CN109133464A - 火力发电厂全厂废水零排放工艺系统及方法 - Google Patents
火力发电厂全厂废水零排放工艺系统及方法 Download PDFInfo
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Abstract
本发明公开了一种火力发电厂全厂废水零排放工艺系统及方法，将火力发电厂全厂废水整体考虑，从软化到浓缩，到蒸发结晶，其膜化馏装置产生的部分浓水重复利用水处理软化系统再生；在软化器及管式微滤中加入烟气系统中的CO2及Na2SO4加药装置的Na2SO4，采用较低价格药剂和废气，使软化成本大幅降低，解决目前行业遇到的软化问题。
Description
技术领域
本发明涉及火力发电厂全厂废水零排放技术领域，具体涉及一种火力发电厂全厂废水零排放工艺系统及方法。
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火力发电厂全厂废水零排放工艺系统及方法，将火力发电厂全厂废水整体考虑，从软化到浓缩，到蒸发结晶，其膜化馏装置产生的部分浓水重复利用水处理软化系统再生；在软化器及管式微滤中加入烟气系统中的CO2及Na2SO4加药装置的Na2SO4，采用较低价格药剂和废气，使软化成本大幅降低，解决目前行业遇到的软化问题。
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，提供一种火力发电厂全厂废水零排放工艺系统及方法。
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，本发明采用一种火力发电厂全厂废水零排放工艺系统及方法，此系统包括脱硫处理系统、原水调节池、软化器、管式微滤、特种分离膜、膜化馏装置、蒸发结晶干燥器、水处理软化系统、NaOH装置、Ca(OH)2装置、烟气系统、Na2SO4装置、HCl装置；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，为了有效的去除硬度及碱度，向软化器的不同区域中加入苛性钠、石灰、絮凝剂、助凝剂和烟气系统中的CO2，使水的pH值保持在11，出水硬度降为0.5mmol/L；在超级软化器中发生以下反应：
CO2↑+Ca2++H2O─→CaCO3+2H+
Na2SO4+Ca2+─→CaSO4+2Na+
软化器产生的污泥为CaCO3、CaSO4、Mg(OH)2送入脱硫系统，使其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
CaSO4+2H2O─→CaSO4•2H2O
在管式微滤中加入烟气系统中的CO2和Na2SO4装置的Na2SO4，其与不完全反应的钙生成CaSO4及CaCO3，保证硬度去除；
SO4 2-+Ca2+─→CaSO4
CO2↑+Ca2++H2O─→CaCO3+2H+
此工艺系统包括膜化馏装置，采用膜蒸发、分相、电离其产水回收利用，其浓水可进入水处理软化系统，直接与系统内的再生弱酸阳床及钠床；
特种分离膜产生的浓水主要含有SO4 2-、Ca2+、Mg2+，直接返回脱硫系统，在酸性条件下，产生以下反应：
SO4 2-+2H2O+Ca2+─→CaSO4•2H2O
直接生成沉淀物去除SO4 2-和Ca2+，Mg2+直又被带回软化沉淀器，在内部与NaOH产生以下反应:
Mg2++2OH-─→Mg(OH)2
与现有技术相比，本发明的优越性在于：
（1）废水经软化器软化后，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）水处理软化系统再生利用膜化馏装置浓水，节省药剂同时节省部分废水投资和运行处理成本；
（3）向软化器的不同区域中加入苛性钠、石灰、絮凝剂、助凝剂和烟气系统中的CO2，使水的pH值保持在11，出水硬度降为0.5mmol/L；在超级软化器中发生以下反应：
CO2↑+Ca2++H2O─→CaCO3+2H+
Na2SO4+Ca2+─→CaSO4+2Na+
（4）在管式微滤中加入烟气系统中的CO2和Na2SO4装置的Na2SO4，其与不完全反应的钙生成CaSO4及CaCO3，保证硬度去除；
SO4 2-+Ca2+─→CaSO4
CO2↑+Ca2++H2O─→CaCO3+2H+
（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。
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火力发电厂全厂废水零排放工艺系统及方法的结构示意图。图中，(101)脱硫处理系统、(102)原水调节池、(103)软化器、(104)管式微滤、(105)特种分离膜、(106)膜化馏装置、(107)蒸发结晶干燥器、(108)水处理软化系统、(109)NaOH装置、(110)Ca(OH)2装置、(111)烟气系统、(112)Na2SO4装置、(113)HCl装置。
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火力发电厂全厂废水零排放工艺系统及方法，包括脱硫处理系统(101)、原水调节池(102)、软化器(103)、管式微滤(104)、特种分离膜(105)、膜化馏装置(106)、蒸发结晶干燥器(107)、水处理软化系统(108)、废水池(109)、Ca(OH)2装置(110)、烟气系统(111)、Na2SO4装置(112)、HCl装置(113)、NaOH装置(114)。
为了能够实现火力发电厂全厂废水零排放，此系统通过管道与泵使各装置联接，脱硫废水在原水调节池(102)中汇集，通过泵打入软化器(103)，在软化器(103)的不同区域中加入NaOH装置(114)的苛性钠、Ca(OH)2装置(110)的石灰、絮凝剂、助凝剂和烟气系统中(111)的CO2，Na2SO4装置(112)的Na2SO4，使水的pH值保持在11，出水硬度降为0.5mmol/L；在超级软化器中发生以下反应：
CO2↑+Ca2++H2O─→CaCO3+2H+
Na2SO4+Ca2+─→CaSO4+2Na+
软化器(103)产生的污泥为CaCO3、CaSO4、Mg(OH)2送入脱硫系统(101)，使其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
CaSO4+2H2O─→CaSO4•2H2O
经初步软化的脱硫废水由软化器(103)进入管式微滤(104)，在管式微滤中加入烟气系统(111)的CO2和Na2SO4装置(112)的Na2SO4，其与不完全反应的钙生成CaSO4及CaCO3，保证硬度去除；
SO4 2-+Ca2+─→CaSO4
CO2↑+Ca2++H2O─→CaCO3+2H+
经管式微滤(104)软化后由HCl装置(113)加入HCl降低PH后，进入特种分离膜(105)，在特种分离膜(105)中进行分盐，其浓水主要含有SO4 2-、Ca2+、Mg2+，直接返回脱硫系统，在酸性条件下，产生以下反应：
SO4 2-+2H2O+Ca2+─→CaSO4•2H2O
直接生成沉淀物去除SO4 2-和Ca2+，Mg2+直又被带回软化沉淀器，在内部与NaOH产生以下反应:
Mg2++2OH-─→Mg(OH)2
经特种分离膜(105)后进入膜化馏装置(106)，经膜蒸发、分相、电离其产水回收利用，其浓水部分可进入水处理软化系统(108)，直接与系统内的再生弱酸阳床及钠床，剩下的浓水进入蒸发结晶干燥器(107)，在蒸发结晶系统进行完全分离回收。
特种分离膜产生的浓水主要含有SO4 2-、Ca2+、Mg2+，直接返回脱硫系统(101)，在酸性条件下，产生以下反应：
SO4 2-+2H2O+Ca2+─→CaSO4•2H2O
直接生成沉淀物去除SO4 2-和Ca2+，Mg2+直又被带回软化沉淀器，在内部与NaOH产生以下反应:
Mg2++2OH-─→Mg(OH)2
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 (1)
1.一种火力发电厂全厂废水零排放工艺系统及方法，此系统包括脱硫处理系统、原水调节池、软化器、管式微滤、特种分离膜、膜化馏装置、蒸发结晶干燥器、水处理软化系统、NaOH装置、Ca(OH)2装置、烟气系统、Na2SO4装置、HCl装置；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，为了有效的去除硬度及碱度，向软化器的不同区域中加入苛性钠、石灰、絮凝剂、助凝剂和烟气系统中的CO2，使水的pH值保持在11，出水硬度降为0.5mmol/L；在超级软化器中发生以下反应：
CO2↑+Ca2++H2O─→CaCO3+2H+
Na2SO4+Ca2+─→CaSO4+2Na+
软化器产生的污泥为CaCO3、CaSO4、Mg(OH)2送入脱硫系统，使其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
CaSO4+2H2O─→CaSO4•2H2O
在管式微滤中加入烟气系统中的CO2和Na2SO4装置的Na2SO4，其与不完全反应的钙生成CaSO4及CaCO3，保证硬度去除；
SO4 2-+Ca2+─→CaSO4
CO2↑+Ca2++H2O─→CaCO3+2H+
此工艺系统包括膜化馏装置，采用膜蒸发、分相、电离其产水回收利用，其浓水可进入水处理软化系统，直接与系统内的再生弱酸阳床及钠床；
特种分离膜产生的浓水主要含有SO4 2-、Ca2+、Mg2+，直接返回脱硫系统，在酸性条件下，产生以下反应：
SO4 2-+2H2O+Ca2+─→CaSO4•2H2O
直接生成沉淀物去除SO4 2-和Ca2+，Mg2+直又被带回软化沉淀器，在内部与NaOH产生以下反应:
Mg2++2OH-─→Mg(OH)2。
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