CN113603302A - 一种焦化废水减量化的处理方法 - Google Patents
一种焦化废水减量化的处理方法 Download PDFInfo
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- CN113603302A CN113603302A CN202110942791.XA CN202110942791A CN113603302A CN 113603302 A CN113603302 A CN 113603302A CN 202110942791 A CN202110942791 A CN 202110942791A CN 113603302 A CN113603302 A CN 113603302A
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Abstract
本发明涉及工业废水处理技术领域,尤其涉及一种焦化废水减量化的处理方法。焦化废水经过调节池、气浮除油、混凝沉淀、生化均质池、生物滤池、二沉池、UV高级臭氧氧化、超滤、反渗透、化学软化池、砂滤、树脂、调节池、超滤、纳滤、双极膜电渗析工艺处理后,产生的酸碱可用于处理过程的pH调节等工艺回用,既实现了焦化废水的资源化利用,又减少了试剂的外购费用,工艺过程能耗小,成本低,设备简单,易于操作,处理效果稳定,处理过程中选用的水处理药剂,强化了处理效果。
Description
技术领域
本发明涉及工业废水处理技术领域,尤其涉及一种焦化废水减量化的处理方法。
背景技术
焦化废水是有毒有害、难降解的高浓度有机废水,其中有机物以苯酚类化合物居多,约占总有机物的一半,有机物中还包括多环芳香族化合物和含氮、氧、碳的杂环化合物等,无机污染物主要以氨氮、氰化物、硫化物、硫氰化物为主。
目前,国内大多数焦化厂废水处理***采用一级处理和二级处理工艺,但近几年来也开始采用三级处理工艺。一级处理指高浓度废水中污染物的回收利用,包括氨水脱酚、氨水蒸馏、终冷水脱氰等;二级处理主要指酚氰废水无害化处理,以活性污泥法为主,还包括生物强化技术,如生物铁法、投加生长素法、强化曝气法等;三级深度处理是指在生化处理后的排水仍不能达到排放标准时所采用的再次深度净化,其主要工艺有活性炭吸附法、炭—生物膜法、混凝沉淀法和氧化塘法。国外在二级生化处理之前采取了更为复杂的预处理和其他方法控制进入生化***的水质,防止有毒污染物浓度过高,并在生化处理流程之后采取三级净化***。
经深度处理后的废水,在得到大部分初级纯水的同时也产生了较大比例的高盐度浓水,高浓盐水污染物浓度高、含盐量高,直接排放不能达到排放标准,常规的生化处理难度较大,以往浓盐水的处理是利用其进行冲渣,但浓盐水容易对设备管道和喷头造成腐蚀结垢,也有的企业采取蒸发结晶的方法对其进行处理,但这种方法设备投资与运行费用较高。因此,焦化废水的减量化是焦化废水处理的关键。
而且,随着环保要求越来越严格,焦化厂废水零排放的呼声越来越高,焦化废水的减量化处理是当前研究的热点与难点;开发出一种处理效果好,工艺流程简单,运行稳定且费用比较合理的处理方法,将对焦化废水的最终零排和焦化企业的可持续发展具有重要的现实意义。
发明内容
为了克服现有技术的不足,本发明提供一种焦化废水减量化的处理方法。,处理效果好且稳定,最终达到焦化废水的减量化处理及其资源化利用的目的,对钢铁企业实现绿色生态化发展具有重要意义。
为了达到上述目的,本发明采用以下技术方案实现:
一种焦化废水减量化的处理方法,处理对象为钢铁企业焦化蒸氨废水,其中悬浮物80mg/L~100mg/L,氨氮60mg/L~120mg/L,酚400mg/L~500mg/L,石油类40mg/L~50mg/L,COD4000mg/L~5000mg/L,总氰化物30mg/L~80mg/L。
具体包括如下步骤:
1、焦化蒸氨废水首先进入调节池调节水质水量,出水进入气浮除油装置,气浮装置前端采用曝气气浮法,投加20mg/L~30mg/L的阳离子聚丙烯酰胺(CPAM)和30mg/L~50mg/L的ZnSO4,曝气时间20min~30min,静置30min~40min。
2、上清液进入后端高效浅层离子气浮池,在进口处投加40mg/L~50mg/L的混凝剂FeSO4,10mg/L~20mg/L的助凝剂阴离子聚丙烯酰胺(APAM),停留时间设置为10min~15min,充分混合絮凝后,浮渣通过螺旋浮渣收集装置自流至浮渣池,处理水进入末端的沉淀区,采用斜管沉淀法,利用倾斜的平行管分割成一系列浅层沉淀层,沉淀物在各沉淀浅层中相互运动并分离,达到沉淀的目的。
3、沉淀40min~50min后的澄清水重力流出进入生化均质池,均质均量后的废水通过泵提升进入V型生物滤池,滤料采用改性钢渣,粒径50mm~60mm;
4、出水进入二沉池进行泥水分离,停留时间20min~30min;
5、出水通过泵以4m/s~7m/s的流速流经管道式UV,紫外线波长范围为200nm~275nm,之后通过射流泵增压进入臭氧接触塔反应10min~15min。
6、快速反应后的气液混合物从接触塔罐顶通过管道压力流入脱气塔,在脱气塔中气液混合物进行分离,气体向上通过脱气塔顶部的管道收集正压排出,液体向下通过脱气塔底部的管道收集正压流出即为处理后出水。
7、出水进入超滤+反渗透的双膜法处理装置,产水作为工业新水回用,浓盐水进入化学软化池,加入600mg/L~800mg/L氢氧化钙和300mg/L~400mg/L碳酸钠,搅拌10min~20min,以去除浓盐水中的结垢离子。
8、出水进入砂滤罐过滤,采用石英砂作为滤料,从下往上粒径逐渐减小放置,下层滤料粒径1.0mm~1.5mm,上层滤料粒径0.5mm~1.0mm,
9、过滤后出水进入离子交换树脂,此处采用强酸性阳离子树脂与NaCl反应生成的钠型树脂,可与溶液中残余的Ca2+、Mg2+等阳离子进行交换吸附从而将其去除,减少对后续膜法处理的膜污染。
运行一段时间后,用3.0%~3.5%的NaCl溶液对其进行再生,再生废水回流至调节池,离子交换树脂产水进入超滤***,进入膜单元之前调节pH值6.0~6.6,超滤可去除废水中部分悬浮物和胶体,超滤产水SDI值≤3.0,满足纳滤膜的进水要求,纳滤***回收率95~98%。
10、超滤和纳滤膜的反洗水回流至前端调节池,纳滤产水进入双极膜电渗析***,双极膜装置由两张双极膜、两张阴离子交换膜和一张阳离子交换膜构成,分成4隔室,将水中的盐转化为盐酸和氢氧化钠,从而实现焦化废水的减量化与资源化利用。
与现有方法相比,本发明的有益效果是:
本发明提供了一种焦化废水减量化的处理方法,且产生的酸碱可用于处理过程的pH调节等工艺回用,既实现了焦化废水的资源化利用,又减少了试剂的外购费用,工艺过程能耗小,成本低,设备简单,易于操作,处理效果稳定,处理过程中选用的水处理药剂,强化了处理效果。实现焦化废水的减量化与资源化利用,将对焦化废水的最终零排和焦化企业的可持续发展具有重要的现实意义。
附图说明
图1是本发明工艺流程图。
具体实施方式
本发明公开了一种焦化废水减量化的处理方法。本领域技术人员可以借鉴本文内容,适当改进工艺参数实现。特别需要指出的是,所有类似的替换和改动对本领域技术人员来说是显而易见的,它们都被视为包括在本发明。本发明的方法及应用已经通过较佳实施例进行了描述,相关人员明显能在不脱离本发明内容、精神和范围内对本文所述的方法和应用进行改动或适当变更与组合,来实现和应用本发明技术。
本发明处理对象为钢铁企业焦化蒸氨废水,其中悬浮物80mg/L~100mg/L,氨氮60mg/L~120mg/L,酚400mg/L~500mg/L,石油类40mg/L~50mg/L,COD4000mg/L~5000mg/L,总氰化物30mg/L~80mg/L。
以下结合图1说明介绍本发明的最佳实施方式:
实施例1:
一种焦化废水减量化的处理方法,具体包括如下步骤:
1、焦化蒸氨废水首先进入调节池调节水质水量,出水进入气浮除油装置,气浮装置前端采用曝气气浮法,投加20mg/L的阳离子聚丙烯酰胺(CPAM)和30mg/L的ZnSO4,曝气时间20min,静置30min。
2、上清液进入后端高效浅层离子气浮池,在进口处投加混凝剂40mg/L的FeSO4,助凝剂10mg/L的阴离子聚丙烯酰胺(APAM),停留时间设置为10min,充分混合絮凝后,浮渣通过螺旋浮渣收集装置自流至浮渣池,处理水进入末端的沉淀区,采用斜管沉淀法,利用倾斜的平行管分割成一系列浅层沉淀层,沉淀物在各沉淀浅层中相互运动并分离,达到沉淀的目的。
3、沉淀40min后的澄清水重力流出进入生化均质池,均质均量后的废水通过泵提升进入V型生物滤池,滤料采用改性钢渣,粒径50mm。
4、出水进入二沉池进行泥水分离,停留时间设置为20min。
5、出水通过泵以4m/s的流速流经管道式UV,紫外线波长范围为275nm,之后通过射流泵增压进入臭氧接触塔反应10min。
6、快速反应后的气液混合物从接触塔罐顶通过管道压力流入脱气塔,在脱气塔中气液混合物进行分离,气体向上通过脱气塔顶部的管道收集正压排出,液体向下通过脱气塔底部的管道收集正压流出即为处理后出水。
7、出水进入超滤+反渗透的双膜法处理装置,产水作为工业新水回用,浓盐水进入化学软化池,加入600mg/L氢氧化钙和300mg/L碳酸钠,搅拌10min,以去除浓盐水中的结垢离子。
8、出水进入砂滤罐过滤,采用石英砂作为滤料,从下往上粒径逐渐减小放置,下层滤料粒径1.0mm,上层滤料粒径0.5mm,进一步去除悬浮物。
9、过滤后出水进入离子交换树脂,此处采用强酸性阳离子树脂与NaCl反应生成的钠型树脂,可与溶液中残余的Ca2+、Mg2+等阳离子进行交换吸附从而将其去除,减少对后续膜法处理的膜污染。运行一段时间后,用3.0%的NaCl溶液对其进行再生,再生废水回流至调节池,离子交换树脂产水进入超滤***,进入膜单元之前调节pH值6.0,超滤可去除废水中部分悬浮物和胶体,超滤产水SDI值为3.0,满足纳滤膜的进水要求,纳滤***回收率95%。
10、超滤和纳滤膜的反洗水回流至前端调节池。纳滤产水进入双极膜电渗析***,双极膜装置由两张双极膜、两张阴离子交换膜和一张阳离子交换膜构成,分成4隔室,将水中的盐转化为盐酸和氢氧化钠,从而实现焦化废水的减量化与资源化利用。
实施例2:
一种焦化废水减量化的处理方法,具体包括如下步骤:
1、焦化蒸氨废水首先进入调节池调节水质水量,出水进入气浮除油装置,气浮装置前端采用曝气气浮法,投加25mg/L的阳离子聚丙烯酰胺(CPAM)和40mg/L的ZnSO4,曝气时间25min,静置35min。
2、上清液进入后端高效浅层离子气浮池,在进口处投加混凝剂45mg/L的FeSO4,助凝剂15mg/L的阴离子聚丙烯酰胺(APAM),停留时间设置为13min,充分混合絮凝后,浮渣通过螺旋浮渣收集装置自流至浮渣池,处理水进入末端的沉淀区,采用斜管沉淀法,利用倾斜的平行管分割成一系列浅层沉淀层,沉淀物在各沉淀浅层中相互运动并分离,达到沉淀的目的。
3、沉淀45min后的澄清水重力流出进入生化均质池,均质均量后的废水通过泵提升进入V型生物滤池,滤料采用改性钢渣,粒径55mm。
4、出水进入二沉池进行泥水分离,停留时间设置为25min。
5、出水通过泵以5m/s的流速流经管道式UV,紫外线波长范围为275nm,之后通过射流泵增压进入臭氧接触塔反应13min。
6、快速反应后的气液混合物从接触塔罐顶通过管道压力流入脱气塔,在脱气塔中气液混合物进行分离,气体向上通过脱气塔顶部的管道收集正压排出,液体向下通过脱气塔底部的管道收集正压流出即为处理后出水。
7、出水进入超滤+反渗透的双膜法处理装置,产水作为工业新水回用,浓盐水进入化学软化池,加入700mg/L氢氧化钙和350mg/L碳酸钠,搅拌15min,以去除浓盐水中的结垢离子。
8、出水进入砂滤罐过滤,采用石英砂作为滤料,从下往上粒径逐渐减小放置,下层滤料粒径1.3mm,上层滤料粒径0.8mm,进一步去除悬浮物。
9、过滤后出水进入离子交换树脂,此处采用强酸性阳离子树脂与NaCl反应生成的钠型树脂,可与溶液中残余的Ca2+、Mg2+等阳离子进行交换吸附从而将其去除,减少对后续膜法处理的膜污染,运行一段时间后,用3.2%的NaCl溶液对其进行再生,再生废水回流至调节池,离子交换树脂产水进入超滤***,进入膜单元之前调节pH值6.3,超滤可去除废水中部分悬浮物和胶体,超滤产水SDI值为2.8,满足纳滤膜的进水要求,纳滤***回收率96%。
10、超滤和纳滤膜的反洗水回流至前端调节池。纳滤产水进入双极膜电渗析***,双极膜装置由两张双极膜、两张阴离子交换膜和一张阳离子交换膜构成,分成4隔室,将水中的盐转化为盐酸和氢氧化钠,从而实现焦化废水的减量化与资源化利用。
实施例3:
一种焦化废水减量化的处理方法,具体包括如下步骤:
1、焦化蒸氨废水首先进入调节池调节水质水量,出水进入气浮除油装置,气浮装置前端采用曝气气浮法,投加30mg/L的阳离子聚丙烯酰胺(CPAM)和50mg/L的ZnSO4,曝气时间30min,静置40min。
2、上清液进入后端高效浅层离子气浮池,在进口处投加混凝剂50mg/L的FeSO4,助凝剂20mg/L的阴离子聚丙烯酰胺(APAM),停留时间设置为15min,充分混合絮凝后,浮渣通过螺旋浮渣收集装置自流至浮渣池,处理水进入末端的沉淀区,采用斜管沉淀法,利用倾斜的平行管分割成一系列浅层沉淀层,沉淀物在各沉淀浅层中相互运动并分离,达到沉淀的目的。
3、沉淀50min后的澄清水重力流出进入生化均质池,均质均量后的废水通过泵提升进入V型生物滤池,滤料采用改性钢渣,粒径60mm。
4、出水进入二沉池进行泥水分离,停留时间设置为30min。
5、出水通过泵以7m/s的流速流经管道式UV,紫外线波长范围为275nm,之后通过射流泵增压进入臭氧接触塔反应15min。
6、快速反应后的气液混合物从接触塔罐顶通过管道压力流入脱气塔,在脱气塔中气液混合物进行分离,气体向上通过脱气塔顶部的管道收集正压排出,液体向下通过脱气塔底部的管道收集正压流出即为处理后出水。
7、出水进入超滤+反渗透的双膜法处理装置,产水作为工业新水回用,浓盐水进入化学软化池,加入800mg/L氢氧化钙和400mg/L碳酸钠,搅拌20min,以去除浓盐水中的结垢离子。
8、出水进入砂滤罐过滤,采用石英砂作为滤料,从下往上粒径逐渐减小放置,下层滤料粒径1.5mm,上层滤料粒径1.0mm,进一步去除悬浮物。
9、过滤后出水进入离子交换树脂,此处采用强酸性阳离子树脂与NaCl反应生成的钠型树脂,可与溶液中残余的Ca2+、Mg2+等阳离子进行交换吸附从而将其去除,减少对后续膜法处理的膜污染,运行一段时间后,用3.5%的NaCl溶液对其进行再生,再生废水回流至调节池,离子交换树脂产水进入超滤***,进入膜单元之前调节pH值6.6,超滤可去除废水中部分悬浮物和胶体,超滤产水SDI值为2.5,满足纳滤膜的进水要求,纳滤***回收率98%。
10、超滤和纳滤膜的反洗水回流至前端调节池。纳滤产水进入双极膜电渗析***,双极膜装置由两张双极膜、两张阴离子交换膜和一张阳离子交换膜构成,分成4隔室,将水中的盐转化为盐酸和氢氧化钠,从而实现焦化废水的减量化与资源化利用。
本发明产生的酸碱可用于处理过程的pH调节等工艺回用,既实现了焦化废水的资源化利用,又减少了试剂的外购费用,工艺过程能耗小,成本低,设备简单,易于操作,处理效果稳定,处理过程中选用的水处理药剂,强化了处理效果。实现焦化废水的减量化与资源化利用,将对焦化废水的最终零排和焦化企业的可持续发展具有重要的现实意义。
以上所述,仅为本发明较佳的具体实施方式,但本发明的保护范围并不局限于此,任何熟悉本技术领域的技术人员在本发明揭露的技术范围内,根据本发明的技术方案及其发明构思加以等同替换或改变,都应涵盖在本发明的保护范围之内。
Claims (7)
1.一种焦化废水减量化的处理方法,其特征在于,所述焦化废水为钢铁企业焦化蒸氨废水,其中悬浮物80mg/L~100mg/L,氨氮60mg/L~120mg/L,酚400mg/L~500mg/L,石油类40mg/L~50mg/L,COD4000mg/L~5000mg/L,总氰化物30mg/L~80mg/L;具体包括如下步骤:
1)首先将焦化蒸氨废水送入调节池调节水质水量,出水送入气浮除油装置,气浮装置前端采用曝气气浮法,投加20mg/L~30mg/L的阳离子聚丙烯酰胺和30mg/L~50mg/L的ZnSO4,曝气20min~30min,静置30min~40min;
2上清液进入后端高效浅层离子气浮池,在进口处投加混凝剂与助凝剂,停留10min~15min,充分混合絮凝后,浮渣通过螺旋浮渣收集装置自流至浮渣池,处理水进入末端的沉淀区;
3)沉淀40min~50min后的澄清水重力流出进入生化均质池,均质均量后的废水通过泵提升进入V型生物滤池过滤;
4)出水进入二沉池进行泥水分离,停留20min~30min;
5)出水通过泵以4m/s~7m/s的流速流经管道式UV,紫外线波长范围为200nm~275nm,之后通过射流泵增压进入臭氧接触塔反应10min~15min;
6)反应后的气液混合物从接触塔罐顶通过管道压力流入脱气塔,在脱气塔中气液混合物进行分离,气体向上通过脱气塔顶部的管道收集正压排出,液体向下通过脱气塔底部的管道收集正压流出即为处理后出水;
7)出水进入超滤+反渗透的双膜法处理装置,产水作为工业新水回用,浓盐水进入化学软化池,加入600mg/L~800mg/L氢氧化钙和300mg/L~400mg/L碳酸钠,搅拌10min~20min,以去除浓盐水中的结垢离子;
8)出水进入砂滤罐过滤,采用石英砂作为滤料,从下往上粒径逐渐减小放置,下层滤料粒径1.0mm~1.5mm,上层滤料粒径0.5mm~1.0mm,进一步去除悬浮物;
9)过滤后出水进入离子交换树脂,用3.0%~3.5%的NaCl溶液对其进行再生,再生废水回流至调节池,离子交换树脂产水进入超滤***,进入膜单元之前调节pH值至6.0~6.6,超滤产水SDI值≤3.0,纳滤***回收率95~98%;
10)超滤和纳滤膜的反洗水回流至前端调节池;纳滤产水进入双极膜电渗析***,将水中的盐转化为盐酸和氢氧化钠。
2.根据权利要求1所述的一种焦化废水减量化的处理方法,其特征在于,所述步骤2)混凝剂为40mg/L~50mg/L的FeSO4,助凝剂为10mg/L~20mg/L的阴离子聚丙烯酰胺。
3.根据权利要求1所述的一种焦化废水减量化的处理方法,其特征在于,所述步骤2)沉淀区采用斜管沉淀法,利用倾斜的平行管分割成一系列浅层沉淀层,沉淀物在各沉淀浅层中相互运动并分离,达到沉淀的目的。
4.根据权利要求1所述的一种焦化废水减量化的处理方法,其特征在于,所述步骤3)V型生物滤池滤料采用改性钢渣,粒径50mm~60mm。
5.根据权利要求1所述的一种焦化废水减量化的处理方法,其特征在于,所述步骤8)砂滤罐采用石英砂作为滤料,从下往上粒径逐渐减小放置,下层滤料粒径1.0mm~1.5mm,上层滤料粒径0.5mm~1.0mm。
6.根据权利要求1所述的一种焦化废水减量化的处理方法,其特征在于,所述步骤9)离子交换树脂采用强酸性阳离子树脂与NaCl反应生成的钠型树脂。
7.根据权利要求1所述的一种焦化废水减量化的处理方法,其特征在于,所述步骤10)双极膜电渗析***的双极膜装置由两张双极膜、两张阴离子交换膜和一张阳离子交换膜构成,分成4隔室。
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