CN105174642A - 一种污水高效生物脱氮方法 - Google Patents
一种污水高效生物脱氮方法 Download PDFInfo
- Publication number
- CN105174642A CN105174642A CN201510652387.3A CN201510652387A CN105174642A CN 105174642 A CN105174642 A CN 105174642A CN 201510652387 A CN201510652387 A CN 201510652387A CN 105174642 A CN105174642 A CN 105174642A
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- Prior art keywords
- pond
- sewage
- anoxic pond
- carbon source
- hydrolysis acidification
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- 239000010865 sewage Substances 0.000 title claims abstract description 86
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 45
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 45
- 238000000034 method Methods 0.000 claims abstract description 45
- 241000894006 Bacteria Species 0.000 claims abstract description 37
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 31
- 230000020477 pH reduction Effects 0.000 claims abstract description 31
- 239000010802 sludge Substances 0.000 claims abstract description 28
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- 238000007254 oxidation reaction Methods 0.000 description 1
- ABLZXFCXXLZCGV-UHFFFAOYSA-N phosphorous acid Chemical compound 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Abstract
本发明公开了一种污水高效生物脱氮方法，污水依次流经沉砂池、厌氧池、缺氧池1、缺氧池2、好氧池、沉淀池进行处理；在缺氧池1后面续接混合液水解酸化池，利用兼性微生物和厌氧微生物将污水中不能被反硝化菌利用的有机物和活性污泥中的有机物部分转化为反硝化碳源；在混合液水解酸化池中，缺氧池1出水中的NO3-N被反硝化去除，并在混合液水解酸化池后续接缺氧池2，利用混合液水解酸化池中产生的反硝化碳源进行生物脱氮。本发明方法在不外加碳源、降低电耗、不影响其他污染物去除的前提下，采用活性污泥法，将污水和污泥中原来不能被反硝化菌利用的有机物转化成反硝化碳源，提高污水厂生物脱氮效果，降低污水厂出水中TN浓度，使出水TN达到5.0mg/L以下。
Description
技术领域
[0001] 本发明涉及一种污水高效生物脱氮方法，属于污水处理领域。
背景技术
[0002] 我国现有城镇污水厂3000余座，总处理能力达1.46亿m3/d，实际处理总量约1.2亿m3/d。一般采用二级活性污泥法处理城镇生活污水，主要工艺为A20、氧化沟、SBR。城镇生活污水中的污染物主要包括有机物(以C0D&、BOD5表示)、N污染物(以NH 3_N、TN表示)、P污染物、SS等，大量污水厂的实际运行经验表明，除TN外，其它污染物在污水厂均能很好地被去除，生物脱氮除磷二级污水厂出水C0D&、BOD5, NH3-N, TP、SS等均易达到地表IV类水体要求。但TN的去除率与回流比有关，一般地，回流比(含内回流和外回流)不超过400%，TN去除率亦不超过80%，出水TN在11 ±3mg/L左右，能够达到国家一级A标准，无法达到地表IV类水体要求(S1.5mg/L)。
[0003] 污水厂出水的最终出路多为河流或湖泊，而N元素为主要的植物营养元素之一，污水厂出水TN较高，属于超富营养类型，不利于保持和改善城市水环境，采用再生水补充城市河湖，容易造成水体水质恶化，水体富营养化现象时有发生，为此，许多城市通过提标改造，增建生物脱氮深度处理设施，用来降低出水TN。二级污水厂后续生物脱氮设施，不仅增加了工程投资，工艺流程冗长、占地面积大、管理繁杂，而且由于城镇生活污水中的有机物在二级处理时已经被去除，深度处理生物脱氮时必定要求外加碳源，导致生产再生水的成本高昂。按目前市场价格计算(3000元/吨)，反硝化去除TN = lmg/L，外加碳源费用约0.01元/m3。我国污水处理量约为1.46亿m3/d，则每去除TN = lmg/L,外加碳源费用约为146万元/d、5.33亿元/年；若平均深度处理生物脱氮6mg/L，则外加碳源费用约为31.98亿元/年。深度生物脱氮设施电耗约0.03度/m3.d，电价以0.62元/度计，则深度处理污水1.46亿m3/d，电费需271.6万元/d、9.91亿元/年。以上二者合计，在二级污水处理后建设深度生物脱氮设施，增加的经常性费用约为41.89亿元/年，另外，深度处理设施还增加了运行管理工作量，增加了人工成本。此外，现有生物脱氮污水厂脱氮率低下的原因在于，在污水厂进水中反硝化碳源较少，约占进水有机物的20%，污水中的多数有机物不能被反硝化菌利用，制约了污水厂的生物脱氮效果。
[0004]目前，我国城镇生活污水处理厂出水N指标较高，污水厂出水的最终出路为天然水体，导致我国自然水体和人工水体富营养化，水环境状况持续恶化、生态系统堪忧，为控制和改善水环境状况、提升生态水平，国家每年需要投入大量的经费。因此，科学采用活性污泥法，在不外加碳源、降低电耗的条件下，利用进水中的碳源在污水生物处理厂进行深度生物脱氮，具有巨大的经济效益。而且在污水处理厂进行深度生物脱氮能够缩短工艺流程、减少占地面积，简化运行管理、降低污水厂运行人工费；提高出水水质、提升生态环境水平，具有重大的社会效益和环境效益。
发明内容
[0005] 本发明所要解决的技术问题是针对现有技术中存在的不足，而提供一种污水高效生物脱氮方法，该方法在不外加碳源、降低电耗、不影响其他污染物去除的前提下，采用活性污泥法，将污水中不能被反硝化菌利用的有机物和活性污泥中的有机物转化为反硝化碳源，提高污水厂的生物脱氮效果，降低污水厂出水中TN浓度，使出水TN能够达到5mg/L以下。
[0006] 为了实现上述目的，本发明采用如下技术方案:
[0007] —种污水高效生物脱氮方法，污水依次流经沉砂池、厌氧池、缺氧池1、缺氧池2、好氧池、沉淀池进行处理，在所述的厌氧池和缺氧池I中污水中的既有的反硝化碳源被反硝化菌充分利用，缺氧池I出水中的有机物难于被反硝化菌利用；在所述的缺氧池1、缺氧池2之间续接混合液水解酸化池，经过缺氧池I处理后的出水流入所述的混合液水解酸化池；在混合液水解酸化池内污水中不能被反硝化菌利用的有机物以及活性污泥中的有机物部分转化为反硝化碳源；所述的混合液水解酸化池出水流入缺氧池2内，在缺氧池2中，反硝化菌利用混合液水解酸化池产生的反硝化碳源继续进行生物脱氮处理，提高了污水厂的生物脱氮效果。
[0008] 上述技术方案中，经缺氧池I处理后的出水，部分流入所述的混合液水解酸化池，另一部分流入缺氧池2 (传输量为r3Q)，水解酸化池含有反硝化碳源的出水流入缺氧池2后继续进行处理。
[0009] 上述技术方案中，经过所述的缺氧池2处理后的出水流入好氧池内进行处理，所述的好氧池内含有硝化细菌，污水经过硝化细菌作用后将NH3-N转化为NO3-N,经硝化作用后的出水中富含NO3-N,富含NO3-N的出水回流至缺氧池I (回流量为0)或/和缺氧池2 (回流量为r2Q)，利用反硝化碳源进行生物脱氮处理，实现生物脱氮作用。
[0010] 上述技术方案中，所述的好氧池出水回流至缺氧池I或/和缺氧池2进行处理，最终处理后的出水流入沉淀池进行泥水分离，沉淀池上清液为处理后的洁净水排出即可，沉淀池污泥回流至(回流量为RQ)厌氧池，用以保证生化系统的污泥浓度，剩余污泥排除出活性污泥系统。
[0011] 上述技术方案中，所述的沉淀池回流至厌氧池的回流污泥中NO3-N浓度低，厌氧池内的反硝化菌可以彻底地去除厌氧池中的NO3-N,从而使厌氧池内水体中的NO3-N浓度低，在厌氧池中形成了严格的厌氧条件；厌氧池内的聚磷菌过量吸收的磷被充分释放出来，增强了聚磷菌在好氧池的过量吸磷能力，提高了生物除磷效果，污水厂沉淀池出水TP均值能够直接达到一级A。
[0012] 上述技术方案中，所述的混合液水解酸化池中含有的兼性微生物和厌氧微生物，将污水中不能被反硝化菌利用的有机物以及活性污泥中的有机物部分转化为易生物降解的有机物和挥发性脂肪酸，这些有机物和挥发性脂肪酸可作为反硝化碳源继续利用，从而增加了污水中的反硝化碳源。
[0013] 上述技术方案中，所述的混合液水解酸化池中的反硝化碳源被反硝化菌利用，将污水中在缺氧池I中没有被去除的NO3-N反硝化去除，提高了污水厂的生物脱氮效果。
[0014] 本发明的技术优点在于:
[0015] 在不外加碳源、降低电耗、不影响污水厂对其它污染物去除效果的前提下，采用活性污泥法，将污水中原来不能被反硝化菌利用的有机物和活性污泥中的有机物部分转化为反硝化碳源，增加污水中的反硝化碳源，提高污水厂的生物脱氮效果，降低污水厂出水中TN浓度；该方法提高了污水厂出水水质，减少了深度处理生物脱氮所需投加的碳源量，提升了生态环境水平，具有重大的经济效益、环境效益和社会效益。
附图说明
[0016] 图1:本发明方法的工艺流程图；
[0017] 图2:本发明水解池的结构示意图；
[0018] 图3:实施例1中，本发明方法对NH3-N的去除效果；
[0019] 图4:实施例1中，本发明方法对TN的去除效果；
[0020] 图5:实施例1中，本发明方法对CODfr的去除效果；
[0021 ] 图6:实施例1中，本发明方法对TP的去除效果。
具体实施方式
[0022] 以下对本发明技术方案的具体实施方式详细描述，但本发明并不限于以下描述内容:
[0023] 本发明所述的污水高效生物脱氮方法的具体方案(如图1所示)为:污水厂进水经过沉砂池后依次经过厌氧池和缺氧池1，在厌氧池和缺氧池I中污水中的反硝化碳源被充分用于生物脱氮，剩下的有机物难于被反硝化菌利用，并且有部分NO3-N没有被反硝化去除；这种污水部分流入混合液水解酸化池、部分流入缺氧池2 (流量为r3Q)，或者全部流入混合液水解酸化池。混合液水解酸化池中的兼性微生物和厌氧微生物，将污水中不能被反硝化菌利用的有机物和污泥中的有机物部分转化为易生物降解的有机物和挥发性脂肪酸，增加了污水中的反硝化碳源，同时污水中没有被去除的NO3-N也在水解酸化池中被反硝化去除，提高了污水厂的生物脱氮效果。混合液水解酸化池出水流入缺氧池2，在缺氧池2内反硝化菌利用混合液水解酸化池产生的反硝化碳源继续进行生物脱氮作用，之后的出水流入好氧池。好氧池内含有硝化细菌，将污水中NH3-N转化为NO3-N,经硝化作用后的出水中富含NO3-N,富含NO3-N的出水回流至缺氧池I (回流量为F1Q)或/和缺氧池2 (回流量为r2Q)，利用反硝化碳源进行生物脱氮处理，最终处理后的出水流入沉淀池。在沉淀池内进行泥水分离后，上清液为处理后的洁净水排出即可，沉淀池污泥回流至(回流量为RQ)厌氧池，保持系统中的污泥浓度，剩余污泥排除出活性污泥系统。沉淀池回流至厌氧池的回流污泥中NO3-N浓度低，厌氧池内的反硝化菌可以彻底地去除池中的NO3-N,从而使厌氧池内水体中的NO3-N浓度低，在厌氧池中形成了严格的厌氧条件；厌氧池内的聚磷菌过量吸收的磷被充分释放出来，增强了聚磷菌在好氧池的过量吸磷能力，提高了生物除磷效果，污水厂沉淀池出水TP均值能够直接达到一级A。
[0024] 本发明方法中的设备，按污水流动方向依次包括沉砂池、厌氧池、缺氧池1、混合液水解酸化池、缺氧池2、好氧池、沉淀池:所述的沉砂池、厌氧池、缺氧池1、混合液水解酸化池、缺氧池2、好氧池、沉淀池均为本领域现有技术中的常规设备，并且上述设备各自的内置物(比如聚磷菌、反硝化菌、硝化菌、兼性微生物、厌氧微生物等等)也均为现有技术中的常规物质；其中，所述的混合液水解酸化池，如图2所示:上部为污水区、下部为污泥床，所述的水解池配有搅拌器4，搅拌桨伸入到污泥床中；所述的水解池下部分具有进水管1，污水自缺氧池I经进水管流入水解池中；所述的水解池顶部具有出水口 3，底部具有出泥管2，水解池内的兼性微生物和厌氧微生物将污水和污泥中的有机物降解转化为反硝化碳源，同时将污水中残留的硝氮去除后，污泥自出泥管2流入缺氧池2或排除出活性污泥系统，含有反硝化碳源的污水经出水口 3流入缺氧池2。
[0025] 下面结合具体的实施例对本发明方法进一步描述:
[0026] 实施例1:
[0027] 在我国南方某市的污水厂，采用本发明方法进行污水处理，处理结果如图3、4、5、6所示，其中，图3为本发明方法对NH3-N的去除效果(该附图中，▲代表进水NH3-N浓度，▼代表出水NO3-N浓度，〇代表NH3-N去除率)，图4为本发明方法对TN的去除效果(该附图中，▲代表进水TN浓度，▼代表出水TN浓度，O代表TN去除率)，图5为本发明方法对CODfr的去除效果(该附图中，▲代表进水CODfr浓度，▼代表出水COD &浓度，〇代表COD &去除率)，图6为本发明方法对TP的去除效果(该附图中，▲代表进水TP浓度，▼代表出水TP浓度，〇代表TP去除率):
[0028] 由图3可知，进水NH3-N在16.5-35.lmg/L,均值27.94mg/L ;沉淀池出水NH3-N在0.07-1.45mg/L，均值 0.4lmg/L ;NH3_N 去除率在 93.63-99.73%，均值 98.52%。本发明方法出水NH3-N远优于一级A ( ( 5mg/L)，稳定达到了地表IV类水体要求((1.5mg/L)，表明本发明方法硝化作用充分，能够实现充分的硝化效果。
[0029] 由图4可知，进水TN在19.5-47.lmg/L,均值33.38mg/L ；沉淀池出水TN在
3.03-6.12mg/L，均值 4.6lmg/L ；TN 去除率在 79.85-92.0%，均值 86.03%。本发明方法出水TN稳定达到了一级A(彡15mg/L)。我国城镇污水厂出水TN年均值约12±2mg/L，因此，本发明方法出水TN远优于我国城镇生活污水出水TN，实现了深度生物脱氮；原因在于本发明方法在充分利用污水中的反硝化碳源进行生物脱氮的基础上，后续混合液水解池，将污水中的不能被反硝化菌利用的有机物部分转化为反硝化碳源，增加了系统中的反硝化碳源，从而提高了生物脱氮效果。
[0030] 由图5可知，进水0©&在112-401mg/L，均值249.93mg/L ;沉淀池出水COD &在
11.1-24.7mg/L，均值 16.77mg/L ;0©&去除率在 81.43-96.29%，均值 92.92%。本发明方法出水CODfr远优于一级A( < 50mg/L)，稳定达到了地表IV类水体要求((30mg/L)，表明本发明方法的有机物的碳化作用充分，能够实现充分的碳化效果。我国城镇污水厂出水CODfr年均值约25mg/L，因此，本发明方法出水C0D&优于我国城镇生活污水出水COD &，实现了深度去除有机物；原因在于本发明方法充分发挥了反硝化菌对有机物的去除作用，在提高生物脱氮效果的同时，提高了系统对有机物的去除能力，降低了出水0©&浓度。
[0031] 由图6可知，进水TP在L 4-5.18mg/L，均值3.4lmg/L ;好氧池出水TP在0.12-0.67mg/L，均值0.39mg/L ;生物除磷去除率在78.58-93.36%，均值88.46%。本发明方法生物除磷出水TP均值能够达到一级A ( < 0.5mg/L)，但不能稳定达到一级A，需要后续化学除磷。我国城镇污水厂沉淀池出水TP均值约0.9±0.4mg/L，为保证污水厂出水TP达标排放，并去除沉淀池出水中的SS以提高污水厂出水水质，一般均在生化处理后面续接以絮凝为主的深度处理技术，因此，本发明方法生物除磷效果优于我国城镇污水厂对TP的去除效果，有利于减少深度处理时絮凝剂投加量，实现降耗运行。
[0032] 由上述结果可知:
[0033] 采用本发明方法处理城镇生活污水，将部分不能被反硝化菌利用的有机物转化为反硝化碳源，增加了活性污泥系统的反硝化碳源，生物脱氮效果好，从而降低污水厂出水TN，并提高脱氮率。最终，污水厂出水TN降低6mg/L以上，出水TN约4.61mg/L，使得污水厂脱氮率达到86.03%。
[0034] 我国城镇污水厂厌氧池内水体中的N03-N浓度较高，整个厌氧池没有形成严格的厌氧环境，降低了聚磷菌的生物除磷能力，致使污水厂二级出水TP偏高。采用本发明方法代替原有方法处理过程中，污水厂的生物脱氮效果好，回流污泥中N03-N浓度低，反硝化菌彻底地去除了厌氧池中的N03-N，在厌氧池中形成了严格的厌氧环境，提高了聚磷菌的生物除磷效果，使得污水厂沉淀池出水TP均值降低至0.5mg/L以下。
[0035] 上述实例只是为说明本发明的技术构思以及技术特点，并不能以此限制本发明的保护范围。凡根据本发明的实质所做的等效变换或修饰，都应该涵盖在本发明的保护范围之内。
Claims (7)
1.一种污水高效生物脱氮方法，污水依次流经沉砂池、厌氧池、缺氧池1、缺氧池2、好氧池、沉淀池进行处理；其特征在于:在所述的厌氧池和缺氧池I中污水中的既有的反硝化碳源被反硝化菌充分利用，缺氧池I出水中的有机物难于被反硝化菌利用；在所述的缺氧池1、缺氧池2之间续接混合液水解酸化池，经过缺氧池I处理后的出水流入混合液水解酸化池；在所述的混合液水解酸化池内，污水中不能被反硝化菌利用的有机物和活性污泥中的有机物部分转化为反硝化碳源，混合液水解酸化池出水流入缺氧池2内；在所述的在缺氧池2中，反硝化菌利用混合液水解酸化池产生的反硝化碳源继续进行生物脱氮处理。
2.根据权利要求1所述的方法，其特征在于，经缺氧池I处理后的出水，部分流入所述的混合液水解酸化池，另一部分流入缺氧池2，水解酸化池含有反硝化碳源的出水流入缺氧池2后继续进行处理。
3.根据权利要求1或2所述的方法，其特征在于，经过所述的缺氧池2处理后的出水流入所述的好氧池内进行处理，好氧池内硝化细菌将污水中的NH3-N转化为NO3-N后，富含NO3-N的出水回流至缺氧池I或/和缺氧池2，利用反硝化碳源进行生物脱氮处理，实现生物脱氮作用。
4.根据权利要求3所述的方法，其特征在于，所述的好氧池出水回流至缺氧池I或/和缺氧池2进行处理，最终处理后的出水流入沉淀池进行泥水分离，沉淀池上清液为处理后的洁净水排出即可，沉淀池污泥回流至厌氧池。
5.根据权利要求4所述的方法，其特征在于，所述的沉淀池回流至厌氧池的回流污泥中NO3-N浓度低，厌氧池内的反硝化菌彻底去除了水体中的NO3-N,从而使厌氧池内水体中的NO3-N浓度低，在厌氧池中形成了严格的厌氧条件；厌氧池内的聚磷菌过量吸收的磷被充分释放出来，增强了聚磷菌在好氧池的过量吸磷能力。
6.根据权利要求1所述的方法，其特征在于，所述的混合液水解酸化池中含有的兼性微生物和厌氧微生物，将污水中不能被反硝化菌利用的有机物以及活性污泥中的有机物部分转化为易生物降解的有机物和挥发性脂肪酸，即为所述的反硝化碳源。
7.根据权利要求1所述的方法，其特征在于，所述的混合液水解酸化池中的反硝化碳源被反硝化菌利用，将污水在缺氧池I中没有被去除的NO3-N反硝化去除。
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