CN102101745B - 污泥发酵耦合反硝化处理污泥消化液的控制装置与方法 - Google Patents
污泥发酵耦合反硝化处理污泥消化液的控制装置与方法 Download PDFInfo
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- CN102101745B CN102101745B CN 201110004485 CN201110004485A CN102101745B CN 102101745 B CN102101745 B CN 102101745B CN 201110004485 CN201110004485 CN 201110004485 CN 201110004485 A CN201110004485 A CN 201110004485A CN 102101745 B CN102101745 B CN 102101745B
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- 239000010802 sludge Substances 0.000 title claims abstract description 110
- 238000000855 fermentation Methods 0.000 title claims abstract description 41
- 239000007788 liquid Substances 0.000 title claims abstract description 22
- 230000029087 digestion Effects 0.000 title claims abstract description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances data:image/svg+xml;base64,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 data:image/svg+xml;base64,PD94bWwgdmVyc2lvbj0nMS4wJyBlbmNvZGluZz0naXNvLTg4NTktMSc/Pgo8c3ZnIHZlcnNpb249JzEuMScgYmFzZVByb2ZpbGU9J2Z1bGwnCiAgICAgICAgICAgICAgeG1sbnM9J2h0dHA6Ly93d3cudzMub3JnLzIwMDAvc3ZnJwogICAgICAgICAgICAgICAgICAgICAgeG1sbnM6cmRraXQ9J2h0dHA6Ly93d3cucmRraXQub3JnL3htbCcKICAgICAgICAgICAgICAgICAgICAgIHhtbG5zOnhsaW5rPSdodHRwOi8vd3d3LnczLm9yZy8xOTk5L3hsaW5rJwogICAgICAgICAgICAgICAgICB4bWw6c3BhY2U9J3ByZXNlcnZlJwp3aWR0aD0nODVweCcgaGVpZ2h0PSc4NXB4JyB2aWV3Qm94PScwIDAgODUgODUnPgo8IS0tIEVORCBPRiBIRUFERVIgLS0+CjxyZWN0IHN0eWxlPSdvcGFjaXR5OjEuMDtmaWxsOiNGRkZGRkY7c3Ryb2tlOm5vbmUnIHdpZHRoPSc4NS4wJyBoZWlnaHQ9Jzg1LjAnIHg9JzAuMCcgeT0nMC4wJz4gPC9yZWN0Pgo8dGV4dCB4PScxMy4zJyB5PSc1My42JyBjbGFzcz0nYXRvbS0wJyBzdHlsZT0nZm9udC1zaXplOjIzcHg7Zm9udC1zdHlsZTpub3JtYWw7Zm9udC13ZWlnaHQ6bm9ybWFsO2ZpbGwtb3BhY2l0eToxO3N0cm9rZTpub25lO2ZvbnQtZmFtaWx5OnNhbnMtc2VyaWY7dGV4dC1hbmNob3I6c3RhcnQ7ZmlsbDojRTg0MjM1JyA+SDwvdGV4dD4KPHRleHQgeD0nMjguMicgeT0nNjIuOScgY2xhc3M9J2F0b20tMCcgc3R5bGU9J2ZvbnQtc2l6ZToxNXB4O2ZvbnQtc3R5bGU6bm9ybWFsO2ZvbnQtd2VpZ2h0Om5vcm1hbDtmaWxsLW9wYWNpdHk6MTtzdHJva2U6bm9uZTtmb250LWZhbWlseTpzYW5zLXNlcmlmO3RleHQtYW5jaG9yOnN0YXJ0O2ZpbGw6I0U4NDIzNScgPjI8L3RleHQ+Cjx0ZXh0IHg9JzM1LjAnIHk9JzUzLjYnIGNsYXNzPSdhdG9tLTAnIHN0eWxlPSdmb250LXNpemU6MjNweDtmb250LXN0eWxlOm5vcm1hbDtmb250LXdlaWdodDpub3JtYWw7ZmlsbC1vcGFjaXR5OjE7c3Ryb2tlOm5vbmU7Zm9udC1mYW1pbHk6c2Fucy1zZXJpZjt0ZXh0LWFuY2hvcjpzdGFydDtmaWxsOiNFODQyMzUnID5PPC90ZXh0Pgo8L3N2Zz4K O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 54
- 230000004151 fermentation Effects 0.000 claims abstract description 32
- 238000006243 chemical reaction Methods 0.000 claims abstract description 30
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 19
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 19
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- 238000000034 method Methods 0.000 claims description 41
- 229910052757 nitrogen Inorganic materials 0.000 claims description 36
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- NHNBFGGVMKEFGY-UHFFFAOYSA-N nitrate Chemical compound 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[O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 5
- 238000011068 load Methods 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N acetic acid Chemical compound 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Abstract
本发明公开了一种污泥发酵耦合反硝化处理污泥消化液的控制装置及方法,属于高氨氮废水处理及初沉污泥生化处理技术领域。该装置设有原水水箱、污泥发酵耦合反硝化反应器,沉淀池和污泥贮存池;通过安装在好氧反应区和发酵耦合反硝化反应区的ORP/pH传感器,优化控制曝气量供给,出水回流比例以及初沉污泥投加的频率和质量。本发明适用于投加初沉污泥作为反硝化碳源的污泥消化液处理优化控制,可以节省碳源,提高脱氮效率。并且该控制策略还具有操作简单,效果明显的优点。
Description
污泥发酵耦合反硝化处理污泥消化液的控制装置与方法
技术领域
[0001] 本发明涉及消化污泥脱水液处理工艺的优化控制技术,属于高氨氮废水处理及初沉污泥生化处理技术领域。反应系统以城市污水厂初沉污泥为底物,水解酸化产生的可挥发性有机酸作为反硝化菌去除硝态氮的电子供体,在一体化装置内同时实现消化污泥脱水液的深度脱氮和初沉污泥的初步稳定。通过监控处理过程中PH和ORP的数值和变化,优化运行条件,强化处理效果。
背景技术
[0002] 我国在2002年颁布的《城镇污水处理厂污染物排放标准》(GB18918-2002)中要求所有排污单位出水水质为氨氮小于5mg/L,总氮小于15mg/L (—级A标准)。氮的去除已经成为当今污水处理和再生回用的主要问题。为到达日益严格的排放标准,降低运行成本,许多污水厂面临工艺的升级改造以及工艺的优化运行问题。
[0003] 城市污水处理厂中的污泥厌氧消化过程中,微生物通过脱氨基作用将部分氨氮释放到上清液中,导致污泥消化上清液以及后续的污泥脱水液的氨氮浓度高达500-1000mg/L,碳氮比相对较低。消化污泥脱水液的水量虽然只占整个污水处理厂的2%,但是氨氮负荷占整个污水处理厂的25%左右。传统的方法是将消化污泥脱水液直接回流到污水处理厂前端,但是这明显增大了反应区进水的氨氮负荷,导致出水水质难以到达日益严格的污水处理厂排放标准。消化污泥脱水液氨氮浓度高,水量小,单独处理与回流到主反应区相比,节省占地面积,减少基建投资,更加经济高效。因此合理高效的消化污泥脱水液旁侧处理技术对提高污水处理厂出水水质有重要意义。
[0004] 在消化污泥脱水液生物法脱氮过程中,碳源不足成为限制反硝化效果的主要因素。传统的硝化反硝化反应处理消化污泥脱水液,总氮去除率不高。为解决这一问题,提高总氮去除率,提供额外的碳源强化反硝化效果是有效的方法。将污水处理厂初沉污泥厌氧发酵并控制反应过程在 水解酸化阶段,利用产生的可挥发性脂肪酸等碳源补充反硝化过程中的电子供体,提高反硝化速率和总氮去除率。与此同时,初沉污泥初步稳定,有利于后续的处理和处置。该方法相比传统脱氮工艺可以节省外加碳源,降低运行费用,并同时进行污泥的初步处理,是符合可持续发展规律的工艺,应用市场广阔。
[0005] 发酵耦合反硝化处理消化污泥脱水液工艺的脱氮效果受不同方面的影响。第一,氨氮氧化效果。在后续的反硝化和发酵过程中,都只能去除硝态氮而对氨氮没有去除效果,因此在好氧区未被氧化的氨氮会直接进入出水,降低总氮去除率。第二,反硝化效果。如果反硝化碳源不足,或是反应停留时间太短,硝态氮不能被充分还原成氮气,则会产生亚硝酸盐等中间产物,造成出水总氮升高。第三,在发酵过程中,可能产生部分的氨氮。将发酵产生的氨氮回流到前段可以继续氧化成硝态氮并通过反硝化去除。三个部分的协同配合才能保证出水氨氮低于设定的水平,并且最大限度的利用初沉污泥中的碳源,避免浪费。
[0006] 污水处理工艺的过程控制可大大提高工艺的运行性能、可靠性、灵活性和运行效率,降低污水厂改造或扩建所需的基建费用。国外关于污水处理厂的过程控制和运行优化研究已有相关报道,而国内对活性污泥法过程控制的研究仍然较少。研究消化污泥脱水的液处理的过程控制,可以提高出水水质,充分利用初沉污泥中的碳源。保证了运行的稳定性和抗冲击负荷能力,对整个污水处理厂的升级改造也有重要意义。
发明内容
[0007] 本发明为提高污泥脱水液脱氮处理效率,提出了消化污泥脱水液处理的优化控制技术方法。通过设置在好氧反应器(A/0)和发酵耦合反硝化反应器(Sifeden)中的pH/ORP传感器,控制硝化过程进行到亚硝酸盐,并且控制初沉污泥的投加频率,避免反硝化过程中碳源不足。优化控制手段保证系统的反硝化效果,解决现有工艺处理能力存在的局限性。
[0008] 本发明的具体方案为:一种污泥发酵耦合反硝化处理污泥消化液的控制装置,包括依次连接的原水水箱1、硝化反应器、沉淀池8,其中的硝化反应器由缺氧反应器3、第一好氧反应器4、第二好氧反应器5、第三好氧反应器6、第四好氧反应器7组成,沉淀池部分污泥经污泥回流泵14回流到硝化反应器首段;沉淀池8的出水全部进入发酵耦合反硝化反应器中的反应区9和静置沉淀区10 ;沉淀区的上清液溢流出水,通过出水管路11排出系统;部分出水通过出水回流管路12和出水回流蠕动泵13回流到反应器前端;
[0009] 在硝化生物反应器末端安装硝化区ORP/pH传感器16,在发酵耦合反硝化反应器的反应区9安装发酵/反硝化区ORP/pH传感器17,另外设置与计算机系统21相连的过程控制器20用以接受硝化区ORP/pH传感器16和发酵/反硝化区ORP/pH传感器17的信号;经过程控制器的初沉污泥投加控制信号输出与初沉污泥投加计量泵18和出水回流蠕动泵13相连接;分别用以控制从污泥贮存池19向反应区9投加的污泥量和出水回流到缺氧反应器3的水量。
[0010] 利用上述的污泥发酵耦合反硝化处理污泥消化液的控制装置实现的控制方法,主要包括以下步骤:
[0011] 步骤1:原水水箱I中的高氨氮消化污泥脱水液进入到硝化反应器;缺氧反应器3利用原水中含有的碳源反硝化污泥回流中携带的部分硝态氮,去除部分总氮;在好氧区中,通过空压机15提供氧气,将原水中的氨氮转化为硝态氮;空压机15的气量由过程控制器的输出信号A控制;
[0012] 步骤2:好氧区中的混合液随后进入到沉淀池8进行沉淀;泥水分离后,部分污泥通过蠕动泵14回流以保证反应器的污泥浓度基本稳定,上清液溢流出水进入后续的反应器;
[0013] 步骤3:沉淀池8出水进入污泥发酵耦合反硝化反应器,同时初沉污泥投加计量泵
18将污泥贮存池19中储存的新鲜初沉污泥加入到反应区9;蠕动泵的开启和流量由过程控制器的输出信号C控制;在该反应器内初沉污泥发酵提供给反硝化菌电子供体,硝态氮被还原成氮气,从而达到总氮去除的目的;
[0014] 步骤4:静置沉淀区10进行泥水分离,沉淀污泥直接通过底部回流到反应区9 ;上清液溢流排出系统;部分的出水通过出水回流蠕动泵13和出水回流管路12进入到缺氧反应器3 ;出水回流的流量由过程控制器的输出信号B控制,可以补充原水中缺乏的碱度和碳源,并且将产生的氨氮再次处理,降低出水总氮。
[0015] 本发明通过简单方便的物化指标对高氨氮污泥消化液处理进行过程控制,可以明显提高反应的稳定性和系统的脱氮效率。通过过程控制手段使发酵与耦合反硝化反应器保持在ORP在-300mv以下的厌氧状态,这样初沉污泥发酵过程被控制在产酸段,硝酸盐还原菌利用发酵产物如乙酸等进行反硝化反应,同时达到污泥减量和消化污泥脱水液脱氮的作用。通过好氧反应器末端PH和ORP值,控制曝气量和出水回流。在该种优化控制下,硝化效果得以保证,避免曝气量不足或进水碱度不足导致的氨氮氧化不完全。与传统的污泥碳源开发工艺定时定量投加相比相比,该种工艺对初沉污泥碳源开发和应用灵活高效,通过硝态氮对产甲烷的抑制可以延长固体停留时间,提高碳源的利用效率;通过出水回流可以回收碱度,同时提高发酵过程中的PH值,强化发酵和反硝化效果。此外,本发明具有如下优
占-
^ \\\.[0016] I)经济高效。该优化控制手段只采用两个ORP/pH传感器,设置简单响应时间短,回路少简化了控制算法,提高了控制的效率。与化学指标比如氨氮浓度,硝酸盐浓度在线传感器,或者是利用超声波的泥位控制器相比,成本有明显的降低,运行管理方便。
[0017] 2)初沉污泥充分利用。与传统的污泥发酵淘洗工艺相比,该种优化控制条件下固体平均停留时间增加,产酸菌生存环境适宜。发酵产物被硝酸盐还原菌大量消耗,减弱了底物抑制作用,发酵速率可以进一步提高。
[0018] 3)对总氮去除的控制更加优化。在该工艺的优化控制下,整个系统中的氮转化相关过程,如硝化,反硝化,碳源供给,碱度产生等,进行了有机的结合,使得总氮去除的各个环节都不受到明显的抑制,从而可以保证总氮去除效率。
附图说明
[0019] 图1为本发明装置的结构示意图
[0020] 图2为应用过程优化控制前后的总氮去除效果的情况图
`[0021] 图中:1-原水水箱;2-进水泵;3-缺氧反应器;4-第一好氧反应
器;5—第二好氧反应器;6—第三好氧反应器;7—第四好氧反应器;8—沉淀池;9——Sifeden反应器反应区;10——Sifeden反应器静置沉淀区;11——出水管路;12——
出水回流管路;13-出水回流蠕动泵;14-污泥回流泵;15-空气压缩机;16-硝
化区ORP/pH传感器;17—发酵/反硝化区ORP/pH传感器;18——初沉污泥投加计量泵;
19—污泥贮存池;20—过程控制器;21—计算机。
具体实施方式
[0022] 结合附图和实施例对本申请专利进一步的说明:如图1所示,本发明的污泥发酵耦合反硝化装置,由污泥脱水液的原水水箱1,硝化反应器,沉淀池8,污泥发酵耦合反硝化反应器9-10。原水水箱I为400L,硝化反应器为有机玻璃质地的单廊道反应器,有效容积为36L,其中缺氧反应器体积4L,好氧反应器的体积均为8L。好氧反应器通过空压机提供曝气,曝气头采用砂石曝气头。为避免好氧反应器之间的反混,各个反应器通过隔板分离,隔板上的合适位置设连通管。污泥发酵耦合反硝化反应器的反应区9的有效容积为150L,反应器尺寸为OH=50cmX90cm,静置沉淀区10的容积100L。在缺氧反应器3和污泥发酵耦合反硝化反应器的反应区9都安装搅拌桨进行连续搅拌,保证污泥混合,强化传质作用。在硝化反应器的末端安装硝化区ORP/pH传感器16,其采集的数据通过连接线与过程控制器20连接,并最终输入到与过程控制器相连接的计算机21。在污泥发酵耦合反硝化反应器的反应区安装发酵/反硝化区ORP/pH传感器17,其输出的数据也连接到过程控制器20和计算机21。计算机21运行模拟后的指令通过过程控制器20的A、B、C三个输出端口分别与空气压缩机15,出水回流蠕动泵13,初沉污泥投加计量泵18相连。对曝气的气体流量,出水回流水量,初沉污泥的投加及投加量进行控制。
[0023] 实施例使用的污泥脱水液取自北京市某污水处理厂污泥脱水间,其典型的氨氮浓度值在350-400mg/L,碱度约为2000mg/L(以CaCO3计),碱度不足以充分硝化原水中的氨氮。污泥贮存池中的初沉污泥池的污泥取自污水厂重力浓缩池后的压力管道,该污泥为典型的初沉污泥,浓度15kgMLSS/m3,TCOD为20g/L,挥发性污泥浓度MLVSS与污泥浓度MLSS的比值在0.67〜0.8之间。
[0024] 利用上述装置的操作方法步骤如下:
[0025] I)接种污泥:硝化反应器的接种污泥取自某污水处理厂的二沉池回流污泥,该污泥脱氮效果和沉降性能良好。将该污泥投加到硝化反应器,接种后反应器的混合液污泥浓度约为4000mg/L。此外,取北京某城市污水处理厂新鲜污泥储存于初沉污泥贮存池,并一次性向发酵耦合反硝化反应器的反应区9加入150L新鲜初沉污泥,根据初沉污泥的性质,调整并维持反应区9的污泥浓度范围在10〜15kgMLSS/m3 [0026] 2)启动阶段:硝化反应器启动好氧反应器的曝气系统15进行氨氮的硝化反应,维持溶解氧D0=l-2mg/L,开始间歇式闷曝若干小时。当混合液氨氮NH1-N <25mg/L时,开始启动进蠕动泵2进行连续运行,打开缺氧反应器3的搅拌器,以及污泥回流泵14。按照从低负荷到正常负荷梯度增加的运行方式逐渐提高进水流量,以进行污泥驯化,当沉淀池出水NH; -N<25mg/L时,确认其启动结束进入平稳运行阶段。
[0027] 开启污泥发酵耦合反硝化反应器恒温水浴区的电加热系统,设定反应器温度维持在35°C,启动反应区9反应器的搅拌装置,沉淀池8的溢流进水连续进入反应区9。进水硝态氮浓度在280-350mg/L。控制水力停留时间为10h,使出水中的硝态氮浓度维持在IOmg/L以上。每天定时从反应区排出混合污泥50L,加入新鲜初沉污泥50L。这种运行方式可以使得反硝化菌迅速生长,同时利用产甲烷菌生长世代时间长的特点,通过排泥逐渐将反应器中的产甲烷菌淘洗出系统。在上述条件下运行,反应器的反硝化速率不再进一步提高时,确认启动结束进入平稳运行期。
[0028] 3)连续运行:硝化反应器和污泥发酵耦合反硝化反应器成功启动后,进入连续运行时期。硝化反应器的水流停留时间设为20h,污泥回流比为50%。沉淀池8的出水全部进入到后续的反应区9。静置沉淀区的出水部分回流到硝化反应器的前端,回流水量为原水水量的100%。提供反硝化碳源的初沉污泥为间歇投加。两次投加污泥的中间阶段作为一个运行周期,每次投加新鲜污泥50L。投加方式为排出反应区一定体积污泥,并投加同样体积的新鲜初沉污泥。
[0029] 4)优化控制:待系统连续稳定运行20天后,开启控制回路对整个反应流程进行优化控制。第四好氧反应器7安装ORP/pH在线传感器,在线采集ORP/pH数据,通过实测值和ORP设定范围进行比较来确定空气压缩机的出风量以及出水回流泵的流量。污泥发酵耦合反硝化反应器反应区9安装ORP/pH在线传感器,在线采集ORP/pH数据,将ORP实测值和设定值的偏差e以及两个在线传感器,硝化区ORP/pH传感器16和发酵/反硝化区ORP/pH传感器17的pH值的差值作为初沉污泥投加模糊控制器的输入变量,输入的双变量经模糊化处理,对初沉污泥投加计量泵进行控制。
[0030] 连续的试验结果表明:试验以北京某城市污水处理厂真实的消化污泥脱水液为处理对象。硝化反应器的温度为25°C左右,进水氨氮浓度350-400mg/L,COD浓度250_320mg/L,进水碱度2000mg/L (以CaCOj+)左右。污泥发酵耦合反硝化反应器温度为35°C,污泥浓度MLSS保持在10-15kgMLSS/m3,水力停留时间20h,平均固体停留时间15d,通过过程控制稳定运行3个月。试验结果表明:系统出水N0:、<10mg/L,每个周期TCOD下降到8000mg/L, MLVSS/MLSS的比值下降到0.35,反硝化能力为0.lkgN/kgVSS,当量VFA的产量为0.5mgVFA/ (mgVSS.d)。优 化控制前后的总氮去除变化规律如图2所示。
Claims (2)
1.一种污泥发酵耦合反硝化处理污泥消化液的控制装置,包括依次连接的原水水箱(I)、硝化反应器、沉淀池(8),其特征在于硝化反应器由缺氧反应器(3)、第一好氧反应器(4)、第二好氧反应器(5)、第三好氧反应器(6)、第四好氧反应器(7)组成,沉淀池部分污泥经污泥回流泵(14)回流到硝化反应器首段;沉淀池(8)的出水全部进入发酵耦合反硝化反应器中的反应区(9)和静置沉淀区(10);静置沉淀区的上清液溢流出水,通过出水管路(II)排出系统;部分出水通过出水回流管路(12)和出水回流蠕动泵(13)回流到硝化反应器前端; 在硝化生物反应器末端安装硝化区ORP/pH传感器(16),在发酵耦合反硝化反应器的反应区(9)安装发酵/反硝化区ORP/pH传感器(17),另外设置与计算机系统(21)相连的过程控制器(20)用以接受硝化区ORP/pH传感器(16)和发酵/反硝化区ORP/pH传感器(17)的信号;经过程控制器的初沉污泥投加控制信号输出与初沉污泥投加计量泵(18)和出水回流蠕动泵(13)相连接;分别用以控制从污泥贮存池(19)向反应区(9)投加的污泥量和出水回流到缺氧反应器(3)的水量。
2.利用权 利要求1所述的污泥发酵耦合反硝化处理污泥消化液的控制装置实现控制的方法,其特征在于包括以下步骤: 步骤1:原水水箱(I)中的高氨氮消化污泥脱水液进入到硝化反应器;缺氧反应器(3)利用原水中含有的碳源反硝化污泥回流中携带的部分硝态氮,去除部分总氮;在好氧区中,通过空压机(15)提供氧气,将原水中的氨氮转化为硝态氮;空压机(15)的气量由过程控制器的输出信号A控制; 步骤2:好氧区中的混合液随后进入到沉淀池(8)进行沉淀;泥水分离后,部分污泥通过污泥回流泵(14)回流以保证反应器的污泥浓度基本稳定,上清液溢流出水进入后续的反应器;步骤3:沉淀池(8)出水进入污泥发酵耦合反硝化反应器,同时初沉污泥投加计量泵(18)将污泥贮存池(19)中储存的新鲜初沉污泥加入到反应区(9);初沉污泥投加计量泵(18)的开启和流量由过程控制器的输出信号C控制;在该反应器内初沉污泥发酵提供给反硝化菌电子供体,硝态氮被还原成氮气,从而达到总氮去除的目的; 步骤4:静置沉淀区(10)进行泥水分离,沉淀污泥直接通过底部回流到反应区(9);上清液溢流排出系统;部分的出水通过出水回流蠕动泵(13)和出水回流管路(12)进入到缺氧反应器(3);出水回流的流量由过程控制器的输出信号B控制,可以补充原水中缺乏的碱度和碳源,并且将产生的氨氮再次处理,降低出水总氮。
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