CN104944689B - 一种处理高氨氮废水的装置及方法 - Google Patents
一种处理高氨氮废水的装置及方法 Download PDFInfo
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- CN104944689B CN104944689B CN201510296033.XA CN201510296033A CN104944689B CN 104944689 B CN104944689 B CN 104944689B CN 201510296033 A CN201510296033 A CN 201510296033A CN 104944689 B CN104944689 B CN 104944689B
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- 239000002351 wastewater Substances 0.000 title claims abstract description 130
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound 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[N].N CVTZKFWZDBJAHE-UHFFFAOYSA-N 0.000 title claims abstract description 45
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- 239000012528 membrane Substances 0.000 claims abstract description 80
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 69
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 69
- 238000005273 aeration Methods 0.000 claims abstract description 59
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 59
- -1 nitrate nitrogen Chemical compound 0.000 claims abstract description 54
- 239000010802 sludge Substances 0.000 claims abstract description 52
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N.[O] PDNNQADNLPRFPG-UHFFFAOYSA-N 0.000 description 1
- 239000002033 PVDF binder Substances 0.000 description 1
- 241000282898 Sus scrofa Species 0.000 description 1
- 235000011114 ammonium hydroxide Nutrition 0.000 description 1
- 230000000703 anti-shock Effects 0.000 description 1
- 238000005842 biochemical reaction Methods 0.000 description 1
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- 239000000149 chemical water pollutant Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000003247 decreasing Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
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- 238000009830 intercalation Methods 0.000 description 1
- 230000002687 intercalation Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 238000011068 load Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000006396 nitration reaction Methods 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-M nitrite anion Chemical compound 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[O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- GQPLMRYTRLFLPF-UHFFFAOYSA-N nitrous oxide Inorganic materials 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[O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 1
- 101700010564 penG Proteins 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N phosphorus Chemical compound 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Abstract
本发明公开了一种处理高氨氮废水的装置及方法。该方法包括如下步骤:接种活性污泥至缺氧池和好氧池内,缺氧池充满活性污泥,开启搅拌器,重复下述步骤:1)开启进水泵,采用序批式进水,按照设计处理量,待处理的高氨氮废水被输入缺氧池,经溢流堰流至好氧池;2)缺氧池内,碳源作用下,废水中硝态氮被还原;开启曝气系统,好氧池内,废水中的氨态氮和有机物被氧化,关闭曝气系统;3)膜分离池内,设计处理量经硝化的废水经膜组件中膜的过滤后被排出;缺氧池和膜分离池内,小于3倍设计处理量的废水回流至缺氧池;缺氧池内,等量的经反硝化的废水通过溢流堰流至好氧池。本发明将A/O工艺与膜分离技术结合,可实现高效的泥水分离,获得稳定的出水水质。
Description
技术领域
[0001] 本发明涉及一种处理高氨氮废水的装置及方法,尤其涉及一种利用A/0工艺和膜 处理技术处理高氨氮废水的装置和方法。
背景技术
[0002] 随着我国水污染日益严重,污水排放标准将不断收紧,传统污水生物处理工艺的 处理效率亟待提高。1989年,YamamotoK等发表首篇浸没式MBR的研究以后,浸没式MBR与外 置式MBR相比,因省略了循环栗而降低了能耗、占地紧凑等优点,逐步在研究和工程应用中 受到重视(YamamotoK,HiasaH,TalatM, etal · 1989 ·Direct solid liquid separation using hoi IIowf ibe membranes in activated sludge aeration tanks) 〇 1998年, Hellinga C等利用氨氧化菌世代时间短于硝化菌,选择合适的污泥停留时间(SRT)淘汰硝 化菌而保留氨氧化菌,从而在单个反应器中首先实现了的亚硝化-反亚硝化过程,即氨氮被 氧化成亚硝氮后直接被还原成氮气(Hellinga C,Schellen AAJC,Mulder JW,van LoosdrechtMCM,Heijen,JJ,1998·The SHARON Process:an innovative method for nitrogen removal from ammonium-rich wastewater.Water Sci·Technol·37,135-142) 〇 这在实际运行中,特别是对高氨氮、低碳氮比废水的处理过程中,将大幅减少好氧段内氨氮 氧化成硝氮所需的供氧量以及兼氧段内硝氮还原成氮气所需外部碳源,从而节约运行成 本,提高脱氮效率。研究表明,该工艺相对传统的全程硝化-反硝化最多可节省25%的曝气 量,40%的外部碳源,并减少40%的生物增量。这引起世界各国学者的持续关注,后续的研 究工作旨在拓宽亚硝化一反亚硝化的应用范围或降低其对运行条件的要求,寻求在传统生 物处理设施中快速实现短程脱氮的控制策略,以及传统生物处理工艺与MBR的优化结合。彭 永臻等通过对短程脱氮积累的长期研究,发明了快速实现SBR短程深度脱氮的方法,并搭建 了缺氧/好氧SBR+厌氧氨氧化+好氧SBR工艺处理低C/N生活污水深度脱氮的装置;黄霞等发 明了两级A/0 MBR脱氮除磷装置,处理生活污水达到回用标准。此外,自动控制系统也逐步 应用于污水处理工艺以方便管理,节省人力。G. Andreotto Ia等在采用在线控制小试SBR装 置处理工业废水,氨氮去除率稳定达到99%;秦德韬等以0RP、pH等作为参数建立实施控制 SBR系统,优化曝气时间实现SBR处理畜禽养殖废水短程脱氮。
[0003] 然而对于处理高氨氮、低C/N废水,上述研究中各种组合工艺虽然可取得良好的脱 氮效果,但仍存在⑶D去除不达标、工艺流程复杂或者较高的污泥浓度(10000mg/L以上)造 成了出水沉淀时间较长,出水水质不稳定等诸多问题。因此,开发出一种利用A/Ο工艺和膜 分离技术处理高氨氮废水的装置及方法迫在眉睫。
发明内容
[0004] 本发明的一个目的是提供一种处理高氨氮废水的装置及方法,该方法将传统A/0 工艺与平板膜分离技术进行优化组合,并且建立实时控制系统,用于处理高氨氮、高C0D、低 碳氮比废水。膜分离技术的引入使得传统A/0工艺能够在较高污泥浓度的条件下,实现高效 的泥水分离,获得稳定的出水水质,同时,该发明采用pH、DO (溶解氧)及ORP (氧化还原电位) 电极对反应器进行连续监测建立自控系统,并通过序批式进水,连续出水的控制策略,实现 了A/0 MBR反应器与实时控制系统的优化结合,简化系统运行控制策略,提高反应器处理效 率。
[0005] 本发明提供的一种处理高氨氮废水的装置,它包括进水系统、反应系统、曝气系 统、碳源投加系统和出水系统;
[0006] 所述反应系统包括一反应器,所述反应器为一容器,被分隔成三部分,依次为缺氧 池、好氧池和膜分离池,所述缺氧池的上方设有搅拌器,所述缺氧池与所述好氧池之间设有 溢流堰,所述好氧池的底部与所述膜分离池的底部连通,所述膜分离池内设有膜组件和液 位计,所述好氧池和所述膜分离池的底部设有回流管,通过回流栗将废水回流至所述缺氧 池内;
[0007] 所述进水系统包括一原水箱,所述原水箱内的废水通过进水栗被输送至所述缺氧 池内;
[0008] 所述曝气系统包括空压机、气体流量计和曝气器,所述曝气器置于所述好氧池中;
[0009] 所述碳源投加系统包括一碳源储箱,所述碳源储箱中的碳源通过碳源投加栗被输 送至所述缺氧池内;
[0010] 所述出水系统包括一产水箱,所述膜组件的出水口通过出水栗与所述产水箱连 接。 Won] 本发明装置在运行过程中,首先,将活性污泥接种至所述缺氧池和所述好氧池中; 待处理的高氨氮废水储存于所述原水箱中,在所述进水栗的作用下,所述高氨氮废水被输 送至所述缺氧池内,通过溢流堰流至所述好氧池内;在所述缺氧池内,在碳源的作用下,废 水中的硝态氮被还原为亚硝态氮,亚硝态氮被还原为氮气(反硝化过程);同时,开启所述曝 气系统,在所述好氧池内,所述高氨氮废水中的氨态氮和有机物被氧化,所述氨态氮被氧化 为亚硝态氮,亚硝态氮被氧化为硝态氮,关闭所述曝气系统(硝化过程);
[0012] 上述兼氧和好氧过程结束之后,由于好氧池和所述膜分离池底部是连通的,一部 分废水经过膜分离系统后,被进一步净化,通过所述出水栗被排至所述产水箱内,所述膜分 离池中的膜组件不仅可以截留所述反应器中的微生物,使反应器中的活性污泥浓度大大增 加,使降解污水的生化反应进行得更迅速更彻底;另一方面,由于膜的高过滤精度,保证了 出水的清澈透明,另一部分废水通过所述回流管在所述回流栗的作用下回流至所述缺氧池 内,由于所述缺氧池处于充满状态,等量的经反硝化的废水流至所述好氧池内进行硝化,继 续分成两部分进行循环处理。
[0013] 上述装置中,所述装置还包括一实时控制系统,所述实施控制系统包括探头、集成 电路箱和数字触控板;所述探头包括PH探头、ORP探头和溶解氧DO探头,均与所述集成电路 箱连接,所述集成电路箱与所述数字触控板连接;所述ORP探头探头置于所述缺氧池内,所 述pH探头和溶解氧探头置于所述好氧池内;
[0014] 通过所述集成电路箱和所述数字触控板,记录和计算所述pH探头、所述ORP探头和 所述溶解氧DO探头的实时监测数据,从而根据设定的程序控制进出水栗、碳源投加栗、曝气 系统及搅拌器的启停,实时控制各反应单元的交替进行。
[0015] 上述装置中,在所述缺氧池的底端设有一回流液进水口,所述混合液通过所述回 流液进水口回流至所述缺氧池内,通过此设置可以使所述缺氧池内经反硝化的废水溢流至 所述好氧池内,与待处理的废水混合,进一步发生硝化,以除去废水中的氨态氮和有机物;
[0016] 所述膜组件置于所述膜分离池的侧壁处,以避免阻碍所述反应器上方的搅拌器的 运行,避免所述反应器及所述搅拌器的损坏;所述膜组件为板框式膜组件,所述板框式膜组 件包括1~2个膜单元,每个所述膜单元由两片膜组成;所述膜的材质为聚偏氟乙烯,孔径< 0. Ιμπι;每个所述膜元件的有效面积为0.5m2;所述膜组件的内部还设有曝气器,依次与另一 空压机和另一气体流量计连接,为所述膜曝气,降低所述膜的污染,延长所述膜的使用寿 命。
[0017] 上述装置中,所述曝气系统中,所述曝气器具体可置于所述好氧池的底部,以充分 曝气。
[0018] 本发明进一步提供了一种利用上述装置处理高氨氮废水的方法,包括如下步骤:
[0019] 接种活性污泥至所述缺氧池和所述好氧池内,整个所述缺氧池充满所述活性污 泥,开启所述搅拌器,重复下述步骤(1)-步骤(3):
[0020] (1)进水阶段:开启所述进水栗,采用序批式进水,按照设计处理量,待处理的所述 高氨氮废水被输入所述缺氧池内,经过所述溢流堰流至所述好氧池内;
[0021] (2)兼氧阶段和好氧阶段:在所述缺氧池内,在碳源的作用下,废水中的硝态氮被 还原为亚硝态氮,亚硝态氮被还原为氮气;开启所述曝气系统,在所述好氧池内,所述高氨 氮废水中的氨态氮和有机物被氧化,所述氨态氮被氧化为亚硝态氮,亚硝态氮被氧化为硝 态氮,关闭所述曝气系统;
[0022] (3)排水和回流阶段:在所述膜分离池内,设计处理量的经硝化的所述废水经过所 述膜组件中的膜的过滤后被排出;在所述缺氧池和所述膜分离池内,小于3倍设计处理量 的废水回流至所述缺氧池内;在所述缺氧池内,等量的经反硝化的废水通过所述溢流堰流 至所述好氧池内。
[0023] 上述方法中,所述实时控制系统全程开启,监测所述高氨氮废水中的氧化还原电 极电位、pH值和溶解氧的大小;
[0024] 所述膜组件中的曝气器全程开启,曝气流量可为5~15L/min,具体可为10~15L/ min、10L/min或15L/min〇
[0025] 上述方法中,所述接种的活性污泥的浓度可为5000mg/L~5500mg/L,具体可为 5500mg/L,可接种来自城市污水处理厂的回流污泥,由于本发明高氨氮废水的处理需要在 高污泥浓度下进行,梯度提高污水的进水浓度,可将活性污泥浓度增高至6500mg/L~ 12000mg/L,具体可提升至6500 ~9500mg/L、6500 ~7500mg/L 或 7500 ~9500mg/L;
[0026] 所述梯度提高分为三个阶段,第一个阶段可为5~10日,进水稀释至为原污水浓度 的1/4;第二个阶段可为5~10日,进水稀释至原污水浓度的1/2;第三个阶段可为40~55日, 至启动阶段完成;所述梯度提高中,第一阶段具体可为7日,第二阶段具体可为7日,第三阶 段具体可为40~45日、40日或45日。
[0027] 当所述高氨氮废水中氨态氮的去除率(进水氨氮浓度/出水氨氮浓度)大于80%, 排出的废水中的硝态氮占所述废水中总氮的含量大于70%时,反应器达到稳定全程脱氮, 启动阶段完成,梯度提高可使所述污泥中的微生物尽快适应所述原污水水质和反应器环境 条件;接种之后缺氧池内充满活性污泥混合液,缺氧池与好氧池内活性污泥混合液的体积 比为I: (2~3),具体可为1:2,在废水处理过程中缺氧池的液面始终高于好氧池的液面。
[0028] 上述方法中,步骤(1)中,所述缺氧池内开始接纳高氨氮废水,由于缺氧池始终处 于充满状态,废水通过所述溢流堰流至所述好氧池内,与所述好氧池内的活性污泥混合液 混合;
[0029] 所述高氨氮废水中氨态氮的浓度500~900mg/L,COD含量为2000~6000mg/L;
[0030] 所述高氨氮废水来自畜禽养殖废水、垃圾渗滤液或污泥消化液;
[0031] 所述设计处理量可为0 · 5~2 ·OL/cycle,具体可为1 · 5~2· OL/cycle、1 · 5L/cycle 或2.0L/cycle;
[0032] 所述输入的流量可为〇 . 3~lL/min,具体可为0.3~0.5L/min、0.3L/min或0.5L/ min,快速输入可保证A段向0段实现推流,将A段完成反硝化的高氨水送至0段。
[0033] 上述方法中,步骤(2)中,所述缺氧池内,废水中的硝态氮被还原为亚硝态氮,亚硝 态氮被还原为氮气,即为反硝化过程;所述高氨氮废水中的有机物可优先作为碳源为所述 兼氧阶段中硝态氮和亚硝态氮的还原提供电子,当所述废水中的碳源不足时,再及时开启 所述碳源投加栗为所述缺氧池投加碳源,通过此种方式可使碳源的投加量更加的准确,节 省碳源,降低成本;所述缺氧池内,当废水的氧化还原电极电位随时间的变化值即dORP/dt 为0~-5时,判定碳源不足,开启所述碳源投加栗,为所述缺氧池投加碳源,每次开启时间可 为0 · 5~lmin,具体可为0 · 5min或Imin,保持10~20min后,具体可在保持10~15min、IOmin 或15min后进入下一次判定;当所述dORP/dt小于-5时,判定反硝化完成,延时10~40min,具 体可延时 20 ~40min、20 ~30min、30 ~40min、20min、30minS40min。
[0034] 所述好氧池内,待处理的废水中的氨态氮在污泥中氨氧化细菌的作用下被氧化为 亚硝态氮,亚硝态氮在亚硝酸氧化细菌的作用下被氧化为硝态氮,即为硝化过程;所述曝气 系统可为所述好氧池内的废水提供氧气;
[0035] 所述曝气系统的曝气流量可为0.5~10L/min,具体可为1.5~2L/min、l .5L/min或 2L/min〇
[0036] 上述方法中,步骤(3)中,当所述膜分离池的液位高于液位计时,开启蠕动栗抽吸 排水;当所述膜分离池的液位低于液位计时,关闭蠕动栗;
[0037] 所述出水栗为间歇式抽吸,每开8~10分钟停2~4分钟,具体可为每开8分钟停2分 钟;
[0038] 在所述好氧池和所述膜分离池内,小于3倍设计处理量的废水(即回流比小于等于 300%,具体可为200 %)回流至所述缺氧池内,具体可回流至所述缺氧池的底部;在所述缺 氧池内,等量的、缺氧池上方的经反硝化的废水通过所述溢流堰流至所述好氧池内。
[0039] 进入下一次循环时,待处理的废水通过所述溢流堰直接流至所述好氧池内,与由 于回流导致的缺氧池内废水溢流至好氧池内的废水混合,再次经步骤⑵中的硝化,废水中 的有机物和氨态氮被氧化;同时,所述缺氧池内,经过硝化的回流液发生反硝化,硝态氮和 亚硝态氮被还原;所述膜分离池内,设计处理量的废水通过所述膜组件排出系统;所述好氧 池和所述膜分离池内,按照回流比(回流量与设计处理量的比值)小于3的量,混合液回流至 所述缺氧池内;
[0040] 以此类推,进入下一个循环。
[0041] 上述方法中,所述反应器的温度可为15~30°C,具体可为20~25°C、20°C或25°C。
[0042] 上述方法中,为了将全程硝化-反硝化转变为短程硝化-反硝化,需要促进氨氧化 细菌(AOB)生长,抑制亚硝酸氧化菌(NOB)生长,可可利用下述1) -3)中至少一种方法将全程 硝化-反硝化转化为短程硝化-反硝化:
[0043] 1)优化曝气时间法:脱氮稳定后,在每轮循环的所述好氧阶段,当废水中的pH值随 时间不发生改变即dpH/dt = 0时,关闭所述曝气系统;
[0044] 2)自由氨受控累积法:脱氮稳定后,在所述好氧阶段,降低所述曝气系统的曝气流 量,当废水中自由氨的浓度升高至大于等于20mg/L时,恢复曝气流量;
[0045] 所述曝气系统整个循环中的曝气流量被降低至0.2~lL/min;
[0046] 上述1)和2)中所述脱氮稳定均是指当所述废水中的氨态氮的去除率大于80%,且 排出的废水中的硝态氮占所述废水中总氮的含量大于70%时;
[0047] 3) SRT控制法:所述方法还包括排泥的步骤,所述排泥在所述好氧阶段之后,控制 所述反应器中的污泥的平均停留时间为12~15天。
[0048] 上述方法1)中,在每轮循环的好氧单元,根据pH连续监测曲线上的"氨谷点" (ammoniaval ley)实时控制好氧单元的时长,即先采用合适的曝气流量持续曝气,当pH连续 监测曲线出现"氨谷点"后立即停止曝气。通过优化曝气时间以逐步减少亚硝氮的氧化,从 而使脱氮过程逐渐由全程硝化-反硝化转变为短程硝化反硝化,亚硝化率可以持续增高并 最终达到80 %。
[0049] 上述方法2)中,通过降低曝气流量,控制偏低的溶解氧(DO)使反应体系内自由氨 浓度(FA)升高至大于等于20mg/L,同时氨氧化细菌的生长速率大于亚硝酸氧化菌。然后将 曝气流量恢复至合适的曝气流量持续曝气直到亚硝化率达到80%以上,之后重新恢复正常 进出水处理循环,实现氨氮废水处理的短程硝化-反硝化。
[0050] 上述方法3)中,由于氨氧化细菌的污泥龄一般在10~12天,而亚硝酸氧化菌的污 泥龄则一般在18~20天,控制系统污泥平均停留时间12~15天可以使数量逐渐减少,从而 使得氨氧化细菌在真个硝化菌群中的比例不断提高,亚硝化率得以持续增长。
[0051] 利用本发明装置和方法可实现亚硝化-反亚硝化途径处理高氨氮废水(亚硝化率 达到80 %),保证反应器高效去除氮(约95 %TN,约99 %NH3-N及约98 % C0D),减少了水力停 留时间,降低了曝气能耗,并节省了外部碳源。
[0052] 本发明处理高氨氮废水的装置和方法具有如下优点:
[0053] 1)本发明将传统A/0工艺与平板膜分离技术进行优化组合,保留了A/0工艺处理效 率高、流程简单、抗冲击负荷强的特点,同时引入膜分离技术使得传统A/0工艺能够在较高 污泥浓度的条件下,实现高效的泥水分离,获得稳定的出水水质,简化了传统A/0工艺的混 凝沉淀工序,缩短了HRT;
[0054] 2)采用序批式进水,连续出水的控制策略,实现了A/0 MBR反应器与实时控制系统 的优化结合,简化系统运行控制策略,提高反应器处理效率;
[0055] 3)本发明采用pH探头在线监测好氧池内(0段)氨氧化反应进程,利用pH单位时间 变化值判定亚硝酸盐最大积累时间(dpH/dt = 0),优化曝气时间以节约曝气量降低污水处 理成本;
[0056] 4)本发明采用ORP探头在线监测缺氧池内(A段)反硝化反应进程,利用ORP的单位 时间变化值作为反亚硝化进程的判断依据(dORP/dt〈设定值),控制碳源投加栗进行脉冲式 投加,提高了碳源投加的精确性,节约外部碳源投加量降低污水处理成本。
附图说明
[0057] 图1为本发明处理高氨氮废水的装置的结构示意图。
[0058] 图2为实施例2中25 °C左右pH实时曲线上"氨谷点"优化曝气时间实现亚硝化-反亚 硝化的示意图。
[0059] 图3为实施例中处理高氨氮废水的运行逻辑图。
[0060] 图1中各标记如下:
[0061] 1.1原水箱、1.2进水栗、2.0缺氧池、2.1搅拌器、2.2采样阀1、2.3回流液进水口、 2.40RP探头、2.5碳源储箱、2.6碳源投加栗、2.7加碳管、3.0好氧池、3.1溢流堰、3.2pH探头、 3.3溶解氧DO探头、3.4采样阀2、3.5排泥阀、3.6第一空压机、3.7第一气体流量计、3.8曝气 砂条、4.0膜分离池、4.1平板膜膜单元、4.2有机玻璃外壳、4.3板框式膜组件出水口、4.4微 孔管式曝气器、4.5第二空压机、4.6第二气体流量计、4.7回流管、4.8回流栗、5.1产水箱5.2 液位计、5.3蠕动栗、5.4压力表、6.1集成电路箱、6.2数字触控板。
具体实施方式
[0062] 下述实施例中所使用的实验方法如无特殊说明,均为常规方法。
[0063] 下述实施例中所用的材料、试剂等,如无特殊说明,均可从商业途径得到。
[0064] 下述实施例中对污泥厌氧消化液、垃圾渗滤液处理时,采用的反硝化碳源为工业 用甲醇。而畜禽养殖废水的处理为节约运行成本采用畜禽奠便浓衆(Manure Slurry)作为 反硝化碳源。畜禽粪便浓浆制备方法为:将猪粪研磨过筛后(10目)用水稀释成浓浆状,其 COD 含量为 50000-100000mg/L。
[0065] 下述实施例中通过如下经验公式计算反应器中需要的曝气流量:
[0066] Q = q X MLSS X In (公式1)
[0067] 其中,Q-合适的曝气流量,单位为L/min;
[0068] MLSS (混合液悬浮物浓度)一用来表示活性污泥浓度,单位为mg/L;
[0069] In-进水NH3-N浓度,单位为mg/L;
[0070] q-经验计算常数,来自于实验。对于合适的曝气流量,其取值为200~400。
[0071] 下述实施例中通过如下公式计算平板膜组件中膜需要的曝气流量:
[0072] 膜元件需要的曝气量=n Xq (公式2)
[0073] 其中,η-膜元件数量(片);
[0074] q-单片膜所需气量(L/min),来自于实验。对于合适的曝气流量,其取值为5~15。
[0075] 下述实施例中,通过排泥将MLSS控制在约9000mg/L~11000mg/L。
[0076] 下述实施例中废水的化学需氧量(COD)、磷的含量(TP)、生化需氧量(BOD5)、氨态 氮(NH3-N)的含量、亚硝态氮(N02_N)的含量和硝态氮(N03_N)的含量可通过下表1中方法和 仪器检测得到:
[0077] 表1测定指标和研究方法
[0079] 下面结合说明书附图对本发明做进一步说明,但本发明并不局限于下述实施例。
[0080] 实施例1、处理高氨氮废水的装置
[0081] 如图1所示,本发明处理高氨氮废水的装置,它包括进水系统、反应系统、曝气系 统、碳源投加系统、出水系统和实时控制系统;
[0082] 所述反应系统包括一反应器,所述反应器为一具盖容器,被分隔为三部分,依次为 缺氧池(2.0)、好氧池(3.0)和膜分离池(4.0):
[0083] 所述缺氧池的上方设有搅拌器(2.1),所述缺氧池的侧壁设有一采样阀1 (2.2),侧 壁的底端设有一回流液进水口(2.3),内部设有一ORP探头(2.4);
[0084] 所述缺氧池与所述好氧池之间设有溢流堰(3.1),所述好氧池内设有pH探头 (3.2)、溶解氧DO探头(3.3)、采样阀2 (3.4)和排泥阀(3.5);
[0085] 所述好氧池的底部与所述膜分离池的底部连通,所述膜分离池内的侧壁上设有一 材质为有机玻璃的板框式膜组件和一液位计(5.2),该膜组件由1~2个平板膜膜单元(下述 实施例中如无特殊说明,均为1个平板膜膜单元)(4.1)和外部的有机玻璃外壳(4.2)构成, 其上下与外界污水连通,每个平板膜膜单元(4.1)由两片平板膜(材质为:聚偏氟乙烯PVDF, 有效膜面积:0.25m 2,膜孔径<0. Ιμπι)固定于膜框上得到,每个膜框上设有一分出水口,整 个板框式膜组件的上方设有一与各个分出水口连通的出水口(4.3),有机玻璃外壳(4.2)的 底部设有一微孔管式曝气器(4.4),与第二空压机(4.5)、第二气体流量计(4.6)连接,构成 曝气系统Π ,为板框式膜组件中的膜进行冲刷,避免污染;
[0086] 所述好氧池和所述膜分离池的底部设有回流管(4.7),通过回流栗(4.8)将混合液 回流至所述缺氧池内;
[0087] 所述进水系统包括一原水箱(I. 1),所述原水箱中的废水通过进水栗(1.2)被输送 至所述缺氧池内;
[0088] 所述碳源投加系统包括一碳源储箱(2.5),通过碳源投加栗(2.6)与所述缺氧池内 的加碳管(2.7)连接;
[0089] 所述曝气系统I包括第一空压机(3.6)、第一气体流量计(3.7)和置于所述好氧池 底部的曝气砂条(3.8);
[0090] 所述出水系统包括一产水箱(5.1),通过膜分离池内的侧壁上设置的液位计(5.2) 控制蠕动栗(5.3)与板框式膜组件的出水口(4.3)连接进行抽吸排水(混合液渗过平板膜膜 面),使用压力表(5.4)监控跨膜压差,经过膜分离的污水被抽至产水箱中;
[0091] 所述实施控制系统包括pH探头(3.2)、ORP探头(2.4)和溶解氧DO (3.3)探头,三个 探头在使用时插入反应器中的废水中,并分别与集成电路箱(6.1)连接,集成电路箱(6.1) 与数字触控板(6.2)连接,根据设定的程序控制进出水栗即进水栗和蠕动栗、碳源投加栗、 曝气系统及搅拌器的启停,从而实时控制各反应单元的交替进行。
[0092] 实施例2、采用A/0 MBR半连续运行工艺对畜禽养殖废水进行处理
[0093] 采用实施例1中的装置对某集约化畜禽养殖废水进行处理,反应器温度控制在25 ±0.5°C下,包括如下步骤:
[0094] 将浓度为5500mg/L的城市污水处理厂回流污泥接种至缺氧池和好氧池中,开启搅 拌器、曝气系统I (曝气流量为2L/min)、曝气系统Π (曝气流量为10L/min,整个膜冲刷的曝 气量,按两片膜设定)、进水栗和实施控制系统,采用梯度进水(污水)的方式,使污泥浓度逐 步增长至8500~9500mg/L,梯度进水控制如下:第一个阶段为7日,进水稀释至为原污水浓 度的1/4,第二个阶段为7日,进水稀释至原污水浓度的1/2,第三个阶段开始,进水使用原污 水,待污水中氨态氮的去除率(进水氨氮浓度/出水氨氮浓度)大于80%,排出的废水中的硝 态氮占所述废水中总氮的含量大于70%时,反应器达到稳定全程脱氮(第三阶段共45日), 接种之后整个缺氧池充满所述活性污泥混合液,缺氧池和好氧池内活性污泥混合液的体积 比为1:2,启动阶段完成,关闭进水栗和曝气系统I,重复循环下述步骤(1)-步骤(3):
[0095] (1)进水阶段:开启进水栗,采用序批式进水,按照设计处理量(1.5L/Cy Cle),待处 理的养殖废水被输入缺氧池内(〇.5L/min),经过溢流堰在整个反应器内形成推流,流至好 氧池内,完成进水后,关闭进水栗,保持5min;
[0096] (2)兼氧阶段和好氧阶段:在缺氧池内,在碳源的作用下,养殖废水中的硝态氮被 还原为亚硝态氮,亚硝态氮被还原为氮气;当dORP/dt大于-5时,判定养殖废水中的碳源不 足不能进行完全反亚硝化,及时开启碳源投加栗进行脉冲式投加为反应器添加碳源,每次 开启时间为Imin,保持IOmin后,之后继续以dORP/dt的值为判断依据,如此循环,直至适量 的外加碳源保证完全反亚硝化即在dORP/dt值小于-5时,如图2中长方形方框处,判定碳源 足够,延长30min,保证反亚硝化顺利进行。
[0097] 开启曝气系统I,在好氧池内,养殖废水中的氨态氮和有机物被氧化,氨态氮被氧 化为亚硝态氮,亚硝态氮被氧化为硝态氮,通过采用pH、D0探头在线监测氨氧化过程中pH和 DO的值,根据pH连续监测值计算dpH/dt。当dpH/dt = 0,如图2中椭圆处,判定氨氧化完成,关 闭曝气系统I,以免亚硝态氮被进一步氧化成硝态氮。
[0098] (3)排水和回流阶段:在膜分离池内,通过膜池位置的液位计,控制蠕动栗启闭,在 系统运行过程中连续出水,蠕动栗的运行方式是每开Smin停2min,抽吸产水量约为lL/h,设 计处理量(1.5L/cy Cle)的经硝化的养殖废水经过膜组件中的膜的过滤后被排出。
[0099] 在缺氧池和膜分离池内,2倍设计处理量(3.OL/cycle)的废水(回流比为200%)回 流至缺氧池的底端;在缺氧池内,等量的(3. OL/cycle)经反硝化的废水通过溢流堰流至好 氧池内。
[0100] 本实施例中的运行逻辑图如图3所示,进水结束之后,开启曝气装置,硝化过程和 反硝化过程同时进行,如图2所示,由于一般情况下反硝化过程先于硝化过程结束,因此在 硝化过程结束之后,再次判定dORP/dt的值,确认反硝化过程是否结束,以保证硝化过程和 反硝化过程均完成后,再经排水、回流后进入下一个循环。
[0101] 本实施例中通过如下两种方法将全程硝化-反硝化过程控制为短程硝化-反硝化 过程中:
[0102] (1)优化曝气时间法:
[0103] 反应器在稳定运行后的前20天,进水NH3-N平均浓度为605.4mg/L;出水NH 3-N始终 维持在低浓度水平,平均仅为2.4mg/L;出水中氮类污染物的主要组分为NO3-N,平均为 26mg/L;而NO 2-N平均仅为1 · 2mg/L,亚硝化率Ν〇2-ΝΛΝ〇2-Ν+Ν〇3-Ν)平均仅为4 · 4 %。第20天 至第32天,曝气流量维持在3. OL/min,根据pH实时监测曲线上的"氨谷点"优化曝气时间,如 图2所示,当dpH/dt = 0,如图中2中椭圆形处,判定氨氧化完成,关闭曝气装置;体系内NH3-N 逐渐升高,而NO3-N则迅速降低,出水中NO3-N由26mg/L逐渐降低至8mg/L;相应的NO 2-N则由 2.7mg/L逐渐升高至27mg/L。亚硝化率Ν02-ΝΛΝ02-Ν+Ν03-Ν)在这一过程中达到77.1%,表明 反应器出水中氮类污染物主要组分为Ν0 2-Ν。并且在全程脱氮想短程脱氮转变的过程中,脱 氮的效能没有降低。反应器连续长期运行的亚硝化率最高达到80%。
[0104] ⑵SRT控制法:
[0105] 本实施例中控制系统污泥平均停留时间为15天,由于在本实施例控制条件下(Τ = 25°C,pH多7.0)氨氧化细菌的污泥龄一般在10-12天,而亚硝酸氧化菌的污泥龄则一般在 18-20天,可以使亚硝酸氧化细菌数量逐渐减少,从而使得氨氧化细菌在真个硝化菌群中的 比例不断提高,亚硝化率得以持续增长。
[0106] 经过上述步骤处理前后的畜禽养殖废水中即进出水中的污染物浓度及去除率见 表1。
[0107] 表1、25°C条件下畜禽养殖废水亚硝化一反亚硝化运行结果
[0109] ND:未检出
[0110] 实施例3、采用A/0 MBR半连续运行工艺对垃圾渗滤液进行处理
[0111] 采用实施例1中的装置对某垃圾渗滤液进行处理,反应器温度控制在25 ±0.5°C 下,包括如下步骤:
[0112] 将浓度为5500mg/L的城市污水处理厂回流污泥接种至缺氧池和好氧池中,开启搅 拌器、曝气系统I (曝气流量为1.5L/min)、曝气系统Π (曝气流量为15L/min)、进水栗和实施 控制系统,采用梯度进水(污水)的方式,使污泥浓度逐步增长至6500~7500mg/L,梯度进水 控制如下:第一个阶段为7日,进水稀释至为原污水浓度的1/4,第二个阶段为7日,进水稀释 至原污水浓度的1/2,第三个阶段开始,进水使用原污水,待污水中氨态氮的去除率(进水氨 氮浓度/出水氨氮浓度)大于80%,排出的废水中的硝态氮占所述废水中总氮的含量大于 70 %时,反应器达到稳定全程脱氮(第三个阶段共45日),接种之后整个缺氧池充满所述活 性污泥混合液,缺氧池和好氧池内活性污泥混合液的体积比为1: 2,启动阶段完成,关闭进 水栗和曝气系统I,重复循环下述步骤(1)-步骤(3):
[0113] (1)进水阶段:开启进水栗,采用序批式进水,按照设计处理量(2.0L/cyCle),待处 理的养殖废水被输入缺氧池内(〇.5L/min),经过溢流堰流至好氧池内,在整个反应器内形 成推流,关闭进水栗,保持5min;
[0114] (2)兼氧阶段和好氧阶段:在缺氧池内,在碳源的作用下,养殖废水中的硝态氮被 还原为亚硝态氮,亚硝态氮被还原为氮气;当dORP/dt大于-5时,判定养殖废水中的碳源不 足不能进行完全反亚硝化,及时开启碳源投加栗进行脉冲式投加为反应器添加碳源,每次 开启时间为2min,保持15min后,之后继续以dORP/dt的值为判断依据,如此循环,直至适量 的外加碳源保证完全反亚硝化即在dORP/dt值小于-5时,判定碳源足够,延长40min,保证反 亚硝化顺利进行。
[0115] 开启曝气系统I,在好氧池内,养殖废水中的氨态氮和有机物被氧化,氨态氮被氧 化为亚硝态氮,亚硝态氮被氧化为硝态氮,关闭曝气系统I。
[0116] (3)排水和回流阶段:在膜分离池内,通过膜池位置的液位计,控制蠕动栗启闭,在 系统运行过程中连续出水,懦动栗的运行方式是每开8min停2min,抽吸产水量约为1.5L/h, 设计处理量(2L/cy Cle)的经硝化的养殖废水经过膜组件中的膜的过滤后被排出。
[0117] 在缺氧池和膜分离池内,2倍设计处理量(4.OL/cycle)的废水(回流比为200%)回 流至缺氧池的底端;在缺氧池内,等量的(4. OL/cycle)经反硝化的废水通过溢流堰流至好 氧池内。
[0118] 本实施例中的运行逻辑图同实施例2;此外,由于垃圾渗滤液水质水量的季节性差 异较大,因此为保证反亚硝化顺利进行,碳源投加栗每次开启时间为2min,好氧延时相应的 延长为40min,以保证出水C0D。
[0119] 本实施例中通过如下两种方法将全程硝化-反硝化过程控制为短程硝化-反硝化 过程中:
[0120] (1)优化曝气时间法:
[0121] 反应器运行前30天,进水NH3-N平均浓度为811.4mg/L;出水NH 3-N稳定在低浓度水 平,平均仅为6. lmg/L;出水中氮类污染物的主要组分为NO3-N,平均为35mg/L;而NO2-N平均 仅为1.9mg/L,亚硝化率N0 2-rV(N02-N+N〇3-N)平均仅为5.1 %。第30天至第44天,曝气流量维 持在2.0L/min,根据pH实时监测曲线上的"氨谷点"优化曝气时间,当dpH/dt = 0,判定氨氧 化完成,关闭曝气装置;出水中NO3-N由35mg/L逐渐降低至Ilmg/L;相应的NO 2-N则由1.9mg/L 逐渐升高至31mg/L。亚硝化率Ν02-ΝΛΝ02-Ν+Ν03-Ν)在这一过程中达到73.8%,表明反应器 出水中氮类污染物主要组分为NO 2-N,并且在全程脱氮想短程脱氮转变的过程中,脱氮的效 能没有降低。反应器连续长期运行的亚硝化率可稳定达到80%。
[0122] (2) SRT控制法:
[0123] 本实施例中控制系统污泥平均停留时间为15天,由于在本实施例控制条件下(T = 25°C,pH多7.0)氨氧化细菌的污泥龄一般在10-12天,而亚硝酸氧化菌的污泥龄则一般在 18-20天,可以使亚硝酸氧化细菌数量逐渐减少,从而使得氨氧化细菌在真个硝化菌群中的 比例不断提高,亚硝化率得以持续增长。
[0124] 经过上述步骤处理前后的垃圾渗滤液中即进出水中的污染物浓度及去除率见表 2〇
[0125] 表2、25 °C条件下垃圾渗滤液亚硝化一反亚硝化运行结果
[0127] ND:未检出
[0128] 实施例4、采用A/0 MBR半连续运行工艺对污泥厌氧消化液进行处理
[0129] 采用实施例1中的装置对某污泥消化液进行处理,反应器的温度控制在20±0.5 °C,包括如下步骤:
[0130] 将浓度为5500mg/L的城市污水处理厂回流污泥接种至缺氧池和好氧池中,开启搅 拌器、曝气系统I (曝气流量为2L/min)、曝气系统Π (曝气流量为10L/min)、进水栗和实施控 制系统,采用梯度进水(污水)的方式,使污泥浓度逐步增长至6500~7500mg/L,梯度进水控 制如下:第一个阶段为7日,进水稀释至为原污水浓度的1/4,第二个阶段为7日,进水稀释至 原污水浓度的1/2,第三个阶段开始,进水使用原污水,待污水中氨态氮的去除率(进水氨氮 浓度/出水氨氮浓度)大于80%,排出的废水中的硝态氮占所述废水中总氮的含量大于70% 时,反应器达到稳定全程脱氮(第三个阶段共40日),接种之后整个缺氧池充满所述活性污 泥混合液,缺氧池和好氧池内活性污泥混合液的体积比为1:2,启动阶段完成,关闭进水栗 和曝气系统I,重复循环下述步骤(1)-步骤(3):
[0131] (1)进水阶段:开启进水栗,采用序批式进水,按照设计处理量(1.5L/Cy Cle),待处 理的养殖废水被输入缺氧池内(〇.3L/min),经过溢流堰流至好氧池内(在整个反应器内形 成推流),关闭进水栗,保持5min;
[0132] (2)兼氧阶段和好氧阶段:在缺氧池内,在碳源的作用下,养殖废水中的硝态氮被 还原为亚硝态氮,亚硝态氮被还原为氮气;当dORP/dt大于-5时,判定养殖废水中的碳源不 足不能进行完全反亚硝化,及时开启碳源投加栗进行脉冲式投加为反应器添加碳源,每次 开启时间为〇.5min,保持IOmin后,之后继续以dORP/dt的值为判断依据,如此循环,直至适 量的外加碳源保证完全反亚硝化即在dORP/dt值小于-5时,判定碳源足够,延长20min,保证 反亚硝化顺利进行。
[0133] 开启曝气系统I,在好氧池内,养殖废水中的氨态氮和有机物被氧化,氨态氮被氧 化为亚硝态氮,亚硝态氮被氧化为硝态氮,关闭曝气系统I。
[0134] (3)排水和回流阶段:在膜分离池内,通过膜池位置的液位计,控制蠕动栗启闭,在 系统运行过程中连续出水,懦动栗的运行方式是每开8min停2min,抽吸产水量约为1.5L/h, 设计处理量(2L/cy Cle)的经硝化的养殖废水经过膜组件中的膜的过滤后被排出。
[0135] 在缺氧池和膜分离池内,2倍设计处理量(4.OL/cycle)的废水(回流比为200%)回 流至缺氧池的底端;在缺氧池内,等量的(4. OL/cycle)经反硝化的废水通过溢流堰流至好 氧池内。
[0136] 本实施例中的运行逻辑图同实施例2;此外,由于污泥厌氧消化液碳源相对充足, 因此,为节约碳源,缩短停留时间,降低运行成本,碳源投加栗每次开启时间为〇.5min,好养 延时相应的缩短为20min。
[0137] 本实施例中通过如下两种方法将全程硝化-反硝化过程控制为短程硝化-反硝化 过程中:
[0138] (1)优化曝气时间法:
[0139] 反应器运行前20天,进水NH3-N平均浓度为604mg/L;出水NH 3-N稳定在低浓度水平, 平均仅为5.5mg/L;出水中氮类污染物的主要组分为NO3-N,平均为34.6mg/L;而NO 2-N平均仅 为2.9mg/L,亚硝化率Ν02-ΝΛΝ02-Ν+Ν03-Ν)平均仅为7.7 %。第20天至第35天,曝气流量维持 在2. OL/min,根据pH实时监测曲线上的"氨谷点"优化曝气时间,当dpH/dt = 0,判定氨氧化 完成,关闭曝气装置;出水中NO3-N由34.6mg/L逐渐降低至10.3mg/L;相应的NO 2-N则由 2·9mg/L逐渐升高至27·4mg/L。亚硝化率N02-rV(N02-N+N〇3-N)在这一过程中达到72·7%,表 明反应器出水中氮类污染物主要组分为NO 2-N,并且在全程脱氮想短程脱氮转变的过程中, 脱氮的效能没有降低。反应器连续长期运行的亚硝化率可稳定达到80%。
[0140] ⑵SRT控制法:
[0141] 本实施例中控制系统污泥平均停留时间为15天,由于在本实施例控制条件下(T = 20±0.5°C,pH多7.0)氨氧化细菌的污泥龄一般在10-12天,而亚硝酸氧化菌的污泥龄则一 般在18-20天,可以使亚硝酸氧化细菌数量逐渐减少,从而使得氨氧化细菌在真个硝化菌群 中的比例不断提高,亚硝化率得以持续增长。
[0142] 经过上述步骤处理前后的污泥消化液中即进出水中的污染物浓度及去除率见表 3〇
[0143] 表3、20±0.5°C条件下污泥厌氧消化液亚硝化一反亚硝化运行结果
Claims (3)
1. 一种利用高氨氮废水的装置处理高氨氮废水的方法,其特征在于: 所述装置包括进水系统、反应系统、曝气系统、碳源投加系统和出水系统; 所述反应系统包括一反应器,所述反应器为一容器,被分隔成三部分,依次为缺氧池、 好氧池和膜分离池,所述缺氧池的上方设有搅拌器,所述缺氧池与所述好氧池之间设有溢 流堰,所述好氧池的底部与所述膜分离池的底部连通,所述膜分离池内设有膜组件和液位 计,所述好氧池和所述膜分离池的底部设有回流管,通过回流栗将废水回流至所述缺氧池 内; 所述进水系统包括一原水箱,所述原水箱中的废水通过进水栗被输送至所述缺氧池 内; 所述曝气系统包括空压机、气体流量计和曝气器,所述曝气器置于所述好氧池中; 所述碳源投加系统包括一碳源储箱,所述碳源储箱中的碳源通过碳源投加栗被输送至 所述缺氧池内; 所述出水系统包括一产水箱,所述膜组件的出水口通过出水栗与所述产水箱连接; 所述装置还包括一实时控制系统,所述实施控制系统包括探头、集成电路箱和数字触 控板; 所述探头包括pH探头、ORP探头和溶解氧DO探头,均与所述集成电路箱连接,所述集成 电路箱与所述数字触控板连接; 所述ORP探头置于所述缺氧池内,所述pH探头和溶解氧DO探头置于所述好氧池内; 所述缺氧池的底端设有一回流液进水口,所述废水通过所述回流液进水口回流至所述 缺氧池内; 所述膜组件置于所述膜分离池的侧壁处;所述膜组件为板框式膜组件,所述板框式膜 组件包括1~2个膜单元,每个所述膜单元由两片膜组成,所述膜的材质为聚偏氟乙烯,孔径 <0. Ιμπι;每个所述膜单元的有效面积为0.5m2;所述膜组件的内部还设有曝气器,依次与另 一空压机和另一气体流量计连接,为所述膜曝气; 所述方法包括如下步骤: 接种活性污泥至所述缺氧池和所述好氧池内,整个所述缺氧池充满所述活性污泥,开 启所述搅拌器,重复下述步骤(1)-步骤(3): (1) 进水阶段:开启所述进水栗,采用序批式进水,按照设计处理量,待处理的高氨氮废 水被输入所述缺氧池内,经过所述溢流堰流至所述好氧池内; 所述高氨氮废水中氨态氮的浓度500~900mg/L,COD含量为2000~6000mg/L; 所述高氨氮废水来自畜禽养殖废水、垃圾渗滤液或污泥消化液; 所述设计处理量为〇. 5~2. OL/cycle; 所述输入的流量为〇. 3~lL/min; (2) 兼氧阶段和好氧阶段:在所述缺氧池内,在碳源的作用下,所述废水中的硝态氮被 还原为亚硝态氮,亚硝态氮被还原为氮气;开启所述曝气系统,在所述好氧池内,所述废水 中的氨态氮和有机物被氧化,所述氨态氮被氧化为亚硝态氮,亚硝态氮被氧化为硝态氮,关 闭所述曝气系统; 所述缺氧池内,当废水的氧化还原电极电位随时间的变化值即dORP/dt为0~-5时,判 定碳源不足,开启所述碳源投加栗,为所述反应器投加碳源,每次开启时间为0.5~lmin,保 持10~20min后,进入下一次判定;当所述dORP/dt小于-5时,判定反硝化完成,延时10~ 40min; 所述好氧池内,所述曝气系统的曝气流量为0.5~10L/min; (3)排水和回流阶段:在所述膜分离池内,设计处理量的经硝化的所述废水经过所述膜 组件中的膜的过滤后被排出;在所述缺氧池和所述膜分离池内,小于3倍设计处理量的废水 回流至所述缺氧池内;在所述缺氧池内,等量的经反硝化的废水通过所述溢流堰流至所述 好氧池内; 步骤(3)中,当膜池液位高于液位计时,开启蠕动栗抽吸排水;当膜池液位低于液位计 时,关闭蠕动栗; 所述出水栗为间歇式抽吸,每开8~10分钟停2~4分钟; 小于3倍设计处理量的废水回流至所述缺氧池的底部; 利用下述1) -3)中至少一种方法将全程硝化-反硝化转化为短程硝化-反硝化: 1) 优化曝气时间法:脱氮稳定后,在每轮循环的所述好氧阶段,当废水中的pH值随时间 不发生改变即dpH/dt = 0时,关闭所述曝气系统; 2) 自由氨受控累积法:脱氮稳定后,在所述好氧阶段,降低所述曝气系统的曝气流量, 当废水中自由氨的浓度升高至大于等于20mg/L时,恢复曝气流量; 所述曝气系统的曝气流量被降低至0.2~lL/min; 上述1)和2)中所述脱氮稳定均是指当所述废水中的氨态氮的去除率大于80%,且排出 的废水中的硝态氮占所述废水中总氮的含量大于70%时; 3. SRT控制法:所述方法还包括排泥的步骤,所述排泥在所述好氧阶段之后,控制所述 反应器中的污泥的平均停留时间为12~15天。
2. 根据权利要求1所述的方法,其特征在于:所述实时控制系统全程开启,监测所述高 氨氮废水中的氧化还原电极电位、pH值和溶解氧的大小; 所述膜组件中的曝气器全程开启,曝气流量为5~15L/min。
3. 根据权利要求1或2所述的方法,其特征在于:所述接种的活性污泥的浓度为5000mg/ L~5500mg/L,梯度提高污水的进水浓度,将活性污泥浓度增高至6500mg/L~12000mg/L; 所述梯度提高分为三个阶段,第一个阶段为5~10日,进水稀释至为原污水浓度的1/4; 第二个阶段为5~10日,进水稀释至原污水浓度的1/2;第三个阶段为40~45日。
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