CN204022558U - 一种节能型mbr氧化沟污水处理装置 - Google Patents
一种节能型mbr氧化沟污水处理装置 Download PDFInfo
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- CN204022558U CN204022558U CN201420274630.3U CN201420274630U CN204022558U CN 204022558 U CN204022558 U CN 204022558U CN 201420274630 U CN201420274630 U CN 201420274630U CN 204022558 U CN204022558 U CN 204022558U
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- 238000011030 bottleneck Methods 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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- ABLZXFCXXLZCGV-UHFFFAOYSA-N phosphorous acid Chemical compound 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OP(O)=O ABLZXFCXXLZCGV-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N phosphorus Chemical compound 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Abstract
本实用新型涉及利用生物技术处理污水的技术领域，提出一种节能型MBR氧化沟污水处理装置，其包括氧化沟生化反应区和膜区，膜区的直廊道与氧化沟生化反应区的S形廊道首尾对接构成循环廊道，膜区底部架空设置有穿孔花墙平板，穿孔花墙平板将膜区上、下分成膜池和配水区，穿孔花墙平板上均匀分布有配水孔，膜区进水口位于配水区的前端；膜池内设有膜组件和出水管，氧化沟生化反应区设置有进水装置、剩余污泥排放口、推流装置和曝气装置。本实用新型将氧化沟工艺与膜生物反应器有机结合，利用氧化沟工艺大流量循环推流态的水力运行特征，使沟槽内的混合液循环并迅速流经MBR膜组器实现固液分离，有结构简单紧凑、运行能耗低、占地面积小、投资省、污染物去除效率高等优点。
Description
技术领域
[0001] 本实用新型涉及利用生物技术处理污水的技术领域，是一种MBR氧化沟污水处理 装直。
背景技术
[0002] 水环境质量恶化态势的加剧，对污水处理率及处理程度提出了更高的标准；与此 同时，随着城市化进程的加快，对污水处理程度、处理设施的用地、及其建成后对周边环境 的不利影响都提出了更为严格的要求。在这之中，高效、低耗的污水深度处理工艺及设备的 开发与应用成为当前水环境治理的热点。
[0003] MBR (膜生物反应器）是一种将膜分离技术与生物处理相结合的污水处理技术，它 具有固液分离效果好(采用膜过滤方式)、占地面积小(省去了二沉池)、剩余污泥排放少(污 泥浓度高、泥龄长)、自动化程度高等诸多优点，因此，该技术开发至今备受国内外的关注。
[0004] 但是，MBR工艺自身固有的高运行能耗、高处理费用、以及除磷效果不佳等缺陷也 成为了该技术推广应用的瓶颈；另一方面，我国南方城市因气候和生活习惯不同，城市污水 中污染物浓度通常较低（CODcr浓度通常都低于300 mg/L)，污水中一低两高(低碳高氮磷） 的现状，导致城市污水处理厂污泥负荷处于较低水平、污泥活性降低，进而限制了出水水质 的进一步提高；此外，为维持膜组器良好的出水效果，MBR工艺在运行过程中必须采取强曝 气的方式对膜丝表面进行吹扫，由此而带来大量的能耗。这些都限制了 MBR工艺的进一步 推广应用。
[0005] 而现有传统的MBR工艺是将A2O工艺(或其衍生工艺）的各生化单元与膜单元简 单串联，两单元各自独立运行，仅通过混合液回流维系二者的联系。其缺点表现在以下几 个方面：X能耗高，吨水能耗基本在〇. 7fcTl. OKw之间，其能耗主要发生在生化池曝气、膜 池气扫风量(气水比15:1)、膜池产水系统及内回流系统，其中膜池气扫能耗约占总能耗的 3(T40%; t污泥浓度的差异，膜池高、生化池低，这与污水生化处理相悖(生化池高污泥浓 度利于污染物降解，膜池低污泥浓度利于固液分离、降低气扫风量）；:f系统复杂、运行管理 难度较大，A 2O-MBR工艺各单元之间存在较复杂的混合液回流(一般至少三套内循环系统， 即膜池至好氧区、好氧区至缺氧区、缺氧区至厌氧区)，不仅增加了工程投资和运行费用，而 且使系统变得更加复杂，增加了运行管理难度。
[0006] 因此，若要推广MBR工艺在污水处理领域中的应用，需要对以下几个方面进行深 入的探讨和研究：其一为膜污染和膜成本，在降低膜成本的同时提高膜的寿命，解决膜污染 问题，降低能耗，减少运行成本；其二为膜运行能耗的降低，为降低膜污染需大量的鼓风曝 气对膜表面进行吹扫，浪费了大量的能源，应对膜吹扫能源的再利用进行研究，进一步降低 MBR膜过滤工艺的运行能耗；其三，需要研发活性污泥工艺与MBR工艺组合的新技术流程， 以期利用最低成本获得最佳出水效果。
[0007] 氧化沟工艺污泥负荷低、水力停留时间长、循环流量大、抗冲击负荷强，可不设初 沉池和污泥消化池，流程简单、维护管理方便、处理效果稳定、运行成本低，是备受欢迎的二 级处理工艺。通过对目前国内成功运行的污水处理厂抽样调查分析显示，氧化沟工艺的COD 平均处理成本仅为其它工艺的90% ;氧化沟工艺的吨水电耗平均为0. 30kW. h/m3, A2O工艺的 吨水电耗平均为0. 34 kW. h/m3, SBR工艺的污水处理厂的吨水电耗平均为0. 31 kW. h/m3。
[0008] 经过几十年的实践和发展，氧化沟处理技术被认为是出水水质好、运行可靠、运行 费用低的污水生物处理方法，美国环境保护署的报告指出："氧化沟能够通过最低限度的操 作，稳定地达到BOD和TSS的去除率要求。"美国曾对13种处理水平、24种二级生化及二级 处理系统进行技术经济比较，结果表明，除去渗滤系统外，氧化沟是最为经济的。但是，传统 氧化沟工艺固有的曝气方式单一、充氧效率低、池体水深浅、占地面积大、污泥膨胀等缺点 亦限制了该技术的应用。
[0009] 因此，需要开发一种多工艺优化组合的低能耗、高效能的污水处理工艺。 实用新型内容
[0010] 本实用新型的目的是提供一种节能型MBR氧化沟污水处理装置，将MBR池与氧化 沟有机结合，具有占地面积少、投资省、运行维护简单、低能耗高效能的优点。
[0011] 一种节能型MBR氧化沟污水处理装置，包括氧化沟生化反应区和膜区，氧化沟生 化反应区为S形廊道，膜区为直廊道，膜区的直廊道与氧化沟生化反应区的S形廊道首尾对 接构成循环廊道，膜区的两端分别设有第一导流墙和第二导流墙；第一导流墙的下端开有 膜区进水口，第二导流墙的上端开有膜区出水口，膜区底部架空设置有穿孔花墙平板，穿孔 花墙平板将膜区上、下分成膜池和配水区，穿孔花墙平板分布配水孔，膜区进水口位于配水 区的前端。
[0012] 第一导流墙使氧化沟生化反应区流至此处的混合液从膜区进水口进入膜区底部 的配水区，再通过穿孔花墙平板的配水孔均匀向上流入膜池；膜池混合液经第二导流墙上 方的膜区出水口流入氧化沟生化反应区。
[0013] 膜池内设有膜组件和出水管，膜组件和出水管连接通；氧化沟生化反应区的侧壁 底部设置有剩余污泥排放口以及共壁设置的剩余污泥排放装置，氧化沟生化反应区的上方 设有进水装置，氧化沟生化反应区内设有推流装置和曝气装置。
[0014] 优化方案是：氧化沟生化反应区具有并排且共壁设置的第一直廊道、第二直廊道 和第三直廊道，相互间由小弧廊道连接通，第三直廊道与膜区并排共壁设置，第三直廊道端 通过小弧廊道与膜区的一端连接通，膜区的另一端通过大弧廊道与第一直廊道端连接通， 进水装置分别于第一直廊道、第二直廊道和第三直廊道的上方设有进水口。
[0015] 进一步优化方案是：膜区底部的配水区为前深后浅的渐变截面结构，近膜区进水 口端较深。
[0016] 再优化方案是：用隔板将膜区按顺水流方向分隔成独立的左膜区和右膜区，相对 应地膜池也被分为左膜池和右膜池，配水区被分为左配水区和右配水区，右膜区近第一导 流墙端设有前右闸门，近第二导流墙端设有后右闸门，左膜区近第一导流墙端设有前左闸 门，近第二导流墙端设有后左闸门，这样的设置是可以在系统正常运行时分别对左膜池和 右膜池的膜组件进行各自独立清洗。
[0017] 本实用新型应用时与现有工艺相比具有以下优点：
[0018] (I)MBR与氧化沟融为一体，可借助氧化沟大流量水力循环的特点，将膜区高浓度 溶解氧迅速推流入生化区用于有机物降解，一方面消除了高浓度污泥对膜池泥水分离的不 利影响；另一方面可迅速将膜池中的高富氧混合液推流入生化池内，膜池高溶氧得到有效 利用，降低了膜吹扫及生化区的鼓风曝气量。
[0019] ( 2 )膜池进水通过导流墙、从底部穿孔花墙配水孔进入膜区，水流方向与气流及膜 丝方向保持一致，在消除水流对膜丝横向不利剪切的同时，对膜丝产生了坚向水力吹扫的 动力，可降低用于膜吹扫的鼓风曝气量，延长了膜组件的使用寿命。
[0020] (3)膜区底部的配水区的变截面结构设计，可有效消除廊道内的污泥沉降。
[0021] (4)利用氧化沟自身特点，在沟槽内自然实现低氧区与缺氧区的交替运行，同时配 置以多点进水，提高了系统的脱氮效能。
[0022] (5)实现了膜组件的在线清洗，在线清洗时，可关闭膜区的一侧闸门，同时开启另 一侧闸门，将水流切换至膜区的一侧，依次进行在线清洗，清洗完成后，恢复正常运行。
[0023] (6)膜区与生化区混合液浓度基本一致，可在整个池体的任一部分排除剩余污泥。
[0024] (7)本实用新型取消了传统MBR工艺的三大内循环系统，简化了污水处理工艺流 程，降低了运行费用。
[0025] 建议设计时将氧化沟与污泥浓缩池合建，重力排除剩余污泥，浓缩后上清液泵提 至氧化沟廊道内。
[0026] 本技术方案的有益效果是将氧化沟工艺与MBR工艺有机结合起来，不仅可以较好 地解决传统MBR工艺所存在的缺陷，而且可以大幅度降低系统运行能耗，从而降低污水处 理费用，使污水处理工艺流程更加简洁，也使运行维护管理更加方便。本实用新型可用于生 物脱氮除磷污水处理厂的新建和改造工程，可减少城市污水厂占地面积和处理能耗(单位 处理能耗降低10%以上)，提商城市污水厂出水品质。
附图说明
[0027] 图1是本实用新型的一实施例结构平面示意图。
[0028] 图2是图1的膜区池体底部穿孔花墙配水孔分布示意图。
[0029] 图3是图1的膜区池体剖面示意图。
具体实施方式
[0030] 下面用一优选实施例对本实用新型作进一步说明。
[0031] 实施例一
[0032] 参考图1、图2、图3, 一种节能型MBR氧化沟污水处理装置，包括氧化沟生化反应区 1和膜区2,氧化沟生化反应区1为S形廊道，膜区2为直廊道，膜区2的直廊道与氧化沟生 化反应区1的S形廊道首尾对接构成循环廊道，氧化沟生化反应区1具有并排且相邻接的 第一直廊道11、第二直廊道12和第三直廊道13,相互间由小弧廊道连接通，第三直廊道13 与膜区2并排邻接，第三直廊道13端通过小弧廊道与膜区2的一端连接通，膜区2的另一 端通过大弧廊道14与第一直廊道11端连接通。
[0033] 膜区2的两端设有第一导流墙21和第二导流墙22 ;第一导流墙21的下端开有膜 区进水口 20,第二导流墙的上端设有膜区出水口 10,膜区底部架空设置有穿孔花墙平板5， 穿孔花墙平板5将膜区2上、下分成膜池2b和配水区2a，穿孔花墙平板5均匀分布配水孔 50,膜区进水口 20位于配水区2a的前端。
[0034] 第一导流墙21使氧化沟生化反应区1流至此处的混合液从膜区进水口 20进入膜 区2底部的配水区2a，再通过穿孔花墙平板5的配水孔50均匀向上流入膜池2b ;膜池混合 液经第二导流墙22上方的膜区出水口 10流入氧化沟生化反应区1。
[0035] 膜池2b内设有膜组件d和出水管4,膜组件d和出水管4连接通；氧化沟生化反 应区1的侧壁底部设置有剩余污泥排放口 6以及共壁设置的剩余污泥排放装置e，氧化沟生 化反应区1的上方设有进水装置7,氧化沟生化反应区1内设有推流装置a和曝气装置b。
[0036] 进水装置7于第一直廊道11、第二直廊道12和第三直廊道13的上方分别设有带 调节阀的进水口 71、72和73。
[0037] 用隔板8将膜区2按顺水流方向分隔成独立的左膜区和右膜区，相对应地膜池2b 也被分为左膜池和右膜池，配水区2a被分为左配水区和右配水区。
[0038] 右膜区近第一导流墙21端设有前右闸门cl，近第二导流墙22端设有后右闸门 c3,左膜区近第一导流墙21端设有前左闸门c2,近第二导流墙22端设有后左闸门c4。
[0039] 膜区2底部的配水区2a为前深后浅的渐变截面结构，近膜区进水口 20端较深，底 面倾斜度为3°。
[0040] 试验采用某城市污水为原水，进水中的主要水质指标为：C0Dcr为25(T350 mg/L， TSS 为 240 mg/L，NH4+-N 为 25〜30 mg/L，TN 为 30〜35 mg/L，TP 为 3· 0〜5· 0 mg/L ;试验中所 采用的分析方法均按照《水和废水监测分析方法(第四版)》中的标准方法。
[0041] 应用本实用新型的具体运行操作如下：
[0042] 正常运行时，前右闸门cl、前左闸门c2、后右闸门c3、后左闸门c4全部打开。
[0043] 预处理后污水流入氧化沟中部的进水渠7中，预处理后的污水按3:2:1的比例分 别由进水口 71、72、73进入池体的第一直廊道11、第二直廊道12和第三直廊道13 ;在推流 器a的作用下，待处理污水与池体中的混合液迅速混合并推流至整个池体；混合液推流至 膜区2前时，经第一导流墙21的膜区进水口 20进入膜区池体底部的配水区2a ;配水区2a 中的混合液经池体底部的穿孔花墙配水孔50均匀向上流至膜池2b，上向流水流与膜组件 中的鼓风吹扫曝气共同坚向流，对膜丝产生抖动、吹扫作用；而后，混合液经第二导流墙22 流出膜区2进入氧化沟生化区1 ;部分剩余污泥经污泥排放口 6流出池体；膜池2b中的混 合液经膜组件d分离后，处理后的清水经出水管4流出。
[0044] 本实施例污水处理规模为2万m3/d，池体中污泥浓度为6000mg/L，污泥龄25d ;生 化区水力停留时间为9. 2h，池体有效水深4. 0m，膜区水力停留时间为I. 2h，氧化沟沟槽总 长度为406m。
[0045] 按照上述具体实施方式的步骤，活性污泥在系统中经过2个月的驯化和培养后， 出水 〇©(^、55、順4+，、了队了？的平均浓度为17.8 11^/1、5.0 11^/1、0.3 11^/1、7.6 11^/1、0.35 mg/L。出水水质优于《污水综合排放标准（GB8978-1996)》一级A标准要求；膜区气水比为 8:1，与传统A2O-MBR工艺相比，降耗约40%、吨水运行成本降低0. 2元/吨水。
[0046] 本实用新型可实现膜组件的在线连续清洗，对系统的正常运行无任何影响，具体 操作如下。
[0047] (1)当要清洗右膜池中的膜组件时，将前右闸门cl和后右闸门c3关闭，此时，右膜 池和右配水区相对独立于整个处理系统之外，可对该池中的膜组件执行清洗措施；而前左 闸门c2和后左闸门c4保持打开，整个系统中的混合液均经膜区进水口 20进入左配水区后 经穿孔花墙配水孔50进入左膜池，系统继续正常运行。
[0048] (2)当要清洗左膜池中的膜组件时，开启前右闸门cl和后右闸门c3,关闭前左闸 门c2和后左闸门c4,使左膜池和和左配水区相对独立于整个处理系统之外，可对该池中的 膜组件执行清洗措施；整个系统中的混合液均经膜区进水口 20进入右配水区后经穿孔花 墙配水孔50进入右膜池，系统维持正常运行。
[0049] 左、右膜池中的膜组件全部清洗完毕后，将前右闸门cl、前左闸门c2、后右闸门 c3、后左闸门c4全部打开，恢复正常运行状态。
[0050] 实施例二
[0051] 本实施例与实施例一的区别是：取消隔板8、前右闸门cl、前左闸门c2、后右闸门 c3、和后左闸门c4。
[0052] 本实施例不能实现膜组件的在线连续清洗，运行时没有前右闸门cl、前左闸门 c2、后右闸门c3、后左闸门c4的操作，其它操作与实施例一相同。
Claims (6)
1. 一种节能型MBR氧化沟污水处理装置，包括氧化沟生化反应区（I)和膜区（2)，其特 征是：氧化沟生化反应区（1)为S形廊道，膜区（2)为直廊道，膜区（2)的直廊道与氧化沟生 化反应区（1)的S形廊道首尾对接构成循环廊道，膜区的两端分别设有第一导流墙（21)和 第二导流墙（22);第一导流墙（21)的下端开有膜区进水口（20)，第二导流墙（22)的上端设 有膜区出水口（10)，膜区底部架空设置有穿孔花墙平板（5)，穿孔花墙平板（5)将膜区（2) 上、下分成膜池（2b)和配水区（2a)，穿孔花墙平板（5)上均匀分布有配水孔（50)，膜区进水 口（20)位于配水区（2a)的前端； 第一导流墙（21)使氧化沟生化反应区（1)流至此处的混合液从膜区进水口（ 20)进入 膜区（2)底部的配水区（2a)，再通过穿孔花墙平板（5)的配水孔（50)均匀向上流入膜池 (2b);膜池混合液经第二导流墙（22)上方的膜区出水口（ 10)流入氧化沟生化反应区（1); 膜池（2b)内设有膜组件（d)和出水管（4)，膜组件（d)和出水管（4)连接通；氧化沟 生化反应区（1)的侧壁底部设置有剩余污泥排放口（6)以及共壁设置的剩余污泥排放装置 (e)，氧化沟生化反应区（1)的上方设有进水装置（7)，氧化沟生化反应区（1)内设有推流装 置（a)和曝气装置（b)。
2. 根据权利要求1所述的节能型MBR氧化沟污水处理装置，其特征在于，氧化沟生化 反应区（1)具有并排共壁设置的第一直廊道（11 )、第二直廊道（12)和第三直廊道（13)，相 互间由小弧廊道连接通，第三直廊道（13)与膜区（2)并排共壁设置，第三直廊道（13)端通 过小弧廊道与膜区（2)的一端连接通，膜区（2)的另一端通过大弧廊道（14)与第一直廊道 (11)端连接通。
3. 根据权利要求2所述的节能型MBR氧化沟污水处理装置，其特征在于，进水装置（7 ) 分别位于第一直廊道（11)、第二直廊道（12)和第三直廊道（13)的上方设置有带调节阀的 进水口。
4. 根据权利要求1或2或3所述的节能型MBR氧化沟污水处理装置，其特征在于：膜 区（2)底部的配水区（2a)为前深后浅的渐变截面结构，近膜区进水口（20)端较深。
5. 根据权利要求1或2或3所述的节能型MBR氧化沟污水处理装置，其特征在于：用 隔板（8)将膜区（2)按顺水流方向分隔成独立的左膜区和右膜区，相对应地膜池（2b)被分 为左膜池和右膜池，配水区（2a)被分为左配水区和右配水区，右膜区近第一导流墙（21)端 设有前右闸门（cl)，近第二导流墙（22)端设有后右闸门（c3)，左膜区近第一导流墙（21)端 设有前左闸门（c2)，近第二导流墙（22)端设有后左闸门（c4)。
6. 根据权利要求5所述的节能型MBR氧化沟污水处理装置，其特征在于：膜区（2)底部 的配水区（2a)为前深后浅的渐变截面结构，近膜区进水口（20)端较深。
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103951063A (zh) * | 2014-05-27 | 2014-07-30 | 广州市市政工程设计研究院 | 一种节能型mbr氧化沟污水处理装置 |
| CN107434298A (zh) * | 2017-08-23 | 2017-12-05 | 长沙中联重科环境产业有限公司 | 廊道式污水处理系统和采用该系统进行污水处理的方法 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103951063A (zh) * | 2014-05-27 | 2014-07-30 | 广州市市政工程设计研究院 | 一种节能型mbr氧化沟污水处理装置 |
| CN103951063B (zh) * | 2014-05-27 | 2015-04-29 | 广州市市政工程设计研究院 | 一种节能型mbr氧化沟污水处理装置 |
| CN107434298A (zh) * | 2017-08-23 | 2017-12-05 | 长沙中联重科环境产业有限公司 | 廊道式污水处理系统和采用该系统进行污水处理的方法 |
| CN107434298B (zh) * | 2017-08-23 | 2021-03-02 | 长沙中联重科环境产业有限公司 | 廊道式污水处理系统和采用该系统进行污水处理的方法 |
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