2
- 208000028659 discharge Diseases 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 229910052748 manganese Inorganic materials 0.000 description 2
- 239000011572 manganese Substances 0.000 description 2
- 238000001471 micro-filtration Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000007935 neutral effect Effects 0.000 description 2
- 239000004254 Ammonium phosphate Substances 0.000 description 1
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- VEQPNABPJHWNSG-UHFFFAOYSA-N Nickel(2+) Chemical compound [Ni+2] VEQPNABPJHWNSG-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 229910000148 ammonium phosphate Inorganic materials 0.000 description 1
- 235000019289 ammonium phosphates Nutrition 0.000 description 1
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 1
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 1
- 235000011130 ammonium sulphate Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910001437 manganese ion Inorganic materials 0.000 description 1
- 229910001453 nickel ion Inorganic materials 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 230000003204 osmotic effect Effects 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000007774 positive electrode material Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- 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
- C02F2101/20—Heavy metals or heavy metal compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
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- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The application discloses a ferric phosphate wastewater treatment device and a treatment method. The iron phosphate wastewater treatment method comprises a first concentration process, a second concentration process and a fresh water purification process. The first concentration process comprises: concentrating the wastewater with low salt content by adopting a first reverse osmosis device, wherein the wastewater with low salt content comprises rinsing water; mixing first concentrated water generated by a first reverse osmosis device with mother liquor with high salt content; treating the primary mixed liquid obtained in the mixing step by using a filtering device to remove heavy metal ions; the second concentration process comprises: concentrating the obtained mixed solution by adopting a reverse osmosis device so as to obtain a concentrated solution with high salt content and produced water with low salt content, wherein the concentrated solution is suitable for an evaporative crystallization process; the fresh water purification process comprises the following steps: and desalting the produced water obtained by the second-step concentration process by using a reverse osmosis device to obtain fresh water suitable for industrial production.
Description
Technical Field
The application relates to the field of industrial wastewater treatment, in particular to a ferric phosphate wastewater treatment device and a treatment method.
Background
One important use of iron phosphate is as a positive electrode material for batteries, and the production process of battery-grade iron phosphate mainly comprises the following steps: pre-dissolving, synthesizing, filter pressing and washing, high-temperature aging, filter pressing and washing, drying, crushing and packaging. The ferric phosphate wastewater generated in the process comprises mother liquor and rinsing water, wherein the mother liquor is mainly generated by rough washing and first filter pressing washing of a synthesis tank, and the rinsing water is mainly generated by second filter pressing washing. The salt content of the mother liquor is about 4-10 times of that of the rinsing water. The pH value of the wastewater is low, wherein the wastewater contains a large amount of ammonium ions, phosphate radicals, sulfate radicals and magnesium ions, and a small amount of calcium ions, fluorine ions, iron ions, manganese ions, nickel ions and other heavy metal ions exist. Because the iron phosphate wastewater contains a large amount of nutrient elements such as sulfur, phosphorus, ammonia and the like, the zero discharge treatment of the wastewater is realized, and the recycling is the main process path for the iron phosphate wastewater treatment at present.
In the Chinese patent with publication number CN105000744B, a ferric phosphate wastewater treatment and recycling device and a treatment and recycling method thereof are disclosed, liquid ammonia is firstly added to adjust the PH value, tubular microfiltration is used for filtering heavy metal pollutants, the effluent of a tubular microfiltration membrane passes through a primary reverse osmosis device, a concentrated water reverse osmosis device and a secondary reverse osmosis device, fresh water produced by the secondary reverse osmosis device is used as ferric phosphate flushing water for recycling, and concentrated water of the concentrated water reverse osmosis device and mother liquor enter an MVR evaporation system together for recycling ammonium sulfate and ammonium phosphate.
In chinese patent publication No. CN108623040A, a high recovery rate inorganic wastewater treatment process is disclosed, comprising the following steps: the method comprises the steps of concentrating pretreated wastewater through a first-stage reverse osmosis device to obtain first concentrated water and first-stage produced water, concentrating the first concentrated water through the concentrated water reverse osmosis device again to obtain second concentrated water and second-stage produced water, concentrating the second concentrated water through a purification reverse osmosis device to obtain third concentrated water and third-stage produced water, further concentrating the first-stage produced water through the second-stage reverse osmosis device to obtain produced water for recycling, and refluxing the second-stage produced water, the third-stage produced water and the concentrated water obtained by the treatment of the second-stage reverse osmosis device into the first-stage reverse osmosis device for purification and concentration again. For containing NH 4+ 、PO 4 3- 、SO 4 2 And the high-concentration industrial wastewater containing inorganic salts is subjected to multistage treatment by adopting a multistage reverse osmosis device, so that water resources can be recovered to the maximum extent, the concentration of the wastewater is improved, the water content in the wastewater is reduced, and the load of subsequent treatment equipment is reduced.
However, the existing wastewater treatment process has the following defects:
(1) the salt content of the concentration of the combined process is not high enough, the water inflow of an evaporative crystallization system is large, the salt content is low, and the investment cost and the operation cost of the evaporative crystallization process are high;
(2) the overall energy consumption of the wastewater treatment system is high;
(3) in the pretreatment of the wastewater, heavy metals such as iron, manganese and the like cannot be completely removed, and the concentration of ions such as iron, manganese and the like is increased after primary reverse osmosis concentration, so that the pollution and blockage of a subsequent concentrated reverse osmosis membrane can be caused;
(4) after reverse osmosis treatment, the temperature of concentrated water is increased, the desalination rate of a reverse osmosis membrane is reduced at high temperature, and the salt concentration multiple is reduced, so that the quality of final reuse water is deteriorated.
Disclosure of Invention
An object of the application is to provide a ferric phosphate wastewater treatment system and a treatment method with high overall recovery rate.
Another object of the present application is to provide a system and a method for treating iron phosphate wastewater with high concentration factor.
Another object of the present application is to provide a system and a method for treating iron phosphate wastewater with low energy consumption.
In order to achieve the above purpose, the application provides a method for treating iron phosphate wastewater, comprising a first concentration process, a second concentration process and a fresh water purification process,
the first concentration process comprises:
a low-salt-content wastewater concentration step, wherein a first reverse osmosis device is adopted to concentrate wastewater with low salt content, and the wastewater with low salt content comprises rinsing water;
a mixing step, namely mixing the first concentrated water generated by the first reverse osmosis device with the mother liquor with high salt content;
a heavy metal ion removing step of removing heavy metal ions by treating the primary mixed liquid obtained in the mixing step with a filtering device;
the second concentration process comprises: concentrating the mixed solution obtained by the first concentration process by using a reverse osmosis device so as to obtain a concentrated solution with high salt content and produced water with low salt content, wherein the concentrated solution is suitable for an evaporative crystallization process;
the fresh water purification process comprises the following steps: and desalting the produced water obtained by the second-step concentration process by using a reverse osmosis device to obtain fresh water suitable for industrial production.
Further, the second concentration process includes: a first reverse osmosis treatment step, namely performing first concentration on the mixed liquor obtained by the first concentration process by adopting a concentrated water reverse osmosis device to obtain second concentrated water and second produced water; a heat exchange step of carrying out heat exchange on the second concentrated water to adjust the second concentrated water to a preset temperature; and a second reverse osmosis treatment step, namely concentrating the second concentrated water after temperature adjustment by using a concentration reverse osmosis device to obtain the concentrated solution with high salt content and third produced water with low salt content.
Further, adjusting the ph of the mixed solution to be 5.5 +/-0.5, and after the mixed solution is pressurized and subjected to security filtration, conveying the mixed solution into the concentrated water reverse osmosis device through a high-pressure pump; and adjusting the ph of the second concentrated water to be 5.5 +/-0.5, and after the second concentrated water is pressurized and subjected to security filtration, conveying the second concentrated water into the concentration reverse osmosis device through a high-pressure pump.
The fresh water purification process comprises the following steps:
a first desalting step: desalting the second produced water and the third produced water by adopting a second reverse osmosis device to obtain fourth concentrated water and fourth produced water, wherein the fourth concentrated water is suitable for being mixed with rinsing water and then subjected to the low-salt-content wastewater concentration step;
and a second desalting step: and desalting the fourth produced water and the first produced water of the first reverse osmosis device by adopting a terminal reverse osmosis device to obtain fifth concentrated water and fresh water suitable for industrial production, wherein the fifth concentrated water is suitable for being mixed with the second produced water and the third produced water and then is subjected to the first desalting step.
Further, the second produced water, the third produced water and the fifth concentrated water are mixed, ph is adjusted to 7.0 +/-0.5, and after pressurization and security filtration, the mixture is input into the second reverse osmosis device through a high-pressure pump; and mixing the first produced water and the fourth produced water, adjusting the ph to 7.0 +/-0.5, and after pressurization and security filtration, inputting the mixture into the terminal reverse osmosis device through a high-pressure pump.
Further, adjusting the ph of the wastewater to be 5.5 +/-0.5, pressurizing and filtering the wastewater with security, and inputting the wastewater into a first reverse osmosis device through a high-pressure pump, wherein the recovery rate of the first reverse osmosis device is 75-87.5%; and adjusting the ph of the primary mixed liquid of the first concentrated water and the mother liquid to 7.0 +/-0.5, and then inputting the primary mixed liquid into a filtering device by utilizing a booster pump to remove heavy metal ions to obtain the mixed liquid.
The application still provides a ferric phosphate effluent treatment plant, includes:
a first reverse osmosis device for concentrating the rinse water having a low salt content to produce a first concentrated water and a first produced water;
the first concentrated water tank is used for mixing the first concentrated water and the mother liquor with high salt content to obtain primary mixed liquor;
the resin bed is used for removing heavy metal ions in the primary mixed liquid to obtain mixed liquid;
the concentrated water reverse osmosis device is used for concentrating the mixed solution to obtain second concentrated water and second produced water;
the concentration reverse osmosis device is used for concentrating the second concentrated water to obtain concentrated solution and third produced water;
a second water producing tank for mixing the second produced water and the third produced water;
the second reverse osmosis device is used for desalting the liquid in the second water producing pool to obtain fourth concentrated water and fourth produced water;
a first water producing tank for mixing the fourth water producing and the first water producing;
and the terminal reverse osmosis device is used for desalting the liquid in the first water producing tank to obtain fresh water and fifth concentrated water which are suitable for industrial production, and the fifth concentrated water is suitable for being input into the second water producing tank.
Further, the system also comprises a heat exchanger and a second concentrated water tank, wherein the heat exchanger is used for adjusting the temperature of the second concentrated water, and the second concentrated water after temperature adjustment is stored in the second concentrated water tank.
Further, the system also comprises a first energy recovery device for recovering the high-pressure energy of the second concentrated water, and the energy of the first energy recovery device is used for pressurizing the mixed liquor.
Further, the energy recovery device is used for recovering the high-pressure energy of the concentrated solution, and the energy of the second energy recovery device is used for pressurizing the second concentrated water.
Compared with the prior art, the beneficial effect of this application lies in:
(1) according to the method, the heavy metal ions in the mixed liquid are removed in the first concentration process, the operation safety of the reverse osmosis device in the second concentration process can be protected, and the maintenance cost is reduced;
(2) the application adopts an efficient reverse osmosis combined design, so that the overall recovery rate of the system is improved, and the water reuse rate of the system reaches 98%;
(3) the salt content of the concentrated solution obtained by the method can be 180000mg/L, and the water quantity of an evaporative crystallization system can be effectively reduced, so that the investment and operation cost of the evaporative crystallization system are reduced.
(4) This application is through adopting the heat exchange step, can realize the regulation to concentration reverse osmosis unit inlet water temperature, thereby guarantee concentration reverse osmosis unit's osmotic pressure and dense water salinity at the optimum, because behind dense water penetrant unit, the temperature of dense water risees, if do not control concentration reverse osmosis unit's the temperature of intaking, the reverse osmosis membrane desalination reduces under the high temperature, the salt concentration multiple reduces, can lead to the quality of water variation of reuse water, consequently, adopt heat exchange step control entering temperature, also be favorable to ensureing the high desalination of reverse osmosis membrane.
Drawings
FIG. 1 is a schematic step diagram of an embodiment of a method for treating iron phosphate wastewater according to the present application;
FIG. 2 is a schematic step diagram of an embodiment of a first concentration process of the iron phosphate wastewater treatment method of the present application;
FIG. 3 is a schematic step diagram of an embodiment of a second concentration process of the iron phosphate wastewater treatment method of the present application;
FIG. 4 is a schematic view of an embodiment of an iron phosphate wastewater treatment apparatus according to the present application;
FIG. 5 is a partial schematic view of an embodiment of an iron phosphate wastewater treatment apparatus according to the present application;
FIG. 6 is a partial schematic view of an embodiment of an iron phosphate wastewater treatment plant according to the present application;
FIG. 7 is a partial schematic view of an embodiment of an iron phosphate wastewater treatment plant according to the present application;
FIG. 8 is a partial schematic view of an embodiment of an iron phosphate wastewater treatment plant according to the present application;
FIG. 9 is a partial schematic view of an embodiment of an iron phosphate wastewater treatment plant according to the present application;
FIG. 10 is a schematic view of an embodiment of an iron phosphate wastewater treatment device according to the present application, showing the water quality and quantity of inlet water and outlet water of each device;
in the figure: 100. a first concentration process; 101. concentrating the low-salt wastewater; 102. a mixing step; 103. removing heavy metal ions; 200. a second concentration process; 201. a first reverse osmosis treatment step; 202. a heat exchange step; 203. a second reverse osmosis treatment step; 300. fresh water purification process; 301. a first desalting step; 302. a second desalting step; 600. an evaporative crystallization process; 11. a first reverse osmosis unit; 12. a first concentrate tank; 13. a resin bed; 14. a first booster pump; 15. a first security filter; 16. a first high pressure pump; 21. a concentrated water reverse osmosis device; 22. a heat exchanger; 23. a second concentrated water tank; 24. a concentration reverse osmosis device; 31. an evaporative crystallization device; 41. a second water producing tank; 42. a second reverse osmosis unit; 43. a first water producing tank; 44. a terminal reverse osmosis device; 50. a fresh water tank.
Detailed Description
The present application is further described below with reference to specific embodiments, and it should be noted that, without conflict, any combination between the embodiments or technical features described below may form a new embodiment.
It is noted that the terms first, second and the like in the description and in the claims of the present application are used for distinguishing between similar elements and not necessarily for describing a particular sequential or chronological order.
The terms "comprises," "comprising," and "having," and any variations thereof, in the description and claims of this application are intended to cover a non-exclusive inclusion, such that a process, method, system, article, or apparatus that comprises a list of steps or elements is not necessarily limited to those steps or elements explicitly listed, but may include other steps or elements not expressly listed or inherent to such process, method, article, or apparatus.
As shown in fig. 1, the application provides a method for treating iron phosphate wastewater, which includes a first concentration process 100, a second concentration process 200, and a fresh water purification process 300, wherein a mixed solution obtained through the first concentration process 100 is concentrated through the second concentration process 200 to obtain a concentrated solution, and water is recovered through the fresh water purification process 300. The concentrated solution obtained from the second concentrated water process 200 is suitable for recovering salts through the evaporative crystallization process 600, thereby realizing zero discharge of wastewater.
As shown in FIG. 2, the first concentration process 100 includes
Low salt-containing wastewater concentration step 101: concentrating the wastewater with low salt content by using a first reverse osmosis device 11, wherein the wastewater with low salt content comprises rinsing water;
a mixing step 102: mixing concentrated water generated by the first reverse osmosis device 11 with mother liquor with high salt content;
heavy metal ion removal step 103: the primary mixed liquor obtained in the mixing step 102 is treated with a filtration device to remove heavy metal ions.
Because the salt content difference in rinsing water and the mother liquor is great, this application adopts first reverse osmosis unit 11 to carry out the concentrated processing to the rinsing water of low salt content at first, and the dense water after the concentration mixes with the higher mother liquor of salt content and obtains the first mixed liquid, and before the first mixed liquid got into second concentration technology 200, carry out heavy metal ion earlier to it and get rid of step 103, so be favorable to guaranteeing follow-up second concentration technology 200 in reverse osmosis unit's the operation, prevent reverse osmosis membrane scale deposit.
It is worth mentioning that in the first concentration process 100, both the rinse water and the mother liquor are pre-treated to meet the requirements of reverse osmosis operation.
In one embodiment, the filtering means in step 103 is a resin bed 13.
As shown in fig. 3 and 4, the second concentration process 200 includes: and (3) concentrating the mixed solution obtained in the first concentration process 100 by using a reverse osmosis device to obtain a concentrated solution with high salt content and produced water with low salt content.
The fresh water purification process 300 includes: the produced water obtained by the second concentration process 200 is desalinated by using a reverse osmosis device to obtain fresh water suitable for industrial production, and the concentrated water produced by the fresh water purification process 300 is suitable for being mixed with rinse water and then subjected to the low-salt wastewater concentration step 101 of the first concentration process 100.
It is worth mentioning that the evaporative crystallization process 600 may produce distilled water with a low salt content, which may be processed by the fresh water purification process 300 to increase the water recovery, as shown in fig. 4.
In a preferred embodiment, as shown in FIG. 3, the second concentrate process 200 includes
A first reverse osmosis treatment step 201: carrying out first concentration on the mixed solution by adopting a concentrated water reverse osmosis device 21 to obtain second concentrated water and second produced water;
a heat exchange step 202: performing heat exchange on at least one part of the second concentrated water to adjust the second concentrated water to a preset temperature;
second reverse osmosis treatment step 203: the second concentrated water after temperature adjustment is concentrated again by the concentration reverse osmosis device 24 to obtain a concentrated solution with high salt content and a third produced water with low salt content, and the obtained concentrated solution is also the concentrated solution used in the evaporative crystallization process 600.
The concentrated solution obtained by the method is concentrated water with high salt content, and the high salt content can reduce water entering the evaporative crystallization process 600, so that the investment and the operation cost of the evaporative crystallization process 600 are reduced.
Since the temperature of the concentrated water rises after passing through the concentrated water osmosis device, if the water inlet temperature of the concentration reverse osmosis device 24 is not controlled, the desalination rate of the reverse osmosis membrane is reduced and the salt concentration multiple is reduced at high temperature, so that the quality of the reused water is deteriorated. Thus, the present application controls the feed water temperature of the concentrating reverse osmosis unit 24 via the heat exchange step 202 to ensure that the concentrating reverse osmosis unit 24 is at an optimal feed water pressure and high efficiency desalination of the membrane.
In a preferred embodiment, the fresh water purification process 300 includes
A first desalination step 301: desalting the second produced water and the third produced water generated by the second concentration process 200 by using a second reverse osmosis device 42 to obtain fourth concentrated water and fourth produced water, wherein the fourth concentrated water is suitable for being mixed with rinsing water and then is subjected to the low-salt-content wastewater concentration step 101 of the first concentration process 100;
second desalination step 302: and (3) desalting the fourth produced water and the first produced water of the first reverse osmosis device 11 by using a terminal reverse osmosis device 44 to obtain fifth concentrated water and fresh water suitable for industrial production, wherein the fifth concentrated water is suitable for being mixed with the second produced water and the third produced water and then is subjected to a first desalting step 301.
Further, the low salinity wastewater concentration step 101 includes: adding sulfuric acid to adjust the ph of the wastewater to be 5.5 +/-0.5, pressurizing the wastewater to be treated by adopting a first pressurizing pump 14, introducing the wastewater after adjusting the ph into a first safety filter 15 for treatment, and conveying the wastewater output by the first safety filter 15 into a first reverse osmosis device 11 by a first high-pressure pump 16, as shown in fig. 5.
The first reverse osmosis device 11 outputs first concentrated water, that is, concentrated water generated in the low salt-containing wastewater concentration step 101, and first produced water. Preferably, the recovery rate of the first reverse osmosis device 11 is determined according to the salt content of the mother liquor, and the salt content of the first concentrated water is equal to that of the mother liquor, so that the recovery rate of the first reverse osmosis device 11 is 75-87.5%, and the total dissolved solid concentration TDS of the concentrated water is about 56000 +/-20% mg/L.
Further, the mixing step 102 includes: respectively conveying the first concentrated water generated in the low-salt wastewater concentration step 101 and the mother liquor with high salt content to a first concentrated water tank 12 for mixing to obtain a primary mixed solution, adding ammonia water to adjust the ph of the primary mixed solution to be 7.0 +/-0.5, and conveying the primary mixed solution to a filtering device (such as a resin bed 13) by using a second booster pump 17 for carrying out a heavy metal ion removal step 103.
Further, the heavy metal ion removing step 103 includes: the primary mixed liquid obtained in the mixing step 102 is treated by a filtering device (such as a resin bed 13) to remove heavy metal ions to obtain a mixed liquid, then sulfuric acid is added to adjust the ph of the mixed liquid to be 5.5 +/-0.5, the mixed liquid after the ph is adjusted enters a second security filter 18 for treatment, and the mixed liquid output by the second security filter 18 is conveyed into a concentrated water reverse osmosis device 21 by a second high-pressure pump 19.
In some embodiments, the high pressure energy of the second concentrated water output by the concentrated water reverse osmosis device 21 is recovered by the first energy recovery device 22 and then used for pressurizing the mixed liquid, that is, the mixed liquid treated by the second cartridge filter 18 is pressurized by the second high pressure pump 19 and the first energy recovery device 22 to be delivered into the concentrated water reverse osmosis device 21, as shown in fig. 6.
Preferably, the concentrated water reverse osmosis device 21 adopts a reverse osmosis membrane with high recovery rate and high desalination rate, adopts a two-section design, and adopts a two-section design to increase the pressure between sections, so that the energy consumption can be reduced by 40%. The total dissolved solids TDS of the second concentrate output by the concentrate reverse osmosis device 21 is about 110000 plus or minus 20% mg/L, and the second product water of the concentrate reverse osmosis device 21 is suitable for entering the second product water tank 41.
Further, in the heat exchange step 202, a part of the second concentrated water passes through the heat exchanger 22 and then is sent to the second concentrated water tank 23, another part of the second concentrated water is directly sent to the second concentrated water tank 23, and after the second concentrated water with different temperatures is mixed in the second concentrated water tank 23, the temperature of the second concentrated water in the second concentrated water tank 23 is kept at 30-35 ℃. Of course, all the second concentrated water can also be subjected to heat exchange through the heat exchanger 22 so as to control the temperature to be 30-35 ℃. Then, sulfuric acid is added into the second concentrated water to adjust ph to 5.5 +/-0.5, the second concentrated water after ph adjustment is input into a third security filter 26 by a third booster pump 25, and the second concentrated water passing through the third security filter 26 is boosted by a third high-pressure pump 27 and then is conveyed to a concentration reverse osmosis device 24.
In some embodiments, the high pressure energy of the concentrated solution output by the reverse osmosis device 24 is recovered by the second energy recovery device 28 and then used for pressurizing the second concentrated water, that is, the second concentrated water processed by the third cartridge filter 26 is pressurized by the third high pressure pump 27 and the second energy recovery device 28 and then input to the reverse osmosis device 24, as shown in fig. 7.
The concentration reverse osmosis device 24 adopts an ultrahigh-pressure high-desalination reverse osmosis membrane, adopts a two-section design, the membrane shell is 6-core-packed, a booster pump is arranged between sections, the design can reduce the energy consumption by 48%, the water inlet pressure of the concentration reverse osmosis device 24 is about 8-12 MPa, the total dissolved solid TDS of the concentrated solution can be increased to 180000mg/L to enter an evaporative crystallization process 600, and the third product water of the concentration reverse osmosis device 24 enters a second product water pool 41.
Further, in the first desalting step 301, the second produced water, the third produced water, the distilled water with low salt content produced by the evaporative crystallization process 600 and the fifth concentrated water are fed into the second water producing tank 41 to be mixed, ammonia water is added to adjust ph to be neutral, the liquid in the second water producing tank 41 is conveyed to the fourth cartridge filter 46 by using the fourth booster pump 45, and then conveyed to the second reverse osmosis device 42 by using the fourth high-pressure pump 47, as shown in fig. 8. The fourth produced water of the second reverse osmosis device 42 enters the first water producing tank 43, and the fourth concentrated water of the second reverse osmosis device 42 is mixed with the rinsing water and then subjected to the low salinity wastewater concentration step 101 of the first concentration process 100. The second reverse osmosis device 42 can achieve a high recovery rate of 85% by taking into account the quality of the feed water to the second reverse osmosis device 42, and the like.
Further, in the second desalination step 302, the first produced water and the fourth produced water output by the first reverse osmosis device 11 are respectively input into the first water producing tank 43 to be mixed, ammonia water is added to adjust ph to be neutral, the liquid in the first water producing tank 43 is conveyed to the fifth safety filter 49 by the fifth booster pump 48, and then conveyed to the terminal reverse osmosis device 44 by the fifth high-pressure pump 40 for desalination treatment. The recovery rate of the terminal reverse osmosis device 44 is 85%, the conductivity of the produced fresh water is below 10 mu s/cm, the requirement of the production water is met, and fifth concentrated water of the terminal reverse osmosis device 44 is input into the second water producing tank 41.
As shown in fig. 4, the present application also provides an iron phosphate wastewater treatment apparatus, including:
a first reverse osmosis device 11 for concentrating the rinse water having a low salt content to produce a first concentrated water and a first produced water;
a first concentrated water tank 12 for mixing the first concentrated water and the mother liquor having a high salt content to obtain a primary mixed solution;
a resin bed 13 for removing heavy metal ions in the primary mixed liquid to obtain a mixed liquid;
a concentrated water reverse osmosis device 21 for concentrating the mixed solution to obtain second concentrated water and second produced water;
a concentration reverse osmosis device 24 for concentrating the second concentrated water to obtain a concentrated solution and a third produced water;
a second water producing tank 41 for mixing the second water produced, the third water produced, and the water with a low salt content produced by the evaporative crystallization device 31;
the second reverse osmosis device 42 is used for desalting the liquid in the second water production tank 41 to obtain fourth concentrated water and fourth produced water;
a first water producing tank 43 for mixing the fourth water producing water and the first water producing water;
and a final reverse osmosis device 44 for desalinating the liquid in the first water producing tank 43 to obtain fresh water suitable for industrial production and fifth concentrated water suitable for being input into the second water producing tank 41.
In a preferred embodiment, the iron phosphate wastewater treatment device further comprises a heat exchanger 22 and a second concentrated water tank 23, wherein the heat exchanger 22 is used for adjusting the temperature of the second concentrated water, and the adjusted temperature second concentrated water is stored in the second concentrated water tank 23. By providing the heat exchanger 22, the inlet water temperature of the concentrating reverse osmosis unit 44 can be adjusted to ensure that the concentrating reverse osmosis unit 24 is at an optimal inlet water pressure and high efficiency desalination of the membrane.
In a preferred embodiment, the iron phosphate wastewater treatment device further comprises a first energy recovery device 22 for recovering high-pressure energy of the second concentrated water, and the energy of the first energy recovery device 22 can be used for pressurizing the mixed liquid.
In a preferred embodiment, the iron phosphate wastewater treatment device further comprises a second energy recovery device 28 for recovering high-pressure energy of the concentrated solution, and the energy of the second energy recovery device 28 can be used for pressurizing the second concentrated water.
Further, as shown in fig. 5, the iron phosphate wastewater treatment device further comprises a first booster pump 14, a first safety filter 15, a first high-pressure pump 16 and a first concentrated water tank 12, wherein the first booster pump 14 is used for delivering pretreated rinsing water to the first safety filter 15, the rinsing water output by the first safety filter 15 is suitable for entering the first reverse osmosis device 11 through the first high-pressure pump 16, the first concentrated water generated by the first reverse osmosis device 11 is suitable for being input into the first concentrated water tank 12, and the pretreated mother liquor is also suitable for being input into the first concentrated water tank 12, so that the rinsing liquid and the mother liquor are mixed in the first concentrated water tank 12.
Further, as shown in fig. 6, the iron phosphate wastewater treatment device further includes a second booster pump 17, a second cartridge filter 18 and a second high-pressure pump 19, the second booster pump 17 is used for inputting the primary mixed liquid of the first concentrated water tank 12 into the resin bed 13, the mixed liquid passing through the resin bed 13 enters the second cartridge filter 18, and the mixed liquid output by the second cartridge filter is suitable for entering the concentrated water reverse osmosis device 21 through the second high-pressure pump 19 and the lifting of the first energy recovery device 22.
Further, as shown in fig. 7, the iron phosphate wastewater treatment device further includes a third booster pump 25, a third cartridge filter 26 and a third high-pressure pump 27, the third booster pump 25 is used for delivering the second concentrated water from the second concentrated water tank 23 to the third cartridge filter 26, and the second concentrated water output from the third cartridge filter 26 is lifted by the third high-pressure pump 27 and the second energy recovery device 28 and enters the concentration reverse osmosis device 24.
Further, as shown in fig. 8, the iron phosphate wastewater treatment device further includes a fourth booster pump 45, a fourth cartridge filter 46, and a fourth high-pressure pump 47, wherein the fourth booster pump 45 is used for delivering the liquid in the second water production tank 41 into the fourth cartridge filter 46, and the liquid output from the fourth cartridge filter 46 is lifted by the fourth high-pressure pump 47 to enter the second reverse osmosis device 42.
Further, as shown in fig. 9, the iron phosphate wastewater treatment device further comprises a fifth pressurizing pump 48, a fifth safety filter 49 and a fifth high-pressure pump 40, wherein the fifth pressurizing pump 48 is used for conveying the liquid in the first water production tank 43 into the fifth safety filter 49, and the liquid output by the fifth safety filter 49 enters the terminal reverse osmosis device 44 through the lifting of the fifth high-pressure pump 40.
[ example 1 ]
As shown in FIG. 10, rinse water having TDS (Total dissolved solids concentration) of 14000. + -. 20% mg/L was supplied at a flow rate of 350m 3 Inputting the fourth concentrated water into a rinsing water pretreatment module at a speed of TDS 7500 +/-20% mg/L and a flow rate of 34m 3 Inputting the rinsing water pretreatment module; the treated rinse water was at TDS 14000 + -20% mg/L, a flow rate of 384m 3 H is fed into the first reverse osmosis unit 11, the recovery rate of the first reverse osmosis unit 11 is 75%, the second reverse osmosis unitThe first concentrated water generated by a reverse osmosis device 11 has TDS 56000 +/-20% mg/L and flow rate of 96m 3 Inputting the water into a first concentrated water tank 12, and generating first produced water with TDS 140 +/-20% mg/L and flow rate of 288m 3 Input/h into the first product water tank 43; the mother liquor is TDS 50000 +/-20% mg/L with flow rate of 64m 3 Inputting the treated mother liquor into a mother liquor pretreatment module at a TDS 50000 +/-20% mg/L flow rate of 64m 3 The/h is input into a first concentrated water tank 12; the primary mixed liquid of the first concentrated water tank 12 is treated with TDS 55000 +/-20% mg/L and the flow rate of 160m 3 Input to the resin bed 13; the mixed liquid passing through the resin bed 13 is treated with TDS 55000 +/-20% mg/L and the flow rate is 160m 3 Inputting the second concentrated water into a second concentrated water tank 23, wherein the second concentrated water obtained by the concentrated water reverse osmosis device 21 is input into the concentrated water reverse osmosis device 21 at a TDS 1100 +/-20% mg/L flow rate of 80m 3 H is input into a second water producing tank 41; the second concentrated water of the second concentrated water tank 23 is TDS 110000 +/-20% mg/L with the flow rate of 80m 3 Inputting the concentrated solution into a concentration reverse osmosis device 24 at a speed of 24 hours, wherein the recovery rate of the concentration reverse osmosis device 24 is 35 percent, and the concentrated solution obtained by the concentration reverse osmosis device 24 is at the TDS 170000 +/-6 percent mg/L with the flow rate of 52m 3 The third produced water is input into an evaporative crystallization device 31, and the obtained third produced water has the TDS 2200 +/-20% mg/L and the flow rate of 28m 3 H is input into a second water producing tank 41; the distilled water generated by the evaporative crystallization device 31 has TDS 800mg/L and flow rate of 46.8m 3 H is input into a second water producing tank 41; the liquid of the second water producing tank 41 has TDS 1135 +/-20% mg/L and flow rate 227m 3 The water/h is input into the second reverse osmosis device 42, the recovery rate of the second reverse osmosis device 42 is 85 percent, and the fourth produced water of the second reverse osmosis device 42 is TDS 1135 +/-20 percent mg/L with the flow rate of 193m 3 Input/h into the first product water tank 43; the liquid of the first water producing pool 43 has TDS 140 +/-20% mg/L and flow rate of 481m 3 Inputting the water/h into a terminal reverse osmosis device 44, wherein the recovery rate of the terminal reverse osmosis device 44 is 85 percent, the conductivity of the terminal reverse osmosis device 44 is less than 10 mu s/cm, and the flow rate is 409m 3 Fresh water per hour, the fifth concentrated water is obtained with TDS 900 +/-20% mg/L and flow rate of 72.2m 3 And/h is fed to a second product water tank 41.
The salt content of the concentrated solution obtained by the concentration reverse osmosis device 24 of the embodiment can be 170000mg/L, the amount of water entering the evaporative crystallization device 31 is less, and the operation cost of the evaporative crystallization device 31 is favorably reduced. The water reuse rate of the whole system of the embodiment reaches 98 percent.
The foregoing has described the general principles, essential features, and advantages of the application. It will be understood by those skilled in the art that the present application is not limited to the embodiments described above, which are merely illustrative of the principles of the application, but that various changes and modifications may be made without departing from the spirit and scope of the application, and these changes and modifications are intended to be within the scope of the application as claimed. The scope of protection claimed by this application is defined by the following claims and their equivalents.
Claims (10)
1. A method for treating iron phosphate wastewater is characterized by comprising a first concentration process, a second concentration process and a fresh water purification process,
the first concentration process comprises:
a low-salt-content wastewater concentration step, wherein a first reverse osmosis device is adopted to concentrate wastewater with low salt content, and the wastewater with low salt content comprises rinsing water;
a mixing step, namely mixing the first concentrated water generated by the first reverse osmosis device with the mother liquor with high salt content;
a heavy metal ion removing step of removing heavy metal ions by treating the primary mixed liquid obtained in the mixing step with a filtering device;
the second concentration process comprises: concentrating the mixed solution obtained by the first concentration process by using a reverse osmosis device so as to obtain a concentrated solution with high salt content and produced water with low salt content, wherein the concentrated solution is suitable for an evaporative crystallization process;
the fresh water purification process comprises the following steps: and desalting the produced water obtained by the second-step concentration process by using a reverse osmosis device to obtain fresh water suitable for industrial production.
2. The iron phosphate wastewater treatment method according to claim 1, wherein the second concentration process comprises:
a first reverse osmosis treatment step, namely performing primary concentration on the mixed liquor obtained by the first concentration process by adopting a concentrated water reverse osmosis device to obtain second concentrated water and second produced water;
a heat exchange step of carrying out heat exchange on the second concentrated water to adjust the second concentrated water to a preset temperature;
and a second reverse osmosis treatment step, namely concentrating the second concentrated water after temperature adjustment by using a concentration reverse osmosis device to obtain the concentrated solution with high salt content and third produced water with low salt content.
3. The iron phosphate wastewater treatment method according to claim 2, wherein the ph of the mixed solution is adjusted to 5.5 ± 0.5, and the mixed solution is pressurized and subjected to cartridge filtration and then is fed into the concentrated water reverse osmosis device through a high-pressure pump; and adjusting the ph of the second concentrated water to be 5.5 +/-0.5, and after the second concentrated water is pressurized and subjected to security filtration, conveying the second concentrated water into the concentration reverse osmosis device through a high-pressure pump.
4. The iron phosphate wastewater treatment method according to claim 2, wherein the fresh water purification process comprises:
a first desalting step: desalting the second produced water and the third produced water by adopting a second reverse osmosis device to obtain fourth concentrated water and fourth produced water, wherein the fourth concentrated water is suitable for being mixed with rinsing water and then subjected to the low-salt-content wastewater concentration step;
and a second desalting step: and desalting the fourth produced water and the first produced water of the first reverse osmosis device by adopting a terminal reverse osmosis device to obtain fifth concentrated water and fresh water suitable for industrial production, wherein the fifth concentrated water is suitable for being mixed with the second produced water and the third produced water and then is subjected to the first desalting step.
5. The iron phosphate wastewater treatment method according to claim 4, wherein the second produced water, the third produced water and the fifth concentrated water are mixed, ph is adjusted to 7.0 ± 0.5, and after pressurization and security filtration, the mixture is fed into the second reverse osmosis device through a high-pressure pump; and mixing the first produced water and the fourth produced water, adjusting the ph to 7.0 +/-0.5, and after pressurization and security filtration, inputting the mixture into the terminal reverse osmosis device through a high-pressure pump.
6. The iron phosphate wastewater treatment method according to any one of claims 1 to 5, wherein the pH of the wastewater is adjusted to 5.5 +/-0.5, the wastewater is pressurized and subjected to security filtration and then is fed into a first reverse osmosis device through a high-pressure pump, and the recovery rate of the first reverse osmosis device is 75-87.5%; and adjusting the ph of the primary mixed liquid of the first concentrated water and the mother liquid to 7.0 +/-0.5, and then inputting the primary mixed liquid into a filtering device by utilizing a booster pump to remove heavy metal ions to obtain the mixed liquid.
7. The utility model provides an iron phosphate effluent treatment plant which characterized in that includes:
a first reverse osmosis device for concentrating the rinse water having a low salt content to produce a first concentrated water and a first produced water;
the first concentrated water tank is used for mixing the first concentrated water and the mother liquor with high salt content to obtain primary mixed liquor;
the resin bed is used for removing heavy metal ions in the primary mixed liquid to obtain mixed liquid;
the concentrated water reverse osmosis device is used for concentrating the mixed solution to obtain second concentrated water and second produced water;
the concentration reverse osmosis device is used for concentrating the second concentrated water to obtain concentrated solution and third produced water;
a second water producing tank for mixing the second produced water and the third produced water;
the second reverse osmosis device is used for desalting the liquid in the second water producing pool to obtain fourth concentrated water and fourth produced water;
a first water producing tank for mixing the fourth water producing and the first water producing;
and the terminal reverse osmosis device is used for desalting the liquid in the first water producing tank to obtain fresh water and fifth concentrated water which are suitable for industrial production, and the fifth concentrated water is suitable for being input into the second water producing tank.
8. The iron phosphate wastewater treatment device according to claim 7, further comprising a heat exchanger and a second concentrated water tank, wherein the heat exchanger is used for adjusting the temperature of the second concentrated water, and the adjusted temperature second concentrated water is stored in the second concentrated water tank.
9. The iron phosphate wastewater treatment device according to claim 8, further comprising a first energy recovery device for recovering high-pressure energy of the second concentrated water, wherein the energy of the first energy recovery device is used for pressurizing the mixed liquid.
10. The iron phosphate wastewater treatment device according to claim 8, further comprising a second energy recovery device for recovering high-pressure energy of the concentrated solution, wherein the energy of the second energy recovery device is used for pressurizing the second concentrated water.
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