CN104211252B - 垃圾渗滤液短程硝化反硝化脱氮工艺 - Google Patents
垃圾渗滤液短程硝化反硝化脱氮工艺 Download PDFInfo
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- CN104211252B CN104211252B CN201410409480.7A CN201410409480A CN104211252B CN 104211252 B CN104211252 B CN 104211252B CN 201410409480 A CN201410409480 A CN 201410409480A CN 104211252 B CN104211252 B CN 104211252B
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- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 12
- 239000001301 oxygen Substances 0.000 claims abstract description 12
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- 239000007787 solid Substances 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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[C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 14
- 229910052799 carbon Inorganic materials 0.000 abstract description 14
- -1 nitrite nitrogen Chemical compound 0.000 abstract description 13
- 238000009825 accumulation Methods 0.000 abstract description 6
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 239000000126 substance Substances 0.000 abstract description 3
- 238000005273 aeration Methods 0.000 abstract 1
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound 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Abstract
一种垃圾渗滤液短程硝化反硝化脱氮工艺，首先通过厌氧反应将渗滤液中大分子难降解有机物分解为小分子可生化碳源，充分利用渗滤液中原有的碳源进行短程硝化反硝化脱氮，减少了外加碳源的投加量，经济效果显著；其次可严格控制较低、稳定的溶解氧浓度，保证亚硝态氮积累率高且稳定，具有较高的脱氮效率，且脱氮过程中减少了曝气量，节省能耗，运行成本低；最后可实现不同负荷下的渗滤液的脱氮处理，保证出水水质达到设计标准。
Description
技术领域
[0001]本发明属于环保技术领域，具体讲就是涉及一种垃圾渗滤液短程硝化反硝化脱氮工艺。
背景技术
[0002]垃圾处理不管是采取填埋，还是焚烧的方式，垃圾渗滤液的处理都是其中的技术难题。垃圾渗滤液是一种高氨氮高浓度有机废水，水质水量稳定性差，微生物营养元素比例失调，氨氮元素过高导致废水污染土壤和环境，随着人们生活水平的提高，人们环保意识日益加强，对垃圾渗滤液的脱氮处理势在必行。目前高氨氮渗滤液脱氮过程中处理难点和重点在于，反硝化所需的碳源严重不足。
[0003]传统的生物脱氮工艺包括自养硝化与异养反硝化两个阶段，这种工艺适用于高碳源低氨氮有机废水的脱氮处理，对于高氨氮垃圾渗滤液不仅抑制硝化菌生长，而且较低的C/N比在反硝化脱氮过程中远远不能满足碳源的需求，致使脱氮过程中需要大量投加反硝化有机碳源;另外，这种传统工艺过程中硝化细菌增殖速度慢引起总水力停留时间较长，使得构筑物体积增大，从而导致整个工艺存在运行费用较高的不足之处，不能广泛适用于大规模地工程化应用。
[0004]为了进一步提高现有垃圾渗滤液的脱氮能力，市场上开发出一种新型的生物脱氮工艺短程硝化反硝化工艺。短程硝化反硝化工艺是将氨氣的氧化控制在亚硝氣阶段，达到系统内亚硝酸盐氮的大量积累，系统内的亚硝酸氮能够以氨氮或有机物基质作为氧化还原的电子供体，直接反应生成氮气，达到去除总氮的目的。此工艺缩短了反应历程，不需要外加碳源，溶解氧浓度低，具有较高的脱氮效率等。但是，这种工艺的短程硝化反硝化的两个主要反应步骤中，反硝化阶段容易控制，但是如何将NH/-N氧化控制在N02—-N阶段，阻止其进一步氧化的不易控制，使整个处理过程中亚硝氮积累不稳定且积累率低、总氮去除效率低。
发明内容
[0005] 本发明的目的是针对上述现有垃圾渗滤液脱氮硝化处理工艺中，亚硝氮积累不稳定且积累率低、总氮去除效率低的技术缺陷，提供垃圾渗滤液脱氮工艺及其专用装置，将圾渗滤液脱氮硝化处理工艺中的NH/-N氧化控制在NO2--N阶段，阻止其进一步氧化，有效提高了总氣去除效率。
[0006]技术方案
[0007]为了实现上述技术目的，本发明设计一种垃圾渗滤液短程硝化反硝化脱氮工艺，其特征在于，它包括以下几个步骤:
[0008]第一步，厌氧处理:将垃圾渗滤液进行厌氧处理，使其实现气液固三相分离，得到厌氧出水；
[0009]第二步，反硝化:将步骤I中的厌氧出水进行反硝化处理，降低含氮量；
[0010]第三步，硝化:将步骤2的反硝化出水，进行硝化处理，得到硝化出水；
[0011]第四步，多级反硝化:将步骤3硝化池出水进行多级反硝化作用，得到多级反硝化出水；
[0012]第五步，多级硝化:将步骤4得到的多级反硝化池出水进行多级硝化处理，得到多级硝化出水；
[0013]第六步，泥水分离:将步骤5得到的多级硝化出水通入泥水分离设备，进行泥水分离，出水进入产水箱。
[0014]进一步，所述第一步中厌氧反应温度控制在25〜55°C的范围。
[0015] 所述第二步中反硝化反应温度为20〜40°C、pH为7.0〜8.3、溶解氧DOS 0.2mg/L。
[0016] 所述第三步中硝化反应温度为20〜40 °C，DO为0.6〜1.2mg/L，pH值为7.0〜8.6。
[0017] 所述第四步中多级反硝化反应温度为20〜40 °C、pH值为7.0〜-8.3、溶解氧DOg0.2mg/L0
[0018] 所述第五步中多级硝化反应温度为20〜40°C，D0为0.6〜1.2mg/L，pH为7.0〜8.6。
[0019] 所述第六步中泥水分离反应温度为20〜40°C，00为1.0〜4.011^/1，？!1值为7.0〜
8.6ο
[0020]用于上述垃圾渗滤液短程硝化反硝化脱氮的专用装置，其特征在于:它包括厌氧反应器，反硝化池，硝化池，多级反硝化池，多级硝化池，泥水分离设备，原水箱，进水栗，产水箱；
[0021]原水箱与厌氧反应器连接，连接管路上装有进水栗，厌氧反应器输出端连接反硝化池，反硝化池输出端连接到硝化池，硝化池输出端连接到多级反硝化池，多级反硝化池输出端连接到多级硝化池，多级硝化池输出端连接到泥水分离设备，泥水分离设备输出端连接产水箱。
[0022]进一步，所述厌氧反应器中设有恒温控制器，厌氧反应器底部与上部之间连接有循环回流栗；
[0023]进一步，所述反硝化池中设有第一搅拌机；
[0024]进一步，所述硝化池中设有第一曝气器，硝化池与反硝化池之间有回流管路连接，连接管路上装有第一硝化液回流栗。
[0025]进一步，所述多级反硝化池中设有第二搅拌机。
[0026]进一步，所述多级硝化池中设有第二曝气器，多级硝化池与多级反硝化池之间有回流管路连接，连接管路上装有第二硝化液回流栗。
[0027]进一步，所述泥水分离设备中设有第三曝气器，泥水分离设备与反硝化池之间有污泥回流栗连接，可将泥水分离设备中的污泥部分回流至反硝化池。
[0028] 有益效果
[0029]本发明首先通过厌氧反应将渗滤液中大分子难降解有机物分解为小分子可生化碳源，充分利用渗滤液中原有的碳源进行短程硝化反硝化脱氮，减少了外加碳源的投加量，经济效果显著;其次可严格控制较低、稳定的溶解氧浓度，保证亚硝态氮积累率高且稳定，具有较高的脱氮效率，且脱氮过程中减少了曝气量，节省能耗，运行成本低;最后可实现不同负荷下的渗滤液的脱氮处理，保证出水水质达到设计标准。
附图说明
[0030]附图1是本发明的工艺流程图。
[0031]附图2是本发明的设备连接关系示意图。
具体实施方式
[0032]下面结合附图和实施例，对本发明做进一步说明。
[0033] 实施例
[0034]如附图2所示，用于上述垃圾渗滤液短程硝化反硝化脱氮的专用装置，其特征在于:它包括厌氧反应器I，反硝化池2，硝化池3，多级反硝化池4，多级硝化池5，泥水分离设备6，原水箱7，进水栗8，产水箱12;
[0035]原水箱7与厌氧反应器I连接，连接管路上装有进水栗8，厌氧反应器I输出端连接反硝化池2，反硝化池2输出端连接到硝化池3，硝化池3输出端连接到多级反硝化池4，多级反硝化池4输出端连接到多级硝化池5，多级硝化池5输出端连接到泥水分离设备6，泥水分离设备6输出端连接产水箱12。
[0036]所述厌氧反应器I中设有恒温控制器13，厌氧反应器I底部与上部之间连接有循环回流栗9;
[0037]所述反硝化池2中设有第一搅拌机14;
[0038]所述硝化池3中设有第一曝气器15，硝化池3与反硝化池2之间有回流管路连接，连接管路上装有第一硝化液回流栗10。
[0039]所述多级反硝化池4中设有第二搅拌机14’。
[0040]所述多级硝化池5中设有第二曝气器15’，多级硝化池5与多级反硝化池4之间有回流管路连接，连接管路上装有第二硝化液回流栗10’。
[0041]所述泥水分离设备6中设有第三曝气器15”，泥水分离设备6与反硝化池2之间有污泥回流栗11连接，可将泥水分离设备6中的污泥部分回流至反硝化池2。
[0042] 利用上述专用装置进行垃圾渗滤液脱氮处理的工艺过程是:
[0043]第一步厌氧处理:垃圾渗滤液从厌氧反应器的底部进入，在循环回流栗的作用下，废水与污泥充分混合并快速上升，在反应温度为25〜55°C的条件下，大量有机物被分解产生沼气迅速上升，气液固三相上升至三相分离器后，污泥经三相分离器的沉降面返回厌氧反应器主体，沼气经由三相分离器的集气室排出，含有悬浮污泥的污水进入三相分离器的沉降区，经沉淀后从厌氧反应器顶部出水口排出。
[0044]第二步反硝化:上述厌氧出水与硝化池的硝化回流液、泥水分离设备中回流污泥混合进入反硝化池，反硝化池中设有搅拌机，在温度为20〜40 °C、溶解氧DO < 0.2mg/L、pH=7.0〜8.3的条件下进行反硝化反作用，将亚硝态氮和硝态氮转变为氮气从反应器中溢出，出水进入硝化池。
[0045]第三步硝化:上述第二步的反硝化池出水进入硝化池，微生物在温度为20〜40 °C、溶解氧DO = 0.6〜1.2mg/L、pH = 7.0〜8.6的条件下，进行硝化作用，将废水中的氨氮转化成亚硝态氮和硝态氮，同时，按照R ^ 30的回流比将最终硝化液回流至反硝化池，为反硝化过程提供充足的电子受体，硝化池出水进入多级反硝化池。
[0046]第四步多级反硝化:上述第三步的硝化池出水进入多级反硝化池，根据有机负荷的不同，可将硝化反硝化系统设置为多级。其中，多级反硝化池中反应温度为20〜40°C、pH=7.0〜8.3、溶解氧DO < 0.2mg/L，通过该级的回流硝化液提供充足的亚硝态氮和硝态氮，可进行反硝化脱氮。
[0047]第五步多级硝化:上述第四步的多级反硝化池出水进入多级硝化池，多级硝化池中反应温度为20〜40°(:，00 = 0.6〜1.21^/1，？!1=7.0〜8.6，同时将硝化液回流至多级反硝化池，回流比R <30。
[0048] 第六步泥水分离:上述第五步硝化池出水进入泥水分离设备，在温度为20〜40 °C、溶解氧DO= 1.0〜4.0mg/L,pH = 7.0〜8.6的条件下，一方面是将前面生化处理后的泥水混合物进行分离，另一方面是将水中SS、C0D、氨氮和总氮等污染物进行降解，同时将底部污泥按照一定比例回流至反硝化池，防止系统污泥量减少并提高氮的去除率，剩余污泥进行定期排放，经泥水分离后的出水进入产水箱。
[0049]本发明首先通过厌氧反应将渗滤液中大分子难降解有机物分解为小分子可生化碳源，充分利用渗滤液中原有的碳源进行短程硝化反硝化脱氮，减少了外加碳源的投加量，经济效果显著;其次可严格控制较低、稳定的溶解氧浓度，保证亚硝态氮积累率高且稳定，具有较高的脱氮效率，且脱氮过程中减少了曝气量，节省能耗，运行成本低;最后可实现不同负荷下的渗滤液的脱氮处理，保证出水水质达到设计标准。
Claims (1)
1.一种垃圾渗滤液短程硝化反硝化脱氮工艺，其特征在于，它包括以下几个步骤: (1)厌氧处理:将垃圾渗滤液进行厌氧处理，使其实现气液固三相分离，得到厌氧出水； (2)反硝化:将步骤(I)中的厌氧出水进行反硝化处理，降低含氮量； (3)硝化:将步骤⑵的反硝化出水，进行硝化处理，得到硝化出水； (4)多级反硝化:将步骤(3)硝化池出水进行多级反硝化作用，得到多级反硝化出水； (5)多级硝化:将步骤(4)得到的多级反硝化池出水进行多级硝化处理，得到多级硝化出水； (6)泥水分离:将步骤(5)得到的多级硝化出水通入泥水分离设备，进行泥水分离，出水进入广水箱； 所述步骤(I)中厌氧反应温度控制在25〜55°C的范围； 所述步骤(2)中反硝化反应温度为20〜40 °C、pH为7.0〜8.3、溶解氧DO < 0.2mg/L; 所述步骤(3)中硝化反应温度为20〜40 0C，DO为0.6〜1.2mg/L，pH值为7.0〜8.6; 所述步骤(4)中多级反硝化反应温度为20〜40°C、pH值为7.0〜8.3、溶解氧DO < 0.2mg/L； 所述步骤(5)中多级硝化反应温度为20〜40°C，DO为0.6〜1.2mg/L，pH为7.0〜8.6; 所述步骤(6)中泥水分离反应温度为20〜400C，DO为1.0〜4.0mg/L，pH值为7.0〜8.6。
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