CN103288185B - 一种利用外循环电絮凝技术处理重金属离子废水的方法 - Google Patents

一种利用外循环电絮凝技术处理重金属离子废水的方法 Download PDF

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CN103288185B
CN103288185B CN201310188850.4A CN201310188850A CN103288185B CN 103288185 B CN103288185 B CN 103288185B CN 201310188850 A CN201310188850 A CN 201310188850A CN 103288185 B CN103288185 B CN 103288185B
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outer circulation
heavy metal
electrocoagulation
waste water
floccules
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CN103288185A (zh
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陆君
马晓云
陆鸿飞
李艳
蔡星伟
潘龙
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Honeycomb Activated Carbon Co ltd
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Jiangsu Tongrui Environmental Protection Science & Technology Development Co Ltd
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Abstract

本发明公开了一种利用外循环电絮凝技术处理重金属离子废水的方法,包括如下步骤:首先预处理废水,然后进行外循环电絮凝处理,其中在电絮凝电解槽底部设有导出管,在管道上安装流体循环泵,并控制该循环泵产生的强制对流流量。本发明的优点为电絮凝过程中通过强制外循环形成的流体湍流破碎絮体,相比普通电絮凝,强制外循环电絮凝将使得吸附絮体尺寸更小,絮体外表面羟基密度更高,絮体内表面相对无效的羟基吸附位更少,絮体分布得更均匀,从而离子吸附率能够提高到80%~95%以上。

Description

一种利用外循环电絮凝技术处理重金属离子废水的方法
技术领域
本发明涉及一种处理重金属离子废水的方法,尤其涉及一种利用外循环电絮凝技术处理重金属离子废水的方法。
背景技术
当前重金属废水的处理工艺主要有化学沉淀、化学絮凝、电解还原、膜分离法等,前三种方法存在的问题主要归纳为二次污染严重、有效治理率低、维护困难、废水回用率低等,而膜分离法存在因为膜污染、膜成本高和膜寿命短等问题。近年来在重金属废水处理领域中,电絮凝技术应用得越来越广泛,也颇具竞争力,这是由于电絮凝过程包含了电解气浮和吸附絮凝两种反应、且协同作用,因而可以快速、高效地处理重金属离子废水。传统的一级电絮凝系统在反应初期废水中的重金属离子和絮体充分接触、碰撞,随着时间的推移在反应后期重金属离子浓度和絮体含量减少,絮体吸附利用率下降,一级电絮凝处理结束后还需要后续处理才能将废水中的重金属离子去除,工艺复杂、能耗大。
发明内容
发明目的:本发明的目的是提供一种能够提高重金属离子去除率、利用外循环电絮凝技术处理重金属离子废水的方法。
技术方案:本发明所述的一种利用外循环电絮凝技术处理重金属离子废水的方法,包括如下步骤:首先调节废水的pH值为4~6.5,电导率为500~7000us/cm;然后进行外循环电絮凝处理:低压脉冲电源控制每对电极之间的平均电流密度为2~8.5mA/cm2,电极间距为5~30mm,电解时间为10~90min,同时电絮凝电解槽底部设有导出管,在管道上安装流体循环泵,控制该循环泵产生的强制对流流量为1~20L/min。
其中,所述废水的重金属离子含量为50~400mg/L。所述废水的重金属离子含量为100~310mg/L。所述废水的pH值为4.5~6,电导率为1200~5000us/cm,每对电极之间的平均电流密度为3~7.5mA/cm2,电极间距为9~25mm,电解时间为20~70min,强制对流流量为5~15L/min。
反应机理:电絮凝主要通过阳极金属电解产生铁离子或铝离子,这些离子通过水解产生氢氧化物吸附絮体,该絮体通过配合作用吸附污染物实现重金属离子的分离,因此电絮凝过程中吸附絮体的产生量及其吸附率对重金属离子去除率和反应能耗影响重大。絮体的内表面和外表面同时存在羟基吸附位,内表面的羟基吸附位的吸附效率要低于外表面的吸附效率;同摩尔絮体总量下,小尺寸的絮体有着较高的比表面积,其外表面上的羟基吸附位的体积密度也较高,故较小尺寸的絮体,其吸附总量和吸附密度也要高于大尺寸的絮体。本发明在电絮凝系统中增设强制外循环工艺,通过循环泵将流体从槽底引入到槽口,再从槽口流向槽底,实现电解槽内流体强制循环流动,对絮体进行破碎和均匀化处理,减小吸附絮体的尺寸,以增大吸附絮体的比表面和羟基吸附位密度。
有益效果:本发明与现有技术相比,其显著优点为电絮凝过程中通过强制外循环形成的流体湍流破碎絮体,相比普通电絮凝,强制外循环电絮凝将使得吸附絮体尺寸更小,絮体外表面羟基密度更高,絮体内表面相对无效的羟基吸附位更少,絮体分布得更均匀,从而离子吸附去除率能够达到80%~95%。
具体实施方式:
实施例1:一种含镍重金属废水,其镍含量为50mg/L,首先调节废水的pH值为4,电导率为7000us/cm;然后将废水置于电解槽中进行外循环电絮凝处理:低压脉冲电源控制每对电极之间的平均电流密度为8.5mA/cm2,电极间距为5mm,电解时间为90min,同时电絮凝电解槽底部设有导出管,在管道上安装流体循环泵,控制该循环泵产生的强制对流流量为20L/min,处理结束后,镍含量为2.5mg/L,镍去除率为95%。
实施例2:一种含钴重金属废水,其钴含量为100mg/L,首先调节废水的pH值为4.5,电导率为5000us/cm;然后将废水置于电解槽中进行外循环电絮凝处理:低压脉冲电源控制每对电极之间的平均电流密度为7.5mA/cm2,电极间距为9mm,电解时间为70min,同时电絮凝电解槽底部设有导出管,在管道上安装流体循环泵,控制该循环泵产生的强制对流流量为15L/min,处理结束后,钴含量为10mg/L,钴去除率为90%。
实施例3:一种含镉重金属废水,其镉含量为150mg/L,首先调节废水的pH值为5,电导率为3500us/cm;然后将废水置于电解槽中进行外循环电絮凝处理:低压脉冲电源控制每对电极之间的平均电流密度为6.5mA/cm2,电极间距为12mm,电解时间为50min,同时电絮凝电解槽底部设有导出管,在管道上安装流体循环泵,控制该循环泵产生的强制对流流量为12L/min,处理结束后,镉含量为15mg/L,镉去除率为90%。
实施例4:一种含镉重金属废水,其镉含量为220mg/L,首先调节废水的pH值为5.5,电导率为2000us/cm;然后将废水置于电解槽中进行外循环电絮凝处理:低压脉冲电源控制每对电极之间的平均电流密度为4.5mA/cm2,电极间距为18mm,电解时间为30min,同时电絮凝电解槽底部设有导出管,在管道上安装流体循环泵,控制该循环泵产生的强制对流流量为8L/min,处理结束后,镉含量为44mg/L,镉去除率为80%。
实施例5:一种含铬重金属废水,其铬含量为310mg/L,首先调节废水的pH值为6,电导率为1200us/cm;然后将废水置于电解槽中进行外循环电絮凝处理:低压脉冲电源控制每对电极之间的平均电流密度为3mA/cm2,电极间距为25mm,电解时间为20min,同时电絮凝电解槽底部设有导出管,在管道上安装流体循环泵,控制该循环泵产生的强制对流流量为5L/min,处理结束后,铬含量为31mg/L,铬去除率为90%。
实施例6:一种含铬重金属废水,其铬含量为400mg/L,首先调节废水的pH值为6.5,电导率为500us/cm;然后将废水置于电解槽中进行外循环电絮凝处理:低压脉冲电源控制每对电极之间的平均电流密度为2mA/cm2,电极间距为30mm,电解时间为10min,同时电絮凝电解槽底部设有导出管,在管道上安装流体循环泵,控制该循环泵产生的强制对流流量为1L/min,处理结束后,铬含量为20mg/L,铬去除率为95%。

Claims (4)

1.一种利用外循环电絮凝技术处理重金属离子废水的方法,其特征在于:首先调节废水的pH值为4~6.5,电导率为500~7000us/cm;然后进行外循环电絮凝处理:低压脉冲电源控制每对电极之间的平均电流密度为2~8.5mA/cm2,电极间距为5~30mm,电解时间为10~90min,同时电絮凝电解槽底部设有导出管,在管道上安装流体循环泵,控制该循环泵产生的强制对流流量为1~20L/min,通过强制外循环形成的流体湍流破碎电絮凝产生的絮体。
2.根据权利要求1所述利用外循环电絮凝技术处理重金属离子废水的方法,其特征在于:所述废水的重金属离子含量为50~400mg/L。
3.根据权利要求2所述利用外循环电絮凝技术处理重金属离子废水的方法,其特征在于:所述废水的重金属离子含量为100~310mg/L。
4.根据权利要求1所述利用外循环电絮凝技术处理重金属离子废水的方法,其特征在于:所述废水的pH值为4.5~6,电导率为1200~5000us/cm,每对电极之间的平均电流密度为3~7.5mA/cm2,电极间距为9~25mm,电解时间为20~70min,强制对流流量为5~15L/min。
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