WO2010143623A1 - メッキ洗浄排水からの水及び金属の回収方法 - Google Patents

メッキ洗浄排水からの水及び金属の回収方法 Download PDF

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Publication number
WO2010143623A1
WO2010143623A1 PCT/JP2010/059680 JP2010059680W WO2010143623A1 WO 2010143623 A1 WO2010143623 A1 WO 2010143623A1 JP 2010059680 W JP2010059680 W JP 2010059680W WO 2010143623 A1 WO2010143623 A1 WO 2010143623A1
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Prior art keywords
water
metal
crystallization
plating
iron
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PCT/JP2010/059680
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English (en)
French (fr)
Japanese (ja)
Inventor
一郎 住田
勇一 村松
孝之 篠崎
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栗田工業株式会社
新日本製鐵株式会社
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Priority to CN201080025924.7A priority Critical patent/CN102459096B/zh
Publication of WO2010143623A1 publication Critical patent/WO2010143623A1/ja

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    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B7/00—Working up raw materials other than ores, e.g. scrap, to produce non-ferrous metals and compounds thereof; Methods of a general interest or applied to the winning of more than two metals
    • C22B7/006—Wet processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D9/00—Crystallisation
    • B01D9/0036—Crystallisation on to a bed of product crystals; Seeding
    • 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
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/44—Treatment or purification of solutions, e.g. obtained by leaching by chemical processes
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25D—PROCESSES FOR THE ELECTROLYTIC OR ELECTROPHORETIC PRODUCTION OF COATINGS; ELECTROFORMING; APPARATUS THEREFOR
    • C25D21/00—Processes for servicing or operating cells for electrolytic coating
    • C25D21/16—Regeneration of process solutions
    • C25D21/20—Regeneration of process solutions of rinse-solutions
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/06—Controlling or monitoring parameters in water treatment pH
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the present invention relates to a method for efficiently recovering water and valuable metals from plating washing wastewater, and in particular, efficiently recovers both water and valuable metals such as nickel and zinc from washing wastewater in the electroplating process.
  • the present invention relates to a method for reducing the amount of sludge generated by wastewater treatment.
  • the plating washing wastewater discharged from the plating factory generally has a pH of 2 to 3, and in many cases contains valuable metals such as nickel, zinc, chromium and copper in addition to divalent iron. It is desirable to reuse.
  • a neutralization coagulation precipitation method (hydroxide precipitation method) has been adopted as a method for treating plating washing wastewater.
  • the pH of the waste water is made alkaline, and metal ions are precipitated as hydroxides and separated and removed.
  • a method of coagulating and precipitating under different pH conditions is employed. That is, this is a method in which Fe 2+ is oxidized to Fe 3+ in the presence of an oxidizing agent or the like at pH 3 to 6, and then precipitated and removed as a hydroxide, and then nickel and zinc are precipitated and separated at pH 7 to 10.
  • nickel and zinc are precipitated and separated, and then solid-liquid separation such as sand filtration and ultrafiltration, or reverse osmosis (RO) membrane treatment is performed according to the required water quality of the collected water. .
  • RO reverse osmosis
  • treatment methods for metal-containing wastewater include the sulfide precipitation method, ion exchange method, chelate resin method, and membrane separation method.
  • the sulfide precipitation method is a method in which a metal is precipitated as a sulfide by adding sodium sulfide.
  • a metal is precipitated as a sulfide by adding sodium sulfide.
  • metals can be treated at a lower concentration from the viewpoint of wastewater treatment.
  • the ion exchange method is to remove the metal ions in the waste water by adsorbing to the ion exchange resin, and if used within the range of the adsorption capacity of the ion exchange resin, the ion exchange method is reliable. It is possible to remove metal ions.
  • the chelate resin method uses a chelate resin having selectivity for a specific metal to adsorb and remove the metal. As with the ion exchange resin, it is possible to reliably remove metal ions, but the chelate resin has selectivity for the metal, and a metal that can be adsorbed and removed is specified.
  • the membrane separation method uses a RO membrane to remove metal ions, and provides a good treated water quality.
  • each method has the following problems when recovering both water and valuable metals from the metal-containing wastewater.
  • Sulfide precipitation method Sulfide has a low solubility product and can reduce the metal ion concentration. However, since the sulfide precipitate is fine, precipitation separation is poor. Further, since sulfides generate hydrogen sulfide under acidic conditions, there is a safety problem.
  • the object of the present invention is to solve the above-mentioned conventional problems and to provide a method for efficiently recovering water and metal from plating washing waste water.
  • the method for recovering water and metal from the plating cleaning wastewater according to the first aspect is a method of recovering water and metal from the plating cleaning wastewater, adjusting the plating cleaning wastewater to pH 3 to 6 in the presence of an oxidizing agent,
  • the iron insolubilization step of oxidizing the divalent iron ions into trivalent iron ions and precipitating iron hydroxide, and the treated water in the iron insolubilization step are separated into solid and liquid using a microfiltration membrane, ultrafiltration membrane or filter
  • a solid-liquid separation step, a reverse osmosis membrane separation process in which the separated water separated in the solid-liquid separation step is subjected to a reverse osmosis membrane separation process, and the permeate is taken out of the system as treated water
  • the method for recovering water and metal from the plating washing waste water according to the second aspect is the metal recovery according to the first aspect, wherein, in the crystallization step, the metal carbonate precipitated on the seed crystal is dissolved in an acid to obtain a metal salt solution. It has the process.
  • the third aspect of the method for recovering water and metal from the plating washing wastewater is characterized in that the metal salt solution obtained in the metal recovery step is reused as a plating solution.
  • the fourth aspect of the method for recovering water and metal from the plating washing wastewater is characterized in that, in any one of the first to third aspects, the treated water of the crystallization step is returned to the iron insolubilization step for treatment. To do.
  • water and metal can be efficiently recovered from the plating washing waste water.
  • iron is precipitated as iron hydroxide (Fe (OH) 3 ) in the iron insolubilization step, and this is separated and removed in the solid-liquid separation step. Since this solid-liquid separation is performed with a microfiltration (MF) membrane, an ultrafiltration (UF) membrane, or a filter, the solid-liquid separation is excellent. Since the pH is adjusted to 3 to 6 in the iron precipitation step, iron hydroxide is precipitated, but metal ions such as nickel and zinc are dissolved. Therefore, the separated water containing the dissolved metal ions is obtained from the solid-liquid separation step.
  • MF microfiltration
  • UF ultrafiltration
  • this solid-liquid separated water is first concentrated by RO membrane separation treatment.
  • RO membrane permeated water has a water quality as good as pure water, and can be taken out of the system as treated water and reused as plating cleaning water, or used at other points of use.
  • Metal ions such as nickel and zinc concentrated in the RO-concentrated water are precipitated as metal carbonates on the seed crystal by the subsequent crystallization treatment.
  • the metal can be recovered as metal carbonate particles having good dehydration properties.
  • the crystallization method does not require a sedimentation basin or dehydration equipment as in the neutralization precipitation method.
  • Nickel and zinc can also be insolubilized as hydroxides, but hydroxides are not suitable for crystallization because they generate flocs with high moisture content including moisture.
  • the metal carbonate precipitated on the seed crystals can be dissolved in an acid and easily recovered as a metal salt solution.
  • this metal salt solution can be reused as a plating solution, and the recovered seed crystals can be reused in the crystallization step.
  • FIG. 1 is a system diagram showing an embodiment of a method for recovering water and metal from plating washing waste water according to the present invention
  • FIG. 2 is a system diagram showing the structure of a crystallizer
  • FIG. 3 is the structure of an acid contact device.
  • the plating cleaning waste water as raw water is introduced into the agglomeration / oxidation tank 1, and an oxidizing agent (sodium hypochlorite (NaClO) in FIG. 1) and a pH adjusting agent (in FIG. 1, as an alkaline agent).
  • an oxidizing agent sodium hypochlorite (NaClO) in FIG. 1
  • a pH adjusting agent in FIG. 1, as an alkaline agent
  • AgOH sodium hypochlorite
  • FeCl 3 a flocculant
  • divalent iron (Fe 2+ ) in the liquid is converted to trivalent iron (Fe 3+ ) at pH 3-6.
  • the oxidizing agent hydrogen peroxide, potassium permanganate, chlorine, ozone, or the like can be used in addition to NaClO.
  • the addition amount of the oxidizing agent may be equal to or more than the equivalent for oxidizing Fe 2+ in the liquid to Fe 3+ .
  • the plating washing wastewater is usually acidic at a pH of less than 3, for example, about pH 2, it needs to be at least pH 3 for precipitation of Fe (OH) 3 , so that NaOH, Ca (OH) are used as pH adjusters.
  • the pH is adjusted by adding alkali such as 2 .
  • the pH is adjusted to 3 to 7, particularly 5 to 6, since nickel and zinc in the liquid are precipitated when the pH exceeds 7.
  • a flocculant such as FeCl 3 may be added in order to improve the sedimentation of Fe (OH) 3 floc.
  • a flocculant such as FeCl 3
  • the sedimentation property of the insolubilized particles is improved, the sedimentation efficiency in the subsequent sedimentation tank 2 is increased, and the floc diameter is increased so that the downstream UF membrane device 3
  • the filterability of can also be improved.
  • the addition of a flocculant is also preferable in order to agglomerate organic substances in the plating washing waste water to reduce the load on the subsequent RO membrane device 6 and to prevent contamination of the RO membrane.
  • Amount of FeCl 3 is generally 10 ⁇ 200mg / L, preferably about 100 ⁇ 150mg / L.
  • the liquid in which the floc of Fe (OH) 3 is precipitated in the coagulation / oxidation tank 1 is then solid-liquid separated by an MF membrane, a UF membrane or a filter (for example, a sand filter).
  • MF membrane separation device MF membrane separation device
  • the separation liquid pump P A is introduced into the UF membrane device 3, is a membrane filtration.
  • the UF membrane device 3 is regularly backwashed, and the collected Fe (OH) 3 sludge is discharged out of the system together with the backwash drainage.
  • the filtered water of the UF membrane device 3 is introduced into the adjustment tank 5 through the UF treatment water tank 4 and the water quality is adjusted in the adjustment tank 5. That is, prior to processing the filtered water of the UF membrane device 3 by the RO membrane device (RO membrane separation device) 6, sodium bisulfite (NaHSO 3 ) and sodium sulfite (Na 2 ) are added to the UF membrane filtered water to protect the RO membrane. It is necessary to add a reducing agent such as SO 4 ) or contact with activated carbon to remove the remaining oxidizing agent, and to prevent precipitation of metal hydroxides such as nickel and zinc by concentration in the RO membrane device 6. Accordingly, a pH adjusting agent is added to adjust the pH of the water (RO feed water) supplied to the RO membrane device 6 to 4 to 6, preferably 4 to 5.
  • the amount of the reducing agent added to the UF membrane filtered water is usually 5 to 20 mg / L, preferably 10 to 15 mg / L in excess of the equivalent of the remaining oxidizing agent.
  • the water whose water quality has been adjusted in the adjustment tank 5 is introduced into the RO membrane device 6 by the pump P B and subjected to membrane separation treatment into permeated water (RO permeated water) and concentrated water (RO concentrated water). A part of the concentrated water is supplied to the RO concentrated water tank 7, and the remaining part is circulated.
  • the treatment with the RO membrane device 6 is performed at a concentration factor of 5 to 10 times and a water recovery rate of 80 to 90%, so that metal ions can be highly concentrated and the water recovery rate can be increased without causing operational troubles. It is preferable in terms of enhancement.
  • RO permeated water obtained by the RO membrane device 6 has the same good water quality as pure water, it can be reused as plating cleaning water. Moreover, this RO permeated water can also be used at other use points.
  • the metal ions in the RO concentrated water are concentrated to 5 to 10 times the metal ion concentration in the plating washing wastewater.
  • This RO concentrated water is introduced into the crystallizer 8 through the RO concentrated water tank 7 and crystallized. Is done.
  • the crystallization apparatus 8 is not particularly limited as long as it can promote the precipitation of metal carbonate.
  • a seed crystal is packed in the crystallization reaction tower 10 as shown in FIG.
  • a tower reactor in which RO concentrated water is passed from the bottom of the tower to form a fluidized bed of seed crystals in the tower can be suitably used.
  • the raw crystallization water is passed from the lower part of the reaction tower 10 through the pipe 11 by the pump P 1 , and the treated water flows out from the pipe 12 and is introduced into the treated water tank 9. From the tower top part of the treated water is processed is circulated to the bottom of the column by the circulation pipe 14 and a circulation pump P 2.
  • Alkali carbonate such as sodium carbonate (Na 2 CO 3 ) or a mixed solution of sodium bicarbonate (NaHCO 3 ) and caustic soda (NaOH) is injected from the upper part of the crystallization reaction tower 13.
  • a metal carbonate precipitates on the seed crystal flowing in the tower in accordance with a reaction between sodium carbonate and metal ions, for example, according to the following reaction.
  • the metal carbonate needs to be precipitated by raising the pH of the crystallization raw water to 7 to 10, preferably 8 to 9. Therefore, the alkali carbonate injected into the crystallization tower reaction tower 10 is an amount necessary for forming the metal carbonate, and the liquid pH in the crystallization tower is such an amount. When the pH is less than 7, carbonate is not precipitated, and when it exceeds 10, zinc carbonate is easily dissolved again.
  • acid-insoluble particles that are not dissolved by acid treatment in the subsequent metal recovery step are used as seed crystals.
  • acid-insoluble particles sand (silica sand), anthracite and the like can be used as the acid-insoluble particles.
  • the seed crystal grain size is suitably about 0.1 to 1 mm, particularly about 0.2 to 0.4 mm.
  • metal ions in the crystallization raw water are insolubilized as metal carbonates and precipitate on the seed crystal surface.
  • the seed crystal particles grow by precipitation of the metal carbonate and increase to a particle size of 0.3 to 1.5 mm.
  • the increased particles are extracted from the crystallizer and fed to the metal recovery process.
  • the treated water of the crystallizer 8 is introduced into the crystallized water tank 9.
  • the recovery rate of metal ions is often 70 to 90%, generally about 80%. For this reason, it is preferable to return a part of this crystallization treatment water to the iron insolubilization step and to circulate it together with the raw water plating washing waste water. Thereby, the metal ions which could not be recovered by one crystallization process can be repeatedly crystallized, and the overall metal recovery rate can be increased.
  • the ratio of the crystallized water to be circulated is 10 to 80% of the water introduced into the crystallized water tank 9, the total water recovery rate is 70 to 90%, and the metal recovery rate is 80%. It is preferable to perform the treatment under the condition of about 95%.
  • the crystallizer 8 when an acid such as sulfuric acid or hydrochloric acid is brought into contact with particles having a metal carbonate such as nickel or zinc attached using an acid-insoluble seed crystal as a nucleus, the metal carbonate such as nickel or zinc is redissolved. Thus, a highly concentrated solution of metal sulfate or chloride is obtained. In the treatment of the electroplating washing waste water, the high-concentration metal sulfate aqueous solution thus obtained can be reused as it is in the plating bath. In addition, after the recovered particles are brought into contact with an acid to dissolve the metal carbonate, acid-insoluble seed crystal particles remain, but these seed crystal particles should be used again as seed crystals in a crystallizer. Can do. By reusing seed crystal particles in this way, particle size management in the crystallizer becomes easy.
  • the device for bringing the particles extracted from the crystallizer 8 (particles having a metal carbonate deposited on the surface of the seed crystal) into contact with the acid is not particularly limited as long as it can efficiently bring both into contact with each other.
  • an acid contact device as shown in FIG. 3 can be used.
  • This acid contact device has an acid contact tower 20 into which the drawn particles from the crystallizer 8 are charged, and a water collecting plate (porous) through which only water can pass without passing through the particles in the lower part of the tower. Plate or mesh).
  • the valves V 1 and V 2 are opened, the other valves are closed, the extracted particles are put into the acid contact tower 20 from the pipe 21, and moisture is supplied to the pipe 23, Extract from 24. This water is returned to the crystallization water tank 9.
  • the valves V 3 and V 4 are opened, the other valves are closed, and an acid such as sulfuric acid is passed through the pipes 25 and 23 from the lower part of the acid contact tower 20 by the pump P 3 to contact the acid and the particles.
  • a solution containing metal ions in which the metal carbonate is dissolved is taken out via the pipe 26.
  • this metal salt solution since a high concentration solution of about 5 to 15% by weight of metal ions is usually obtained, this metal salt solution can be suitably reused as a plating solution.
  • valves V 2 and V 5 After dissolving the metal carbonate on the surface of the seed crystal, the valves V 2 and V 5 are opened, the other valves are closed, and the water is acidified at a high flow rate through the pipes 24 and 23 by a pump (not shown). and passed through from the bottom of the contact tower 20, the seed crystals through the valve V 5 to return to reuse the crystallizer 8.
  • the acid used for dissolving the metal carbonate on the seed crystal is preferably a high concentration sulfuric acid aqueous solution of about 50 to 98% by weight or a 20 to 35% by weight hydrochloric acid aqueous solution.
  • the amount of waste water and the amount of discharged metal are reduced, the amount of sludge generated in the entire system is greatly reduced, and water and valuable metals are efficiently recovered from the plating washing waste water. can do.
  • Example 1 Water and metal were recovered from the plating washing waste water by the method shown in FIG.
  • the treatment liquid in the flocculation / oxidation tank 1 was introduced into the precipitation tank 2 and most of the generated floc was settled and separated, and then the separation liquid in the precipitation tank 2 was subjected to membrane filtration with the UF membrane device 3. This UF membrane device 3 was regularly backwashed.
  • the filtered water of the UF membrane device 3 is introduced into the adjustment tank 5 through the UF treatment water tank 4, and after adding residual sodium bisulfite 15mg / L to remove residual chlorine, it is supplied to the RO membrane apparatus 6 (RO supply water) ), RO permeated water was recovered, and RO concentrated water was supplied to the crystallizer 8 through the RO concentrated water tank 7 for crystallization treatment.
  • the water recovery rate of this RO membrane device 6 was 80%.
  • the crystallization apparatus 8 is a crystallization reaction tower 10 as shown in FIG. 2 filled with sand having a particle size of about 0.2 mm.
  • RO concentrated water is passed from the lower part of the crystallization reaction tower 10 to sand.
  • the pH in the fluidized bed was adjusted to 9 by adding sodium carbonate (Na 2 CO 3 ) to the fluidized bed. Crystallized water from the crystallizer 8 was received in a crystallized water tank 9.
  • Table 1 shows the water quality for each process in this treatment.
  • Iron was insolubilized by the iron insolubilization treatment, and was removed to a level that was not detected at the stage of RO supply water.
  • Nickel and zinc were hardly insolubilized up to the RO membrane device 6 and were in a dissolved state.
  • About 80% of nickel and zinc concentrated in a dissolved state on the RO concentrated water side were removed by crystallization treatment (metal recovery rate 80%).
  • metal recovery rate 80% nickel and zinc were deposited on the surface of sand introduced as seed crystals, and an increase in seed crystal particle diameter was observed.
  • Example 2 In Example 1, the seed crystal having a particle size increased to about 0.3 to 0.4 mm by the crystallization treatment is guided to the acid contact tower 20 shown in FIG. A weight% aqueous sulfuric acid solution was injected. The water content of the particles after draining was 10% by weight. By injecting sulfuric acid from the lower part of the tower, nickel and zinc adhering to the seed crystal surface were dissolved, and a sulfate solution of nickel and zinc was obtained from the upper part of the tower. The nickel and zinc concentrations of this solution were 1.5 wt% and 17 wt%, respectively. As a result, nickel and zinc in plating washing wastewater in the raw water are concentrated 600 times and 577 times, respectively.
  • Example 3 In Example 1, 90% of the crystallization treated water was returned to the inlet side of the flocculation / oxidation tank 1 and treated in the same manner as in the treatment with the plating washing waste water.
  • the one-pass metal recovery rate in the crystallization treatment is not changed to 80%, but by returning the crystallization treatment water and treating it again, the crystallization treatment is repeated and the entire metal is recovered. The recovery increased to 98%. The water recovery rate was improved to 92%.

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PCT/JP2010/059680 2009-06-11 2010-06-08 メッキ洗浄排水からの水及び金属の回収方法 WO2010143623A1 (ja)

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US8747787B2 (en) 2010-07-28 2014-06-10 Sumitomo Metal Mining Co., Ltd. Method for producing raw material for ferronickel smelting from low grade nickel oxide ore
CN104724857A (zh) * 2015-03-27 2015-06-24 天津大学 漂粉精生产过程中漂洗液的资源化处理方法
EP3015160A4 (en) * 2013-12-18 2016-12-21 Mitsubishi Heavy Ind Ltd TARTER DETECTION DEVICE AND METHOD FOR CONCENTRATING DEVICE AND WATER RECYCLING TREATMENT SYSTEM
EP3156508A1 (en) * 2015-10-16 2017-04-19 Vito NV Recovery process for metal-containing byproducts of metal production and processing
CN106587478A (zh) * 2017-01-22 2017-04-26 青岛北方节能环保有限公司 一种热镀锌废酸资源化处理方法
CN107253775A (zh) * 2017-06-22 2017-10-17 广东益诺欧环保股份有限公司 一种电镀废水污泥减量装置
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CN108147622A (zh) * 2018-01-16 2018-06-12 张家港市佰坤物资有限公司 一种电解铜废水处理工艺
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