CN201598224U - 一种脱氮除磷生物处理与过滤一体化的污水处理系统 - Google Patents
一种脱氮除磷生物处理与过滤一体化的污水处理系统 Download PDFInfo
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- CN201598224U CN201598224U CN2009203519325U CN200920351932U CN201598224U CN 201598224 U CN201598224 U CN 201598224U CN 2009203519325 U CN2009203519325 U CN 2009203519325U CN 200920351932 U CN200920351932 U CN 200920351932U CN 201598224 U CN201598224 U CN 201598224U
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- 239000010865 sewage Substances 0.000 title claims abstract description 37
- IJGRMHOSHXDMSA-UHFFFAOYSA-N nitrogen Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 24
- OAICVXFJPJFONN-UHFFFAOYSA-N phosphorus Chemical compound 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[P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 title claims abstract description 14
- 229910052698 phosphorus Inorganic materials 0.000 title claims abstract description 14
- 239000011574 phosphorus Substances 0.000 title claims abstract description 14
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 39
- 239000007788 liquid Substances 0.000 claims abstract description 38
- 238000005273 aeration Methods 0.000 claims abstract description 27
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 238000001914 filtration Methods 0.000 claims description 58
- 238000005276 aerator Methods 0.000 claims description 12
- 239000000835 fiber Substances 0.000 claims description 5
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- 241000276438 Gadus morhua Species 0.000 description 2
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N 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
本实用新型提供了一种脱氮除磷生物处理和过滤一体化的污水处理系统,按污水流向依次包括:反应池、好氧主曝气池、设有三相分离器的好氧固液分离池和过滤池,所述好氧固液分离池分别与所述反应池、所述好氧主曝气池通过管道相连,用于提供回流污泥。本实用新型通过生物处理和过滤工艺的有机结合,充分利用过滤工艺高效固液分离能力,以保证生物处理池达到较高污泥浓度,缩小反应池容,并通过过滤使出水悬浮物等指标达到更高标准。
Description
一种脱氮除磷生物处理与过滤一体化的污水处理系统
技术领域 [0001] 本实用新型涉及污水处理技术,具体地说,涉及一种脱氮除磷生物处理与过滤一 体化的污水处理系统。
背景技术
[0002] 生物处理工艺是污水处理中使用最广泛的处理工艺,这种工艺处理效率高,运行 稳定,是市政和工业污水处理的主流工艺。
[0003] 常规的生物处理反应池中微生物浓度只有2_4g/L,构筑物体积较大,建设投资高。 如何提高生物处理池中的微生物浓度,是改进生物处理工艺的一个主要方向。目前,提高生 物处理池中微生物浓度的方式主要有两种,一是投加生物填料,采用这种方式,好氧反应池 中污泥浓度会提高l_5g/L,对有机物的降解,特别是硝化反应,都有很大好处,池容可以缩 小1/3-1/2。另一种方式是采用膜生物反应器,最大限度地截留随出水带走的微生物,提高 反应器内的污泥浓度。膜生物反应器内,污泥浓度通常可以达到10g/L左右,可以省掉二沉 池和过滤等后续处理过程,简化污水处理流程。但膜生物反应器建设投资较高,运行能耗大 大高于常规处理工艺,膜组件寿命较短,运行维护比较复杂;这些问题,在一定程度上,限制 了膜生物反应器的推广应用。如何采用一种经济实用的方式提高生物反应池污泥浓度,是 改进生物反应器的一个主要方向。
[0004] 过滤是污水深度处理的核心工艺。近年来,污水处理厂出水排放标准不断提高,使 得过滤在污水处理过程中大量应用,过滤工艺过程和设备都有了很大改进。主要的过滤形 式有传统过滤、机械过滤等几类。与其他技术相比,过滤技术具有投资省、占地面积少和运 行成本低等特点。直接过滤或者混凝_沉淀_过滤是发达国家的城市污水厂普遍采用的深 度处理工艺。常见滤池包括普通砂滤池、移动罩滤池、V型滤池、T型滤池、D型滤池等。传 统砂滤技术存在如下缺点:占地面积大、投资高、能耗高,运行管理比较复杂;有时为防止 滋生藻类,砂滤系统还需增加预加氯装置。
[0005] 琥珀Rodisc和西门子Disk Filter的表面式过滤器是近年来发展起来的新型高 效过滤器,这类过滤器占地面积小、滤速高、过滤精度较高,但不足之处是反冲洗所需压力 较高,导致运行费用较高。织物材料过滤技术采用纤维织物介质作为过滤介质,纤维过滤设 备具有水头损失少、附属设备少、占地少、运行费用低等优点,因此,在原二级污水处理厂的 基础上,进行改造扩建变得简单易行,运行维护也更加简单方便。
[0006] 新型的过滤设备体积小,运行自动化程度高,能承受较高的处理负荷。传统的生物 处理工艺中,生物反应池污泥浓度主要靠沉淀污泥回流来保证,本实用新型采用以过滤工 艺来保证好氧池污泥浓度的好氧_过滤一体化工艺,突出过滤在整体工艺中的作用,削弱 沉淀过程,以期缩短工艺流程,减少土建投资,并提高出水水质标准。
实用新型内容
[0007] 本实用新型的目的是提供一种脱氮除磷生物处理和过滤一体化的污水处理系统,其充分利用过滤池高效固液分离能力保证好氧池达到较高污泥浓度,缩小反应池容,并通 过过滤使出水悬浮物等指标达到更高标准。
[0008] 为了实现本实用新型目的,本实用新型的一种脱氮除磷生物处理和过滤一体化的 污水处理系统,按污水流向依次包括:反应池、好氧主曝气池、设有三相分离器的好氧固液 分离池和过滤池,所述好氧固液分离池分别与所述反应池、所述好氧主曝气池通过管道相 连,用于提供回流污泥。
[0009] 其中,所述反应池为缺氧池或厌氧缺氧池。所述厌氧缺氧池由厌氧池和缺氧池组 成。
[0010] 所述反应池内设有搅拌器。
[0011] 所述好氧主曝气池采用推流或完全混合池型。
[0012] 所述好氧主曝气池内设置曝气器。
[0013] 所述好氧固液分离池内设置曝气器。
[0014] 所述过滤池内设置表面式过滤器及曝气器。
[0015] 所述表面式过滤器的过滤介质可采用纤维介质,也可采用金属介质,表面负荷 5-10m/h。
[0016] 所述表面式过滤器还与所述反应池通过管道相连,提供反抽吸污水至反应池。
[0017] 本实用新型所述污水处理系统在反应池前,还包括格栅处理池和沉砂池。
[0018] 采用本实用新型的脱氮除磷生物处理和过滤一体化的污水处理系统处理的方法, 包括以下步骤:
[0019] 1)污水先进入反应池,与来自好氧固液分离池的回流污泥混合,完成厌氧释磷和 反硝化过程;
[0020] 2)反应池的出水再进入好氧池主曝气池,完成有机物氧化和硝化过程;
[0021] 3)好氧池主曝气池出水进入好氧池固液分离池,继续完成硝化反应,并通过三相 分离器完成初步气、液、固分离过程;回流污泥从好氧固液分离池回流至反应池;
[0022] 4)好氧池固液分离池出水进入过滤池过滤并排出,过滤反冲洗水回流至反应池。
[0023] 其中,步骤1)中,通过进水情况和反应池I内ORP (氧化还原电位)值和污泥浓度 控制回流量,HRT(水力停留时间)为1-1. 5h。回流污泥与进水比例为100-300%。
[0024] 步骤2)中好氧主曝气池内设置设置曝气器7,并进行在线DO测控,控制DO浓度在 2-4之间。
[0025] 步骤3)中,所述三相分离器可根据一般厌氧UASB (升流式厌氧污泥床)反应器计 算,整体上升流速l_4m/h (通过控制进水量和增加导流措施实现)。控制出水SS (悬浮物) 在50mg/L左右。回流污泥和剩余污泥都从该好氧池固液分离池排出。在此反应器中,逐 步完成污泥颗粒化,形成好氧菌在外层,兼性菌和厌氧菌在内层的结构,实现同步硝化反硝 化。
[0026] 步骤4)中,过滤采用机械表面过滤器(比如表面式过滤器),滤速l-10m/h,过滤 过程中持续曝气,以增加过滤介质表面液体流速,避免堵塞过滤器。根据采集的液位差数据 控制反冲洗过程,过滤器定时或进行反冲洗,反冲洗采用抽吸原理,利用反抽吸泵用滤后水 进行反冲洗,同时排出过滤池积泥,滤池底部设有排泥管,利用反抽吸泵排泥。
[0027] 步骤4)中,好氧池固液分离池内的剩余的活性污泥还可通过管道定期进行排放。[0028] 污水在进入反应池前,还包括对所述污水进行预处理,所述预处理包括格栅处理 和沉砂池处理;采用格栅从污水中去除可能堵塞水泵机组及管道阀门的较粗大悬浮物,并 保证后续处理设施能正常运行;采用沉砂池从污水中去除砂子、煤渣等比重较大的颗粒,以 免这些杂质影响后续处理构筑物的正常运行。
[0029] 与现有技术相比,本实用新型的技术方案具有如下优点:
[0030] 1)缩短流程,减少反应器体积,减少建设投资:传统的脱氮除磷工艺一般包括厌 氧、缺氧、好氧、沉淀、过滤等工艺过程,流程较长,大中型工程中采用的沉淀池通常是圆形, 无法与其他构筑物合建,使得各构筑物必须分体建设,占地面积较大,建设投资较高。本实 用新型采用三相分离技术代替沉淀,利用过滤技术实现最终固液分离,缩短工艺过程,减少 构筑物数量,减少建设投资。另一方面,由于不需要依靠回流污泥保证生物反应器内的污泥 浓度,可以大大提高生物反应器内的污泥量,提高反应速度,缩小反应器体积。
[0031] 2)与投加填料增加生物反应池污泥浓度的方法相比,节省生物填料投资,避免了 填料运行管理上的问题,无须提高生物池内DO浓度(溶解氧浓度)维持生物处理运行,节 省能耗。
[0032] 3)最终采用过滤技术实现固液分离,出水水质好,对一般城市污水,出水可以达到 《城镇污水处理厂水污染物排放标准》一级A标准。
[0033] 4)生物池内采用三相分离器,升流速度较高,有利于排出部分絮状污泥,逐步实现 污泥颗粒化,进一步提高污泥浓度,增强同步硝化反硝化效果,提高TN去除率。
附图说明
[0034] 图1为本实用新型所述脱氮除磷生物处理与过滤一体化的污水处理系统的流程 图。
[0035] 图2为本实用新型所述厌氧缺氧池的结构示意图。
[0036] 图中:
[0037] I 缺氧或厌氧缺氧反应池 II好氧池主曝气池
[0038] III好氧池固液分离池 IV过滤池
[0039] V 出水池 1 进水
[0040] 2 出水 3 压缩空气
[0041] 4 剩余污泥 5 回流污泥
[0042] 6 搅拌器 7 曝气器
[0043] 8 三相分离器 9 表面式过滤器
[0044] 10回流污泥泵 11剩余污泥泵
[0045] 12 阀门 13 出水堰
[0046] 14 回流泵 15 反抽吸污水
具体实施方式
[0047] 以下实施例用于说明本实用新型,但不用来限制本实用新型的范围。
[0048] 实施例1
[0049] 如图1所示,本实用新型脱氮除磷生物处理与过滤一体化的污水处理方法,其处理过程为:原污水1首先进入反应池I,根据进水水质和出水要求,反应池I可以设置为单独的缺氧池或厌氧和缺氧池。在反应池I内设置搅拌器6,完成反硝化和厌氧释磷过程后, 进入好氧主曝气池II,完成有机物降解和硝化过程,而后进入好氧固液分离池III。在好氧 固液分离池III,设置三相分离器8,污泥混合液利用三相分离器,完成初步固液分离过程, 上清液进入过滤池IV,在过滤池IV中进一步完成精细过滤过程,使出水达到排放标准,进 入出水池V,最终排放。设置污泥内回流泵10,完成从好氧固液分离池III到反应池I和好 氧主曝气池II的污泥回流,保证反应池污泥浓度,实现反硝化和除磷。设置剩余污泥泵11, 完成剩余污泥排放过程,保证合适的污泥龄和污泥浓度。
[0050] 本实用新型一种脱氮除磷生物处理与过滤一体化的污水处理系统,依次包括如 下:
[0051] 1.反应池I
[0052] 反应池I可采用两种形式,单独缺氧池或厌氧缺氧池。单独作为缺氧池时,原污水 与回流污泥同时进入反应池I,回流比100-300%,停留时间根据进水浓度计算。作为厌氧 缺氧池时,反应池I分为两格,原污水1进入第一格Ia厌氧池,回流污泥5进入第二格Ib 缺氧池,第二格设置内回流泵14,将泥水混合物回流到第一格,见图2所示。反应池I设置 搅拌器6a、6b,搅拌器的形式和功率根据池型计算得到,保证泥水混合均勻。
[0053] 在反应池I内设置在线ORP仪和污泥浓度计,根据ORP值和污泥浓度值控制回流 污泥阀门12,控制回流量。HRT(水力停留时间)为1-1. 5h。
[0054] 2.好氧主曝气池II
[0055] 好氧主曝气池II可采用推流或完全混合池型,设置曝气器7,压缩空气3经曝气器 7,进入曝气池内。停留时间根据水质计算得到。部分回流污泥进入好氧主曝气池II,保证 污泥浓度。
[0056] 好氧主曝气区内设置在线DO仪,控制DO浓度在2-4之间。
[0057] 3.好氧固液分离池III
[0058] 好氧主曝气池II的泥水混合物通过池底的导流装置(设于池的侧壁上)进入好 氧固液分离池III,要保证在池宽方向布水均勻。固液分离区上升流速为l_4m/h,采用三相 分离器进行气液固分离,三相分离器计算与厌氧反应器类似,出水经出水堰13进入过滤池 IV。好氧固液分离区也设置曝气器7,继续完成生物反应。在池底设置回流污泥泵10和剩 余污泥泵11,污泥回流量为进水量的100-300%,剩余污泥泵根据水质计算流量。
[0059] 好氧固液分离区内设置在线DO仪,控制DO浓度在2-4之间。
[0060] 4.过滤池 IV
[0061] 过滤池IV内设置表面式过滤器9,过滤后的水由外侧进入表面式过滤器中心管 内,流到出水池。过滤池内沿表面式过滤器设置曝气器,通过曝气加强表面式过滤器表面液 体流动,减轻表面式过滤器表面污染,增加过滤周期,曝气强度为2-4m3/m2.h。经过一段时 间过滤,表面式过滤器表面有一定污染物,造成过滤池IV液位增加,启动过滤器反抽吸机 构,进行在线清洗。表面式过滤器过滤介质可采用纤维介质,也可采用金属介质,表面负荷 5-10m/h。
[0062] 在过滤池IV中设置液位计,根据液位或时间控制反抽吸过程。反抽吸污水15回 到反应池I或好氧主曝气区II。[0063] 5.出水池V [0064] 过滤后出水进入出水池V,排放或回用。
[0065] 本实用新型所涉及的表面式过滤器、曝气器、搅拌器等设备均可采用本领域熟知 的设备。
[0066] 试验例
[0067] 以某生活污水处理工程为例,对本实用新型脱氮除磷生物处理与过滤一体化的污 水处理系统的应用情况进行说明测试。
[0068] 某污水处理项目,进水以生活污水为主,水量IOOOm3AL进水污染物浓度如下:
[0069] 表1污染物浓度指标
[0070]
[0071] 缺氧池、好氧主曝气池和好氧固液分离区总有效容积520m3,其中缺氧池有效容积 104m3,水深4米,HRT2. 5h,好氧固液分离池有效容积104m3,回流比150%,上升流速4m/h, 水深4米,好氧主曝气区有效容积312m3。过滤单元采用纤维转盘过滤器,滤盘直径2米,数 量2个,有效过滤面积10. 4m2,滤速10m/h。经过各处理单元处理后,处理出水污染物变化 情况如下:
[0072] 表2各处理单元出水情况
[0073]
[0074] 其中TN出水浓度与碳源有关,在本项目中,出水要求《城镇污水处理厂污染物排 放》一级B标准,因此未考虑外加碳源。如果要求继续降低TN出水浓度,可以考虑增加外加 碳源,TN出水浓度可以控制在15mg/L左右。
[0075] 虽然,上文中已经用一般性说明及具体实施方案对本实用新型作了详尽的描述, 但在本实用新型基础上,可以对之作一些修改或改进,这对本领域技术人员而言是显而易 见的。因此,在不偏离本实用新型精神的基础上所做的这些修改或改进,均属于本实用新型 要求保护的范围。
Claims (7)
- 一种脱氮除磷生物处理和过滤一体化的污水处理系统,其特征在于,按污水流向依次包括:反应池、好氧主曝气池、设有三相分离器的好氧固液分离池和过滤池,所述好氧固液分离池分别与所述反应池、所述好氧主曝气池通过管道相连,用于提供回流污泥。
- 2.根据权利要求1所述的污水处理系统,其特征在于,所述反应池为缺氧池或厌氧缺氧池。
- 3.根据权利要求1或2所述的污水处理系统,其特征在于,所述反应池内设有搅拌器。
- 4.根据权利要求1或2所述的污水处理系统,其特征在于,所述好氧主曝气池内、所述 好氧固液分离池内分别设置曝气器。
- 5.根据权利要求1或2所述污水处理系统,其特征在于,所述过滤池内设置表面式过滤 器及曝气器。
- 6.根据权利要求5所述污水处理系统,其特征在于,所述表面式过滤器的过滤介质采 用纤维介质或采用金属介质,表面负荷5-10m/h。
- 7.根据权利要求1或2所述污水处理系统,其特征在于,所述污水处理系统在反应池 前,还包括格栅处理池和沉砂池。
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CN102173537A (zh) * | 2011-03-15 | 2011-09-07 | 北京科泰兴达高新技术有限公司 | 一体化生化过滤污水处理设备 |
CN101746931B (zh) * | 2009-12-30 | 2012-08-15 | 浦华环保有限公司 | 一种脱氮除磷生物处理与过滤一体化的污水处理系统及其方法 |
CN102963976A (zh) * | 2011-09-01 | 2013-03-13 | 株式会社水环境研究所 | 有机性排水的处理方法及有机性排水处理系统 |
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CN103787497A (zh) * | 2012-10-29 | 2014-05-14 | 浦华环保有限公司 | 一种污水处理系统及其应用 |
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