CN105293787B - 一种冷轧碱性排放废水深度处理回用工艺系统和方法 - Google Patents
一种冷轧碱性排放废水深度处理回用工艺系统和方法 Download PDFInfo
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- CN105293787B CN105293787B CN201410234020.5A CN201410234020A CN105293787B CN 105293787 B CN105293787 B CN 105293787B CN 201410234020 A CN201410234020 A CN 201410234020A CN 105293787 B CN105293787 B CN 105293787B
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- 238000006065 biodegradation reaction Methods 0.000 description 2
- OYPRJOBELJOOCE-UHFFFAOYSA-N calcium Chemical compound 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[Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 2
- 239000011575 calcium Substances 0.000 description 2
- 229910052791 calcium Inorganic materials 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound 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O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
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- 230000001473 noxious Effects 0.000 description 2
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- 239000000047 product Substances 0.000 description 2
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- ZAMOUSCENKQFHK-UHFFFAOYSA-N chlorine atom Chemical compound 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[Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- ZCDOYSPFYFSLEW-UHFFFAOYSA-N chromate(2-) Chemical compound 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Abstract
本发明公开了一种冷轧碱性排放废水深度处理回用的工艺系统。包括电氧化气浮装置、无机超滤装置,超滤循环池,超滤循环泵,超滤清洗槽,超滤产水池,反渗透供水泵,保安过滤器,反渗透高压泵,二段式反渗透装置,反渗透产水池,反渗透浓水池,反渗透清洗槽,反渗透清洗泵及管道混合器。并公开了各部分之间的连接关系。本发明还提供了一种利用该系统处理废水的方法。本发明处理废水效果稳定,能有效去除废水中的有机物、悬浮物、油类和盐分等污染物,到达废水回用的目的;且生产运行成本低,自动化操作程度高,操作运行简便。
Description
一种冷轧碱性排放废水深度处理回用工艺系统和方法
技术领域
[0001] 本发明属于水处理技术领域,具体涉及一种钢铁行业冷乳碱性排放废水的深度处 理回用工艺系统。
背景技术
[0002] 钢铁行业在高速发展的同时又面临着全球能源、水资源短缺和生态环境恶化的严 峻挑战。水是生命的源泉、工业的血液、城市的命脉。在水资源十分匮乏水质污染日趋严重 的当今世界,如何降低水耗、减少水污染物排放量,发展循环经济、实行清洁生产,保护生态 环境,是钢铁企业生存发展面临的现实课题。
[0003] 冷乳废水种类繁多,主要包括乳化液废水、浓油强碱废水、平整液废水、稀油弱碱 废水、酸性废水、含铬废水等。碱性最终排放水主要是来自乳化液废水、浓油强碱废水、平整 液废水和稀油弱碱废水经过除油、PH调整、生化等工序处理后的废水,废水水质情况如下: pH6-9,电导率2500-4000us/cm,悬浮物5-20mg/L,C0Dcr20-60mg/L,碱度50-200mg/L,氯离 子 600-1200mg/L,硫酸根 20-50mg/L,二氧化硅 2-8mg/L,钙硬度 50-100mg/L,镁硬度 20-50mg/L,总铁 0 · 2_2mg/L,油类 l_3mg/L。
[0004] 深度处理的工艺较多,如离子交换器、电渗析(ED)、电去离子交换器(EDI)、电吸附 (EST)、反渗透、纳滤、蒸馏等。如实用新型装置《含油碱性废水的处理系统》(专利申请号: 200720015816.7)所述,含油碱性废水经过传统pH调整、混凝、气浮、生化后的出水经过生物 滤池,出水⑶Dcr<80mg/L,悬浮物<10mg/L总油<5mg/L。此深度处理工艺仅可去除部分 CODcr、总油及悬浮物,但无法除盐,无法达到工业水水质要求。
[0005] 近年来,随着反渗透膜元件的成熟及普及,反渗透工艺已广泛应用于废水深度处 理及回用领域。根据冷乳碱性排放废水水质特点,废水中总硬度相较于最终排放废水较低, 反渗透膜结垢倾向较低,可采用反渗透装置达到废水回收利用的目的,实现企业可持续发 展和节能减排、提高综合竞争力具有重要意义。
发明内容
[0006] 因此,本发明要解决的技术问题是,针对冷乳碱性排放废水水质特点,本发明提供 了一种适用于冷乳碱性排放废水深度处理回用的工艺系统,能有效去除废水中的有机物、 悬浮物、油类和盐分等污染物,到达废水回用的目的;具有生产运行成本低,自动化操作程 度高,操作运行简便的特点。可广泛应用冷乳及硅钢碱性排放废水的深度处理工艺。
[0007] 本发明的技术方案是,一种冷乳碱性排放废水深度处理回用工艺系统,
[0008] 包括电氧化气浮装置、无机超滤装置,超滤循环池,超滤循环栗,超滤清洗槽,超滤 产水池,反渗透供水栗,保安过滤器,反渗透高压栗,二段式反渗透装置,反渗透产水池,反 渗透浓水池,反渗透清洗槽,反渗透清洗栗及管道混合器;
[0009] 所述电氧化气浮装置与所述超滤循环池连接,所述超滤循环池与超滤循环栗、无 机超滤装置依次连接,所述超滤清洗槽连接在所述超滤循环栗、无机超滤装置上;所述无机 超滤装置的出口连接有超滤产水池,超滤产水池的出口再与反渗透供水栗、管道混合器、保 安过滤器、反渗透高压栗依次连接,所述反渗透高压栗连接有二段式反渗透装置,所述的二 段式反渗透装置包括第一段反渗透装置和第二段反渗透装置;
[0010] 所述的第一段反渗透装置进口与反渗透高压栗连接,第一段反渗透装置出口与反 渗透产水池连接,第一段反渗透装置出口还与第二段反渗透装置相连;
[0011] 所述的第二段反渗透装置进口与第一段反渗透装置相连,第二段反渗透装置出口 与反渗透产水池连接,还与反渗透浓水池连接;
[0012] 所述电氧化气浮装置内设置有电氧化气浮电极板和电氧化气浮刮渣机,电氧化气 浮上部进口接碱性排放废水,电氧化气浮出口接超滤循环池;所述电氧化气浮装置下部连 接有一废液收集槽。
[0013] 电氧化气浮不仅可通过气浮作用去除水中杂质,而且降解废水中的有机物,特别 是难生物降解的有机物。有机物降解原理如下:
[0014] 1)直接氧化即污染物直接在阳极失去电子而发生氧化,有机物的直接电催化转化 分两类进行:一是电化学转换,即把有毒物质转变为无毒物质,或把非生物兼容的有机物转 化为生物兼容的物质(如芳香物开环氧化为脂肪酸),以便进一步生物降解;二是电化学燃 烧,即直接将有机物深度氧化为二氧化碳。
[0015] 2)间接氧化即通过阳极反应生成具有强氧化作用的中间产物(如· 0H、· 02、· HO2 等自由基),最终达到氧化降解污染物的目的。有机物在含氧自由基的作用下降解,提高了 电流效率,节省了电能消耗。
[0016]电氧化气浮通过氧化作用,可将废水中的Fe2+氧化为Fe3+,作为絮凝剂提高废水的 气浮效果。因此,电氧化气浮在不添加任何化学药剂的情况下,达到降解有机物,去除悬浮 物及杀菌灭藻的作用。
[0017] 根据本发明的冷乳碱性排放废水深度处理回用工艺系统,优选的是,所述的超滤 清洗槽进口连接有清洗药剂、工业水管网及蒸汽管网;所述超滤清洗槽出口与超滤循环栗 连接,所述无机超滤装置出口接超滤清洗槽。
[0018] 其中,所述所述保安过滤器入口通过管道混合器连接有盐酸管道、阻垢剂管道和 还原剂管道。
[0019] 其中,所述的反渗透产水池出口通过一产水输送栗连接至工业水管网;所述的反 渗透产水池出口通过反渗透冲洗栗连接至第一段反渗透装置进口。
[0020] 其中,所述的反渗透浓水池出口通过浓水输送栗连接至浓盐水处理装置;所述反 渗透浓水池出口连接浓盐水处理装置,出口不与反渗透连接。所述反渗透浓水池进口与反 渗透装置的第二段连接。
[0021] 所述的反渗透清洗水箱进口与清洗药剂、工业水管网连接,通过反渗透清洗栗连 接至反渗透清洗保安过滤器;
[0022] 所述反渗透清洗保安过滤器分别于第一段反渗透装置和第二段反渗透装置连接, 第一段反渗透装置二个出口和第二段反渗透装置二个出口还与反渗透清洗水箱连接。
[0023] 根据本发明的冷乳碱性排放废水深度处理回用工艺系统,优选的是,所述的电氧 化气浮装置,采用纯钛电极板;所述的两段式反渗透装置,采用抗污染膜元件。
[0024] 根据本发明的冷乳碱性排放废水深度处理回用工艺系统,优选的是,所述的无机 超滤装置,采用多通道陶瓷膜管,组件采用SS316外壳;所述的保安过滤器及反渗透清洗保 安过滤器,采用小于5um PP棉滤芯。
[0025] 进一步地,所述多通道陶瓷膜管的超滤孔径不超过50nm。
[0026] 本发明还提供了冷乳碱性排放废水深度处理方法,将冷乳碱性排放废水通过电氧 化气浮装置去除水中的杂质,并降解废水中的有机物,然后废水进入超滤循环池,并通过超 滤循环栗进入超滤装置,经过无机超滤装置产水后,通入超滤产水池,然后废水再进一步通 过反渗透供水栗、管道混合器进入保安过滤器,通过两段式反渗透装置,进入反渗透产水 池。
[0027] 所述的无机超滤装置,采用多通道陶瓷膜管,组件采用SS316外壳。无机陶瓷膜具 有良好的化学稳定性,以及耐酸、碱、有机溶剂,耐高温,抗微生物的能力,适用pH范围为0〜 14,适用温度范围在0〜300°(:。一般操作压力约为0.2-0.31〇^,设计通量为10017(1112·!!)。
[0028] 本发明的有益效果是:
[0029] 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:
[0030] 采用本发明的工艺系统,处理效果稳定、生产运行成本低、操作运行简便,出水水 质能达到工业水水质指标,达到回用目的。采用本发明的工艺系统,可避免使用混凝剂和氧 化剂,达到去除COD和油类的效果,降低废水处理运行成本。
附图说明
[0031] 图1是本发明的系统示意图。
[0032] 图2是本发明的超滤清洗槽连接示意图。
[0033] 图3是本发明的反渗透清洗槽连接示意图.
[0034] 图4是本发明的工艺流程图。
[0035] 图中,1-电氧化气浮装置,2-超滤循环池,3-超滤循环栗,4-无机超滤装置,5-超滤 清洗槽,6-超滤产水池,7-反渗透供水栗,8-管道混合器,9-保安过滤器,10-反渗透高压栗, 11-反渗透清洗槽,12-反渗透清洗栗,13-反渗透清洗保安过滤器,14-反渗透浓水池,15-浓 水输送栗,16-反渗透产水池,17-产水输送栗,18-反渗透冲洗栗,19-二段式反渗透装置, 20-电极板,21-刮渣机,22-废液收集槽。
具体实施方式
[0036] 下面结合附图和实施例对本发明做详细说明。
[0037] 如图1所示,一种冷乳碱性排放废水深度处理回用工艺系统,它包括电氧化气浮装 置1、无机超滤装置4,超滤循环池2,超滤循环栗3,超滤清洗槽5,超滤产水池6,反渗透供水 栗7,保安过滤器9,反渗透高压栗10,二段式反渗透装置19,反渗透产水池16,反渗透浓水池 14,反渗透清洗槽11,反渗透清洗栗12及管道混合器8.
[0038] 图2是超滤清洗槽的具体连接方式,即图1中标有“超滤清洗槽”的两个箭头所连接 之处。图3是反渗透清洗槽的具体连接方式。所述的第一段反渗透装置进口与反渗透高压栗 连接,第一段反渗透装置出口与反渗透产水池连接,第一段反渗透装置出口还与第二段反 渗透装置相连;第二段反渗透装置进口与第一段反渗透装置相连,第二段反渗透装置出口 与反渗透产水池连接,还与反渗透浓水池连接。
[0039] 电氧化气浮装置1内设置电氧化气浮电极板20和电氧化气浮刮渣机21。电氧化气 浮上部进口接碱性排放废水,电氧化气浮出口接超滤循环池;所述电氧化气浮装置下部连 接有一废液收集槽22。交流电通过整流设备被转化成直流电后通过电极板,电极板产生微 小气泡,通过产生电解混凝等效应,水中的杂质被微小气泡带至水面被刮渣机刮至浮渣槽。
[0040] 电氧化气浮电极板20采用纯钛电极,电极分正极和负极,正负极通过交叉排列组 合形式重叠成电极组。电极组运行时需定时倒换电极的正负极性(一般运行4小时倒极运行 1小时),以避免电极被钝化,保证电极组时刻处于最佳的运行状态。
[0041] 电氧化气浮不仅可通过气浮作用去除水中杂质,而且降解废水中的有机物,特别 是难生物降解的有机物。有机物降解原理如下:
[0042] 1)直接氧化即污染物直接在阳极失去电子而发生氧化,有机物的直接电催化转化 分两类进行:一是电化学转换,即把有毒物质转变为无毒物质,或把非生物兼容的有机物转 化为生物兼容的物质(如芳香物开环氧化为脂肪酸),以便进一步生物降解;二是电化学燃 烧,即直接将有机物深度氧化为二氧化碳。
[0043] 2)间接氧化即通过阳极反应生成具有强氧化作用的中间产物(如· 0H、· 02、· HO2 等自由基),最终达到氧化降解污染物的目的。有机物在含氧自由基的作用下降解,提高了 电流效率,节省了电能消耗。
[0044] 电氧化气浮通过氧化作用,可将废水中的Fe2+氧化为Fe3+,作为絮凝剂提高废水的 气浮效果。因此,电氧化气浮在不添加任何化学药剂的情况下,达到降解有机物,去除悬浮 物及杀菌灭藻的作用。
[0045] 无机超滤装置4采用大错流过滤形式,无机超滤装置4产水进入超滤产水池6,浓水 进入超滤循环池。在一定的压差和紊流流动的情况下,使废水中大部分极性分子通过膜,而 所有非极性分子(如胶体、油类、微粒等)和相对分子质量较大的物质被截留,从而使废水得 到去除废水净化。
[0046] 无机超滤装置4,采用多通道陶瓷膜管(超滤孔径不超过50nm),组件采用SS316外 壳。无机陶瓷膜具有良好的化学稳定性,以及耐酸、碱、有机溶剂,耐高温,抗微生物的能力, 适用pH范围为0〜14,适用温度范围在0〜300°C。一般操作压力约为0.2-0.3MPa,设计通量 为 100lV(m2 · h)。
[0047] 无机超滤装置运行一定时间(一般为20-30d),系统通量下降或压差升高时,需要 进行化学清洗。根据冷乳碱性排放废水水质情况,分析超滤膜污堵的主要原因为有机物的 污染,一般单独碱洗5个周期,再进行1次酸碱联合清洗。
[0048] 经过电氧化气浮及超滤处理后,出水水质水质如下:COD彡30mg/L,油类彡lmg/L, SDK 3,基本满足反渗透进水水质要求。
[0049] 保安过滤器采用5um PP棉滤芯,用于拦截异常情况下的大颗粒污染物,保证反渗 透膜稳定运行。当保安过滤器进出口压差增大的情况下更换,一般更换周期为2-3个月。
[0050] 二段式反渗透装置采用抗污染膜元件,两段排列方式为2 : 1。废水在背压(1.2-1.5MPa)的条件下,拦截大分子有机物、微生物及大部分可溶性盐分,小部分可溶性盐分可 选择性通透,被拦截的水溶性杂质被浓缩,以浓水的形式排入反渗透浓水池。整个系统的脱 盐率达95%,回收率达75 %。
[0051] 反渗透装置运行一定时间(一般为60-90d),系统通量下降或段间压差升高时,需 要进行化学清洗。分析超滤膜污堵的主要原因为有机物的污染,以碱洗为主,酸洗为辅,清 洗温度为40-60 °C。
[0052] 系统停机或清洗结束需采用反渗透产水对膜进行冲洗,其主要目的是用反渗透产 水置换停机后膜中滞留的浓水,防止浓水侧结垢。
[0053] 最终产水水质满足工业水水质标准,其中pH7 · 0-8 · 0,电导率<500us/cm,SS〈10mg/ L,全硬度〈150mg/L,|丐硬度〈100mg/L,碱度〈110mg/L,氯离子<60mg/L,硫酸根<50mg/L,全铁 <lmg/L,可溶性 Si〇2〈6mg/L,蒸发残渣<300mg/L;
[0054] 以下通过具体实施例对本发明做进一步的阐述。
[0055] 实施例采用冷乳废水站碱性排放废水作为原水,处理量为1.0m3/h,处理流程参考 附图。系统进出水水质情况如下表所述:
[0056] 表一:工艺系统进出水水质情况
[0057]
[0059] 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,出水水质能达到工业水水质指标,达到回用目的。
[0060] 当然,本技术领域内的一般技术人员应当认识到,上述实施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、变形 都将落在本发明权利要求范围内。
Claims (9)
1. 一种冷乳碱性排放废水深度处理回用工艺系统,其特征在于: 包括电氧化气浮装置、无机超滤装置、超滤循环池、超滤循环栗、超滤清洗槽、超滤产水 池、反渗透供水栗、保安过滤器、反渗透高压栗、二段式反渗透装置、反渗透产水池、反渗透 浓水池、反渗透清洗槽、反渗透清洗栗及管道混合器; 所述电氧化气浮装置与所述超滤循环池连接,所述超滤循环池与超滤循环栗、无机超 滤装置依次连接,所述超滤清洗槽连接在所述超滤循环栗、无机超滤装置上;所述无机超滤 装置的出口连接有超滤产水池,超滤产水池的出口再与反渗透供水栗、管道混合器、保安过 滤器、反渗透高压栗依次连接,所述反渗透高压栗连接有二段式反渗透装置,所述的二段式 反渗透装置包括第一段反渗透装置和第二段反渗透装置; 所述的第一段反渗透装置进口与反渗透高压栗连接,第一段反渗透装置出口与反渗透 产水池连接,第一段反渗透装置出口还与第二段反渗透装置相连; 所述的第二段反渗透装置进口与第一段反渗透装置相连,第二段反渗透装置出口与反 渗透产水池连接,还与反渗透浓水池连接; 所述电氧化气浮装置内设置有电氧化气浮电极板和电氧化气浮刮渣机,电氧化气浮上 部进口接碱性排放废水,电氧化气浮出口接超滤循环池;所述电氧化气浮装置下部连接有 一废液收集槽;所述的电氧化气浮装置,采用纯钛电极板;所述的二段式反渗透装置,采用 抗污染膜元件。
2. 根据权利要求1所述的冷乳碱性排放废水深度处理回用工艺系统,其特征在于,所述 的超滤清洗槽进口连接有清洗药剂、工业水管网及蒸汽管网;所述超滤清洗槽出口与超滤 循环栗连接,所述无机超滤装置出口接超滤清洗槽。
3. 根据权利要求1所述的冷乳碱性排放废水深度处理回用工艺系统,其特征在于,所述 保安过滤器入口通过管道混合器连接有盐酸管道、阻垢剂管道和还原剂管道。
4. 根据权利要求1所述的冷乳碱性排放废水深度处理回用工艺系统,其特征在于,所述 的反渗透产水池出口通过一产水输送栗连接至工业水管网;所述的反渗透产水池出口通过 反渗透冲洗栗连接至第一段反渗透装置进口。
5. 根据权利要求1所述的冷乳碱性排放废水深度处理回用工艺系统,其特征在于,所述 的反渗透浓水池出口通过浓水输送栗连接至浓盐水处理装置;所述反渗透浓水池出口连接 浓盐水处理装置,所述反渗透浓水池进口与反渗透装置的第二段连接; 所述的反渗透清洗水箱进口与清洗药剂、工业水管网连接,通过反渗透清洗栗连接至 反渗透清洗保安过滤器; 所述反渗透清洗保安过滤器分别于第一段反渗透装置和第二段反渗透装置连接,第一 段反渗透装置二个出口和第二段反渗透装置二个出口还与反渗透清洗水箱连接。
6. 根据权利要求1所述的冷乳碱性排放废水深度处理回用工艺系统,其特征在于,所述 的无机超滤装置,采用多通道陶瓷膜管,组件采用SS316外壳;所述的保安过滤器及反渗透 清洗保安过滤器,采用小于5um PP棉滤芯。
7. 根据权利要求6所述的冷乳碱性排放废水深度处理回用工艺系统,其特征在于,所述 多通道陶瓷膜管的超滤孔径不超过50nm。
8. —种冷乳碱性排放废水深度处理方法,采用权利要求1所述的冷乳碱性排放废水深 度处理回用工艺系统,其特征在于,该方法包括:将冷乳碱性排放废水通过电氧化气浮装置 去除水中的杂质,并降解废水中的有机物,然后废水进入超滤循环池,并通过超滤循环栗进 入超滤装置,经过无机超滤装置产水后,通入超滤产水池,然后废水再进一步通过反渗透供 水栗、管道混合器进入保安过滤器,通过二段式反渗透装置,进入反渗透产水池。
9.根据权利要求8所述的冷乳碱性排放废水深度处理方法,其特征在于,所述的无机超 滤装置,采用多通道陶瓷膜管,组件采用SS316外壳。
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