CN109205895A - 一种高盐废水处理工艺系统及方法 - Google Patents
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Abstract
本发明公开了一种高盐废水处理工艺系统及方法，包括脱硫处理系统、原水调节池、超级软化沉淀池、超臭氧装置、清水池、多介质过滤器、弱酸阳床、钠床、紫外线装置、管式膜、保安过滤器、SCRO、特种分离膜、高压反渗透、烟道蒸发结晶干燥器、废水池、回用水池；为保证此工艺系统的长期稳定运行，还包括相关配套的清洗装置、加药装置、电气系统及仪表控制，具有加药少、重复利用、节省部分废水投资和运行处理成本等优点，解决目前工业废水零排放遇到的问题。
Description
技术领域
本发明涉及工业废水处理环保技术领域，具体涉及一种高盐废水处理工艺系统及方法。
背景技术
目前我国经济高速发展，同时伴随着能源的巨大消耗，环境问题也日益严重。为了使当前的环境局面得以改善，国家对三废的管理也越来越严，工业废水零排放为众多企业和专业人事所接受，同时逐渐的开始在工业领域进行实施。而水作为工业领域必不可少的资源，其浓缩后浓盐水的排放作为一项重要的环保指标。我国工业废水领域实施的零排放，特别在火力发电厂，关键问题是脱硫废水运行成本及投资成本太高，而且缺少稳定运行经验，现正在探索如何实验找到更稳定的处理方法和运行费用较低技术。
本发明专利申请整体考虑一种高盐废水处理工艺系统及方法，将高盐废水与电厂脱硫系统整体考虑，将脱硫系统产生的废水经超级软化沉淀池软化后，污泥重新进入脱硫系统与SO2进行反应生成石膏；同时钠床的再生采用高压反渗透的浓水，再生废水部分直接进入脱硫系统与SO2进行反应生成石膏；其他水经过软化后，进入膜系统，由特种分离膜进行分盐，产生的浓水直接返回脱硫系统，与SO2在吸收塔发生反应生成石膏，产水进入高压反渗透浓缩后，进入烟道蒸发结晶干燥器后，水被烟气带走，在脱硫提供进行冷凝回收，剩下的盐直接被烟气干燥，达到工业盐一级标准。实现完全零排放，同时有工业级别的产品得以利用。
目前常见的国内正在探索和实验阶段的为膜法+蒸发结晶和烟气余热蒸发两种，膜法有正渗透和高压反渗透，烟道余热蒸发分为除尘器前喷淋和除尘器后喷淋。烟气余热蒸产生的为杂盐，可能下一阶段会受环保政策的影响，而膜法+蒸发结晶，其软化药剂成本过高，运行及检修要求较高。
发明内容
本发明克服了现有技术的不足，提供一种高盐废水处理工艺系统及方法。
考虑到现有技术的上述问题，根据本发明的一个方面，为解决上述的技术问题，本发明采用一种高盐废水处理工艺系统及方法，此系统包括脱硫处理系统、原水调节池、超级软化沉淀池、超臭氧装置、清水池、多介质过滤器、弱酸阳床、钠床、紫外线装置、管式膜、保安过滤器、SCRO、特种分离膜、高压反渗透、烟道蒸发结晶干燥器、废水池、回用水池；为保证此工艺系统的长期稳定运行，还包括相关配套的清洗装置、加药装置、电气系统及仪表控制，其特征在于:
在工艺系统中，为了有效的去除SiO2、硬度及碱度，向超级软化沉淀池的不同区域中加入苛性钠、石灰、絮凝剂、纯碱和助凝剂，使水的pH值保持在11，出水硬度降为0.5mmol/L；
超级软化沉淀池产生的污泥为CaCO3、Mg(OH)2送入脱硫系统，使其与SO2在吸收塔发生以下反应：
CaCO3+SO2+1/2H2O─→CaSO3•1/2H2O+CO2↑
2CaSO3•1/2H2O+O2+3H2O─→2CaSO4•2H2O
Mg(OH)2+SO2+5H2O─→MgSO3•6H2O
超臭氧装置在运行过程中对废水COD及细菌进行催化氧化，将COD降为10mg/L以下；
弱酸阳床及钠床对水中的硬度再次进行去除，保证后端硬度降为0.1mmol/L；
高压反渗透产生的浓水一部分直接再生弱酸阳床及钠床；将其再生液体与冲洗水分开处理，冲洗水至多介质过滤器，再生废水进入脱硫系统，使其与SO2在吸收塔发生以下反应：
CaCO3+SO2+1/2H2O─→CaSO3•1/2H2O+CO2↑
2CaSO3•1/2H2O+O2+3H2O─→2CaSO4•2H2O
Mg(OH)2+SO2+5H2O─→MgSO3•6H2O
特种分离膜产生的浓水直接返回脱硫系统，与脱硫系统内的吸收塔发生反应生成石膏，SO4 2-、Ca2+、Mg2+，保证去除率为95%以上；
SCRO采用一级两段，段间采用增压泵回流，其回收率为40~75%；特种分离膜采用一级两段，段间采用增压泵回流，其回收率为60~75%，高压反渗透回收率为70%；经高压反渗透的浓水进入烟道蒸发结晶干燥器，水被烟气带走，在脱硫提供进行冷凝回收，剩下的盐直接被烟气干燥，达到工业盐一级标准。实现完全零排放，同时有工业级别的产品得以利用。
为了更好地实现本发明，进一步的技术方案是：
作为优选，所述高盐工业废水COD为5~300mg/L、SO4 2-为500~40000mg/L、Ca2+为50~50000mg/L、Mg2+为10~30000mg/L。
作为优选，按照权利要求1所述的絮凝剂为羧甲基纤维素。
与现有技术相比，本发明的优越性在于：
（1）废水经超级软化沉淀池软化后，污泥重新进入脱硫系统与SO2进行反应生成生成石膏，节省脱硫系统的石灰石；
（2）特种分离膜产生的浓水直接回至脱硫系统，直接与SO2生成石膏，节省脱硫系统的石灰石；
（3）钠床再生利用高压反渗透浓水，节省药剂同时节省部分废水投资和运行处理成本；
（4）直接在烟道进行蒸发结晶干燥器后，水被烟气带走，剩下的盐直接被烟气干燥，达到工业盐一级标准；
（5）各单元可独立运行，调节能力较强；
（6）工艺流程相对较短，节省投资及运行费用；
（7）清洗频率相对较低，这是因为在高pH条件下，细菌难以繁殖，不易产生潜在的污染；
（8）软化效果较好，最后浓缩完后利用烟气余热进行分盐，达到相对较好的运行效果。
附图说明
为了更清楚的说明本申请文件实施例或现有技术中的技术方案，下面将对实施例或现有技术的描述中所需要使用的附图作简单的介绍，显而易见地，下面描述中的附图仅是对本申请文件中一些实施例的参考，对于本领域技术人员来讲，在不付出创造性劳动的情况下，还可以根据这些附图得到其它的附图，也可对其中的某一部分进行调整后使用。
图1示出了根据本发明一个实施例的高盐废水处理工艺系统及方法的结构示意图。图中，(100)脱硫处理系统、(101)原水调节池、(102)超级软化沉淀池、(103)清水池、(104)超臭氧装置、(105)多介质过滤器、(106)弱酸阳床、(107)钠床、(108)紫外线装置、(109)管式膜、(110)保安过滤器、(111)SCRO、(112)特种分离膜、(113)高压反渗透、(114)烟道蒸发结晶干燥器、(115)废水池、(116)回用水池。
具体实施方式
下面结合实施例对本发明作进一步地详细说明，但本发明的实施方式不限于此。
图1示出了根据本发明一个实施例的高盐废水处理工艺系统及方法，包括
(100)脱硫处理系统、(101)原水调节池、(102)超级软化沉淀池、(103)清水池、(104)超臭氧装置、(105)多介质过滤器、(106)弱酸阳床、(107)钠床、(108)紫外线装置、(109)管式膜、(110)保安过滤器、(111)SCRO、(112)特种分离膜、(113)高压反渗透、(114)烟道蒸发结晶干燥器、(115)废水池、(116)回用水池。
为了能够实现高盐工业废水零排放，此系统通过管道与泵使各装置联接，高盐工业废水在原水调节池(101)中汇集，通过泵打入超级软化沉淀池（102)，在超级软化沉淀池(102)不同区域中加入苛性钠、石灰、羧乙基纤维素、纯碱和助凝剂，使水的pH值保持在11，出水硬度降为0.5mmol/L，超级软化沉淀池(102)产生的污泥为CaCO3、Mg(OH)2送入脱硫系统(100)，使其与SO2在吸收塔中发生以下反应：
CaCO3+SO2+1/2H2O─→CaSO3•1/2H2O+CO2↑
2CaSO3•1/2H2O+O2+3H2O─→2CaSO4•2H2O
Mg(OH)2+SO2+5H2O─→MgSO3•6H2O
超级软化沉淀池(102)澄清软化后的水进入清水池(103)，然后通过泵进入多介质过滤器(105)，在多介质过滤器(105)由(104)超臭氧装置产生的超臭氧对废水进行催化氧化，将COD降为10mg/L以下；其产水进入弱酸阳床(106)后进入钠床(107)过滤，对废水中的硬度再次进行去除，保证后端硬度降为0.1mmol/L；
钠床(107)产水由紫外线装置(108)消毒后，进入管式膜(109)进行再次软化，软化后进入保安过滤器(110)和SCRO(111)，经除盐后，其产水进行回收利用，浓水进入特种分离膜(112)，特种分离膜(112)产生的浓水直接返回脱硫系统(100)，在吸收塔发生反应生成石膏，SO4 2-、Ca2+、Mg2+，保证去除率为95%以上；
SCRO(111)采用一级两段，段间采用增压泵回流，其回收率为40~75%；特种分离膜(112)采用一级两段，段间采用增压泵回流，其回收率为60~75%；
特种分离膜(112)产水进入高压反渗透(113)，其回收率为70%，高压反渗透(113)产水进行回收利用，其产水的一部分浓水直接再生弱酸阳床(106)及钠床(107)，其他部分浓水进入烟道蒸发结晶干燥器(114)，浓水在烟道蒸发结晶干燥器(114)进行蒸发后被烟气带走，在脱硫系统(100)中的吸收塔进行冷凝回收，剩下的盐直接被烟气干燥，达到工业盐一级标准。
弱酸阳床(106)及钠床(107)再生液体与冲洗水分开处理，冲洗水至回收水池(116)，多介质过滤器(105)冲洗水也接至回收水池(116)，然后通过泵至清水池(103)回用；弱酸阳床(106)及钠床(107)再生废水接至废水池(115)，然后进入脱硫系统(100)，使其与SO2在吸收塔中发生以下反应：
CaCO3+SO2+1/2H2O─→CaSO3•1/2H2O+CO2↑
2CaSO3•1/2H2O+O2+3H2O─→2CaSO4•2H2O
Mg(OH)2+SO2+5H2O─→MgSO3•6H2O
为保证此工艺系统的长期稳定运行，实现完全零排放，同时产品得以利用，还包括相关配套的清洗装置、加药装置、电气系统及仪表控制参于此一种高盐废水处理工艺系统及方法的运行。
在本说明书中所谈到的“一个实施例”及“实施例”等，指的是结合该实施例描述的具体特征、结构或者特点包括在本申请概括性描述的至少一个实施例中。在说明书中多个地方出现同种表述不是一定指的是同一个实施例。进一步来说，结合任一实施例描述一个具体特征、结构或者特点时，所要主张的是结合其他实施例来实现这种特征、结构或者特点也落在本发明的范围内。
尽管这里参照本发明的多个解释性实施例对本发明进行了描述，但是，应该理解，本领域技术人员可以设计出很多其他的修改和实施方式，这些修改和实施方式将落在本申请公开的原则范围和精神之内。更具体地说，在本申请公开、附图和权利要求的范围内，可以对主题组合布局的组成部件和/或布局进行多种变型和改进。除了对组成部件和/或布局进行的变型和改进外，对于本领域技术人员来说，其他的用途也将是明显的。
Claims (4)
1.一种高盐废水处理工艺系统及方法，此系统包括脱硫处理系统、原水调节池、超级软化沉淀池、超臭氧装置、清水池、多介质过滤器、弱酸阳床、钠床、紫外线装置、管式膜、保安过滤器、SCRO、特种分离膜、高压反渗透、烟道蒸发结晶干燥器、废水池、回用水池；为保证此工艺系统的长期稳定运行，还包括相关配套的清洗装置、加药装置、电气系统及仪表控制，其特征在于:
在工艺系统中，为了有效的去除SiO2、硬度及碱度，向超级软化沉淀池的不同区域中加入苛性钠、石灰、絮凝剂、纯碱和助凝剂，使水的pH值保持在11，出水硬度降为0.5mmol/L；
超级软化沉淀池产生的污泥为CaCO3、Mg(OH)2送入脱硫系统，使其与SO2在吸收塔发生以下反应：
CaCO3+SO2+1/2H2O─→CaSO3•1/2H2O+CO2↑
2CaSO3•1/2H2O+O2+3H2O─→2CaSO4•2H2O
Mg(OH)2+SO2+5H2O─→MgSO3•6H2O
超臭氧装置在运行过程中对废水COD及细菌进行催化氧化，将COD降为10mg/L以下；
弱酸阳床及钠床对水中的硬度再次进行去除，保证后端硬度降为0.1mmol/L；
高压反渗透产生的浓水一部分直接再生弱酸阳床及钠床；弱酸阳床及钠床再生液体与冲洗水分开处理，冲洗水至回收水池，多介质过滤器冲洗水也接至回收水池，然后通过泵至清水池回用；弱酸阳床及钠床再生废水接至废水池，然后进入脱硫系统，使其与SO2在吸收塔发生以下反应：
CaCO3+SO2+1/2H2O─→CaSO3•1/2H2O+CO2↑
2CaSO3•1/2H2O+O2+3H2O─→2CaSO4•2H2O
Mg(OH)2+SO2+5H2O─→MgSO3•6H2O
特种分离膜产生的浓水直接返回脱硫系统，在脱硫系统内的吸收塔发生反应生成石膏，SO4 2-、Ca2+、Mg2+，保证去除率为95%以上；
SCRO采用一级两段，段间采用增压泵回流，其回收率为40~75%；特种分离膜采用一级两段，段间采用增压泵回流，其回收率为60~75%，高压反渗透回收率为70%；经高压反渗透的浓水进入烟道蒸发结晶干燥器，水被烟气带走，在脱硫提供进行冷凝回收，剩下的盐直接被烟气干燥，达到工业盐一级标准。
2.实现完全零排放，同时有工业级别的产品得以利用。
3.根据权利要求1所述的高盐废水处理工艺系统及方法，其特征在于，所述高盐工业废水COD为5~300mg/L、SO4 2-为500~40000mg/L、Ca2+为50~50000mg/L、Mg2+为10~30000mg/L。
4.按照权利要求1 所述的高盐废水处理工艺系统及方法，其特征在于所述絮凝剂为羧乙基纤维素。
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