CN101723548B - 一种焦化废水回用处理系统 - Google Patents
一种焦化废水回用处理系统 Download PDFInfo
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- CN101723548B CN101723548B CN2009102001934A CN200910200193A CN101723548B CN 101723548 B CN101723548 B CN 101723548B CN 2009102001934 A CN2009102001934 A CN 2009102001934A CN 200910200193 A CN200910200193 A CN 200910200193A CN 101723548 B CN101723548 B CN 101723548B
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- reverse osmosis
- pond
- filter
- water
- connects
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- 239000002351 wastewater Substances 0.000 title claims abstract description 37
- 238000004939 coking Methods 0.000 title claims abstract description 29
- 238000004064 recycling Methods 0.000 title claims abstract description 17
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 147
- 239000011901 water Substances 0.000 claims abstract description 120
- 238000006243 chemical reactions Methods 0.000 claims abstract description 38
- 238000007254 oxidation reactions Methods 0.000 claims abstract description 32
- 230000003647 oxidation Effects 0.000 claims abstract description 31
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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Abstract
本发明涉及一种焦化废水回用处理系统，包括电絮凝气浮池、电絮凝气浮刮渣机、电催化氧化池、膜生物反应池、膜生物反应器出水泵、多介质过滤器、活性炭过滤器、保安过滤器、反渗透高压泵、反渗透装置、反渗透产水池、反渗透产水输送泵、过滤器反洗水池、过滤器反洗泵、反渗透清洗水池、反渗透清洗泵、反渗透浓水池、反渗透浓水输送泵以及管道混合器。电絮凝气浮池内设置电絮凝电极、电气浮电极。电催化氧化池内设置电催化氧化电极。膜生物反应池内设置膜生物反应器。采用本发明的处理系统，处理效果稳定、生产运行成本低、操作运行简便，能处理采用生化沉淀池出水，避开常规生化处理后的物化处理段，避免大量使用药剂，减少系统污泥处理量，降低废水处理运行成本。
Description
一种焦化废水回用处理系统
技术领域
[0001] 本发明属于水处理领域，具体地说是涉及一种焦化废水回用处理系统。 背景技术
[0002] 废水回用是企业节能减排的实施手段。由于焦化废水有机物种类多，处理难度大， 人们对焦化废水回用的关注较少。目前已实施的废水回用技术偏简单化，如钢铁行业大多采取预处理及生化处理后送煤场喷煤、炼钢除尘以及焦炉熄焦等，造成污染物转移，还可能影响钢铁产品的质量。
[0003] 根据2009年1月1日起实施的《焦化行业准入条件》对焦炉建设提出的要求：钢铁企业新建焦炉要同步配套建设干熄焦装置并配套建设相应的除尘装置。湿法熄焦工艺将逐步被干法熄焦代替，焦化废水回用至焦炉熄焦也将无法实施。同时，国家已将“焦化废水达标排放与回用技术”列入“国家重大技术装备研制和重大产业技术研发专项规划”，这进一步说明了废水回用的迫切性。
[0004] 国内的焦化废水回用目前处于探索阶段，各家企业对废水回用单元性的技术核查分析做的很多，系统、全面地分析研究及工业化应用则很少。如专利文献200710068327. 2， 采用生化出水经过氧化絮凝+气浮+阴阳离子交换+反渗透制备工业用水；专利文献 200810022437. X，采用焦化废水原水经除油处理后经过多介质过滤+保安过滤+ —级反渗透+ 二级反渗透；均属于近年来对焦化废水回用研究较为详尽、但未进行实际应用的例子。
[0005] 因此，加大对焦化废水回用的研究力度，制定具有针对性的处理方案，探索针对焦化废水回用的策略与技术并应用于工业生产，对实现企业的可持续性发展和节能减排、提高综合竞争力具有重要意义。
发明内容
[0006] 为了解决上述现有技术所存在的问题，本发明的目的是提供一种焦化废水回用处理系统，采用该处理系统，处理效果稳定，生产运行成本较低，操作运行简便。
[0007] 本发明的技术解决方案如下：
[0008] 一种焦化废水回用处理系统，包括电絮凝气浮池、电絮凝电极、电气浮电极、电絮凝气浮刮渣机、电催化氧化池、电催化氧化电极、膜生物反应池、膜生物反应器、膜生物反应器出水泵、多介质过滤器、活性炭过滤器、保安过滤器、反渗透高压泵、第一段反渗透装置、 第二段反渗透装置、反渗透产水池、反渗透产水输送泵、过滤器反洗水池、过滤器反洗泵、反渗透清洗水池、反渗透清洗泵、反渗透浓水池、反渗透浓水输送泵、第一管道混合器、第二管道混合器以及第三管道混合器；
[0009] 所述电絮凝气浮池内设置电絮凝电极、电气浮电极以及电絮凝气浮刮渣机，电絮凝气浮池上部进口接反渗透浓水泵来水管，电絮凝气浮池下部出口回接反渗透浓水泵来水管，电絮凝气浮池出口连接电催化氧化池；
[0010] 所述电催化氧化池内设置电催化氧化电极，电催化氧化池出口连接膜生物反应池；
[0011] 所述膜生物反应池内设置膜生物反应器，膜生物反应池入口接生化沉淀池来水， 膜生物反应器通过膜生物反应池出口连接膜生物反应器出水泵，再连接多介质过滤器；
[0012] 所述多介质过滤器入口通过第一管道混合器连接助凝剂管道、絮凝剂管道以及氧化剂管道，多介质过滤器出口通过第二管道混合器连接活性炭过滤器；
[0013] 所述活性炭过滤器入口通过第二管道混合器连接还原剂管道，活性炭过滤器出口通过第三管道混合器连接保安过滤器；
[0014] 所述保安过滤器入口通过第三管道混合器连接阻垢剂管道，保安过滤器出口通过反渗透高压泵连接第一段反渗透装置；
[0015] 所述反渗透清洗水池入口接工业用水管网，反渗透清洗水池出口通过反渗透清洗泵连接第一段反渗透装置和第二段反渗透装置；
[0016] 所述第一段反渗透装置出口连接第二段反渗透装置，第一段反渗透装置出口还连接反渗透产水池；
[0017] 所述反渗透产水池通过反渗透产水输送泵连接过滤器反洗水池和工业用水管网；
[0018] 所述第二段反渗透装置出口连接反渗透产水池，第二段反渗透装置出口还连接反渗透浓水池；
[0019] 所述反渗透浓水池通过反渗透浓水输送泵连接反渗透浓水处理装置；
[0020] 所述膜生物反应池、多介质过滤器和活性炭过滤器分别接低压空气管道；
[0021 ] 所述过滤器反洗水池入口接工业用水管网，过滤器反洗水池出口通过过滤器反洗泵连接多介质过滤器及活性炭过滤器，过滤器反冲洗水接至废水站地坑。
[0022] 所述膜生物反应池入口还接清洗剂管道。
[0023] 所述膜生物反应池内装有连续空气曝气装置。
[0024] 所述膜生物反应器采用内置有机板式膜的形式，采用改性纳米材料制成，为微滤膜，膜孔径0. lym。
[0025] 所述保安过滤器的滤芯为可更换卡式PP滤芯。
[0026] 本发明由于采用了以上技术方案，使之与现有技术相比，具有以下优势：
[0027] 采用本发明的处理系统，处理效果稳定、生产运行成本低、操作运行简便，能处理采用生化沉淀池出水，避开常规生化处理后的物化处理段，避免大量使用药剂，减少系统污泥处理量，降低废水处理运行成本。
附图说明
[0028] 附图是本发明的一种焦化废水回用处理系统的结构示意图。
[0029] 1为电絮凝气浮池，2为电絮凝电极，3为电气浮电极，4为电絮凝气浮刮渣机，5为电催化氧化池，6为电催化氧化电极，7为膜生物反应池，8为膜生物反应器，9为膜生物反应器出水泵，10为多介质过滤器，11为活性炭过滤器，12为保安过滤器，13为反渗透高压泵， 14为第一段反渗透装置，15为第二段反渗透装置，16为反渗透产水池，17为反渗透产水输送泵，18为过滤器反洗水池，19为过滤器反洗泵，20为反渗透清洗水池，21为反渗透清洗泵，22为反渗透浓水池，23为反渗透浓水输送泵，24为第一管道混合器，25为第二管道混合器26为第三管道混合器。 具体实施方式
[0030] 下面结合附图和实施例对本发明作详细说明。
[0031] 参看附图，本发明是一种焦化废水回用处理系统，它包括电絮凝气浮池1、电絮凝电极2、电气浮电极3、电絮凝气浮刮渣机4、电催化氧化池5、电催化氧化电极6、膜生物反应池7、膜生物反应器8、膜生物反应器出水泵9、多介质过滤器10、活性炭过滤器11、保安过滤器12、反渗透高压泵13、第一段反渗透装置14、第二段反渗透装置15、反渗透产水池16、反渗透产水输送泵17、过滤器反洗水池18、过滤器反洗泵19、反渗透清洗水池20、反渗透清洗泵21、反渗透浓水池22、反渗透浓水输送泵23第一管道混合器M、第二管道混合器25以及第三管道混合器26。
[0032] 电絮凝气浮池1内设置电絮凝电极2、电气浮电极3以及电絮凝气浮刮渣机4。电絮凝气浮池1上部进口接反渗透浓水泵来水管，电絮凝气浮池1下部出口回接反渗透浓水泵来水管。电絮凝气浮池1出口连接电催化氧化池5。
[0033] 电催化氧化池5内设置电催化氧化电极6，电催化氧化池5出口连接膜生物反应池 7。
[0034] 膜生物反应池7内设置膜生物反应器8。膜生物反应池7入口接生化沉淀池来水。 膜生物反应器8通过膜生物反应池7出口连接膜生物反应器出水泵9，膜生物反应出水泵9 通过管道连接多介质过滤器10。膜生物反应池7入口还接清洗剂管道。膜生物反应池7内装有连续空气曝气装置。膜生物反应器8采用内置有机板式膜的形式，采用改性纳米材料制成，为微滤膜，膜孔径0.1 μ m。
[0035] 多介质过滤器10入口通过第一管道混合器M连接助凝剂管道、絮凝剂管道以及氧化剂管道，第一管道混合器M安装在膜生物反应器出水泵9与多介质过滤器10之间的连接管道上。多介质过滤器10出口通过第二管道混合器25连接活性炭过滤器11。
[0036] 活性炭过滤器11入口通过第二管道混合器25连接还原剂管道，第二管道混合器 25安装在多介质过滤器10与活性炭过滤器11之间的连接管道上。活性炭过滤器11出口通过第三管道混合器沈连接保安过滤器12。
[0037] 保安过滤器12入口通过第三管道混合器沈连接阻垢剂管道，第三管道混合器沈安装在活性炭过滤器11与保安过滤器12之间的连接管道上。保安过滤器12出口通过反渗透高压泵13连接第一段反渗透装置14。保安过滤器12的滤芯为可更换卡式PP滤芯。
[0038] 反渗透清洗水池20入口接工业用水管网，反渗透清洗水池20出口通过反渗透清洗泵21连接第一段反渗透装置14和第二段反渗透装置15。
[0039] 第一段反渗透装置14出口连接第二段反渗透装置15，第一段反渗透装置14出口还连接反渗透产水池16。第二段反渗透装置15出口连接反渗透产水池16，第二段反渗透装置15出口还连接反渗透浓水池22。
[0040] 反渗透产水池16通过反渗透产水输送泵17连接过滤器反洗水池和工业用水管网。
[0041] 反渗透浓水池22通过反渗透浓水输送泵23连接反渗透浓水处理装置。
[0042] 膜生物反应池7、多介质过滤器10和活性炭过滤器11分别接低压空气管道。
5[0043] 过滤器反洗水池18入口接工业用水管网，过滤器反洗水池18出口通过过滤器反洗泵19连接多介质过滤器10及活性炭过滤器11，过滤器反冲洗水接至废水站地坑。
[0044] 本发明采用电絮凝气浮，将电絮凝与电气浮组合在一个池体内，实现了电絮凝与电气浮的协同，可有效减少溶性电极的消耗并提高处理效果，优选电絮凝气浮表面负荷 δπι3/!!!2·!!，水力停留时间为15min。电絮凝、电气浮分别采用溶性1½/!½板式电极及不溶性 Ti/DSA网式电极，与水流同向布置。电气浮采用反转电极控制程序，电极采用硅整流柜使交流电变直流，运行每Im3焦化废水优选电耗：电流13A，电压6V。
[0045] 本发明采用电催化氧化，控制电催化氧化反应处于电化学转换阶段，减低运行能耗，即把废水中的部分有毒物质转变为无毒物质，或把不可生物降解的有机物转化为具有可生物降解的有机物（如发生水解酸化反应），以提高废水的可生化性。优选电催化氧化水力停留时间为30min。采用不溶性Ti/DSA网式电极，与水流同向布置，电气浮采用反转电极控制程序，电极采用硅整流柜使交流电变直流，运行每Im3焦化废水优选电耗：电流300A， 电压24V。
[0046] 本发明采用电絮凝气浮及电催化氧化后，出水水质如下：CODcr ( 80mg/l、 T-CN 彡 lmg/l、r 彡 60mg/l、油份彡 lmg/l、N(V 彡 150mg/l、SS 彡 10mg/l、电导率彡 6000 μ m/ cm。
[0047] 本发明采用膜生物反应器，能进一步降低生化处理出水中的有机物、油分、悬浮物等污染物。膜生物反应器采用内置有机板式膜的形式，采用改性纳米材料制成，为微滤膜， 膜孔径0. 1 μ m，这种形式的膜生物反应器使固液分离更加彻底，同时防止废水中油份污染膜表面，代替传统的二沉池，保证出水流量稳定，同时膜生物反应池内设置充分的停留时间，使有机物在连续曝气的条件下进行再次生化降解，起到二级好氧的作用。池内连续曝气，供气量13L/min，膜生物反应池水力停留时间4h，采用氯酸钠定期清洗，清洗周期6个月。
[0048] 膜生物反应器出水进入多介质过滤器、活性炭过滤器及保安过滤器，用于除去水中的浊度及部分有机物、游离氯，去除水中异味、色度和臭味，可有效防止膜污染。保安过滤器选用更换卡式PP滤芯，优选过滤精度5 μ m，用于拦截异常情况下的大颗粒物质，以保证后续反渗透膜的稳定运行，滤芯定期更换，更换周期为60天。多介质过滤器及活性炭过滤器前分别设置强氧化剂、絮凝剂、助凝剂、还原剂及阻垢剂投加装置。
[0049] 保安过滤器出水设高压泵，在背压1. 4MPa的条件下进入反渗透装置，小部分污染物质可选择性地透过，拦截绝大部分可溶性盐分、胶体、有机物及微生物，随着装置运行时间不断增加，被截留的水溶液杂质不断浓缩，以浓水形式排放。反渗透膜组件采用抗污染膜，采用一级两段组合，排列方式2 ： 1，具体方法是高压泵将过滤器来水打入一段反渗透， 一段浓水利用出水余压进入二段反渗透进行再次浓缩，一段及二段产水直接进工业用水管网。反渗透产生的浓水送至浓水处理装置单独处理后达标外排。系统除盐率95%，得水率 70%，运行温度25 °C。
[0050] 根据反渗透膜的运行污染情况，需定期配置一定浓度的特定的清洗溶液进行清洗，以恢复膜的特性。清洗剂的选择与反渗透膜配套，清洗结束后再对膜进行冲洗，冲洗的作用是用反渗透产水置换停机后膜中滞留的浓水，防止浓水侧亚稳态的结垢物质出现结垢。还原剂用于还原多余的氧化剂，保护反渗透膜，同时防止反渗透膜内细菌繁殖，还原剂选用亚硫酸氢纳。
[0051] 本实施例对焦化废水进行处理后回用。首先，焦化废水经生化沉淀后进入电絮凝气浮池1，电絮凝气浮池1内设置电絮凝电极2和电气浮电极3，通入直流电反应15min后， 电絮凝阳极产生多价金属离子如狗2+、阴极电解H2O产生·0Η等与废水中的T-CN、C0D及油份等污染物发生氧化、絮凝和吸附反应，形成(Fe (CN)) 6络合物及絮凝浮渣等污染物，被电气浮产生的微气泡粘附而上浮到液面，再由电絮凝气浮刮渣机4刮出，实现固液分离的效果。
[0052] 电絮凝气浮溢流出水重力自流至电催化氧化池5，电催化氧化池5内设置电催化氧化电极6，通入直流电反应30min后，阳极电解水产生的活性氧氧化水中的有机物等污染物，把不可生物降解的有机物转化为具有可生物降解的有机物，出水重力自流至膜生物反应池7，膜生物反应池7内设连续空气曝气装置，对膜生物反应器8进行不断冲刷，防止堵塞
[0053] 同时，废水在池停留并充分反应降解有机物，在膜生物反应器出水泵9的抽吸作用下，废水经过膜生物反应器8进行泥水分离，并由膜生物反应器出水泵9提升至多介质过滤器10，多介质过滤器10出水利用余压进入活性炭过滤器11，降低废水中的浊度及部分有机物、游离氯，去除水中异味、色度和臭味，防止后续反渗透膜的污染。
[0054] 为防止被截留的污染物沉积在过滤器滤料表面，影响过滤能力和过滤器的产水质量，过滤器需定期反冲洗，过滤器设置定期自动反冲洗装置。反冲洗时，过滤器反洗泵19 从过滤器反洗水池18中抽水分别送入多介质过滤器10和活性炭过滤器11，反冲洗时间约 3〜8min，反冲洗水排至废水站地坑。
[0055] 过滤器出水经过保安过滤器12，保安过滤器12出水用反渗透高压泵13提升至反渗透装置14、15，反渗透装置设一级两段，反渗透高压泵13出口压力为1. 4MPa，泵出水进入第一段反渗透装置14，第一段反渗透装置14产生的浓水利用出水余压进入第二段反渗透装置15，整套系统除盐率约95%，得水率约70%。
[0056] 废水经过反渗透装置14、15后，水中绝大部分的可溶性盐分、胶体、有机物及微生物被拦截，出水进入反渗透产水池16，用反渗透产水输送泵17输送至工业用水管网，同时， 可以根据需要将反渗透产水用反渗透产水输送泵17送至过滤器反洗水池18。随着装置运行时间不断增加，被截留的水溶液杂质不断浓缩，最后以浓水的形式排放至反渗透浓水池 22。再用反渗透浓水输送泵23送至装置单独处理，达标后外排。
[0057] 反渗透装置需根据运行情况定期清洗，清洗时，将清洗药剂与清水同时加入反渗透清洗水池20，选择的清洗剂与反渗透膜配套，混合均勻后用反渗透清洗泵21送入第一段反渗透装置14及第二段反渗透装置15，清洗完成后再通入清水冲洗，清洗及冲洗水排至废水站地坑。
[0058] 多介质过滤器10及活性炭过滤器11前分别投加强氧化剂、絮凝剂、助凝剂、还原剂及阻垢剂，氧化剂、絮凝剂及助凝剂用于杀灭原水中的细菌及藻类，加快混凝沉淀，还原剂用于分解多余的氧化剂，阻垢剂用于防止水中离子结垢，保护反渗透膜的寿命。上述药剂均采用管道混合器M、25J6混合均勻后投加。
[0059] 本发明的处理系统适用于焦化废水处理，处理前后数据见下表。
[0060] 焦化废水回用处理前后数据表[0061]
[0062] 综上可知，采用本发明的处理系统，处理效果稳定，生产运行成本低，操作运行简便，能处理采用生化沉淀池出水，避开常规生化处理后的物化处理段，避免大量使用药剂， 减少系统污泥处理量，降低废水处理运行成本。
[0063] 当然，本技术领域内的一般技术人员应当认识到，上述实施例仅是用来说明本发明，而并非用作对本发明的限定，只要在本发明的实质精神范围内，对上述实施例的变换、 变型都将落在本发明权利要求的范围内。
Claims (5)
1. 一种焦化废水回用处理系统，其特征在于，包括电絮凝气浮池、电絮凝电极、电气浮电极、电絮凝气浮刮渣机、电催化氧化池、电催化氧化电极、膜生物反应池、膜生物反应器、 膜生物反应器出水泵、多介质过滤器、活性炭过滤器、保安过滤器、反渗透高压泵、第一段反渗透装置、第二段反渗透装置、反渗透产水池、反渗透产水输送泵、过滤器反洗水池、过滤器反洗泵、反渗透清洗水池、反渗透清洗泵、反渗透浓水池、反渗透浓水输送泵、第一管道混合器、第二管道混合器以及第三管道混合器；所述电絮凝气浮池内设置电絮凝电极、电气浮电极以及电絮凝气浮刮渣机，电絮凝、电气浮分别采用溶性1¾/!½板式电极及不溶性Ti/DSA网式电极，与水流同向布置；所述电絮凝气浮池上部进口接反渗透浓水输送泵来水管，电絮凝气浮池下部出口回接反渗透浓水输送泵来水管，电絮凝气浮池出口连接电催化氧化池；所述电催化氧化池内设置电催化氧化电极，电催化氧化池出口连接膜生物反应池； 所述膜生物反应池内设置膜生物反应器，膜生物反应池入口接生化沉淀池来水，膜生物反应器通过膜生物反应池出口连接膜生物反应器出水泵，再连接多介质过滤器；所述多介质过滤器入口通过第一管道混合器连接助凝剂管道、絮凝剂管道以及氧化剂管道，多介质过滤器出口通过第二管道混合器连接活性炭过滤器；所述活性炭过滤器入口通过第二管道混合器连接还原剂管道，活性炭过滤器出口通过第三管道混合器连接保安过滤器；所述保安过滤器入口通过第三管道混合器连接阻垢剂管道，保安过滤器出口通过反渗透高压泵连接第一段反渗透装置；所述反渗透清洗水池入口接工业用水管网，反渗透清洗水池出口通过反渗透清洗泵连接第一段反渗透装置和第二段反渗透装置；所述第一段反渗透装置出口连接第二段反渗透装置，第一段反渗透装置出口还连接反渗透产水池；所述反渗透产水池通过反渗透产水输送泵连接过滤器反洗水池和工业用水管网； 所述第二段反渗透装置出口连接反渗透产水池，第二段反渗透装置出口还连接反渗透浓水池；所述反渗透浓水池通过反渗透浓水输送泵连接反渗透浓水处理装置； 所述膜生物反应池、多介质过滤器和活性炭过滤器分别接低压空气管道； 所述过滤器反洗水池入口接工业用水管网，过滤器反洗水池出口通过过滤器反洗泵连接多介质过滤器及活性炭过滤器，过滤器反冲洗水接至废水站地坑。
2.根据权利要求1所述的焦化废水回用处理系统，其特征在于，所述膜生物反应池入口还接清洗剂管道。
3.根据权利要求1所述的焦化废水回用处理系统，其特征在于，所述膜生物反应池内装有连续空气曝气装置。
4.根据权利要求1所述的焦化废水回用处理系统，其特征在于，所述膜生物反应器采用内置有机板式膜的形式，采用改性纳米材料制成，为微滤膜，膜孔径0. 1 μ m。
5.根据权利要求1所述的焦化废水回用处理系统，其特征在于，所述保安过滤器的滤芯为可更换卡式PP滤芯。
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