CN103880248B - 一种焦化废水处理系统及处理方法 - Google Patents
一种焦化废水处理系统及处理方法 Download PDFInfo
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- CN103880248B CN103880248B CN201410106108.9A CN201410106108A CN103880248B CN 103880248 B CN103880248 B CN 103880248B CN 201410106108 A CN201410106108 A CN 201410106108A CN 103880248 B CN103880248 B CN 103880248B
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- aerobic nitrification
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- anoxic denitrification
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- 238000004939 coking Methods 0.000 title claims abstract description 67
- 238000000034 method Methods 0.000 title claims description 45
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- 239000000463 material Substances 0.000 claims description 96
- 238000009826 distribution Methods 0.000 claims description 71
- 229910052799 carbon Inorganic materials 0.000 claims description 59
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 56
- 238000010992 reflux Methods 0.000 claims description 53
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- 229910052757 nitrogen Inorganic materials 0.000 claims description 26
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound 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[N].N CVTZKFWZDBJAHE-UHFFFAOYSA-N 0.000 claims description 21
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- 229910052760 oxygen Inorganic materials 0.000 claims description 21
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[Na+].CC([O-])=O VMHLLURERBWHNL-UHFFFAOYSA-M 0.000 claims description 3
- 239000001632 sodium acetate Substances 0.000 claims description 3
- 235000017281 sodium acetate Nutrition 0.000 claims description 3
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OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 238000003911 water pollution Methods 0.000 description 2
- 208000007502 Anemia Diseases 0.000 description 1
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- JMANVNJQNLATNU-UHFFFAOYSA-N Cyanogen Chemical compound 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- KSSNXJHPEFVKHY-UHFFFAOYSA-N phenol;hydrate Chemical compound 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O.OC1=CC=CC=C1 KSSNXJHPEFVKHY-UHFFFAOYSA-N 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 238000009938 salting Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
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Abstract
本发明公开了一种焦化废水处理系统,它包括上流式厌氧污泥床反应器、缺氧反硝化生物滤池和好氧硝化生物滤池、多级铁碳微电解耦合芬顿氧化床反应器、好氧硝化生物滤池和缺氧反硝化生物滤池。一种焦化废水处理方法,焦化废水由焦化废水原水进水管自下而上进入上流式厌氧污泥床反应器、缺氧反硝化生物滤池、好氧硝化生物滤池、多级铁碳微电解耦合芬顿氧化床反应器、好氧硝化生物滤池、缺氧反硝化生物滤池而排出。本发明占地面积小、耗能低,并具有高效的废水处理效能,降低废水处理的运行成本,具有处理负荷高、能耗低、产泥量少的特点。
Description
技术领域
[0001] 本发明属于水处理技术领域,具体涉及一种焦化废水处理的系统及方法。
背景技术
[0002] 焦化废水是煤焦化过程中产生的一种含大量油、酚、氨氮等有害、有毒物质的难降解废水。该类废水具有成分复杂、污染物浓度高等特点,其有机组分除85%的酚类化合物以夕卜,还包括脂肪族化合物、多环芳烃(PAHs)和含氧、氮、硫元素的杂环化合物等。有机污染物的排入水体会消耗水中溶解氧,最终会导致水体缺氧进而弓I起水中的水生动物的无法呼吸而死亡,其尸体会在水中厌氧分解产生甲烷、硫化氢等恶臭气体,同时使水体发黑变臭,使水体流域环境发生恶化。氮等营养元素的排入水体会导致水体的富营养化,使大量藻类和微生物繁殖进而影响水源水质。同时因废水中含有酚类化合物,其可通过皮肤、黏膜的接触和经口服侵入人体内部,使人体细胞失去活力,还可进一步向深部渗透,引起深部组织损伤或坏死,长期饮用含酚水会引起头晕、贫血以及各种神经系统病症。另外,未经达标排放的废水直接灌溉农田,会使农作物减产和枯死,废水中的油类物质会堵塞土壤孔隙,使土壤盐碱化。水污染已经成为我国水源性缺水及环境污染的主要问题,同时按照人均水资源量我国也是严重贫水国,水体不断受到污染导致了我国很多城市和地方出现了水源性缺水,大量废水的排放不仅导致水体污染严重加剧也导致了水资源的浪费。随着我国钢铁产能的过剩发展,焦化废水的数量也在与日倶增,再加上焦化行业新标准和综合排放标准对污染物排放指标的要求日趋严格,焦化废水的达标排放问题严重制约了焦化行业和钢铁行业的可持续发展。整个行业对经济合理、新型高效的焦化废水处理技术的需求非常迫切。因此,如何采用经济、高效和稳定的处理方法,使处理后的焦化废水能够达到最新《钢铁工业水污染物排放标准》,对于钢铁行业和焦化行业的发展显得十分必要,符合我国可持续经济发展的要求。
[0003] 长期以来,国内焦化厂普遍采用生化法对焦化废水进行处理,且80%以上采用普通生化法,但是现有工艺虽能将焦化废水中的酚、氰等有机物有效去除,但仍存在COD很难达标,氨氮超标严重,处理后的水色度和气味较重等问题。为此,生化后出水需要进行深度处理,但是深度处理费用昂贵,成本压力大。因此,寻求和研究新的焦化废水处理工艺是提高废水处理效能的关键所在。
发明内容
[0004] 本发明所要解决的技术问题是提供一种焦化废水处理系统及处理方法,解决传统焦化废水处理工艺对难降解复杂有机污染物去除效果不理想而导致出水中C0D、氨氮、总氮及色度不达标等问题,与传统工艺相比,占地面积小、耗能低,并具有高效的废水处理效能,降低废水处理的运行成本,具有处理负荷高、能耗低、产泥量少的特点。
[0005] 为实现上述目的,本发明提供一种焦化废水处理系统,它包括上流式厌氧污泥床反应器、缺氧反硝化生物滤池和好氧硝化生物滤池,所述的缺氧反硝化生物滤池和好氧硝化生物滤池组成缺氧反硝化生物滤池/好氧硝化生物滤池系统,上流式厌氧污泥床反应器包括焦化废水原水进水管、上流式厌氧污泥床反应器本体、厌氧颗粒污泥床区、厌氧悬浮污泥层区、三相分离器、甲烷集气室、过流缝、上循环□、回流管、回流栗、甲烷气输送管、固液沉降分离区、出水渠、出水管道和中间水池,所述的焦化废水原水进水管与上流式厌氧污泥床反应器本体相连通,厌氧颗粒污泥床区设置在上流式厌氧污泥床反应器本体下部,厌氧悬浮污泥层区设置在厌氧颗粒污泥床区上部,上流式厌氧污泥床反应器本体池壁间设置过流缝,三相分离器设置在上流式厌氧污泥床反应器本体内、厌氧悬浮污泥层区上部,三相分离器上部为固液沉降分离区,上循环口设置在厌氧污泥床反应器本体上侧,回流管一端连通上循环口,回流管另一端通过回流栗与厌氧污泥床反应器本体下部连通;三相分离器一端连接甲烷集气室,甲烷集气室连接甲烷气输送管,在上循环口上部设置出水渠,出水渠通过出水管道与中间水池连接;缺氧反硝化生物滤池包括提升栗、进水管道、缺氧反硝化生物滤池本体、反硝化生物滤料层、缺氧反硝化生物滤池布水系统、清水区、出水渠、出水管和缺氧反硝化生物滤池配水室,进水管道一端与上流式厌氧污泥床反应器中间水池连接,另一端通过提升栗后与缺氧反硝化生物滤池本体下部连通,缺氧反硝化生物滤池配水室设置在缺氧反硝化生物滤池本体下部,缺氧反硝化生物滤池布水系统设置在缺氧反硝化生物滤池配水室内,反硝化生物滤料层设置在缺氧反硝化生物滤池布水系统上部,清水区在反硝化生物滤料层的上部,在清水区开有出水渠,出水渠通过出水管连接好氧硝化生物滤池本体下部;好氧硝化生物滤池包括好氧硝化生物滤池配水室、好氧硝化生物滤池布水系统、好氧硝化生物滤池本体、硝化生物滤料层、清水区、出水渠、出水管和中间水池,好氧硝化生物滤池配水室设置在好氧硝化生物滤池本体下部,好氧硝化生物滤池布水系统设置在好氧硝化生物滤池配水室内,硝化生物滤料层设置在好氧硝化生物滤池配水室上部,硝化生物滤料层上部是清水区,清水区与出水渠连通,出水渠通过出水管连接中间水池。
[0006] 所述的一种焦化废水处理系统还包括多级铁碳微电解耦合芬顿氧化床反应器和沉淀池,多级铁碳微电解耦合芬顿氧化床反应器包括提升水栗、进水管道、过氧化氢投加装置、进水管道混合器、配水室、多级铁碳微电解耦合芬顿氧化床反应器本体、取换料口、单质铁和颗粒活性碳混合物层、出水澄清区、筛板布水系统、排泥口、反应器出水渠和出水管,沉淀池包括沉淀池本体、出水管道和排泥管道,所述的进水管道一端与好氧硝化生物滤池中间水池相连接,另一端通过提升水栗后连通多级铁碳微电解耦合芬顿氧化床反应器本体下部,在提升水栗与多级铁碳微电解耦合芬顿氧化床反应器本体之间的一段进水管道上设置过氧化氢投加装置和进水管道混合器,配水室设置在多级铁碳微电解耦合芬顿氧化床反应器本体下部,在配水室下部设置排泥口,单质铁和颗粒活性碳混合物层设置在多级铁碳微电解耦合芬顿氧化床反应器本体内、配水室上部,在单质铁和颗粒活性碳混合物层下部设置筛板布水系统,在单质铁和颗粒活性碳混合物层左侧设置取换料口,单质铁和颗粒活性碳混合物层上部为出水澄清区,出水澄清区连通反应器出水渠,反应器出水渠通过出水管与沉淀池相连,沉淀池本体中上部连接出水管道,底部连接排泥管道。
[0007] 所述的单质铁和颗粒活性碳混合物层、筛板布水系统、取换料口设置多组。
[0008] 所述的多级铁碳微电解耦合芬顿氧化床反应器还包括上循环口、回流管道、循环栗和下循环口,上循环口设置在反应器出水渠底部,下循环口设置在配水室上部,回流管道一端连接上循环口,另一端穿过循环栗后连接下循环口。
[0009] 所述的多级铁碳微电解耦合芬顿氧化床反应器还包括pH在线监测仪、碱液自动投加系统和出水管道混合器,PH在线监测仪、碱液自动投加系统和出水管道混合器设置在反应器出水渠与沉淀池之间的出水管上。
[0010] 所述的一种焦化废水处理系统还包括好氧硝化生物滤池和缺氧反硝化生物滤池,好氧硝化生物滤池和缺氧反硝化生物滤池组成了好氧硝化生物滤池/缺氧反硝化生物滤池系统,好氧硝化生物滤池包括进水管道、配水室、布水系统、球形轻质多孔生物滤料层、好氧硝化生物滤池本体、出水区、出水渠和连接管道,进水管道一端与沉淀池出水管道相连接,另一端连通好氧硝化生物滤池本体,配水室设置在好氧硝化生物滤池本体下部,布水系统设置在配水室内,在布水系统上部设置球形轻质多孔生物滤料层,球形轻质多孔生物滤料层上部为出水区,出水区开有出水渠,出水渠通过连接管道与缺氧反硝化生物滤池连接;缺氧反硝化生物滤池包括配水区、布水系统、反硝化生物滤料层、缺氧反硝化生物滤池本体、清水区、出水渠和排放管道,配水区设置在缺氧反硝化生物滤池本体下部,布水系统设置在配水区上部,在布水系统上部设置反硝化生物滤料层,反硝化生物滤料层上部为清水区,清水区上部开有出水渠,出水渠底部连通排放管道;缺氧反硝化生物滤池还包括碳源储罐和碳源投放栗,碳源储罐和碳源投放栗设置在好氧硝化生物滤池和缺氧反硝化生物滤池之间的连接管道上。
[0011] 所述的好氧硝化生物滤池还包括高效空气扩散器系统、在线溶解氧测定仪和PLC计算机工作系统,高效空气扩散器系统包括控制线缆、变频器、鼓风机和空气管道,空气管道一端伸入好氧硝化生物滤池本体、硝化生物滤料层下部,另一端连接鼓风机,鼓风机通过控制线缆与变频器相连接,变频器通过控制线缆与PLC计算机工作系统相连接,所述的在线溶解氧测定仪连接在出水渠的出水管上,其输出信号与PLC计算机工作系统相连接。
[0012] 在所述的缺氧反硝化生物滤池和好氧硝化生物滤池之间还设置有硝化液回流管道和硝化液回流栗,硝化液回流管道一端连通好氧硝化生物滤池中间水池,另一端连接缺氧反硝化生物滤池进水管道,在硝化液回流管道中端设置硝化液回流栗。
[0013] —种焦化废水处理系统及方法,其具体技术方案为:
[0014] 1、焦化废水由焦化废水原水进水管自下而上进入上流式厌氧污泥床反应器,上流式厌氧污泥床反应器内有预先接种并驯化好的适应焦化废水水质的厌氧颗粒污泥床区及厌氧悬浮污泥层区,厌氧颗粒污泥床区和厌氧悬浮污泥层区中分别生长有以颗粒和絮状污泥状态存在的水解酸化菌和产甲烷菌等多种微生物,在厌氧条件下水解酸化菌首先将废水中的大部分复杂大分子有机物进行分解并转化为如有机酸等小分子物质,同时厌氧氨氧化菌和反硝化细菌利用废水中的碳源可对废水中的氨氮和硝态氮进行部分厌氧氨氧化和反硝化作用而完成脱除部分氮,然后产甲烷菌可将有机酸等小分子物质进一步分解为以甲烷为主的生物气,最终使水中的有机物和氮的含量得以降低。随着废水水流不断上升流动,导致甲烷气、水、污泥进入三相分离器中,甲烷气首先被集气罩收集分离,并通过甲烷集气室和甲烷气输送管排出上流式厌氧污泥床反应器,而污泥和废水则通过三相分离器与反应器池壁间的过流缝进入固液沉降分离区进行固液分离,部分废水经上循环口和回流管再由回流栗回流至反应器底部下与原水混合一起进入上流式厌氧污泥床反应器,通过过流缝进入固液沉降分离区的废水和污泥靠重力作用进行分离,密度较水重的污泥则沉降分离并通过过流缝重新回落至反应器中,而澄清的出水则溢流进入出水渠并通过出水管道进入中间水池。
[0015] 2、经过上流式厌氧污泥床反应器处理后进入中间水池的废水,首先由提升栗并经进水管道送入缺氧反硝化生物滤池,缺氧反硝化生物滤池内设有缺氧反硝化生物滤池布水系统和填装其上的反硝化生物滤料层,该生物滤料上面附着生长有高密度的专性反硝化菌,经过上流式厌氧污泥床反应器处理后仍含有大量有机物和氨氮的焦化废水与经好氧硝化生物滤池处理后通过硝化液回流栗和硝化液回流管道回流到进水端来的富含硝酸盐氮的硝化液混合,然后共同进入缺氧反硝化生物滤池,并经缺氧反硝化生物滤池配水室、缺氧反硝化生物滤池布水系统将废水送入反硝化生物滤料层,反硝化生物滤料层上的专性反硝化菌利用废水中的有机物作为碳源,将来自于好氧硝化生物滤池回流硝化液中的硝酸盐氮还原为氮气,从而实现脱氮和去除有机物的功能,同时生物滤料具有过滤截留悬浮物的作用,一方面使专性反硝化菌不易流失,同时使废水得到澄清;缺氧反硝化生物滤池的出水流经清水区、出水渠并通过出水管流入好氧硝化生物滤池,并经好氧硝化生物滤池配水室、好氧硝化生物滤池布水系统将废水送入硝化生物滤料层;生长在硝化生物滤料层上的少量除碳菌和大量专性硝化菌,在鼓风机、空气管道和安装在池内硝化生物滤料层下部的高效空气扩散器系统向水中供氧的条件下,除碳菌将废水中剩余的易降解有机物通过微生物的新陈代谢氧化为二氧化碳和水,专性硝化菌将废水中的氨氮氧化为硝酸盐氮,其出水经清水区、出水渠并通过出水管进入中间水池,该出水一部分根据计算的回流比由硝化液回流栗和硝化液回流管道回流到缺氧反硝化生物滤池的进水端进入缺氧反硝化生物滤池进行反硝化脱氮,剩余的出水进入多级铁碳微电解耦合芬顿氧化床反应器进行再处理;鼓风机的供气量由在线溶解氧测定仪所测数据反馈给PLC计算机工作系统进行计算,再通过控制线缆将控制信号传输给变频器来调节鼓风机的转速,使鼓风机提供合适的供气量。
[0016] 3、中间水池中的好氧硝化生物滤池出水,经调节pH至3.0-5.0,然后由提升水栗、进水管道并经管道混合器送入多级铁碳微电解耦合芬顿氧化床反应器进行氧化处理;过氧化氢投加装置投加的过氧化氢经管道混合器与由进水管道输送来的废水混合后进入多级铁碳微电解耦合芬顿氧化床反应器配水室,在多级铁碳微电解耦合芬顿氧化床反应器内的筛板布水系统上部分级填装有混合均匀的单质铁和颗粒活性碳混合物层,该反应器出水渠中设置有上循环口,上循环口通过回流管道、循环栗和配水室侧壁的下循环口相连接,废水经由筛板布水系统向上流经多级铁碳微电解耦合芬顿氧化床,通过铁碳微电解产生的羟基的氧化还原作用去除废水中的部分杂环类有机物和色度,同时利用微电解产生的Fe2+与废水中投加的过氧化氢构成芬顿(Fenton)试剂的强氧化性,在铁碳微电解-Fenton耦合氧化体系内使废水中的难降解多环、杂环类有机物和有毒有害物质开环、断链降解为易被微生物吸收降解的小分子物质、氨氮、水和二氧化碳,由于铁碳微电解耦合芬顿氧化床设计为多级叠加,水流为上向流柱推形式,所以每一级的氧化对象和产生的氧化后物质均不同,一般来讲从下至上所氧化对象由难变易,确保了反应器最终的氧化效果。由于通过该反应器处理后的溢流出水具有强酸性,需进行中和处理,所以反应器出水渠的溢流出水经过设置在出水管上的PH在线监测仪,将监控信号反馈到碱液自动投加系统,并由碱液自动投加系统的PLC系统根据流量和监测的pH值向管道混合器进行碱液自动精确投加混合,以实现程序调节PH值至6〜9,经过碱液投加中和以后的处理出水排入沉淀池,以促进酸碱中和过程生成的Fe (OH) JPFe(OH) 3等胶体通过沉淀池进行絮凝沉淀,中和后的澄清液由出水管道排入下一个处理单元,而沉淀污泥则由排泥管道排出进行脱水处置。
[0017] 所述的一种焦化废水处理方法,经过多级铁碳微电解耦合芬顿氧化床反应器处理后的废水由出水管道送入后置反硝化脱氮生物滤池处理系统进行进一步的脱氮除碳,该系统的功能是将前段工序在对难降解多环、杂环类有机物和有毒有害物质开环、断链降解为易被微生物吸收降解的小分子有机物、氨氮进行进一步处理。出水管道送来的废水首先由进水管道进入好氧硝化生物滤池的配水区并经布水系统进入球形轻质多孔生物滤料层进行生物好氧氧化处理,球形轻质多孔生物滤料层填装于布水系统上部,通过鼓风机、供气管道和安装在池内的高效空气扩散器系统向池内水中供氧,附着生长在球形轻质多孔生物滤料层上的专性好氧微生物在有氧呼吸的条件下,通过其新陈代谢作用将废水中剩余的小分子有机污染物直接分解为二氧化碳和水,将氨氮氧化为硝酸盐氮,好氧净化后的废水由出水区进入出水渠;并由连接管道送入缺氧反硝化生物滤池的配水区并经布水系统进入反硝化生物滤料层进行反硝化脱氮处理,反硝化生物滤料层上附着生长的专性反硝化菌在外加碳源的条件下将废水中的硝酸盐氮还原为氮气而完成脱氮过程,同时使废水中的大部分悬浮物被截留在反硝化生物滤料层的滤料间空隙中,使废水得到澄清,最终处理出水由清水区并经出水渠通过排放管道排出,最终所排出的焦化尾水中的C0D、氨氮、总氮和色度等指标能稳定达到国家《污水综合排放标准》(GB8978-1996)和《钢铁工业水污染物排放标准》(GB123456-2012)—级排放标准,反硝化过程中所需的外加碳源可以选用甲醇、乙酸、乙酸钠或葡萄糖等物质的溶液,由碳源储罐储存并经碳源投加栗根据计算需要精确投加于缺氧反硝化生物滤池的进水端管道中。
[0018] 本发明所提出的一种焦化废水处理系统及处理方法,解决了传统焦化废水处理工艺对难降解复杂有机污染物去除效果不理想而导致出水中C0D、氨氮、总氮及色度不达标等问题,与传统工艺相比,占地面积小、耗能低,并具有高效的废水处理效能,降低废水处理的运行成本,具有处理负荷高、能耗低、产泥量少的特点。
附图说明
[0019] 图1是本发明各处理单元工艺流程示意图。
[0020] 图2是上流式厌氧污泥床反应器结构和系统示意图。
[0021] 图3是缺氧反硝化生物滤池/好氧硝化生物滤池结构、系统、控制示意图。
[0022]图4是多级铁碳微电解耦合芬顿氧化床反应器及沉淀池的结构、系统、控制示意图。
[0023] 图5是好氧硝化生物滤池/缺氧反硝化生物滤池的结构、系统、控制示意图。
[0024] 图中:A、上流式厌氧污泥床反应器,B、缺氧反硝化生物滤池,C、好氧硝化生物滤池,H1^ B和C组成的缺氧反硝化生物滤池/好氧硝化生物滤池系统,D、多级铁碳微电解耦合芬顿氧化床反应器,E、沉淀池;F、好氧硝化生物滤池,G、缺氧反硝化生物滤池,H2、好氧硝化生物滤池/缺氧反硝化生物滤池系统;
[0025] 1、焦化废水原水进水管,2、上流式厌氧污泥床反应器本体,3、厌氧颗粒污泥床区,
4、厌氧悬浮污泥层区,5、三相分离器,6、澄清的出水,7、甲烷集气室,8、过流缝,9、上循环口,10、回流管,11、回流栗,12、甲烷气输送管,13、固液沉降分离区,14、出水渠,15、出水管道,16、中间水池;17、提升栗,18、进水管道,19、缺氧反硝化生物滤池,20、反硝化生物滤料层,21、缺氧反硝化生物滤池布水系统,22、清水区,23、出水渠,24、出水管,25、缺氧反硝化生物滤池配水室,26、好氧硝化生物滤池配水室,27、好氧硝化生物滤池布水系统,28、高效空气扩散器系统,29、好氧硝化生物滤池,30、硝化生物滤料层,31、清水区,32、出水渠,33、硝化液回流管道,34、硝化液回流栗,35、在线溶解氧测定仪,36、PLC计算机工作系统,37、控制线缆,38、变频器,39、鼓风机,40、空气管道,41、出水管,42、中间水池,43、提升水栗,44、进水管道,45、过氧化氢投加装置,46、管道混合器,47、配水室,48、碳源储罐,49、多级铁碳微电解耦合芬顿氧化床反应器,50、取换料口,51、单质铁和颗粒活性碳混合物层,52、出水澄清区,53、筛板布水系统,54、上循环口,55、回流管道,56、循环栗,57、下循环口,58、排泥口,59、反应器出水渠,60、pH在线监测仪,61、出水管,62、碱液自动投加系统,63、管道混合器,64、沉淀池,65、出水管道,66、排泥管道,67、进水管道,68、配水室,69、布水系统,70、球形轻质多孔生物滤料层,71、好氧硝化生物滤池,72、出水区,73、出水渠,74、连接管道,
75、配水区,76、布水系统,77、反硝化生物滤料层,78、缺氧反硝化生物滤池,79、清水区,80、出水渠,81、排放管道,82、碳源投加栗。
具体实施方式
[0026] 本发明具体实施方式结合附图,进行详细的描述。
[0027] 一种焦化废水处理系统,它包括上流式厌氧污泥床反应器A、缺氧反硝化生物滤池B和好氧硝化生物滤池C,所述的缺氧反硝化生物滤池和好氧硝化生物滤池组成缺氧反硝化生物滤池/好氧硝化生物滤池系统H1,上流式厌氧污泥床反应器包括焦化废水原水进水管1、上流式厌氧污泥床反应器本体2、厌氧颗粒污泥床区3、厌氧悬浮污泥层区4、三相分离器5、甲烷集气室7、过流缝8、上循环口 9、回流管10、回流栗11、甲烷气输送管12、固液沉降分离区13、出水渠14、出水管道15和中间水池16,所述的焦化废水原水进水管与上流式厌氧污泥床反应器本体相连通,厌氧颗粒污泥床区设置在上流式厌氧污泥床反应器本体下部,厌氧悬浮污泥层区设置在厌氧颗粒污泥床区上部,上流式厌氧污泥床反应器本体池壁间设置过流缝,三相分离器设置在上流式厌氧污泥床反应器本体内、厌氧悬浮污泥层区上部,三相分离器上部为固液沉降分离区,上循环口设置在厌氧污泥床反应器本体上侧,回流管一端连通上循环口,回流管另一端通过回流栗与厌氧污泥床反应器本体下部连通;三相分离器一端连接甲烷集气室,甲烷集气室连接甲烷气输送管,在上循环口上部设置出水渠,出水渠通过出水管道与中间水池连接;缺氧反硝化生物滤池包括提升栗17、进水管道18、缺氧反硝化生物滤池本体19、反硝化生物滤料层20、缺氧反硝化生物滤池布水系统21、清水区22、出水渠23、出水管24和缺氧反硝化生物滤池配水室25,进水管道一端与上流式厌氧污泥床反应器中间水池连接,另一端通过提升栗后与缺氧反硝化生物滤池本体下部连通,缺氧反硝化生物滤池配水室设置在缺氧反硝化生物滤池本体下部,缺氧反硝化生物滤池布水系统设置在缺氧反硝化生物滤池配水室内,反硝化生物滤料层设置在缺氧反硝化生物滤池布水系统上部,清水区在反硝化生物滤料层的上部,在清水区开有出水渠,出水渠通过出水管连接好氧硝化生物滤池本体下部;好氧硝化生物滤池包括好氧硝化生物滤池配水室26、好氧硝化生物滤池布水系统27、好氧硝化生物滤池本体29、硝化生物滤料层30、清水区31、出水渠32、出水管41和中间水池42,好氧硝化生物滤池配水室设置在好氧硝化生物滤池本体下部,好氧硝化生物滤池布水系统设置在好氧硝化生物滤池配水室内,硝化生物滤料层设置在好氧硝化生物滤池配水室上部,硝化生物滤料层上部是清水区,清水区与出水渠连通,出水渠通过出水管连接中间水池。
[0028] 所述的好氧硝化生物滤池还包括高效空气扩散器系统、在线溶解氧测定仪和PLC计算机工作系统,高效空气扩散器系统包括控制线缆、变频器、鼓风机和空气管道,空气管道一端伸入好氧硝化生物滤池本体、硝化生物滤料层下部,另一端连接鼓风机,鼓风机通过控制线缆与变频器相连接,变频器通过控制线缆与PLC计算机工作系统相连接,所述的在线溶解氧测定仪一端连接在出水渠的出水管上,其输出信号与PLC计算机工作系统相连接。
[0029] 在所述的缺氧反硝化生物滤池和好氧硝化生物滤池之间还设置有硝化液回流管道和硝化液回流栗,硝化液回流管道一端连通好氧硝化生物滤池中间水池,另一端连接缺氧反硝化生物滤池进水管道,在硝化液回流管道中端设置硝化液回流栗。
[0030] 所述的一种焦化废水处理系统还包括多级铁碳微电解耦合芬顿氧化床反应器D和沉淀池E,多级铁碳微电解耦合芬顿氧化床反应器包括提升水栗43、进水管道44、过氧化氢投加装置45、进水管道混合器46、配水室47、多级铁碳微电解耦合芬顿氧化床反应器本体49、取换料口 50、单质铁和颗粒活性碳混合物层51、出水澄清区52、筛板布水系统53、排泥口 58、反应器出水渠59和出水管61,沉淀池包括沉淀池本体64、出水管道65和排泥管道66,所述的进水管道一端与好氧硝化生物滤池中间水池相连接,另一端通过提升水栗后连通多级铁碳微电解耦合芬顿氧化床反应器本体下部,在提升水栗与多级铁碳微电解耦合芬顿氧化床反应器本体之间的一段进水管道上设置过氧化氢投加装置和进水管道混合器,配水室设置在多级铁碳微电解耦合芬顿氧化床反应器本体下部,在配水室下部设置排泥口,单质铁和颗粒活性碳混合物层设置在多级铁碳微电解耦合芬顿氧化床反应器本体内、配水室上部,在单质铁和颗粒活性碳混合物层下部设置筛板布水系统,在单质铁和颗粒活性碳混合物层左侧设置取换料口,单质铁和颗粒活性碳混合物层上部为出水澄清区,出水澄清区连通反应器出水渠,反应器出水渠通过出水管与沉淀池相连,沉淀池本体中上部连接出水管道,底部连接排泥管道。
[0031] 所述的单质铁和颗粒活性碳混合物层、筛板布水系统、取换料口设置多组。
[0032] 所述的多级铁碳微电解耦合芬顿氧化床反应器还包括上循环口 54、回流管道55、循环栗56和下循环口 57,上循环口设置在反应器出水渠底部,下循环口设置在配水室上部,回流管道一端连接上循环口,另一端穿过循环栗后连接下循环口。
[0033] 所述的多级铁碳微电解耦合芬顿氧化床反应器还包括pH在线监测仪60、碱液自动投加系统62和出水管道混合器63,pH在线监测仪、碱液自动投加系统和出水管道混合器设置在反应器出水渠与沉淀池之间的出水管上。
[0034] 所述的一种焦化废水处理系统还包括好氧硝化生物滤池F和缺氧反硝化生物滤池G,好氧硝化生物滤池和缺氧反硝化生物滤池组成了好氧硝化生物滤池/缺氧反硝化生物滤池系统H2,好氧硝化生物滤池包括进水管道67、配水室68、布水系统69、球形轻质多孔生物滤料层70、好氧硝化生物滤池本体71、出水区72、出水渠73和连接管道74,进水管道一端与沉淀池出水管道相连接,另一端连通好氧硝化生物滤池本体,配水室设置在好氧硝化生物滤池本体下部,布水系统设置在配水室内,在布水系统上部设置球形轻质多孔生物滤料层,球形轻质多孔生物滤料层上部为出水区,出水区开有出水渠,出水渠通过连接管道与缺氧反硝化生物滤池连接;好氧硝化生物滤池还包括高效空气扩散器系统28、在线溶解氧测定仪35和PLC计算机工作系统36,高效空气扩散器系统包括控制线缆37、变频器38、鼓风机39和空气管道40,空气管道一端伸入好氧硝化生物滤池本体、球形轻质多孔生物滤料层下部,另一端连接鼓风机,鼓风机通过控制线缆与变频器相连接,变频器通过控制线缆与PLC计算机工作系统相连接,所述的在线溶解氧测定仪一端连接在出水渠的出水管上,其输出信号与PLC计算机工作系统相连接;缺氧反硝化生物滤池包括配水区75、布水系统
76、反硝化生物滤料层77、缺氧反硝化生物滤池本体78、清水区79、出水渠80和排放管道81,配水区设置在缺氧反硝化生物滤池本体下部,布水系统设置在配水区上部,在布水系统上设置反硝化生物滤料层,反硝化生物滤料层上部为清水区,清水区上部开有出水渠,出水渠底部连通排放管道;缺氧反硝化生物滤池还包括碳源储罐48和碳源投放栗82,碳源投放点设置在好氧硝化生物滤池和缺氧反硝化生物滤池之间的连接管道上。
[0035] —种焦化废水处理方法,其具体技术方案为:
[0036] 1、焦化废水由焦化废水原水进水管I自下而上进入上流式厌氧污泥床反应器2,上流式厌氧污泥床反应器2内有预先接种并驯化好的适应焦化废水水质的厌氧颗粒污泥床区3及厌氧悬浮污泥层区4,3和4中分别生长有以颗粒和絮状污泥状态存在的水解酸化菌和产甲烷菌等多种微生物,在厌氧条件下水解酸化菌首先将废水中的大部分复杂大分子有机物进行分解并转化为如有机酸等小分子物质,同时厌氧氨氧化菌和反硝化细菌利用废水中的碳源可对废水中的氨氮和硝态氮进行部分厌氧氨氧化和反硝化作用而完成脱除部分氮,然后产甲烷菌可将有机酸等小分子物质进一步分解为以甲烷为主的生物气,最终使水中的有机物和氮的含量得以降低。随着废水水流不断上升流动,导致甲烷气、水、污泥进入三相分离器5中,甲烷气首先被集气罩收集分离,并通过甲烷集气室7和甲烷气输送管12排出上流式厌氧污泥床反应器2,而污泥和废水则通过三相分离器5与反应器池壁间的过流缝8进入固液沉降分离区13进行固液分离,部分废水经上循环口 9和回流管10再由回流栗11回流至反应器底部与原水混合一起进入上流式厌氧污泥床反应器2,通过过流缝8进入固液沉降分离区13的废水和污泥靠重力作用进行分离,密度较水重的污泥则沉降分离并通过过流缝8重新回落至反应器中,而澄清的出水6则溢流进入出水渠14并通过出水管道15进入中间水池16。
[0037] 2、经过上流式厌氧污泥床反应器2处理后进入中间水池16的废水,首先由提升栗17并经进水管道18送入缺氧反硝化生物滤池19,缺氧反硝化生物滤池19内设有缺氧反硝化生物滤池布水系统21和填装其上的反硝化生物滤料层20,该生物滤料上面附着生长有高密度的专性反硝化菌,经过上流式厌氧污泥床反应器2处理后仍含有大量有机物和氨氮的焦化废水与经好氧硝化生物滤池29处理后通过硝化液回流栗34和硝化液回流管道33回流到进水端来的富含硝酸盐氮的硝化液混合,然后共同进入缺氧反硝化生物滤池19,并经缺氧反硝化生物滤池配水室25、缺氧反硝化生物滤池布水系统21将废水送入反硝化生物滤料层20,反硝化生物滤料层20上的专性反硝化菌利用废水中的有机物作为碳源,将来自于好氧硝化生物滤池29回流硝化液中的硝酸盐氮还原为氮气,从而实现脱氮和去除有机物的功能,同时生物滤料具有过滤截留悬浮物的作用,一方面使专性反硝化菌不易流失,同时使废水得到澄清;缺氧反硝化生物滤池19的出水流经清水区22、出水渠23并通过出水管24流入好氧硝化生物滤池29,并经好氧硝化生物滤池配水室26、好氧硝化生物滤池布水系统27将废水送入硝化生物滤料层30 ;生长在硝化生物滤料层30上的少量除碳菌和大量专性硝化菌,在鼓风机39、空气管道40和安装在池内硝化生物滤料层30下部的高效空气扩散器系统28向水中供氧的条件下,除碳菌将废水中剩余的易降解有机物通过微生物的新陈代谢氧化为二氧化碳和水,专性硝化菌将废水中的氨氮氧化为硝酸盐氮,其出水经清水区31、出水渠32并通过出水管41进入中间水池42,该出水一部分根据计算的回流比由硝化液回流栗34和硝化液回流管道33回流到缺氧反硝化生物滤池19的进水端进入缺氧反硝化生物滤池19进行反硝化脱氮,剩余的出水进入多级铁碳微电解耦合芬顿氧化床反应器49进行再处理;鼓风机39的供气量由在线溶解氧测定仪35所测数据反馈给PLC计算机工作系统36进行计算,再通过控制线缆37将控制信号传输给变频器38来调节鼓风机的转速,使鼓风机提供合适的供气量。
[0038] 3、中间水池42中的好氧硝化生物滤池出水,经调节pH至3.0-5.0,然后由提升水栗43、进水管道44并经管道混合器46送入多级铁碳微电解耦合芬顿氧化床反应器49进行氧化处理;过氧化氢投加装置45投加的过氧化氢经管道混合器46与由进水管道44输送来的废水混合后进入铁碳微电解耦合芬顿氧化床反应器配水室47,在多级铁碳微电解耦合芬顿氧化床反应器49内的筛板布水系统53上部分级填装有混合均匀的单质铁和颗粒活性碳混合物层51,该反应器出水渠59中设置有上循环口 54,上循环口 54通过回流管道55、循环栗56和配水室47侧壁的下循环口 57相连接,废水经由筛板布水系统53向上流经多级铁碳微电解耦合芬顿氧化床,通过铁碳微电解产生的羟基的氧化还原作用去除废水中的部分杂环类有机物和色度,同时利用微电解产生的Fe2+与废水中投加的过氧化氢构成芬顿(Fenton)试剂的强氧化性,在铁碳微电解-Fenton親合氧化体系内使废水中的难降解多环、杂环类有机物和有毒有害物质开环、断链降解为易被微生物吸收降解的小分子物质、氨氮、水和二氧化碳,由于铁碳微电解耦合芬顿氧化床设计为多级叠加,水流为上向流柱推形式,所以每一级的氧化对象和产生的氧化后物质均不同,一般来讲从下至上所氧化对象由难变易,确保了反应器最终的氧化效果。由于通过该反应器处理后的溢流出水具有强酸性,需进行中和处理,所以反应器出水渠59的溢流出水经过设置在出水管61上的pH在线监测仪60,将监控信号反馈到碱液自动投加系统62,并由碱液自动投加系统62的PLC系统根据流量和监测的PH值向管道混合器63进行碱液自动精确投加混合,以实现程序调节pH值至6〜9,经过碱液投加中和以后的处理出水排入沉淀池64,以促进酸碱中和过程生成的Fe (OH) 2和Fe (OH) 3等胶体通过沉淀池64进行絮凝沉淀,中和后的澄清液由出水管道65排入下一个处理单元,而沉淀污泥则由排泥管道66排出进行脱水处置。
[0039] 4、经过多级铁碳微电解耦合芬顿氧化床反应器49处理后的废水由出水管道65送入后置反硝化脱氮生物滤池处理系统进行进一步的脱氮除碳,该系统的功能是将前段工序在对难降解多环、杂环类有机物和有毒有害物质开环、断链降解为易被微生物吸收降解的小分子有机物、氨氮进行进一步处理。出水管道65送来的废水首先由进水管道67进入好氧硝化生物滤池71的配水区68并经布水系统69进入球形轻质多孔生物滤料层70进行生物好氧氧化处理,球形轻质多孔生物滤料层70填装于布水系统69上部,通过鼓风机75、供气管道76和安装在池内的高效空气扩散器系统77向池内水中供氧,附着生长在球形轻质多孔生物滤料层70上的专性好氧微生物在有氧呼吸的条件下,通过其新陈代谢作用将废水中剩余的小分子有机污染物直接分解为二氧化碳和水,将氨氮氧化为硝酸盐氮,好氧净化后的废水由出水区72进入出水渠73 ;并由连接管道74送入缺氧反硝化生物滤池78的配水区75并经布水系统76进入反硝化生物滤料层77进行反硝化脱氮处理,反硝化生物滤料层77上附着生长的专性反硝化菌在外加碳源的条件下将废水中的硝酸盐氮还原为氮气而完成脱氮过程,同时使废水中的大部分悬浮物被截留在反硝化生物滤料层的滤料间空隙中,使废水得到澄清,最终处理出水由清水区79并经出水渠80通过排放管道81排出,最终处理后由排放管道81排出的焦化废水中的COD、氨氮、总氮和色度等指标能稳定达到国家《污水综合排放标准》(GB8978-1996)和《钢铁工业水污染物排放标准》(GB123456-2012)一级排放标准,反硝化过程中所需的外加碳源可以选用甲醇、乙酸、乙酸钠或葡萄糖等物质的溶液,由碳源储罐48储存并经碳源投加栗82根据计算需要精确投加于缺氧反硝化生物滤池78的进水端管道中。
[0040] 实施例:一座新建的焦化废水处理厂,处理量为200吨/日,采用本发明处理系统和处理方法,废水经过水质调节后,采用潜污栗将焦化废水栗入上流式厌氧污泥床反应器,并经后续的缺氧反硝化生物滤池/好氧硝化生物滤池系统、多级铁碳微电解耦合芬顿氧化床反应器、好氧硝化生物滤池/缺氧反硝化生物滤池系统进行处理,其主要设计参数如下:进水 ρΗ=6.8-8.0,C0Dcr=1700~2300mg/L, B0D5=250~630 mg/L,总氮=400~500mg/L,氨氮=280-350 mg/L, SS=220mg/L,色度 725 倍。
[0041] 上流式厌氧污泥床:该废水经水质调节后首先进入上流式厌氧污泥床反应器,水力停留时间HRT=24h,进水温度30~35°C,上升流速0.5m/h,进水容积负荷2.5Kg/m3.d,经过该上流式厌氧污泥床反应器处理后的出水指标为:C0Dcr=700~1000mg/L,B0D5=280~450mg/L,总氮=340~420mg/L,氨氮=240~380,SS=120mg/L,色度400倍;该反应器为圆筒形,直径4.6m,有效高度12m。
[0042] 缺氧反硝化生物滤池/好氧硝化生物滤池系统:系统总水力停留时间HRT=8h,回流比600%,其中缺氧反硝化生物滤池池体为长方体结构,内分两格,总尺寸为6X3X7m,单池最大上升流速6.5m/h;好氧硝化生物滤池池体为长方体结构,内分四格,总尺寸为12X3X7m,单池最大上升流速 2m/h,出水指标:C0Dcr=180~200mg/L,B0D5=40~80 mg/L,总氮=140~160mg/L,氨氮=10~20 mg/L, SS=10mg/L,色度 250 倍。
[0043] 多级铁碳微电解耦合芬顿氧化床反应器:共设两座,一用一备,采用圆形池结构,单座尺寸为Φ2.7X6m,水力停留时间HRT=3h,上升流速1.5m/h,出水指标:C0Dcr=80~120mg/L, B0D5=25~48 mg/L,总氮=150~180mg/L,氨氮=25~40 mg/L, SS=20mg/L,色度10倍。
[0044] 好氧硝化生物滤池/缺氧反硝化生物滤池系统:好氧硝化生物滤池水力停留时间HRT=4h,池体为长方体结构,内分三格,两用一备,总尺寸为6X2X7m,单池最高上升流速lm/h ;缺氧反硝化生物滤池池体为长方体结构,内分两格,总尺寸为3X2X6.5m,单池最大上升流速2.7m/h,最终出水指标:C0Dcr彡40mg/L,BOD5S 10 mg/L,总氮彡20 mg/L,氨氮(5 mg/L, SS ( 10mg/L,色度5倍,达到了《污水综合排放标准》(GB8978-)和《钢铁工业水污染物排放标准》(GB13456-2012) —级排放标准。
[0045] 本发明所提出的一种焦化废水处理系统及处理方法,解决了传统焦化废水处理工艺对难降解复杂有机污染物去除效果不理想而导致出水中C0D、氨氮、总氮及色度不达标等问题,与传统工艺相比,占地面积小、耗能低,并具有高效的废水处理效能,降低废水处理的运行成本,具有处理负荷高、能耗低、产泥量少的特点。
Claims (10)
1.一种焦化废水处理系统,其特征在于它包括上流式厌氧污泥床反应器、缺氧反硝化生物滤池和好氧硝化生物滤池,所述的缺氧反硝化生物滤池和好氧硝化生物滤池组成缺氧反硝化生物滤池/好氧硝化生物滤池系统,上流式厌氧污泥床反应器包括焦化废水原水进水管、上流式厌氧污泥床反应器本体、厌氧颗粒污泥床区、厌氧悬浮污泥层区、三相分离器、甲烷集气室、过流缝、上循环□、回流管、回流栗、甲烷气输送管、固液沉降分离区、第一出水渠、第一出水管道和第一中间水池,所述的焦化废水原水进水管与上流式厌氧污泥床反应器本体相连通,厌氧颗粒污泥床区设置在上流式厌氧污泥床反应器本体下部,厌氧悬浮污泥层区设置在厌氧颗粒污泥床区上部,上流式厌氧污泥床反应器本体池壁间设置过流缝,三相分离器设置在上流式厌氧污泥床反应器本体内、厌氧悬浮污泥层区上部,三相分离器上部为固液沉降分离区,上循环口设置在厌氧污泥床反应器本体上侧,回流管一端连通上循环口,回流管另一端通过回流栗与厌氧污泥床反应器本体下部连通;三相分离器一端连接甲烷集气室,甲烷集气室连接甲烷气输送管,在上循环口上部设置第一出水渠,第一出水渠通过第一出水管道与第一中间水池连接;缺氧反硝化生物滤池包括提升栗、进水管道、缺氧反硝化生物滤池本体、反硝化生物滤料层、缺氧反硝化生物滤池布水系统、第一清水区、第二出水渠、第二出水管和缺氧反硝化生物滤池配水室,进水管道一端与上流式厌氧污泥床反应器中间水池连接,另一端通过提升栗后与缺氧反硝化生物滤池本体下部连通,缺氧反硝化生物滤池配水室设置在缺氧反硝化生物滤池本体下部,缺氧反硝化生物滤池布水系统设置在缺氧反硝化生物滤池配水室内,反硝化生物滤料层设置在缺氧反硝化生物滤池布水系统上部,第一清水区在反硝化生物滤料层的上部,在清水区开有第二出水渠,第二出水渠通过第二出水管连接好氧硝化生物滤池本体下部;好氧硝化生物滤池包括好氧硝化生物滤池配水室、好氧硝化生物滤池布水系统、好氧硝化生物滤池本体、硝化生物滤料层、第二清水区、第三出水渠、第三出水管和第二中间水池,好氧硝化生物滤池配水室设置在好氧硝化生物滤池本体下部,好氧硝化生物滤池布水系统设置在好氧硝化生物滤池配水室内,硝化生物滤料层设置在好氧硝化生物滤池配水室上部,硝化生物滤料层上部是第二清水区,第二清水区与第三出水渠连通,第三出水渠通过第三出水管连接第二中间水池。
2.根据权利要求1所述的一种焦化废水处理系统,其特征在于它还包括多级铁碳微电解耦合芬顿氧化床反应器和沉淀池,多级铁碳微电解耦合芬顿氧化床反应器包括提升水栗、进水管道、过氧化氢投加装置、进水管道混合器、配水室、多级铁碳微电解耦合芬顿氧化床反应器本体、取换料口、单质铁和颗粒活性碳混合物层、出水澄清区、筛板布水系统、排泥口、反应器出水渠和反应器出水管,沉淀池包括沉淀池本体、沉淀池出水管道和排泥管道,所述的进水管道一端与好氧硝化生物滤池中间水池相连接,另一端通过提升水栗后连通多级铁碳微电解耦合芬顿氧化床反应器本体下部,在提升水栗与多级铁碳微电解耦合芬顿氧化床反应器本体之间的一段进水管道上设置过氧化氢投加装置和进水管道混合器,配水室设置在多级铁碳微电解耦合芬顿氧化床反应器本体下部,在配水室下部设置排泥口,单质铁和颗粒活性碳混合物层设置在多级铁碳微电解耦合芬顿氧化床反应器本体内、配水室上部,在单质铁和颗粒活性碳混合物层下部设置筛板布水系统,在单质铁和颗粒活性碳混合物层左侧设置取换料口,单质铁和颗粒活性碳混合物层上部为出水澄清区,出水澄清区连通反应器出水渠,反应器出水渠通过出水管与沉淀池相连,沉淀池本体中上部连接反应器出水管,底部连接排泥管道。
3.根据权利要求2所述的一种焦化废水处理系统,其特征在于单质铁和颗粒活性碳混合物层、筛板布水系统、取换料口设置多组。
4.根据权利要求2所述的一种焦化废水处理系统,其特征在于所述的多级铁碳微电解耦合芬顿氧化床反应器还包括反应器上循环口、反应器回流管道、反应器循环栗和反应器下循环口,上循环口设置在反应器出水渠底部,下循环口设置在配水室上部,回流管道一端连接上循环口,另一端穿过循环栗后连接下循环口。
5.根据权利要求2所述的一种焦化废水处理系统,其特征在于所述的多级铁碳微电解耦合芬顿氧化床反应器还包括PH在线监测仪、碱液自动投加系统和出水管道混合器,pH在线监测仪、碱液自动投加系统和出水管道混合器设置在反应器出水渠与沉淀池之间的出水管上。
6.根据权利要求1所述的一种焦化废水处理系统,其特征在于所述的一种焦化废水处理系统还包括好氧硝化生物滤池和缺氧反硝化生物滤池,好氧硝化生物滤池和缺氧反硝化生物滤池组成了好氧硝化生物滤池/缺氧反硝化生物滤池系统,好氧硝化生物滤池包括进水管道、配水室、布水系统、球形轻质多孔生物滤料层、好氧硝化生物滤池本体、出水区、出水渠和连接管道,进水管道一端与沉淀池出水管道相连接,另一端连通好氧硝化生物滤池本体,配水室设置在好氧硝化生物滤池本体下部,布水系统设置在配水室内,在布水系统上部设置球形轻质多孔生物滤料层,球形轻质多孔生物滤料层上部为出水区,出水区开有出水渠,出水渠通过连接管道与缺氧反硝化生物滤池连接;好氧硝化生物滤池还包括高效空气扩散器系统、在线溶解氧测定仪和PLC计算机工作系统,高效空气扩散器系统包括控制线缆、变频器、鼓风机和空气管道,空气管道一端伸入好氧硝化生物滤池本体、球形轻质多孔生物滤料层下部,另一端连接鼓风机,鼓风机通过控制线缆与变频器相连接,变频器通过控制线缆与PLC计算机工作系统相连接,所述的在线溶解氧测定仪一端连接出水渠上的出水管上,其输出信号与PLC计算机工作系统相连接;缺氧反硝化生物滤池包括配水区、布水系统、反硝化生物滤料层、缺氧反硝化生物滤池本体、清水区、出水渠和排放管道,配水区设置在缺氧反硝化生物滤池本体下部,布水系统设置在配水区上部,在布水系统上设置反硝化生物滤料层,反硝化生物滤料层上部为清水区,清水区上部开有出水渠,出水渠底部连通排放管道;缺氧反硝化生物滤池还包括碳源储罐和碳源投放栗,碳源储罐和碳源投放栗将碳源投放于好氧硝化生物滤池和缺氧反硝化生物滤池之间的连接管道上。
7.根据权利要求1所述的一种焦化废水处理系统,其特征在于所述的好氧硝化生物滤池还包括高效空气扩散器系统、在线溶解氧测定仪和PLC计算机工作系统,高效空气扩散器系统包括控制线缆、变频器、鼓风机和空气管道,空气管道一端伸入好氧硝化生物滤池本体、硝化生物滤料层下部,另一端连接鼓风机,鼓风机通过控制线缆与变频器相连接,变频器通过控制线缆与PLC计算机工作系统相连接,所述的在线溶解氧测定仪一端连接出水渠上的出水管上,其输出信号与PLC计算机工作系统相连接。
8.根据权利要求6所述的一种焦化废水处理系统,其特征在于在所述的缺氧反硝化生物滤池和好氧硝化生物滤池之间还设置有硝化液回流管道和硝化液回流栗,硝化液回流管道一端连通好氧硝化生物滤池中间水池,另一端连接缺氧反硝化生物滤池进水管道,在硝化液回流管道中端设置硝化液回流栗。
9.一种焦化废水处理方法,其具体技术方案为: 1)焦化废水由焦化废水原水进水管自下而上进入上流式厌氧污泥床反应器,上流式厌氧污泥床反应器内有预先接种并驯化好的适应焦化废水水质的厌氧颗粒污泥床区及厌氧悬浮污泥层区,随着废水水流不断上升流动,甲烷气、水、污泥进入三相分离器中,甲烷气首先被集气罩收集分离,并通过甲烷集气室和甲烷气输送管排出上流式厌氧污泥床反应器,而污泥和废水则通过三相分离器与反应器池壁间的过流缝进入固液沉降分离区进行固液分离,部分废水经上流式厌氧污泥床反应器的上循环口和回流管再由回流栗回流至反应器底部下与原水混合一起进入上流式厌氧污泥床反应器,通过过流缝进入固液沉降分离区的废水和污泥靠重力作用进行分离,密度较水重的污泥则沉降分离并通过过流缝重新回落至反应器中,而澄清的出水则溢流进入第一出水渠并通过第一出水管道进入第一中间水池; 2)经过上流式厌氧污泥床反应器处理后进入第一中间水池的废水,首先由提升栗并经进水管道送入缺氧反硝化生物滤池,缺氧反硝化生物滤池内设有缺氧反硝化生物滤池布水系统和填装其上的反硝化生物滤料层,该生物滤料上面附着生长有高密度的专性反硝化菌,经过上流式厌氧污泥床反应器处理后仍含有大量有机物和氨氮的焦化废水与经好氧硝化生物滤池处理后通过硝化液回流栗和硝化液回流管道回流到进水端来的富含硝酸盐氮的硝化液混合,然后共同进入缺氧反硝化生物滤池,并经缺氧反硝化生物滤池配水室、缺氧反硝化生物滤池布水系统将废水送入反硝化生物滤料层;缺氧反硝化生物滤池的出水流经第一清水区、第二出水渠并通过第二出水管流入好氧硝化生物滤池,并经好氧硝化生物滤池配水室、好氧硝化生物滤池布水系统将废水送入硝化生物滤料层;其出水经第二清水区、第三出水渠并通过第三出水管进入第二中间水池,该出水一部分根据计算的回流比由硝化液回流栗和硝化液回流管道回流到缺氧反硝化生物滤池的进水端进入缺氧反硝化生物滤池进行反硝化脱氮,剩余的出水进入多级铁碳微电解耦合芬顿氧化床反应器进行再处理;鼓风机的供气量由在线溶解氧测定仪所测数据反馈给PLC计算机工作系统进行计算,再通过控制线缆将控制信号传输给变频器来调节鼓风机的转速,使鼓风机提供合适的供气量; 3)第二中间水池中的好氧硝化生物滤池出水,经预先调节pH至3.0-5.0,然后由提升水栗、进水管道并经管道混合器送入多级铁碳微电解耦合芬顿氧化床反应器进行氧化处理;过氧化氢投加装置投加的过氧化氢经管道混合器与由进水管道输送来的废水混合后进入铁碳微电解耦合芬顿氧化床反应器配水室,在多级铁碳微电解耦合芬顿氧化床反应器内的筛板布水系统上部分级填装有混合均匀的单质铁和颗粒活性碳混合物层,该反应器出水渠中设置有多级铁碳微电解耦合芬顿氧化床反应器上循环口,多级铁碳微电解耦合芬顿氧化床反应器上循环口通过多级铁碳微电解耦合芬顿氧化床反应器回流管道、多级铁碳微电解耦合芬顿氧化床反应器循环栗和配水室侧壁的多级铁碳微电解耦合芬顿氧化床反应器下循环口相连接,废水经由筛板布水系统向上流经多级铁碳微电解耦合芬顿氧化床,铁碳微电解耦合芬顿氧化床设计为多级叠加,水流为上向流柱推形式,反应器出水渠的溢流出水经过设置在出水管上的PH在线监测仪,将监控信号反馈到碱液自动投加系统,并由碱液自动投加系统的PLC系统根据流量和监测的pH值向管道混合器进行碱液自动精确投加混合,以实现程序调节pH值至6〜9,经过碱液投加中和以后的处理出水排入沉淀池,中和后的澄清液由出水管道排入下一个处理单元,而沉淀污泥则由排泥管道排出进行脱水处置;
10.根据权利要求9所述的一种焦化废水处理方法,其特征在于经过多级铁碳微电解耦合芬顿氧化床反应器处理后的废水由出水管道送入后置反硝化脱氮生物滤池处理系统进行进一步的脱氮除碳,出水管道送来的废水首先由进水管道进入好氧硝化生物滤池的配水区并经布水系统进入球形轻质多孔生物滤料层进行生物好氧氧化处理,球形轻质多孔生物滤料层填装于布水系统上部,通过鼓风机、供气管道和安装在池内的高效空气扩散器系统向池内水中供氧,好氧净化后的废水由出水区进入出水渠;并由连接管道送入缺氧反硝化生物滤池的配水区并经布水系统进入反硝化生物滤料层进行反硝化脱氮处理,反硝化生物滤料层上附着生长的专性反硝化菌在外加碳源的条件下将废水中的硝酸盐氮还原为氮气而完成脱氮过程,同时使废水中的大部分悬浮物被截留在反硝化生物滤料层的滤料间空隙中,最终处理出水由清水区并经出水渠通过排放管道排出,反硝化过程中所需的外加碳源选用甲醇、乙酸、乙酸钠或葡萄糖等物质的溶液,由碳源储罐储存并经碳源投加栗根据计算需要精确投加于缺氧反硝化生物滤池的进水端管道中。
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