CN111170526A - A kind of treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater - Google Patents
A kind of treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater Download PDFInfo
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- 239000002351 wastewater Substances 0.000 title claims abstract description 123
- 238000003723 Smelting Methods 0.000 title claims abstract description 86
- WFKWXMTUELFFGS-UHFFFAOYSA-N tungsten Chemical compound [W] WFKWXMTUELFFGS-UHFFFAOYSA-N 0.000 title claims abstract description 85
- 229910052721 tungsten Inorganic materials 0.000 title claims abstract description 85
- 239000010937 tungsten Substances 0.000 title claims abstract description 85
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 title claims abstract description 80
- 229910052785 arsenic Inorganic materials 0.000 title claims abstract description 79
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 title claims abstract description 79
- 238000000034 method Methods 0.000 title claims abstract description 73
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 69
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 69
- 239000011574 phosphorus Substances 0.000 title claims abstract description 69
- 239000000460 chlorine Substances 0.000 claims abstract description 52
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 44
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 42
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 57
- 239000010936 titanium Substances 0.000 claims description 22
- 229910052742 iron Inorganic materials 0.000 claims description 18
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 15
- 229910052719 titanium Inorganic materials 0.000 claims description 15
- 230000001376 precipitating effect Effects 0.000 claims description 11
- 238000001179 sorption measurement Methods 0.000 claims description 10
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 9
- 230000009471 action Effects 0.000 claims description 8
- 230000005684 electric field Effects 0.000 claims description 8
- 229910001220 stainless steel Inorganic materials 0.000 claims description 8
- 239000010935 stainless steel Substances 0.000 claims description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 7
- 239000010439 graphite Substances 0.000 claims description 7
- 229910002804 graphite Inorganic materials 0.000 claims description 7
- HTXDPTMKBJXEOW-UHFFFAOYSA-N iridium(IV) oxide Inorganic materials O=[Ir]=O HTXDPTMKBJXEOW-UHFFFAOYSA-N 0.000 claims description 7
- 239000004020 conductor Substances 0.000 claims description 4
- OSVXSBDYLRYLIG-UHFFFAOYSA-N chlorine dioxide Inorganic materials O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 claims description 2
- 229910001914 chlorine tetroxide Inorganic materials 0.000 claims description 2
- TVWHTOUAJSGEKT-UHFFFAOYSA-N chlorine trioxide Chemical compound [O]Cl(=O)=O TVWHTOUAJSGEKT-UHFFFAOYSA-N 0.000 claims description 2
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 claims description 2
- VLTRZXGMWDSKGL-UHFFFAOYSA-M perchlorate Chemical compound [O-]Cl(=O)(=O)=O VLTRZXGMWDSKGL-UHFFFAOYSA-M 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 17
- 239000003513 alkali Substances 0.000 abstract description 9
- 239000003153 chemical reaction reagent Substances 0.000 abstract description 4
- 150000001450 anions Chemical class 0.000 abstract description 3
- 230000007613 environmental effect Effects 0.000 abstract description 3
- 238000001556 precipitation Methods 0.000 abstract description 3
- 230000009467 reduction Effects 0.000 abstract description 3
- 238000004062 sedimentation Methods 0.000 abstract description 3
- 239000007788 liquid Substances 0.000 abstract description 2
- 239000000243 solution Substances 0.000 description 17
- 238000006243 chemical reaction Methods 0.000 description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 238000004065 wastewater treatment Methods 0.000 description 9
- 238000001914 filtration Methods 0.000 description 7
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 5
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000005660 chlorination reaction Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 229910017251 AsO4 Inorganic materials 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- 229910019142 PO4 Inorganic materials 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000010170 biological method Methods 0.000 description 2
- JFBJUMZWZDHTIF-UHFFFAOYSA-N chlorine chlorite Inorganic materials ClOCl=O JFBJUMZWZDHTIF-UHFFFAOYSA-N 0.000 description 2
- 238000000354 decomposition reaction Methods 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 239000010452 phosphate Substances 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- 239000005995 Aluminium silicate Substances 0.000 description 1
- DJHGAFSJWGLOIV-UHFFFAOYSA-K Arsenate3- Chemical compound [O-][As]([O-])([O-])=O DJHGAFSJWGLOIV-UHFFFAOYSA-K 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- AZDRQVAHHNSJOQ-UHFFFAOYSA-N alumane Chemical class [AlH3] AZDRQVAHHNSJOQ-UHFFFAOYSA-N 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- MXZRMHIULZDAKC-UHFFFAOYSA-L ammonium magnesium phosphate Chemical compound [NH4+].[Mg+2].[O-]P([O-])([O-])=O MXZRMHIULZDAKC-UHFFFAOYSA-L 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 239000003957 anion exchange resin Substances 0.000 description 1
- 229940000489 arsenate Drugs 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 159000000007 calcium salts Chemical class 0.000 description 1
- 238000009388 chemical precipitation Methods 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 238000003837 high-temperature calcination Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 159000000003 magnesium salts Chemical class 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 229910052567 struvite Inorganic materials 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 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
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/281—Treatment of water, waste water, or sewage by sorption using inorganic sorbents
-
- 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
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
-
- 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
- C02F2101/103—Arsenic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/16—Nature of the water, waste water, sewage or sludge to be treated from metallurgical processes, i.e. from the production, refining or treatment of metals, e.g. galvanic wastes
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- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
本发明涉及一种钨冶炼废水中的氨氮、磷、砷的处理方法，本发明通过两步电解，第一步实现废水中氨氮的去除，第二步实现废水中磷砷的去除，采用连续电解槽电解，将废水中氨氮氧化为氮气，除氨氮后的废水再浸入还原槽，在还原槽与Fe2+反应，将余氯还原为无害的Cl‑，同时Fe2+氧化为Fe3+，溶液中生成Fe(OH)3，吸附沉降废水中的PO4 3‑与AsO4 3‑等阴离子；无需液氮，无需氯碱装置、无需消耗大量沉淀试剂的专门处理钨冶炼废水的方法，将有助于提升钨冶炼流程的环保性和经济性。
The present invention relates to a method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater. The present invention adopts two-step electrolysis, the first step realizes the removal of ammonia nitrogen in wastewater, the second step realizes the removal of phosphorus and arsenic in wastewater, and continuous electrolysis is adopted. Cell electrolysis, the ammonia nitrogen in the wastewater is oxidized to nitrogen, and the wastewater after removing ammonia nitrogen is then immersed in a reduction tank, where it reacts with Fe 2+ to reduce the residual chlorine to harmless Cl ‑ , and at the same time, Fe 2+ is oxidized to Fe 3+ , Fe(OH) 3 is generated in the solution, and the anions such as PO 4 3- and AsO 4 3- in the sedimentation wastewater are adsorbed; no liquid nitrogen, no chlor-alkali device, and no need to consume a large amount of precipitation reagents. Helps to improve the environmental protection and economy of tungsten smelting process.
Description
Technical Field
The invention belongs to the technical field of wastewater treatment, and particularly relates to a method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater.
Background
China is a big country for smelting tungsten and has tungsten yield accounting for more than 80% of the world. At present, the tungsten smelting process mainly adopts the processes of alkaline decomposition, ammonium salt conversion and high-temperature calcination. The process uses ammonia, so that the smelting wastewater contains about 300mg/L ammonia nitrogen, and if the smelting wastewater enters a natural environment, eutrophication can be caused, so that a water body becomes black and smelly; and the tungsten mineral contains a certain amount of phosphorus and arsenic, and the phosphorus and arsenic can also enter a smelting process and finally enter wastewater in the alkaline decomposition process, and the phosphorus and arsenic can also cause water body pollution. The primary standard of ammonia nitrogen discharge specified in the national integrated wastewater discharge standard is 15mg/L, and the arsenate concentration (measured As)<0.5mg/L, phosphate concentration (in P)<0.5mg/L, so that these contaminants in the tungsten smelting wastewater need to be removed deeply. In addition, because the smelting adopts alkaline leaching and NH method4Cl transformation, the tungsten smelting wastewater is generally alkaline, and the tungsten smelting wastewater also contains 140-7600mg/L Cl-。
The existing industrial ammonia nitrogen treatment methods include biological method, stripping method, precipitation method, ion exchange method, breakpoint chlorination method and the like. Wherein, the biological method has low cost, long treatment time and large occupied space; the stripping method is used for removing ammonia nitrogen in a high-concentration solution, and is difficult to treat low-concentration ammonia nitrogen in a large amount of discharged wastewater; the chemical precipitation method generally generates magnesium ammonium phosphate precipitate by adding phosphate and magnesium salt, and the method has high treatment cost and causes secondary pollution due to the addition of phosphorus; law of breakpoint chlorination using Cl2Oxidizing to convert ammonia nitrogen into N2The method is a high-efficiency method for removing ammonia nitrogen in wastewater, but the method uses chlorine gas, liquid chlorine is a dangerous chemical, and the requirement on storage and use of the dangerous chemical is high, so the process risk is high, and some enterprises can produce the liquid chlorine by establishing a chlor-alkali device to avoid the liquid chlorineDirectly introducing the chlorine into the wastewater. However, the addition of a set of small chlor-alkali device is not economical in both cost and equipment maintenance.
The phosphorus and arsenic in the general industrial wastewater are treated by a precipitation method, an adsorption method, an ion exchange method and the like. The common precipitant is iron salt, calcium salt, aluminum salt, etc., the common adsorbent is fly ash, kaolin, and common ion exchange such as porous strong base anion exchange resin. Although the methods have wide applicability to general industrial wastewater, the purification effect is different according to different components of the wastewater, and even more reagents are needed for adjusting acid and alkali to achieve the purification effect, i.e. a special treatment method is not developed according to the characteristics of tungsten smelting wastewater.
Can aim at harmful substances such as ammonia nitrogen, phosphorus, arsenic and the like contained in the tungsten smelting wastewater and combine OH contained in the tungsten smelting wastewater-And Cl-The method and the device for specially treating the tungsten smelting wastewater, which do not need liquid chlorine, a chlor-alkali device and a large amount of precipitating reagent, are developed, and are favorable for improving the environmental protection and the economical efficiency of the tungsten metallurgy process.
The present invention has been made in view of the above circumstances.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater.
In order to achieve the purpose, the invention adopts the following technical scheme:
a treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater comprises the following steps:
(1) removing ammonia nitrogen: placing a plurality of inert electrodes arranged in parallel in an electrolytic tank containing tungsten smelting wastewater as an anode, wherein the electrolytic tank also comprises an anode arranged between two adjacent cathodes of the plurality of cathodes arranged in parallel, the cathode and the anode are arranged in pairs, under the action of an external electric field, the tungsten smelting wastewater flows in from one side of the electrolytic tank, sequentially passes through each cathode and anode and flows out from the other side corresponding to the electrolytic tank, and the tungsten smelting wastewater is electrolyzed in the electrolytic tank to convert ammonia nitrogen into nitrogen to escape;
(2) removing residual chlorine, phosphorus and arsenic: the wastewater flowing out of the electrolytic bath enters an electrolytic bath for dephosphorization and arsenic to be electrolyzed, residual chlorine is reduced into chloride ions, and Fe (OH) is formed in the solution3Flocculating and precipitating by Fe (OH)3The adsorption of (2) removes phosphorus and arsenic in the wastewater.
The reaction formula mainly carried out in the cathode, the anode and the solution in the ammonia nitrogen removal process is as follows:
anode: cl--2e-+2OH-→ClO-+H2O
Cathode: h2O+e-→0.5H2+OH-
In the solution: 3ClO-+2NH3→3Cl-+N2+3H2O
Cl contained in tungsten smelting wastewater-Oxidized into atomic chlorine or hypochlorite at the anode, oxidize ammonia nitrogen into nitrogen to escape, and reduce the ammonia nitrogen into Cl-(ii) a At the same time, the cathode generates hydrogen evolution reaction and generates corresponding OH-Cl in waste water-The electrolysis process does not need to add chloride, and the alkali in the wastewater and the alkali generated in the electrolysis process are neutralized with the acid generated by the anode, so that the addition of the alkali in the breakpoint chlorination process is avoided, and the ammonia nitrogen is removed without adding.
The reaction formula mainly carried out in the cathode, the anode and the solution in the residual chlorine removing process is as follows:
anode: fe-2e-→Fe2+
Cathode: h2O+e-→0.5H2+OH-
In the solution: ClO-+2Fe2++H2O→2Fe3++Cl-+2OH-
The anode plate of the electrolytic cell is oxidized in the residual chlorine removing process, and Fe is converted into Fe2+Enters the solution to be oxidized with residual chlorine in the wastewaterReduction reaction, residual chlorine is reduced to Cl-，Fe2+Conversion to Fe3+，Fe3+Formation of Fe (OH) in alkaline solution3Flocculating and precipitating PO in the wastewater4 3-、AsO4 3-The anions have strong adsorption capacity, and the removal of phosphorus and arsenic in the wastewater is realized after sedimentation or filtration.
Further, the inert electrode in the step (1) is a graphite plate, a titanium plate or Ti/RuO2-IrO2And the cathode of the DSA electrode is a stainless steel plate or a titanium plate.
Further, the electrolytic cell in the step (1) has a certain included angle a with a horizontal plane, and preferably, the included angle a is 10 ° to 70 °.
The electrolytic bath and the horizontal plane have a certain included angle so as to ensure that the tungsten smelting wastewater flows in from one end of the electrolytic bath and flows out from the other end, so that the tungsten smelting wastewater can fully pass through each cathode and each anode to realize electrolytic reaction.
Furthermore, the number of the cathodes or the anodes in the step (1) is 5-30.
Further, the pH value of the tungsten smelting wastewater is 8-13, and Cl is adopted-The concentration is 140-7600mg/L, the concentration of ammonia nitrogen is 100-1000mg/L, the concentration of arsenic is 1-100mg/L, and the concentration of phosphorus is 1-100 mg/L.
Further, the voltage between the adjacent cathode plate and the anode plate in the step (1) is 2.5-10V.
Further, electrolyzing in the step (1) to generate inorganic acid radical of chlorine, wherein the inorganic acid radical is ClO-，ClO2 -，ClO3 -，ClO4 -One or more of (a).
Further, the concentration of ammonia nitrogen in the wastewater flowing out of the electrolytic cell in the step (1) is less than 15mg/L, the concentration of residual chlorine is 1.5-25mg/L, the concentration of arsenic is 1-100mg/L, and the concentration of phosphorus is 1-100 mg/L.
Further, the cathode in the electrolytic cell for dephosphorization and arsenic in the step (2) is a graphite plate or a conductive material, and the anode is an iron plate.
In the process of removing residual chlorine, phosphorus and arsenic, the anode is used as a consumption material, and 1kg of iron can treat tungsten smelting wastewater of more than 10 t. The capacity of the electrolytic cell is between 1 and 20t, and the electrolyzed wastewater is separated by one or a combination method of standing sedimentation or filter membrane filtration.
Further, the electrolytic potential of the electrolytic bath for dephosphorization and arsenic in the step (2) is 0.5-5V, and the single electrolysis time is 10-60 min.
Furthermore, the concentrations of phosphorus and arsenic in the wastewater treated by the method are less than 0.5mg/L, the concentration of residual chlorine is less than 0.1mg/L, and the concentration of ammonia nitrogen is less than 15 mg/L.
The structure of the electrolytic cell for removing ammonia nitrogen is as follows:
the electrolysis trough include electrolysis trough, a plurality of negative pole that sets up side by side and a plurality of positive pole that sets up side by side, the electrolysis trough include four sides, go up bottom surface and bottom surface down, negative pole fixed connection on last bottom surface, positive pole fixed connection under on the bottom surface, last bottom surface be provided with first terminal, bottom surface down on be provided with the second terminal, first terminal be connected with the negative pole of power, the second terminal be connected with the positive pole of power.
The cathode and anode in the present invention do not contact each other and the adjacent cathode and anode form a small electrolytic cell.
Further, an angle α is formed between the bottom surface and a horizontal plane.
Further, the angle a is 10 to 70 °.
Further, the cathode is connected or welded with the upper bottom surface through bolts, and the anode is connected or welded with the lower bottom surface through bolts.
Further, the cathode and the anode are arranged in pairs.
Further, the number of cathodes and anodes is 5 to 30 pairs.
The angle alpha in the invention can be set according to the flow rate of the internal fluid, the preferred angle in the invention is 10-70 degrees, so that the ammonia nitrogen removal efficiency is higher under the corresponding flow rate, and the number of the working electrolytic plates is correspondingly adjusted according to the actual wastewater treatment capacity.
Furthermore, a water inlet is arranged at the upper end of the first side surface of the electrolytic cell, and a water outlet is arranged at the upper end of the second side surface opposite to the first side surface.
Furthermore, the height of the first side surface is greater than that of the second side surface, so that the electrolytic tank is arranged on the horizontal plane and is in an inclined state.
When the height of the first side surface is larger than that of the second side surface, one end of the lower bottom surface is connected with the second side panel, and the other end of the lower bottom surface is fixed on the first side surface, so that the lower bottom surface and the upper bottom surface are arranged in parallel.
Further, the height of the anode and the cathode is smaller than that of the electrolytic bath.
Furthermore, the lower bottom surface of the electrolytic cell is fixedly connected with a support frame, so that the electrolytic cell is further fixed on a horizontal plane.
Further, the four side surfaces of the electrolytic cell are made of nonconductive plastic, and the upper bottom surface and the lower bottom surface are made of conductive materials.
Compared with the prior art, the invention has the beneficial effects that:
(1) the method aims at high pH and Cl content in the tungsten smelting wastewater-The method is characterized in that continuous electrolysis is adopted to oxidize ammonia nitrogen in the wastewater into nitrogen, the wastewater after ammonia nitrogen removal is immersed into a reduction tank, and the wastewater is treated with Fe in the reduction tank2+Reaction, reducing residual chlorine to harmless Cl-While being Fe2+Oxidation to Fe3+In solution, Fe (OH) is generated3Adsorbing PO in the settling wastewater4 3-With AsO4 3-Plasma anions;
(2) the method can aim at harmful substances such as ammonia nitrogen, phosphorus, arsenic and the like contained in the tungsten smelting wastewater and combine OH contained in the tungsten smelting wastewater-And Cl-The method for specially treating the tungsten smelting wastewater without liquid chlorine, a chlor-alkali device and a large amount of precipitating reagents is developed, and the method is favorable for improving the environmental protection and the economical efficiency of the tungsten smelting process;
(3) aiming at the characteristics of tungsten smelting wastewater, the method realizes the removal of ammonia nitrogen in the wastewater in the first step and the removal of phosphorus and arsenic in the wastewater in the second step by two-step electrolysis, only low-price iron plates and electric energy are consumed, the ammonia nitrogen, the phosphorus and the arsenic in the wastewater reach the national first-level wastewater discharge standard, no secondary pollution is generated, and the method has the characteristics of simple operation and remarkable effect.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic view of the structure of an electrolytic cell for removing ammonia nitrogen in the present invention;
FIG. 2 is a schematic view of the installation structure of the electrolytic cell in the removal of ammonia nitrogen in the present invention.
Reference numerals
1. The device comprises a first side face, 11-a water inlet, 2-a second side face, 21-a water outlet, 3-a lower bottom face, 31-an anode, 32-a second binding post, 4-an upper bottom face, 41-a cathode, 42-a first binding post and 5-a support frame.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be described in detail below. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the examples given herein without any inventive step, are within the scope of the present invention.
Fig. 1-2 show a schematic structural diagram of an electrolytic cell device in ammonia nitrogen removal according to the following embodiment of the present invention, the device includes an electrolytic cell, a plurality of cathodes 41 arranged in parallel and a plurality of anodes 31 arranged in parallel, the electrolytic cell includes four side surfaces, an upper bottom surface 4 and a lower bottom surface 3, the cathodes 41 are fixedly connected to the upper bottom surface 4, the anodes 31 are fixedly connected to the lower bottom surface 3, the upper bottom surface 4 is provided with a first terminal 42, the lower bottom surface 3 is provided with a second terminal 32, the first terminal 42 is connected to a negative electrode of a power supply, and the second terminal 31 is connected to a positive electrode of the power supply.
Further, an angle a is formed between the bottom surface 3 and a horizontal plane, the angle a is 10 ° to 70 °, the flow rate of the wastewater in the electrolytic cell can be controlled, 11 cathodes 41 and 11 anodes 31 are illustrated in the figure, and the number of the cathodes 41 and the anodes 31 can be adjusted according to the treatment capacity of the wastewater and the removal rate of ammonia nitrogen in the actual wastewater treatment process.
The cathodes 41 are welded with the upper bottom surface 4, the anodes 31 are welded with the lower bottom surface 3, and the cathodes 41 and the anodes 31 are arranged in pairs with the same number. The anode is a graphite plate, a titanium plate or a titanium plate, Ti/RuO2-IrO2And the cathode of the DSA electrode is a stainless steel plate or a titanium plate.
The upper end of the first side surface 1 of the electrolytic cell is provided with a water inlet 11, and the upper end of the second side surface 2 which is opposite to the water inlet is provided with a water outlet 21. The tungsten-containing smelting wastewater flows in from the water inlet 11, sequentially passes through the cathode 41 and the anode 31, flows in an up-and-down circulation manner, each cathode 41 and each anode 31 form a small electrolytic tank, the wastewater is fully contacted with the cathode 41 and the anode 31 in the tank, and Cl contained in the tungsten smelting wastewater is driven by an external electric field-Oxidized into atomic chlorine or hypochlorite at the anode, oxidize ammonia nitrogen into nitrogen to escape, and reduce the ammonia nitrogen into Cl-(ii) a At the same time, the cathode generates hydrogen evolution reaction and generates corresponding OH-。
In a further scheme, the electrolytic cell is fixedly arranged with a horizontal plane through a support frame 5, so that the electrolytic cell is in an inclined state, and the flow rate of the wastewater is controlled.
Alternatively, as shown in fig. 2, when the height of the first side surface 1 is greater than that of the second side surface 2, the electrolytic cell is placed in a horizontal inclined state. When the height of the first side surface 1 is greater than that of the second side surface 2, one end of the lower bottom surface 3 is connected with the second side surface plate 2, and the other end is fixed on the first side surface 1, so that the lower bottom surface 3 and the upper bottom surface 4 are arranged in parallel. The height of both the anode 31 and the cathode 41 is less than the height of the cell.
In a further method, the four sides of the cell are made of non-conductive plastic and the top and bottom surfaces are made of conductive material so that the cell is connected to a power source through the first and second terminals 42, 32. The electrolytic cell forms a closed circuit and the cathode 41 and anode 31 operate normally.
Example 1
A treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater comprises the following steps:
(1) removing ammonia nitrogen: in the embodiment, the tungsten smelting wastewater treatment capacity is 50L, wherein the ammonia nitrogen concentration is 400mg/L, the phosphorus concentration is 20mg/L, the arsenic concentration is 15mg/L, the chlorine concentration is 800mg/L, and the pH value is 8.8, a plurality of inert electrodes arranged in parallel are placed in an electrolytic tank containing tungsten smelting wastewater to serve as an anode, the electrolytic tank further comprises a plurality of cathodes arranged in parallel, an anode is arranged between two adjacent cathodes, the cathodes and the anode are arranged in pairs, wherein the area of the single electrode is 100cm2The anode adopts Ti/RuO2-IrO2The method comprises the following steps of (1) adopting a DSA electrode, wherein a negative plate is made of stainless steel, the number of electrode pairs is n & ltSUB & gt 10 & lt/SUB & gt, the inclination angle alpha & ltSUB & gt 30 & lt/SUB & gt of an electrolytic cell is 30 & lt/SUB & gt, under the action of an external electric field, the voltage between the adjacent negative plate and positive plate is 8V, tungsten smelting wastewater flows in from one side of the electrolytic cell, sequentially passes through each cathode and each anode and flows out from the other side corresponding to the electrolytic cell, the tungsten smelting wastewater passes through the electrolytic cell for 8min, the tungsten smelting wastewater is electrolyzed in the;
(2) removing residual chlorine, phosphorus and arsenic: the wastewater flowing out of the electrolytic cell enters an electrolytic cell for dephosphorization and arsenic to carry out electrolytic reaction for 10min, the cathode is a titanium plate, the anode is an iron plate, the volume of the electrolytic cell is 50L, the thickness of the iron anode plate is 20mm, and the area is 400cm2The potential of the cathode and the anode is 3V, residual chlorine is reduced into chloride ions, and Fe (OH) is formed in the solution3Flocculating and precipitating by Fe (OH)3The adsorption of the (1) removes phosphorus and arsenic in the wastewater, and after standing and filtering, the concentration of ammonia nitrogen in the discharged wastewater is 13mg/L, the concentration of phosphorus is 0.4mg/L, the concentration of arsenic is 0.2mg/L, and the concentration of residual chlorine is lower than 0.03 mg/L.
Example 2
A treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater comprises the following steps:
(1) removing ammonia nitrogen: in the embodiment, the tungsten smelting wastewater treatment capacity is 50L, wherein the ammonia nitrogen concentration is 400mg/L, the phosphorus concentration is 20mg/L, the arsenic concentration is 15mg/L, the chlorine concentration is 800mg/L, and the pH value is 8.8, a plurality of inert electrodes arranged in parallel are placed in an electrolytic tank containing tungsten smelting wastewater to serve as an anode, the electrolytic tank further comprises a plurality of cathodes arranged in parallel, an anode is arranged between two adjacent cathodes, the cathodes and the anode are arranged in pairs, wherein the area of the single electrode is 100cm2The anode adopts Ti/RuO2-IrO2The method comprises the following steps of (1) adopting a DSA electrode, wherein a titanium plate is adopted as a cathode plate, the number of electrode pairs is n & ltSUB & gt 10 & lt/SUB & gt, the inclination angle alpha & ltSUB & gt 45 & lt/SUB & gt of an electrolytic cell is 45 & lt/SUB & gt, under the action of an external electric field, the voltage between the adjacent cathode plate and anode plate is 8V, tungsten smelting wastewater flows in from one side of the electrolytic cell, sequentially passes through each cathode and each anode and flows out from the other side corresponding to the electrolytic cell, the tungsten smelting wastewater passes through the electrolytic cell for 5min, the tungsten smelting wastewater is electrolyzed in;
(2) removing residual chlorine, phosphorus and arsenic: the wastewater flowing out of the electrolytic cell enters an electrolytic cell for dephosphorization and arsenic to carry out electrolytic reaction for 10min, wherein the cathode is a stainless steel plate, the anode is a titanium plate, the volume of the electrolytic cell is 50L, the thickness of the iron anode plate is 15mm, and the area of the iron anode plate is 400cm2The potential of the cathode and the anode is 3V, residual chlorine is reduced into chloride ions, and Fe (OH) is formed in the solution3Flocculating and precipitating by Fe (OH)3The adsorption of the (1) removes phosphorus and arsenic in the wastewater, and after standing and filtering, the concentration of ammonia nitrogen in the discharged wastewater is 14mg/L, the concentration of phosphorus is 0.4mg/L, the concentration of arsenic is 0.2mg/L, and the concentration of residual chlorine is lower than 0.03 mg/L.
Example 3
A treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater comprises the following steps:
(1) removing ammonia nitrogen: in the embodiment, the tungsten smelting wastewater treatment capacity is 50L, wherein the ammonia nitrogen concentration is 600mg/L, the phosphorus concentration is 20mg/L, the arsenic concentration is 15mg/L, the chlorine concentration is 800mg/L, and the pH value is 8.8, a plurality of inert electrodes arranged in parallel are placed in an electrolytic tank containing tungsten smelting wastewater to serve as an anode, the electrolytic tank further comprises a plurality of cathodes arranged in parallel, an anode is arranged between two adjacent cathodes, the cathodes and the anode are arranged in pairs, wherein the area of the single electrode is 100cm2The method comprises the following steps that a graphite plate is adopted as an anode, stainless steel is adopted as a cathode plate, the number of electrode pairs is n-5, the inclination angle alpha of an electrolytic cell is 70 degrees, under the action of an external electric field, the voltage between the adjacent cathode plate and anode plate is 8V, tungsten smelting wastewater flows in from one side of the electrolytic cell, sequentially passes through each cathode and anode and flows out from the other side corresponding to the electrolytic cell, the tungsten smelting wastewater passes through the electrolytic cell for 8min, the tungsten smelting wastewater is electrolyzed in the electrolytic cell, and ammonia nitrogen is converted into nitrogen to escape;
(2) removing residual chlorine, phosphorus and arsenic: allowing wastewater flowing out of the electrolytic cell to enter an electrolytic cell for dephosphorization and arsenic to perform electrolytic reaction for 15min, wherein the cathode is a titanium plate, the anode is an iron plate, the volume of the electrolytic cell is 50L, the thickness of the iron anode plate is 10mm, and the area of the iron anode plate is 400cm2The potential of the cathode and the anode is 3V, residual chlorine is reduced into chloride ions, and Fe (OH) is formed in the solution3Flocculating and precipitating by Fe (OH)3The adsorption of the (1) removes phosphorus and arsenic in the wastewater, and after standing and filtering, the concentration of ammonia nitrogen in the discharged wastewater is 13.5mg/L, the concentration of phosphorus is 0.4mg/L, the concentration of arsenic is 0.2mg/L, and the residual chlorine is less than 0.03 mg/L.
Example 4
A treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater comprises the following steps:
(1) removing ammonia nitrogen: in the embodiment, the tungsten smelting wastewater treatment capacity is 50L, wherein the ammonia nitrogen concentration is 400mg/L, the phosphorus concentration is 30mg/L, the arsenic concentration is 20mg/L, the chlorine concentration is 800mg/L, and the pH value is 8.8, a plurality of inert electrodes arranged in parallel are placed in an electrolytic tank containing tungsten smelting wastewater to serve as an anode, the electrolytic tank further comprises a plurality of cathodes arranged in parallel, and two adjacent cathodesAn anode is arranged between the electrodes, the cathode and the anode are arranged in pairs, wherein the area of a single electrode is 100cm2The anode adopts Ti/RuO2-IrO2The method comprises the following steps of (1) adopting a DSA electrode, wherein a negative plate is made of stainless steel, the number of electrode pairs is n & ltSUB & gt 10 & lt/SUB & gt, the inclination angle alpha & ltSUB & gt 30 & lt/SUB & gt of an electrolytic cell is 30 & lt/SUB & gt, under the action of an external electric field, the voltage between the adjacent negative plate and positive plate is 8V, tungsten smelting wastewater flows in from one side of the electrolytic cell, sequentially passes through each cathode and each anode and flows out from the other side corresponding to the electrolytic cell, the tungsten smelting wastewater passes through the electrolytic cell for 8min, the tungsten smelting wastewater is electrolyzed in the;
(2) removing residual chlorine, phosphorus and arsenic: the wastewater flowing out of the electrolytic cell enters an electrolytic cell for dephosphorization and arsenic to carry out electrolytic reaction for 10min, the cathode is a titanium plate, the anode is an iron plate, the volume of the electrolytic cell is 50L, the thickness of the iron anode plate is 20mm, and the area is 400cm2The potential of the cathode and the anode is 3V, residual chlorine is reduced into chloride ions, and Fe (OH) is formed in the solution3Flocculating and precipitating by Fe (OH)3The adsorption of the (1) removes phosphorus and arsenic in the wastewater, and after standing and filtering, the concentration of ammonia nitrogen in the discharged wastewater is 13mg/L, the concentration of phosphorus is 0.4mg/L, the concentration of arsenic is 0.3mg/L, and the concentration of residual chlorine is lower than 0.03 mg/L.
Example 5
A treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater comprises the following steps:
(1) removing ammonia nitrogen: in the embodiment, the tungsten smelting wastewater treatment capacity is 200L, wherein the ammonia nitrogen concentration is 400mg/L, the phosphorus concentration is 20mg/L, the arsenic concentration is 12mg/L, the chlorine concentration is 800mg/L, and the pH value is 9.2, a plurality of inert electrodes arranged in parallel are placed in an electrolytic tank containing tungsten smelting wastewater to serve as an anode, the electrolytic tank further comprises a plurality of cathodes arranged in parallel, an anode is arranged between two adjacent cathodes, the cathodes and the anode are arranged in pairs, wherein the area of the single electrode is 400cm2The anode adopts Ti/RuO2-IrO2The DSA electrode adopts stainless steel as a cathode plate, the number of electrode pairs is n-20, the inclination angle alpha of the electrolytic cell is 30 degrees, and under the action of an external electric field, the voltage between the adjacent cathode plate and anode plate is10V, the tungsten smelting wastewater flows in from one side of the electrolytic cell, sequentially passes through each cathode and each anode, and flows out from the other side corresponding to the electrolytic cell, the tungsten smelting wastewater passes through the electrolytic cell for 24min, the tungsten smelting wastewater is electrolyzed in the electrolytic cell, and ammonia nitrogen is converted into nitrogen to escape;
(2) removing residual chlorine, phosphorus and arsenic: allowing wastewater flowing out of the electrolytic cell to enter an electrolytic cell for dephosphorization and arsenic to perform electrolytic reaction for 30min, wherein the cathode is a titanium plate, the anode is an iron plate, the volume of the electrolytic cell is 200L, the thickness of the iron anode plate is 10mm, and the area of the iron anode plate is 400cm2The potential of the cathode and the anode is 3V, residual chlorine is reduced into chloride ions, and Fe (OH) is formed in the solution3Flocculating and precipitating by Fe (OH)3The adsorption of the (1) removes phosphorus and arsenic in the wastewater, and after standing and filtering, the concentration of ammonia nitrogen in the discharged wastewater is 13mg/L, the concentration of phosphorus is 0.4mg/L, the concentration of arsenic is 0.3mg/L, and the concentration of residual chlorine is lower than 0.03 mg/L.
Example 6
A treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater comprises the following steps:
(1) removing ammonia nitrogen: in the embodiment, the tungsten smelting wastewater treatment capacity is 200L, wherein the ammonia nitrogen concentration is 100mg/L, the phosphorus concentration is 100mg/L, the arsenic concentration is 100mg/L, the chlorine concentration is 140mg/L, and the pH value is 13, a plurality of inert electrodes arranged in parallel are placed in an electrolytic tank containing tungsten smelting wastewater to serve as an anode, the electrolytic tank further comprises a plurality of cathodes arranged in parallel, an anode is arranged between two adjacent cathodes, the cathodes and the anode are arranged in pairs, wherein the area of the single electrode is 400cm2The method comprises the following steps that a graphite plate is adopted as an anode, a titanium plate is adopted as a cathode plate, the number of electrode pairs is n & ltSUB & gt 30 & lt/SUB & gt, the inclination angle alpha & ltSUB & gt 10 & lt/SUB & gt of an electrolytic cell is 10 & lt/SUB & gt, under the action of an external electric field, the voltage between the adjacent cathode plate and anode plate is 2.5V, tungsten smelting wastewater flows in from one side of the electrolytic cell, sequentially passes through each cathode and anode and flows out from the other side corresponding to the electrolytic cell, the tungsten smelting wastewater passes through the electrolytic cell for 24min, the tungsten smelting wastewater is electrolyzed in the electrolytic cell, and;
(2) removing residual chlorine, phosphorus and arsenic: waste water flowing out of the electrolytic cell entersCarrying out electrolytic reaction in an electrolytic tank for removing phosphorus and arsenic for 60min, wherein the cathode is a titanium plate, the anode is an iron plate, the volume of the electrolytic tank is 200L, the thickness of the iron anode plate is 10mm, and the area is 400cm2The potential of the cathode and the anode is 3V, residual chlorine is reduced into chloride ions, and Fe (OH) is formed in the solution3Flocculating and precipitating by Fe (OH)3The adsorption of the (1) removes phosphorus and arsenic in the wastewater, and after standing and filtering, the concentration of ammonia nitrogen in the discharged wastewater is 12mg/L, the concentration of phosphorus is 0.3mg/L, the concentration of arsenic is 0.4mg/L, and the concentration of residual chlorine is lower than 0.04 mg/L.
The above description is only for the specific embodiments of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art can easily conceive of the changes or substitutions within the technical scope of the present invention, and all the changes or substitutions should be covered within the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope of the appended claims.
Claims (10)
1. A treatment method of ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater is characterized by comprising the following steps:
(1) removing ammonia nitrogen: placing a plurality of inert electrodes arranged in parallel in an electrolytic tank containing tungsten smelting wastewater as anodes, wherein the electrolytic tank also comprises a plurality of cathodes arranged in parallel, one anode is arranged between two adjacent cathodes, the cathodes and the anodes are arranged in pairs, under the action of an external electric field, the tungsten smelting wastewater flows in from one side of the electrolytic tank, sequentially passes through each cathode and each anode and flows out from the other side corresponding to the electrolytic tank, and the tungsten smelting wastewater is electrolyzed in the electrolytic tank to convert ammonia nitrogen into nitrogen to escape;
(2) removing residual chlorine, phosphorus and arsenic: the wastewater flowing out of the electrolytic bath enters an electrolytic bath for dephosphorization and arsenic to be electrolyzed, residual chlorine is reduced into chloride ions, and Fe (OH) is formed in the solution3Flocculating and precipitating by Fe (OH)3The adsorption of (2) removes phosphorus and arsenic in the wastewater.
2. The method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater according to claim 1,the inert electrode in the step (1) is a graphite plate, a titanium plate or Ti/RuO2-IrO2And the cathode of the DSA electrode is a stainless steel plate or a titanium plate.
3. The method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater according to claim 1 or 2, wherein the electrolytic cell in step (1) has an angle a with a horizontal plane, and preferably, the angle a is 10 ° to 70 °.
4. The method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater according to claim 1, wherein the number of the cathodes or the anodes in step (1) is 5-30.
5. The method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater according to claim 1 or 2, wherein the pH value of the tungsten smelting wastewater is 8-13, and Cl is adopted-The concentration is 140-7600mg/L, the concentration of ammonia nitrogen is 100-1000mg/L, the concentration of arsenic is 1-100mg/L, and the concentration of phosphorus is 1-100 mg/L.
6. The method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater according to claim 1, wherein the voltage between the adjacent cathode plate and anode plate in step (1) is 2.5-10V.
7. The method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater according to claim 1, wherein inorganic acid radicals of chlorine are generated by electrolysis in step (1), and the inorganic acid radicals are ClO-，ClO2 -，ClO3 -，ClO4 -One or more of (a).
8. The method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater according to claim 1, wherein the concentration of ammonia nitrogen in the wastewater flowing out of the electrolytic cell in the step (1) is less than 15mg/L, the concentration of residual chlorine is 1.5-25mg/L, the concentration of arsenic is 1-100mg/L, and the concentration of phosphorus is 1-100 mg/L.
9. The method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater according to claim 1, wherein the cathode in the electrolytic cell for dephosphorization and arsenic in step (2) is graphite plate or conductive material, the anode is iron plate, preferably, the electrolytic potential of the electrolytic cell for dephosphorization and arsenic is 0.5-5V, and the single electrolysis time is 10-60 min.
10. The method for treating ammonia nitrogen, phosphorus and arsenic in tungsten smelting wastewater according to claim 1, wherein the concentration of phosphorus and arsenic in the wastewater treated by the method is less than 0.5mg/L, the concentration of residual chlorine is less than 0.1mg/L, and the concentration of ammonia nitrogen is less than 15 mg/L.
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