CN220300568U - Ferric phosphate wastewater treatment system - Google Patents
Ferric phosphate wastewater treatment system Download PDFInfo
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- CN220300568U CN220300568U CN202321636972.0U CN202321636972U CN220300568U CN 220300568 U CN220300568 U CN 220300568U CN 202321636972 U CN202321636972 U CN 202321636972U CN 220300568 U CN220300568 U CN 220300568U
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- reverse osmosis
- osmosis device
- water
- mother liquor
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- WBJZTOZJJYAKHQ-UHFFFAOYSA-K iron(3+) phosphate Chemical compound [Fe+3].[O-]P([O-])([O-])=O WBJZTOZJJYAKHQ-UHFFFAOYSA-K 0.000 title claims abstract description 30
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 22
- 239000005955 Ferric phosphate Substances 0.000 title claims description 17
- 229940032958 ferric phosphate Drugs 0.000 title claims description 17
- 229910000399 iron(III) phosphate Inorganic materials 0.000 title claims description 17
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 122
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 86
- 238000005406 washing Methods 0.000 claims abstract description 52
- 239000012452 mother liquor Substances 0.000 claims abstract description 41
- 238000006243 chemical reaction Methods 0.000 claims abstract description 38
- 238000002425 crystallisation Methods 0.000 claims abstract description 24
- 230000008025 crystallization Effects 0.000 claims abstract description 24
- 239000012528 membrane Substances 0.000 claims abstract description 24
- 239000000919 ceramic Substances 0.000 claims abstract description 21
- 238000001704 evaporation Methods 0.000 claims abstract description 20
- 230000008020 evaporation Effects 0.000 claims abstract description 20
- 239000011347 resin Substances 0.000 claims abstract description 15
- 229920005989 resin Polymers 0.000 claims abstract description 15
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 20
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 20
- ATRRKUHOCOJYRX-UHFFFAOYSA-N Ammonium bicarbonate Chemical compound [NH4+].OC([O-])=O ATRRKUHOCOJYRX-UHFFFAOYSA-N 0.000 claims description 19
- 229910000013 Ammonium bicarbonate Inorganic materials 0.000 claims description 19
- 235000012538 ammonium bicarbonate Nutrition 0.000 claims description 19
- 239000001099 ammonium carbonate Substances 0.000 claims description 19
- 239000004254 Ammonium phosphate Substances 0.000 claims description 15
- 229910000148 ammonium phosphate Inorganic materials 0.000 claims description 15
- 235000019289 ammonium phosphates Nutrition 0.000 claims description 15
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 claims description 15
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 8
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 8
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 8
- 238000004519 manufacturing process Methods 0.000 claims description 8
- 238000001556 precipitation Methods 0.000 claims description 7
- ZRIUUUJAJJNDSS-UHFFFAOYSA-N ammonium phosphates Chemical compound [NH4+].[NH4+].[NH4+].[O-]P([O-])([O-])=O ZRIUUUJAJJNDSS-UHFFFAOYSA-N 0.000 claims description 6
- 238000012856 packing Methods 0.000 claims description 6
- 239000002253 acid Substances 0.000 claims description 3
- 150000001768 cations Chemical class 0.000 claims description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims 4
- 239000012267 brine Substances 0.000 claims 3
- 239000010802 sludge Substances 0.000 claims 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims 3
- 229910021529 ammonia Inorganic materials 0.000 claims 2
- 229910000398 iron phosphate Inorganic materials 0.000 abstract description 13
- 239000000463 material Substances 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 239000010842 industrial wastewater Substances 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 14
- 150000003839 salts Chemical class 0.000 description 12
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 10
- 239000002351 wastewater Substances 0.000 description 10
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 239000011777 magnesium Substances 0.000 description 6
- 239000011572 manganese Substances 0.000 description 6
- 239000010413 mother solution Substances 0.000 description 5
- -1 phosphate radicals Chemical class 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 4
- PWHULOQIROXLJO-UHFFFAOYSA-N Manganese Chemical compound [Mn] PWHULOQIROXLJO-UHFFFAOYSA-N 0.000 description 4
- 235000011941 Tilia x europaea Nutrition 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 239000004571 lime Substances 0.000 description 4
- 159000000003 magnesium salts Chemical class 0.000 description 4
- 229910052748 manganese Inorganic materials 0.000 description 4
- 229910001437 manganese ion Inorganic materials 0.000 description 4
- 239000004576 sand Substances 0.000 description 4
- 239000013049 sediment Substances 0.000 description 4
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 3
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 3
- 229910001424 calcium ion Inorganic materials 0.000 description 3
- 229910021645 metal ion Inorganic materials 0.000 description 3
- 229910052698 phosphorus Inorganic materials 0.000 description 3
- 239000011574 phosphorus Substances 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 2
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 2
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 239000006004 Quartz sand Substances 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- LFVGISIMTYGQHF-UHFFFAOYSA-N ammonium dihydrogen phosphate Chemical compound [NH4+].OP(O)([O-])=O LFVGISIMTYGQHF-UHFFFAOYSA-N 0.000 description 2
- 229910000387 ammonium dihydrogen phosphate Inorganic materials 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- GELKBWJHTRAYNV-UHFFFAOYSA-K lithium iron phosphate Chemical compound [Li+].[Fe+2].[O-]P([O-])([O-])=O GELKBWJHTRAYNV-UHFFFAOYSA-K 0.000 description 2
- 229910052749 magnesium Inorganic materials 0.000 description 2
- 229910001425 magnesium ion Inorganic materials 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 235000019837 monoammonium phosphate Nutrition 0.000 description 2
- 239000006012 monoammonium phosphate Substances 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- 239000002244 precipitate Substances 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- JZRWCGZRTZMZEH-UHFFFAOYSA-N Thiamine Natural products CC1=C(CCO)SC=[N+]1CC1=CN=C(C)N=C1N JZRWCGZRTZMZEH-UHFFFAOYSA-N 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 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 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 239000001506 calcium phosphate Substances 0.000 description 1
- 229910000389 calcium phosphate Inorganic materials 0.000 description 1
- 235000011010 calcium phosphates Nutrition 0.000 description 1
- 239000010406 cathode material Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- SURQXAFEQWPFPV-UHFFFAOYSA-L iron(2+) sulfate heptahydrate Chemical compound O.O.O.O.O.O.O.[Fe+2].[O-]S([O-])(=O)=O SURQXAFEQWPFPV-UHFFFAOYSA-L 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 150000003017 phosphorus Chemical class 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 229910052567 struvite Inorganic materials 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- KYMBYSLLVAOCFI-UHFFFAOYSA-N thiamine Chemical compound CC1=C(CCO)SCN1CC1=CN=C(C)N=C1N KYMBYSLLVAOCFI-UHFFFAOYSA-N 0.000 description 1
- 229960003495 thiamine Drugs 0.000 description 1
- 235000019157 thiamine Nutrition 0.000 description 1
- 239000011721 thiamine Substances 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/131—Reverse-osmosis
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The utility model belongs to the technical field of industrial wastewater treatment, and provides an iron phosphate wastewater treatment system which comprises a washing water treatment system, a mother liquor pretreatment system and an MVR evaporation crystallization system; the washing water treatment system comprises a washing water buffer tank, a washing water reaction tank, a washing water ceramic membrane, a multistage reverse osmosis device and a pure water tank which are connected in sequence; the mother liquor treatment system comprises a mother liquor buffer tank, a mother liquor reaction tank, a mother liquor ceramic membrane, a multi-medium filter, a resin tower, an ultrafiltration device and a high-pressure reverse osmosis device which are connected in sequence; the water output end of the high-pressure reverse osmosis device is connected with the input end of the multistage reverse osmosis device, and the three-stage concentrated water output end of the multistage reverse osmosis device is connected with the input end of the high-pressure reverse osmosis device; the input end of the MVR evaporation crystallization system is connected with the concentrated water output end of the high-pressure reverse osmosis device, and the condensed water output end of the MVR evaporation crystallization system is connected with the washing water buffer pool. The system can recycle the alkaline condensate water, save chemical auxiliary materials and ensure that the ammonium radical does not exceed the standard.
Description
Technical Field
The utility model belongs to the technical field of industrial wastewater treatment, and particularly relates to an iron phosphate wastewater treatment system.
Background
The disclosure of this background section is only intended to increase the understanding of the general background of the utility model and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art already known to those of ordinary skill in the art.
Iron phosphate is a precursor for producing lithium iron phosphate cathode materials, and along with the rapid development of the electric automobile industry and the construction of energy storage stations, the market demand of lithium iron phosphate is increasingly larger, and the demand of battery-grade iron phosphate raw materials is also increased year by year. At present, the iron phosphate is mainly prepared by adopting the technical process of taking the byproduct ferrous sulfate heptahydrate of titanium dioxide as an iron source and taking monoammonium phosphate or phosphoric acid as a phosphorus source. The iron phosphate production process produces a large amount of wastewater mainly derived from washing water produced in the crude iron phosphate washing process and high-concentration iron phosphate synthesis mother liquor, and contains sulfate radicals, phosphate radicals, iron, magnesium, manganese, calcium and other metal ion impurities.
Currently, the main methods for iron phosphate production wastewater are classified into a lime precipitation method, a magnesium salt treatment method and a membrane treatment method. Lime precipitation processes remove impurities by adding lime to the wastewater in a manner that forms calcium phosphate, calcium sulfate, and metal precipitates. The magnesium salt treatment method achieves the aim of removing ammonia nitrogen and total phosphorus by adding a magnesium source and forming struvite sediment with the ammonia nitrogen and the total phosphorus, and the redundant ammonia nitrogen is stripped and recovered under alkaline conditions and then is further concentrated and evaporated. The membrane treatment method generates the thiamine fertilizer and the phosphamine fertilizer through a membrane filtration and multi-effect evaporation combined process, and simultaneously recycles distilled water. However, each of the above methods has drawbacks: the lime precipitation method generates new solid waste and the salt content of the discharged water is too high; the magnesium salt treatment method needs a large amount of magnesium salt and steam, and has complex flow and high cost; the membrane treatment method has poor quality of recovered products and higher system operation cost.
In order to solve the defects of the method, in the prior art, ammonia water is added into the wastewater produced by iron phosphate to precipitate metal ions, and ammonium sulfate and ammonium phosphate are recovered, so that new impurity ions are prevented from being introduced, and the wastewater treatment cost is reduced. However, in order to completely precipitate and remove the metal ion impurities contained in the wastewater, a large amount of ammonia water needs to be added, resulting in exceeding of ammonium ion in the recovered pure water after treatment. In order to recover the ammonium ions exceeding the standard, it is necessary to supplement sulfate or phosphate, and the operating pressure of the ammonium sulfate and ammonium phosphate recovery device is increased, resulting in an increase in the operating cost.
Disclosure of Invention
In order to solve the defects in the prior art, the utility model aims to provide an iron phosphate wastewater treatment system. The utility model improves on the basis of the original design, and the MVR evaporation crystallization system is connected with the washing water buffer pool to recycle the alkaline evaporation condensate water, thereby reducing the construction cost and the dosage of chemical auxiliary materials and controlling the content of ammonium ions in the pure water.
In order to achieve the above object, the present utility model is realized by the following technical scheme:
an iron phosphate wastewater treatment system comprises a washing water treatment system, a mother liquor pretreatment system and an MVR evaporation crystallization system;
the washing water treatment system comprises a washing water buffer tank, a washing water reaction tank, a washing water ceramic membrane, a multistage reverse osmosis device and a pure water tank which are connected in sequence;
the mother liquor treatment system comprises a mother liquor buffer tank, a mother liquor reaction tank, a mother liquor ceramic membrane, a multi-medium filter, a resin tower, an ultrafiltration device and a high-pressure reverse osmosis device which are connected in sequence;
the water output end of the high-pressure reverse osmosis device is connected with the input end of the multistage reverse osmosis device, and the three-stage concentrated water output end of the multistage reverse osmosis device is connected with the input end of the high-pressure reverse osmosis device;
the input end of the MVR evaporation crystallization system is connected with the concentrated water output end of the high-pressure reverse osmosis device, and the condensed water output end of the MVR evaporation crystallization system is connected with the washing water buffer pool.
Preferably, the system further comprises a salt mud treatment system, wherein the salt mud treatment system comprises a salt mud tank and a plate-and-frame filter press which are sequentially connected, the input end of the salt mud tank is connected with the precipitation discharge end of the washing water ceramic membrane and the precipitation discharge end of the mother liquor ceramic membrane, and the water output end of the plate-and-frame filter press is connected with the input end of the mother liquor reaction tank.
Preferably, the multistage reverse osmosis device comprises a first stage reverse osmosis device, a second stage reverse osmosis device and a third stage reverse osmosis device; the input end of the first-stage reverse osmosis device is respectively connected with the water production output end of the washing ceramic membrane and the second-stage concentrated water output end of the second-stage reverse osmosis device; the input end of the secondary reverse osmosis device is respectively connected with the primary water output end of the primary reverse osmosis device and the tertiary water output end of the tertiary reverse osmosis device, and the secondary water output end of the secondary reverse osmosis device is connected with a pure water tank; the input end of the three-stage reverse osmosis device is connected with the second-stage concentrated water output end of the first-stage reverse osmosis device, and the third-stage concentrated water output end of the three-stage reverse osmosis device is connected with the input end of the MVR evaporation crystallization system.
Preferably, the washing water reaction tank is provided with an ammonia water dosing system and an ammonium bicarbonate dosing system, and the mother solution reaction tank is provided with an ammonium phosphate salt dosing system, an ammonia water dosing system and an ammonium bicarbonate dosing system.
Preferably, an ammonia water dosing system and an ammonium bicarbonate dosing system are arranged above the washing water reaction tank, and an ammonium phosphate dosing system, an ammonia water dosing system and an ammonium bicarbonate dosing system are arranged above the mother solution reaction tank.
Preferably, the dosing mode of the ammonia water dosing system and the ammonium bicarbonate dosing system to the washing water reaction tank is self-flowing, and the dosing mode of the ammonium phosphate salt dosing system, the ammonia water dosing system and the ammonium bicarbonate dosing system to the mother solution reaction tank is self-flowing.
Preferably, the ammonium phosphate in the ammonium phosphate dosing system is one or two of monoammonium phosphate and ammonium phosphate.
Preferably, the media in the multi-media filter are 4-8mm quartz sand, 0.5-1mm manganese sand and 2-4mm manganese sand.
Preferably, the resin in the resin column is a weak acid cation resin.
Preferably, the MVR evaporative crystallization system is provided with a finished product ammonium sulfate packing system and a finished product ammonium phosphate packing system.
The beneficial effects obtained by one or more of the technical schemes of the utility model are as follows:
according to the utility model, the ferric phosphate wastewater is treated by the combination of the washing water treatment system, the mother solution pretreatment system, the evaporation crystallization system and the salt slurry treatment system, so that the ammonium sulfate and the ammonium phosphate are obtained, the recycling of the wastewater is realized, the alkaline condensate water of the evaporation crystallization is introduced into the washing water buffer pool to adjust the pH, the chemical auxiliary materials are saved, and the ammonium ion in the pure water is ensured not to exceed the standard.
Drawings
The accompanying drawings, which are included to provide a further understanding of the utility model and are incorporated in and constitute a part of this specification, illustrate embodiments of the utility model and together with the description serve to explain the utility model.
FIG. 1 is a schematic diagram of a ferric phosphate wastewater treatment system provided by the utility model;
FIG. 2 is a schematic diagram of the flow of the iron phosphate wastewater treatment system provided by the utility model;
wherein 1 is a washing water buffer pool, 2 is a washing water reaction pool, 3 is a washing water ceramic membrane, 4 is a primary reverse osmosis device, 5 is a secondary reverse osmosis device, 6 is a tertiary reverse osmosis device, 7 is a pure water pool, 8 is a salt mud pool, 9 is a plate-and-frame filter press, 10 is a mother liquor buffer pool, 11 is a mother liquor reaction pool, 12 is a mother liquor ceramic membrane, 13 is a multi-medium filter, 14 is a resin tower, 15 is an ultrafiltration device, 16 is a high-pressure reverse osmosis device, 17 is an MVR evaporative crystallization system, XS represents ferric phosphate washing water, MY represents ferric phosphate mother liquor, NH represents ammonia water, NHC represents ammonium bicarbonate, NP represents ammonium phosphate salt, HS represents sulfuric acid, NS represents ammonium sulfate, LNS represents condensed water, NB represents mud cake.
Detailed Description
In order to enable those skilled in the art to more clearly understand the technical scheme of the present utility model, the technical scheme of the present utility model will be described in detail below with reference to specific examples and comparative examples.
Example 1
The structure of the ferric phosphate wastewater treatment system is shown in figure 1. The ferric phosphate wastewater treatment system comprises a washing water treatment system, a mother liquor pretreatment system, an MVR evaporation crystallization system 17 and a salt slurry treatment system. The washing water treatment system comprises a washing water buffer tank 1, a washing water reaction tank 2, a washing water ceramic membrane 3, a multistage reverse osmosis device and a pure water tank 7 which are sequentially connected, wherein the multistage reverse osmosis device comprises a first stage reverse osmosis device 4, a second stage reverse osmosis device 5 and a third stage reverse osmosis device 6. The mother liquor treatment system comprises a mother liquor buffer tank 10, a mother liquor reaction tank 11, a mother liquor ceramic membrane 12, a multi-medium filter 13, a resin tower 14, an ultrafiltration device 15 and a high-pressure reverse osmosis device 16 which are connected in sequence. The salt mud treatment system comprises a salt mud tank 8 and a plate-and-frame filter press 9 which are connected in sequence.
The first-stage reverse osmosis device 4 is provided with a sulfuric acid dosing system, and the input end of the first-stage reverse osmosis device 4 is respectively connected with the water production output end of the washing water ceramic membrane 3 and the second-stage concentrated water output end of the second-stage reverse osmosis device 5. The second-stage reverse osmosis device 5 is provided with a sulfuric acid dosing system, the input end of the second-stage reverse osmosis device 5 is respectively connected with the first-stage water production output end of the first-stage reverse osmosis device 4 and the third-stage water production output end of the third-stage reverse osmosis device 6, the second-stage water production output end of the second-stage reverse osmosis device 5 is connected with the pure water tank 7, the input end of the third-stage reverse osmosis device 6 is connected with the second-stage concentrated water output end of the first-stage reverse osmosis device 4, and the third-stage concentrated water output end of the third-stage reverse osmosis device 6 is connected with the input end of the MVR evaporative crystallization system 17.
The input end of the salt mud tank 8 is connected with the sediment discharge end of the washing water ceramic membrane 3 and the sediment discharge end of the mother liquor ceramic membrane 12, and the water output end of the plate-and-frame filter press 9 is connected with the input end of the mother liquor reaction tank 11.
The input end of the MVR evaporation crystallization system 17 is connected with the concentrated water output end of the high-pressure reverse osmosis device 16, and the condensed water output end of the MVR evaporation crystallization system 17 is connected with the washing water buffer tank 1. The condensed water of the MVR evaporative crystallization system 17 is output to a washing water buffer pool, so that the pH of washing water can be adjusted, and the consumption of ammonia water in the subsequent flow is reduced. The MVR evaporative crystallization system 17 is provided with a finished product ammonium sulfate packing system and a finished product ammonium phosphate packing system.
An ammonia water dosing system and an ammonium bicarbonate dosing system are arranged above the washing water reaction tank 2, and an ammonium phosphate dosing system, an ammonia water dosing system and an ammonium bicarbonate dosing system are arranged above the mother liquor reaction tank 11. The dosing mode of the ammonia water dosing system and the ammonium bicarbonate dosing system to the washing water reaction tank 2 is self-flowing, and the dosing mode of the ammonium phosphate dosing system, the ammonia water dosing system and the ammonium bicarbonate dosing system to the mother solution reaction tank 11 is self-flowing.
The media in the multi-media filter 13 are 4-8mm quartz sand, 0.5-1mm manganese sand and 2-4mm manganese sand.
The resin in the resin column 14 is a weak acid cation resin.
The operation flow of the ferric phosphate wastewater treatment system is shown in fig. 2. The wastewater contains calcium ions, magnesium ions, iron ions, manganese ions and the like, ammonium bicarbonate and ammonia water are respectively added into a washing water reaction tank and a mother liquor reaction tank by an ammonium bicarbonate dosing system and an ammonia water dosing system, and react with the calcium ions, the magnesium ions, the iron ions and the manganese ions in the wastewater, wherein the reaction formula is as follows:
Ca 2+ +CO 3 2- →CaCO 3 ↓
Fe 3+ +OH - →Fe(OH) 3 ↓
Mn 2+ +OH - →Mn(OH) 2 ↓
the phosphorus salt dosing system adds ammonium phosphate into the mother liquor reaction tank, and the ammonium phosphate can be recycled and reacts with manganese ions in the wastewater:
Mg 2+ +NH 4+ +PO 4- →Mg(NH 4 )PO 4 ↓
Mg 2+ +PO 4- →Mg 3 (PO 4 ) 2 ↓
the pH value of the washing water in the washing water reaction tank is adjusted to 8-9 through the reaction, the washing water in the reaction enters a washing water ceramic membrane, the sediment is filtered to a salt mud tank, and the mud cake pressed by a plate-and-frame filter press is transported outside. The pH value of the inflow water is regulated to be 6-7.5 by adding sulfuric acid in the first-stage reverse osmosis device, the first-stage inflow water of the first-stage reverse osmosis device enters the second-stage reverse osmosis device, the pH value of the inflow water is regulated to be 6-7.5 by adding sulfuric acid in the second-stage reverse osmosis device, the second-stage inflow water of the second-stage reverse osmosis device enters a pure water tank, the second-stage concentrated water of the second-stage reverse osmosis device enters the first-stage reverse osmosis device, the first-stage concentrated water of the first-stage reverse osmosis device enters the third-stage reverse osmosis device, the third-stage inflow water of the third-stage reverse osmosis device enters the second-stage reverse osmosis device, and the third-stage concentrated water of the third-stage reverse osmosis device enters the high-pressure reverse osmosis device of the mother liquor system.
The pH of the mother liquor is regulated to 6.5-8 by the reaction in the mother liquor reaction tank, the produced water of the mother liquor ceramic membrane enters a multi-medium filter to remove manganese ions, then enters a resin tower to further remove calcium ions, passes through an ultrafiltration device and then enters a high-pressure reverse osmosis device, the high-pressure produced water of the high-pressure reverse osmosis device enters a first-stage reverse osmosis device of a washing water treatment system, the high-pressure concentrated water of the high-pressure reverse osmosis device enters an MVR evaporation crystallization system to obtain ammonium sulfate and ammonium phosphate, and the evaporated alkaline condensate water enters a washing water buffer tank.
The above description is only of the preferred embodiments of the present utility model and is not intended to limit the present utility model, but various modifications and variations can be made to the present utility model by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present utility model should be included in the protection scope of the present utility model.
Claims (8)
1. The ferric phosphate wastewater treatment system is characterized by comprising a washing water treatment system, a mother liquor pretreatment system and an MVR evaporation crystallization system;
the washing water treatment system comprises a washing water buffer tank, a washing water reaction tank, a washing water ceramic membrane, a multistage reverse osmosis device and a pure water tank which are connected in sequence;
the mother liquor treatment system comprises a mother liquor buffer tank, a mother liquor reaction tank, a mother liquor ceramic membrane, a multi-medium filter, a resin tower, an ultrafiltration device and a high-pressure reverse osmosis device which are connected in sequence;
the water output end of the high-pressure reverse osmosis device is connected with the input end of the multistage reverse osmosis device, and the three-stage concentrated water output end of the multistage reverse osmosis device is connected with the input end of the high-pressure reverse osmosis device;
the input end of the MVR evaporation crystallization system is connected with the concentrated water output end of the high-pressure reverse osmosis device, and the condensed water output end of the MVR evaporation crystallization system is connected with the washing water buffer pool.
2. The ferric phosphate wastewater treatment system of claim 1, further comprising a brine sludge treatment system comprising a brine sludge pond and a plate and frame filter press connected in sequence, wherein the input end of the brine sludge pond is connected with the precipitation discharge end of the wash water ceramic membrane and the precipitation discharge end of the mother liquor ceramic membrane, and the water-producing output end of the plate and frame filter press is connected with the input end of the mother liquor reaction pond.
3. The ferric phosphate wastewater treatment system of claim 1, wherein the multi-stage reverse osmosis unit comprises a primary reverse osmosis unit, a secondary reverse osmosis unit, and a tertiary reverse osmosis unit; the input end of the first-stage reverse osmosis device is respectively connected with the water production output end of the washing ceramic membrane and the second-stage concentrated water output end of the second-stage reverse osmosis device; the input end of the secondary reverse osmosis device is respectively connected with the primary water output end of the primary reverse osmosis device and the tertiary water output end of the tertiary reverse osmosis device, and the secondary water output end of the secondary reverse osmosis device is connected with a pure water tank; the input end of the three-stage reverse osmosis device is connected with the second-stage concentrated water output end of the first-stage reverse osmosis device, and the third-stage concentrated water output end of the three-stage reverse osmosis device is connected with the input end of the MVR evaporation crystallization system.
4. The ferric phosphate wastewater treatment system of claim 1, wherein the wash water reaction tank is provided with an ammonia water dosing system and an ammonium bicarbonate dosing system, and the mother liquor reaction tank is provided with an ammonium phosphate salt dosing system, an ammonia water dosing system and an ammonium bicarbonate dosing system.
5. The ferric phosphate wastewater treatment system of claim 4, wherein an ammonia water dosing system and an ammonium bicarbonate dosing system are arranged above the wash water reaction tank, and an ammonium phosphate salt dosing system, an ammonia water dosing system and an ammonium bicarbonate dosing system are arranged above the mother liquor reaction tank.
6. The ferric phosphate wastewater treatment system of claim 5, wherein the dosing mode of the ammonia dosing system and the ammonium bicarbonate dosing system to the wash water reaction tank is self-flowing, and the dosing mode of the ammonium phosphate salt dosing system, the ammonia dosing system and the ammonium bicarbonate dosing system to the mother liquor reaction tank is self-flowing.
7. The ferric phosphate wastewater treatment system of claim 1, wherein the resin in the resin tower is a weak acid cation resin.
8. The ferric phosphate wastewater treatment system of claim 1, wherein the MVR evaporative crystallization system is configured with a finished ammonium sulfate packing system and a finished ammonium phosphate packing system.
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