WO2019085128A1 - 处理碱性锌镍合金电镀废水的方法 - Google Patents

处理碱性锌镍合金电镀废水的方法 Download PDF

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WO2019085128A1
WO2019085128A1 PCT/CN2017/113954 CN2017113954W WO2019085128A1 WO 2019085128 A1 WO2019085128 A1 WO 2019085128A1 CN 2017113954 W CN2017113954 W CN 2017113954W WO 2019085128 A1 WO2019085128 A1 WO 2019085128A1
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electroplating wastewater
nickel alloy
alkaline zinc
alloy electroplating
zinc
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PCT/CN2017/113954
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French (fr)
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郭崇武
赖奂汶
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广州超邦化工有限公司
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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
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
    • C02F1/56—Macromolecular compounds
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
    • 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
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions

Definitions

  • the invention belongs to the technical field of wastewater treatment, and particularly relates to a method for treating alkaline zinc-nickel alloy electroplating wastewater, in particular to a method for precipitating zinc and nickel ions in an alkaline zinc-nickel alloy electroplating wastewater.
  • Zinc-nickel alloy coatings have excellent corrosion resistance and have been widely used in protective coatings for automotive and other accessories.
  • the alkaline zinc-nickel alloy plating solution contains about 3% of an aliphatic polyamine complexing agent.
  • the complexing agent has high stability, and oxidation with hydrogen peroxide or bleaching water at normal temperature does not effectively destroy the complexing agent. Therefore, in the promotion and use of the alkaline zinc-nickel alloy electroplating process, it has been facing difficulties in the treatment of electroplating wastewater.
  • the method requires 10 hours of oxidation with hydrogen peroxide, and requires a large reaction equipment.
  • small and medium-sized electroplating enterprises cannot implement docking with the existing wastewater treatment equipment, and the reconstruction of wastewater treatment equipment is subject to the constraints of the site.
  • the present invention provides a method for treating alkaline zinc-nickel alloy electroplating wastewater, which is simple and can effectively solve the current alkaline zinc-nickel alloy electroplating wastewater treatment process and equipment. problem.
  • a method for treating alkaline zinc-nickel alloy electroplating wastewater comprising the steps of:
  • the aqueous solution of the sodium diethyldithiocarbamate aqueous solution in the step (1) has a mass fraction of 13% to 18%.
  • the aqueous solution of the sodium diethyldithiocarbamate aqueous solution in the step (1) has a mass fraction of 15%.
  • the volume ratio of the aqueous sodium diethyldithiocarbamate solution to the alkaline zinc-nickel alloy electroplating wastewater in the step (1) is from 2 to 4:100.
  • the flocculating agent in the step (2) is a polyacrylamide flocculant aqueous solution having a mass concentration of 0.4% to 0.6%.
  • the flocculating agent in step (2) is a polyacrylamide flocculant aqueous solution having a mass concentration of 0.4%.
  • the pH is adjusted in steps (1), (3), (4) using dilute sulfuric acid or a sodium hydroxide solution, which is prepared from concentrated sulfuric acid and water in a volume ratio of 1:8-12.
  • the sodium hydroxide solution has a mass fraction of 3% to 7%.
  • the alkaline zinc-nickel alloy electroplating wastewater in the step (1) is an alkaline zinc-nickel alloy. Rinsing water on the gold plating line.
  • the ORP value in step (4) is 200 millivolts.
  • the sodium hypochlorite solution in the step (4) is prepared from a sodium hypochlorite solution containing 10% of available chlorine in a volume ratio of 1:4 to 6 and water.
  • the present invention has the following beneficial effects:
  • the method for treating alkaline zinc-nickel alloy electroplating wastewater of the present invention uses sodium diethyldithiocarbamate which has a stronger precipitation ability than the conventional sodium dimethyldithiocarbamate, and has more zinc and nickel. Strong sedimentation ability, by controlling the pH of the wastewater in the sedimentation tank between 4.5 and 5.5, the sodium diethyldithiocarbamate and zinc and nickel ions are completely precipitated; and it is not necessary to add hydrogen peroxide to destroy the aliphatic in the wastewater.
  • the amine strong complexing agent simplifies the treatment process, and the treatment process can be docked with the existing electroplating wastewater treatment equipment, which solves the difficulties faced by the current alkaline zinc-nickel alloy electroplating wastewater treatment and has a good market application prospect;
  • the treatment method of the alkaline zinc-nickel alloy electroplating wastewater of the invention increases the process of oxidizing residual sodium diethyldithiocarbamate in the waste water with sodium hypochlorite after the separation of the precipitate, and solves the problem that the COD cannot be discharged due to the standard. problem;
  • Precipitant aqueous solution of sodium diethyldithiocarbamate
  • Flocculant an aqueous solution of polyacrylamide flocculant
  • Dilute sulfuric acid diluted with concentrated sulfuric acid 8 to 12 times;
  • Sodium hydroxide solution a mass fraction of 3% to 7% sodium hydroxide solution
  • Sodium hypochlorite solution The volume ratio of sodium chloride solution to water of 10% of available chlorine is from 1:4 to 1:6.
  • Step one adjust the pH value
  • Step two precipitation of heavy metal ions
  • the electroplating wastewater flows from the inclined tube settling tank into the oxidation reaction tank, the sodium hypochlorite is used to oxidize the residual sodium diethyldithiocarbamate and other reducing compounds in the wastewater, and the potentiometer is used to control the ORP value of the electroplating wastewater by 200 mV, which is automatically adjusted. The amount of sodium hypochlorite solution added.
  • Electroplating wastewater flows from the oxidation reaction tank into the neutralization reaction tank, and the tank liquid is stirred, and dilute sulfuric acid or sodium hydroxide is added. The solution was adjusted to pH 7-8.
  • the treated electroplating wastewater is discharged from the water outlet.
  • the sludge in the inclined tube settling tank is pumped into the plate and frame filter press by the sludge pump, and the filtrate is flowed back to the zinc-nickel alloy electroplating wastewater regulating tank.
  • the filter cake is processed by a qualified electroplating sludge specialist treatment plant.
  • the alkaline zinc-nickel alloy plating solution contains an aliphatic polyamine complexing agent, and the aliphatic polyamine complexing agent can react with an acid under acidic conditions to form a salt, which greatly reduces the coordination ability of the amine group, and therefore, only in acidity Under the conditions, sodium diethyldithiocarbamate can effectively precipitate zinc and nickel ions in the alkaline zinc-nickel alloy plating solution.
  • Sodium diethyldithiocarbamate reacts with acid under strong acidic conditions to form diethyldithiocarbamic acid, which reduces the ability to precipitate heavy metals. Therefore, sodium diethyldithiocarbamate is stronger. Under acidic conditions, it is not effective to precipitate some heavy metal ions.
  • the treatment results meet the requirements of Table 3 of GB 21900-2008 Electroplating Pollutant Emission Standard.
  • Sodium diethyldithiocarbamate has a relatively weak precipitation ability for zinc.
  • pH is ⁇ 4.5, its sodium salt is converted to diethyldithiocarbamic acid, and the precipitation ability of heavy metal ions is reduced, resulting in zinc treatment.
  • the result is not up to standard.
  • the pH is >5.5, the coordination ability of the aliphatic polyamine complexing agent in the electroplating wastewater to nickel is enhanced, and the treatment result of nickel does not meet the requirements of Table 2 of GB 21900-2008.
  • the results in Table 2 show that the concentration of residual zinc and nickel in the test solution increases with the increase of the concentration of aliphatic polyamine in the electroplating wastewater.
  • the alkaline zinc-nickel alloy plating solution is diluted 100 times, the treatment results of zinc and nickel meet the requirements of Table 2 of GB 21900-2008; the alkaline zinc-nickel alloy plating solution is diluted 50-75 times, and the zinc meets the table.
  • nickel can meet the requirements of Table 2.
  • the plating solution is diluted 25 times, zinc can meet the requirements of Table 3, and nickel can only meet the requirements of Table 1.
  • the mass concentration of zinc is 0.48mg/L
  • the mass concentration of nickel is 0.17mg/L
  • the treatment result of nickel meets the GB 21900-2008 Electroplating Pollutant Emission Standard. 2 requirements, but do not meet the requirements of Table 3.
  • the mass concentration of nickel after treatment is 0.08 mg/L, which can meet the requirements of Table 3 of GB 21900-2008 Electroplating Pollutant Emission Standard.

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Removal Of Specific Substances (AREA)

Abstract

一种处理碱性锌镍合金电镀废水的方法，调节碱性锌镍合金电镀废水的pH至3～4，加入二乙基二硫代氨基甲酸钠水溶液，沉淀锌和镍，加入絮凝剂，使沉淀颗粒聚集；调节电镀废水的pH至4.5～5.5，再加入次氯酸钠溶液；调节经处理后的电镀废水的pH为6～9，即得。

Description

处理碱性锌镍合金电镀废水的方法 技术领域
本发明属于废水处理技术领域，特别涉及一种处理碱性锌镍合金电镀废水的方法，尤其是沉淀碱性锌镍合金电镀废水中锌和镍离子的方法。
背景技术
锌镍合金镀层具有优异的耐蚀性，已广泛应用于汽车等配件的防护性镀层。碱性锌镍合金镀液含有3％左右的脂肪族多胺配位剂，这种配位剂的稳定性高，在常温下用双氧水或漂水氧化并不能有效破坏这些配位剂。因此，在碱性锌镍合金电镀工艺的推广使用中，一直面临电镀废水处理的困难。
授权公告号为“CN 104961273 B”的中国发明专利《一种碱性锌-镍合金电镀废水的处理方法》公开了一种技术方案：在pH＝8～13的条件下用双氧水氧化电镀废水中的配位剂，氧化后用焦亚硫酸钠还原残留的双氧水，在pH＝4.5～5.5的条件下用二甲基二硫代氨基甲酸钠沉淀电镀废水中的锌和镍。该方法用双氧水氧化需要10小时，且需要较大的反应设备，目前中小型电镀企业实施这套方案时与现有废水处理设备无法对接，重建废水处理设备又受到场地的制约。
发明内容
基于此，为了克服上述现有技术的缺陷，本发明提供了一种处理碱性锌镍合金电镀废水的方法，该方法简单，可以有效解决目前碱性锌镍合金电镀废水处理工艺与设备配套的问题。
为了实现上述发明目的，本发明采取了以下技术方案：
一种处理碱性锌镍合金电镀废水的方法，包括以下步骤：
(1)、调节碱性锌镍合金电镀废水的pH至3～4，加入二乙基二硫代氨基甲酸钠水溶液，沉淀锌和镍，得到沉淀颗粒；所述二乙基二硫代氨基甲酸钠水溶液与碱性锌镍合金电镀废水的体积用量比为2～5：100；
(2)、加入絮凝剂，使沉淀颗粒聚集；
(3)、调节经步骤(2)处理后的电镀废水的pH至4.5～5.5；
(4)、加入次氯酸钠溶液，根据电镀废水COD达标所需的ORP值，控制次氯酸钠溶液的量；
(5)、调节经步骤(3)处理后的电镀废水的pH为6～9，即得。
在其中一些实施例中，步骤(1)中所述二乙基二硫代氨基甲酸钠水溶液的质量分数为13％～18％。
在其中一些实施例中，步骤(1)中所述二乙基二硫代氨基甲酸钠水溶液的质量分数为15％。
在其中一些实施例中，步骤(1)中所述二乙基二硫代氨基甲酸钠水溶液与碱性锌镍合金电镀废水的体积比为2～4：100。
在其中一些实施例中，步骤(2)中所述絮凝剂为质量浓度为0.4％～0.6％的聚丙烯酰胺絮凝剂水溶液。
在其中一些实施例中，步骤(2)中所述絮凝剂为质量浓度为0.4％的聚丙烯酰胺絮凝剂水溶液。
在其中一些实施例中，步骤(1)、(3)、(4)中采用稀硫酸或氢氧化钠溶液调节pH，所述稀硫酸是由体积比1:8～12的浓硫酸与水配制而得；所述氢氧化钠溶液的质量分数为3％～7％。
在其中一些实施例中，步骤(1)中所述碱性锌镍合金电镀废水为碱性锌镍合 金电镀生产线上的漂洗水。
在其中一些实施例中，步骤(4)中ORP值为200毫伏。
在其中一些实施例中，步骤(4)中所述次氯酸钠溶液是由体积比为1:4～6的含有效氯10％的次氯酸钠溶液与水配制而得。
与现有技术相比，本发明具有以下有益效果：
1、本发明的碱性锌镍合金电镀废水的处理方法，使用了比传统的二甲基二硫代氨基甲酸钠的沉淀能力更强的二乙基二硫代氨基甲酸钠，对锌和镍具有更强的沉淀能力，通过将沉淀池中废水的pH控制在4.5～5.5之间，使二乙基二硫代氨基甲酸钠与锌和镍离子沉淀完全；且不需要加双氧水破坏废水中的脂肪族多胺类强配位剂，简化了处理流程，处理工艺能与现有电镀废水处理设备对接，解决了目前碱性锌镍合金电镀废水处理面临的困难，具有较好的市场应用前景；
2、本发明的碱性锌镍合金电镀废水的处理方法在沉淀物分离后增加了用次氯酸钠氧化废水中残留二乙基二硫代氨基甲酸钠的工序，解决了由其导致的COD不能达标排放的问题；
3、本发明的碱性锌镍合金电镀废水的处理方法，当碱性锌镍合金电镀废水浓度小于碱性锌镍合金镀液浓度的1％时，能够使电镀废水中的锌和镍同时达到GB 21900-2008《电镀污染物排放标准》表3的要求。
具体实施方式
为更好地理解本发明，下面通过以下实施例对本发明作进一步具体的阐述，但不可理解为对本发明的限定，对于本领域的技术人员根据上述发明内容所作的一些非本质的改进与调整，也视为落在本发明的保护范围内。
本发明以下实施例中所使用的主要设备和化学药剂分别如下：
电镀废水调节池；pH调节池；沉淀反应池；絮凝池；斜管沉降池；氧化反应池；中和反应池；板框式压滤机。
沉淀剂：二乙基二硫代氨基甲酸钠水溶液；
絮凝剂：聚丙烯酰胺絮凝剂水溶液；
稀硫酸：将浓硫酸稀释8～12倍；
氢氧化钠溶液：质量分数为3％～7％氢氧化钠水溶液；
次氯酸钠溶液：有效氯10％的次氯酸钠溶液与水的体积比从1:4至1:6。
实施例1
步骤一、调节pH值
将含镍小于10mg/L的碱性锌镍合金电镀废水从电镀废水调节池转入pH调节池，搅拌池液，加稀硫酸调节碱性锌镍合金电镀废水至pH＝3～4。
步骤二、沉淀重金属离子
电镀废水流入沉淀反应池，在搅拌条件下，每吨废水中加入质量分数为15％的二乙基二硫代氨基甲酸钠水溶液20L；电镀废水从沉淀反应池流入絮凝池，加絮凝剂(质量分数为0.4％)使沉淀颗粒聚集；加稀硫酸或氢氧化钠溶液调节电镀废水pH＝4.5～5.5；电镀废水从絮凝池流入斜管沉降池，沉淀物沉入沉降池底部。
步骤三、降低COD
电镀废水从斜管沉降池流入氧化反应池，加入次氯酸钠溶液氧化废水中残留的二乙基二硫代氨基甲酸钠以及其它还原性化合物，用电位计控制电镀废水的ORP值200毫伏，自动调节次氯酸钠溶液的加入量。
步骤四、中和处理
电镀废水从氧化反应池流入中和反应池，搅拌池液，加稀硫酸或氢氧化钠 溶液调节pH＝7～8。
步骤五、废水排放
处理后的电镀废水从出水口排出。
步骤六、沉淀物的处理
用污泥泵将斜管沉降池中的沉淀物泵入板框式压滤机，压滤，滤液流回到锌镍合金电镀废水调节池。滤饼由有资质的电镀污泥专业处理厂处理。
试验例1 pH对处理结果的影响
用二乙基二硫代氨基甲酸钠与锌和镍离子反应生成二乙基二硫代氨基甲酸锌和二乙基二硫代氨基甲酸镍沉淀物，所述沉淀反应受pH影响较大。碱性锌镍合金镀液中含有脂肪族多胺配位剂，脂肪族多胺配位剂在酸性条件下能与酸反应生成盐，大幅度降低胺基的配位能力，因此，只有在酸性条件下，用二乙基二硫代氨基甲酸钠才能有效沉淀碱性锌镍合金镀液中的锌和镍离子。二乙基二硫代氨基甲酸钠在较强的酸性条件下能与酸反应生成二乙基二硫代氨基甲酸，使其沉淀重金属的能力下降，因此，二乙基二硫代氨基甲酸钠在较强的酸性条件下又不能有效沉淀一些重金属离子。
用移液管吸取碱性锌镍合金镀液10mL分别于6只2L烧杯中，加水至1L，加入稀硫酸调节试液的pH＝3～4，向各烧杯中分别加入沉淀剂20mL，搅拌试液，再用稀硫酸或氢氧化钠溶液调节试液的pH分别为4.0、4.5、5.0、5.5和6.0，放置60min后用定量滤纸过滤试液。用原子吸收分光光度法测定滤液中锌和镍的质量浓度，结果列于表1。
表1沉淀时试液pH对锌和镍处理结果的影响
沉淀时试液pH ρ(Zn)/(mg/L) ρ(Ni)/(mg/L)
4.0 4.37 0.07
4.5 0.89 0.07
5.0 0.67 0.08
5.5 0.23 0.09
6.0 0.18 0.53
表1结果表明，在pH＝4.5～5.5的范围内，处理后锌小于1mg/L，镍小于0.1mg/L，处理结果满足GB 21900-2008《电镀污染物排放标准》表3的要求。二乙基二硫代氨基甲酸钠对锌的沉淀能力相对较弱，在pH<4.5时，其钠盐转化为二乙基二硫代氨基甲酸，对重金属离子的沉淀能力减小，致使锌的处理结果不能达标。当pH>5.5时，电镀废水中的脂肪族多胺配位剂对镍的配位能力增强，镍的处理结果不满足GB 21900-2008表2的要求。
试验例2废水浓度对锌和镍处理结果的影响
将碱性锌镍合金镀液分别稀释25、50、75和100倍模拟锌镍合金电镀废水，取各稀释液1L，加入稀硫酸调节试液pH＝3～4，依次加入沉淀剂12、6、4、2mL沉淀锌和镍离子，然后以稀硫酸或氢氧化钠溶液调节试液pH＝5。过滤分离沉淀物后测定滤液中锌和镍的浓度，处理结果列于表2。
表2废水浓度对锌和镍处理结果的影响
稀释倍数 25 50 75 100
加沉淀剂/mL 12 6 4 2
ρ(Zn)/(mg/L) 0.63 0.47 0.45 0.42
ρ(Ni)/(mg/L) 0.58 0.36 0.15 0.07
表2结果表明，随着电镀废水中脂肪族多胺浓度的增加，处理后试液中残留锌和镍的浓度升高。将碱性锌镍合金镀液稀释100倍，锌和镍的处理结果满足GB 21900-2008表3的要求；将碱性锌镍合金镀液稀释50～75倍，锌满足表 3的要求，镍能满足表2的要求。将镀液稀释25倍，锌能够满足表3的要求，镍只能满足表1的要求。
对比例1
按授权专利《一种碱性锌-镍合金电镀废水的处理方法》处理碱性锌镍合金电镀废水中的锌和镍。吸取10mL碱性锌镍合金电镀溶液于2L烧杯中，加水至1L，加稀硫酸调节试液pH＝12，加质量分数30％的双氧水5mL，放置10h，加稀硫酸调节pH＝3.5，加质量分数为10％的二甲基二硫代氨基甲酸钠溶液20mL，搅拌后调节试液pH＝5，60min后用定量滤纸过滤。用原子吸收光谱法测定滤液中锌和镍得到：锌的质量浓度为0.48mg/L，镍的质量浓度为0.17mg/L，镍的处理结果满足GB 21900-2008《电镀污染物排放标准》表2的要求，但不满足表3的要求。
在相同条件下，按本发明的实施例1的处理方法进行处理，处理后镍的质量浓度为0.08mg/L，可以满足GB 21900-2008《电镀污染物排放标准》表3的要求。
以上所述实施例的各技术特征可以进行任意的组合，为使描述简洁，未对上述实施例中的各个技术特征所有可能的组合都进行描述，然而，只要这些技术特征的组合不存在矛盾，都应当认为是本说明书记载的范围。
以上所述实施例仅表达了本发明的几种实施方式，其描述较为具体和详细，但并不能因此而理解为对发明专利范围的限制。应当指出的是，对于本领域的普通技术人员来说，在不脱离本发明构思的前提下，还可以做出若干变形和改进，这些都属于本发明的保护范围。因此，本发明专利的保护范围应以所附权利要求为准。

Claims (10)

  1. 一种处理碱性锌镍合金电镀废水的方法，其特征在于，包括以下步骤：
    (1)、调节碱性锌镍合金电镀废水的pH至3～4，加入二乙基二硫代氨基甲酸钠水溶液，沉淀锌和镍，得到沉淀颗粒；所述二乙基二硫代氨基甲酸钠水溶液与碱性锌镍合金电镀废水的体积比为2～5：100；
    (2)、加入絮凝剂，使沉淀颗粒聚集；
    (3)、调节经步骤(2)处理后的电镀废水的pH至4.5～5.5；
    (4)、加入次氯酸钠溶液，根据电镀废水COD达标所需的ORP值，控制次氯酸钠溶液的量；
    (5)、调节经步骤(4)处理后的电镀废水的pH为6～9，即得。
  2. 根据权利要求1所述的处理碱性锌镍合金电镀废水的方法，其特征在于，步骤(1)中所述二乙基二硫代氨基甲酸钠水溶液的质量分数13％～18％。
  3. 根据权利要求2所述的处理碱性锌镍合金电镀废水的方法，其特征在于，步骤(1)中所述二乙基二硫代氨基甲酸钠水溶液的质量分数15％。
  4. 根据权利要求1所述的处理碱性锌镍合金电镀废水的方法，其特征在于，步骤(1)中所述二乙基二硫代氨基甲酸钠水溶液与碱性锌镍合金电镀废水的体积比为2～4：100。
  5. 根据权利要求1所述的处理碱性锌镍合金电镀废水的方法，其特征在于，步骤(2)中所述絮凝剂为质量浓度为0.4％～0.6％的聚丙烯酰胺絮凝剂水溶液。
  6. 根据权利要求5所述的处理碱性锌镍合金电镀废水的方法，其特征在于，步骤(2)中所述絮凝剂为质量浓度为0.4％的聚丙烯酰胺絮凝剂水溶液。
  7. 根据权利要求1所述的处理碱性锌镍合金电镀废水的方法，其特征在于，步骤(1)、(3)、(4)中采用稀硫酸或氢氧化钠溶液调节pH，所述稀硫酸是由体积比1:8～12的浓硫酸与水配制而得；所述氢氧化钠溶液的质量分数为3％～7％。
  8. 根据权利要求1所述的处理碱性锌镍合金电镀废水的方法，其特征在于，步骤(1)中所述碱性锌镍合金电镀废水为碱性锌镍合金电镀生产线上的漂洗水。
  9. 根据权利要求1所述的处理碱性锌镍合金电镀废水的方法，其特征在于，步骤(4)中ORP值为200毫伏。
  10. 根据权利要求1所述的处理碱性锌镍合金电镀废水的方法，其特征在于，步骤(4)中所述次氯酸钠溶液是由体积比为1:4～6的含有效氯10％的次氯酸钠溶液与水配制而得。
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