CN100534933C - 一种化肥废水的处理工艺 - Google Patents
一种化肥废水的处理工艺 Download PDFInfo
- Publication number
- CN100534933C CN100534933C CNB2007101475169A CN200710147516A CN100534933C CN 100534933 C CN100534933 C CN 100534933C CN B2007101475169 A CNB2007101475169 A CN B2007101475169A CN 200710147516 A CN200710147516 A CN 200710147516A CN 100534933 C CN100534933 C CN 100534933C
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- Prior art keywords
- waste water
- pond
- ammonia nitrogen
- baf
- pool
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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- 239000002351 wastewater Substances 0.000 title claims abstract description 63
- 238000000034 method Methods 0.000 title claims abstract description 18
- 239000003337 fertilizer Substances 0.000 title claims abstract description 14
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound 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[N].N CVTZKFWZDBJAHE-UHFFFAOYSA-N 0.000 claims abstract description 28
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- 241001495402 Nitrococcus Species 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N phosphorus Chemical compound 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Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
一种化肥废水处理工艺，步骤是首先进入调节池均衡水质水量并初步去除废水中较大的悬浮物；然后进入混凝池，投加絮凝剂和助凝剂，在搅拌器作用下与污水中较小的悬浮物及部分胶体充分混合形成矾花；接着进入沉淀池，使混凝池形成的矾花得以从污水中分离；经混凝沉淀处理后废水进入混合池，与回流污泥混合，并调节废水pH至8.0～10.0；最后进入AF-BAF池去除氨氮和COD。多级AF-BAF池水力流态属于混合流与推流之间，有利于生物的多样性，不仅可以同时进行硝化和反硝化反应、提高氨氮的去除效果，而且提高了去除有机物的广谱性。该工艺适用于高氨氮化肥废水的处理，具有同时去除COD和氨氮的功效，COD的去除率达85%以上，氨氮去除率达99%以上，且具有抗冲击的特点。
Description
一种化肥废水的处理工艺
技术领域
本发明涉及一种废水处理方法，尤其是涉及一种用于高氨氮化肥废水的处理 工艺。
背景技术
废水处理技术中，对于高氨氮化肥废水普遍认为生化处理是最为经济有效
的技术。现有的生物脱氮技术主要有AO法，AV0法，CAST法等，这几种工艺 均可去除COD和氨氮，但是对于高氨氮和中氨氮化肥废水脱氮效果不佳。这是 由于处理系统泥龄过长、硝化速度限制、进水负荷限制等，同时硝化和亚硝化 菌等对于营养、生长条件等要求不同。其中硝化菌生长缓慢、世代期长等特性 与其他微生物种群差异很大，要动态控制不同种类的微生物种群的生长条件、 营养物质、N、碳浓度等相当复杂，相当困难。目前广泛采用的脱氮处理工艺 碳氧化和氨氮的硝化是分开进行的，即先进行碳的氧化，再进行硝化，因为硝 化菌和亚硝化菌在有机物存在的情况下不能生存，且硝化菌和亚硝化菌易受到 温度、pH值、氨氮浓度等的抑制。在废水中氨氮浓度超过50mg/L将对硝化过程 产生抑制，导致对于高氨氮和中氨氮化肥废水处理效果不理想。
中国专利CN 1410366A采用双循环两相生物脱氮除磷工艺，该专利的缺点 是运行管理复杂，动力消耗较大，工艺流程长，占地面积大。中国专利CN 1220972A采用两级反硝化——好氧段处理，污泥回流比较大，氨氮去除率不高， 硝化和反硝化分开进行，且硝化反应条件不易控制。中国专利CN1401592A采 用双层曝气生物滤池同步去除COD和氨氮，该专利的缺点是滤池需要反冲洗， 影响硝化菌生长且长期使用容易堵塞。目前，现有技术对此类废水的处理效果都达不到99%以上。常规的脱氮工 艺污泥回流比高，动力消耗较大，占地面积大，投资较高且对于水质水量的抗 冲击能力不高。
汰明内容
为了克服上述缺点，同步实现脱碳和硝化，避免滤池反冲洗影响硝化菌生 长，本发明采用以下技术工艺：
1. 将髙氨氮化肥废水在平流式沉淀池构造的调节池内停留4-6小时，以均 衡水质水量，并初步去除废水中较大的悬浮物；
2. 均衡水质后的废水进入混凝池，停留15〜30min,并投加絮凝剂和助凝 剂PAM和PAC，絮凝剂投加量200-350ppm,在搅拌器作用下与污水中 较小的悬浮物及部分胶体充分混合形成矶花；
3. 以上经过絮凝反应后废水进入斜板沉淀池，沉淀池的表面负荷釆用 1.0-2.0m3/m2 • h，使混凝池形成的矾花得以从污水中分离；
4. 经混凝沉淀处理后废水进入混合池，与回流污泥混合，并投加Na2C03 调节废水pH值至8.0〜10.0;
5. 经调节pH值后废水进入AF-BAF池，该池视水质状况分为3-7级，废 水依次通过AF-BAF池，去除废水中氨氮和COD。
AF-BAF池由进水池和多级AF-BAF池组成；所述进水池4的上部设有配水 槽2，该配水槽2装有进水管4、底部开有布水孔3;进水池4的底部与AF-BAF 池相连，该AF-BAF池装有生物填料床，生物填料床的下方铺设曝气管路7，曝 气生物滤池的底部设有排泥管6; AF-BAF池之间由连接孔9连接，在最后一 级曝气生物滤池a6的上部装有集水堰11、集水渠12和排水管。
4AF—BAF池一般为3-7级，第一级为AF (Anaerobic Filter)池，后边为 BAF (Biological Aeration Filter)池；该AF—BAF池装有生物填料床，生物填料 床由框架和填料组成，填料床通过框架直接固定在壳体上。生物填料床的外表 面是包裹在固定框架上的隔网，填料床的内部由固定在框架上的聚乙烯网丝编 织的隔网分隔成多个空间单元，每个空间单元填充活性生物填料。这样既保证 了填料处于悬浮状态、不易堵塞、水流阻力小，避免了反冲洗；又保证了填料 固定于空间单元内、填料不易被水流冲散流失。AF池不设曝气管道，BAF池 在生物填料床的下方设曝气管路，底部设排泥管。废水首先从底部进入一级AF
池，升流与活性生物填料充分接触，在AF池顶溢流进入BAF池，降流与活性 生物填料充分接触。后面各级依次污水流动同一、二级。
AF—BAF池各反应区生物填料床的高度一般不小于3米，活性生物填料以 高性能填料为载体，活性生物填料具有不规则且直径不同的孔，有利于不同微
生物群落的寄居和繁殖；选用高效工程菌群，工程菌寄居在载体上，这样提高 了生物负载量，提髙水质水量的抗冲击能力。这种结构使得运行过程中载体内 部存在着良好的厌氧区微环境，使其内部形成无数个微型的反硝化反应器，故 而造成在同一个反应器当中同时发生氨氧化、硝化和反硝化联合作用，对氨氮 的去除效率达99.0%以上；同时，通过控制各级AF-BAF反应器的运行参数， 造成宏观厌氧及好氧环境的存在，有利于聚磷菌的释磷和过度摄磷，保证了磷 的去除。载体材料表面所生长的生物量通常为18-25g/L，是普通生物膜法的 1.5-2.0倍，是传统活性污泥法的10-20倍，并且填料不易脱落流失。
废水依次通过多级反应区，水力流态属于混合流与推流之间，有利于维持 生物的多样性，使好氧、厌氧菌及兼性菌同时存在，硝化和反硝化同时进行，从而达到脱氮的目的。生物的多样性，不仅可以进行硝化和反硝化反应、提高 氨氮的去除效果，而且提高了去除有机物的广谱性。
采用本发明处理化肥废水，反应速度快、停留时间短、处理效果可靠。对
于高氨氮化肥废水COD去除率可以达到85%以上、氯氮去除率达到99%以上、 并且该工艺对废水的水质水量变化具有较高的耐受能力和抗冲击能力。
附面斑明
图1为化肥废水处理工艺流程示意图。 图2为AF-BAF池的结构示意图。
具俸实称5^式
下面结合附图进一步说明本发明的具体实施方式，本发明的保护范围不局 限于下述的具体实施方式。
实施例l
取某化肥厂化肥废水（CODcr=700mg/L， SS=400mg/L， NH3-N=500mg/L， PH:8〜9)进行实验。将髙氨氮化肥废水在调节池（采用平流式沉淀池构造）内 停留4小时，以均衡水质水量，并初步去除废水中较大的悬浮物；均衡水质后 的废水进入混凝池，停留20min，并投加絮凝剂和助凝剂PAM和PAC，絮凝剂 投加比300ppm/吨水，在搅拌器作用下与污水中较小的悬浮物及部分胶体充分 混合形成矾花；.经过絮凝反应后进入沉淀池，斜板沉淀池的表面负荷采用 1.5m3/m2*h，废水的温度为28""C， pH值为7-8，使混凝池形成的矾花得以从污 水中分离；经混凝沉淀处理后废水进入混合池，与回流污泥混合，并投加碱 (Na2C03)调节废水pH至9.0，温度为28。C;调节pH值后废水进入AF-BAF池。该池分为6级，第一级为AF池，后面五级为BAF池。废水依次通过6级 AF-BAF池。AF-BAF池废水的温度为28'C,气水比为6: 1， BOD容积负荷为 4.5kg/m3*d，氨氮的容积负荷为0.5kg/m3、d。经过以上工艺处理后，CODcr降为 100mg/L， SS-10mg/L, >JH3-N=5mg/L， PH:8〜9，稳定达到国家一级排放标准。 实施例2
取某化肥厂化肥废水（CODcr=500mg/L， SS=200mg/L， NH3-N=500mg/L， PH:8〜10)进行实验。将高氮氮化肥废水在调节池（采用平流式沉淀池构造） 内停留4小时，以均衡水质水量，并初步去除废水中较大的悬浮物；均衡水质 后的废水进入混凝池，停留20min，并投加絮凝剂和助凝剂PAM和PAC，絮凝 剂投加比300ppm/吨水，.在搅拌器作用下与污水中较小的悬浮物及部分胶体充 分混合形成矾花；经过絮凝反应后进入沉淀池，斜板沉淀池的表面负荷采用 1.5m3/m2*h，废水的温度为28。C， pH值为8-9，使混凝池形成的矾花得以从污 水中分离；经混凝沉淀处理后废水进入混合池，与回流污泥混合，并投加碱 (Na2C03)调节废水pH至10.0,温度为28°C;调节pH值后废水进入AF-BAF 池。该池分为6级，第一级为AF池，后面五级为BAF池。废水依次通过6级 AF-BAF池。AF-BAF池废水的温度为28。C，气水比为6: 1， BOD容积负荷为 4.5kg/m3.d，氨氮的容积负荷为0.5kg/m3.d。经过以上工艺处理后，稳定达到国 家一级排放标准。'
表进水水质与出水标准<table>table see original document page 7</column></row>
<table>
Claims (2)
1、一种高氨氮化肥废水的处理工艺，包括以下步骤： a.将高氨氮化肥废水在平流式沉淀池构造的调节池内停留4-6小时，以均衡水质水量，并初步去除废水中较大的悬浮物； b.均衡水质后的废水进入混凝池，停留15～30min，并投加絮凝剂和助凝剂PAM和PAC，絮凝剂投加量200-350ppm，在搅拌器作用下与污水中较小的悬浮物及部分胶体充分混合形成矾花； c.以上经过絮凝反应后废水进入斜板沉淀池，沉淀池的表面负荷采用1.0-2.0m3/m2·h，使混凝池形成的矾花得以从污水中分离； d.经混凝沉淀处理后废水进入混合池，与回流污泥混合，并投加Na2CO3调节废水pH值至8.0～10.0； e.经调节pH值后废水进入AF-BAF池，该池视水质状况分为3-7级，废水依次通过AF-BAF池，去除废水中氨氮和COD；所述的AF-BAF池第一级为AF池，后边为BAF池。
2、 根据权利要求1所述的高氨氮化肥废水处理工艺，其特征在于所述的AF— BAF池装有生物填料床，生物填料床的外表面是包裹在生物填料固定框架[5] 上的隔网，填料床的内部由固定在生物填料固定框架上的隔网分隔成多个空间 单元，每个空间单元填充活性生物填料；AF池不设曝气管道，BAF池在生物 填料床的下方设曝气管路，底部设排泥管；废水首先从底部进入一级AF池， 升流与活性生物填料充分接触，在AF池顶溢流进入BAF池，降流与活性生物 填料充分接触，后面各级依次污水流动同一、二级。
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