CN105110573B - 一种去除污水总氮的处理方法 - Google Patents
一种去除污水总氮的处理方法 Download PDFInfo
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- CN105110573B CN105110573B CN201510607471.3A CN201510607471A CN105110573B CN 105110573 B CN105110573 B CN 105110573B CN 201510607471 A CN201510607471 A CN 201510607471A CN 105110573 B CN105110573 B CN 105110573B
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- pond
- aerobic
- tank
- anoxic
- sludge
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- 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 72
- 239000010865 sewage Substances 0.000 title claims abstract description 41
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 38
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 62
- 239000010802 sludge Substances 0.000 claims abstract description 43
- 238000004062 sedimentation Methods 0.000 claims abstract description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical group 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- 229910052799 carbon Inorganic materials 0.000 claims description 68
- 238000010992 reflux Methods 0.000 claims description 23
- 230000001105 regulatory Effects 0.000 claims description 18
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- 230000000576 supplementary Effects 0.000 description 3
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound 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Abstract
本发明公开了一种去除污水总氮的处理系统，包括调节池、缺氧池、好氧池和沉淀池，所述调节池的出水口与缺氧池的进水口之间通过输送管道连通，所述缺氧池的出水口与好氧池的进水口之间管道连通，所述好氧池的出水口与沉淀池的进水口通过管道连通，沉淀池的出水口与排放水槽连通，沉淀池的出泥口与污泥池连通，其特征在于：所述处理系统还包括第一回流输送管路和第二回流输送管路，所述第一回流输送管路一端伸入沉淀池的污泥层，另一端分别与缺氧池和好氧池连通；所述第二回流输送管路一端与好氧池的出水口连通，另一端与缺氧池连通。该处理系统利用将沉淀池中的污泥回流至缺氧池和好氧池，将好氧池中处理后的泥水混合液回流至缺氧池中，从而提高了缺氧池的反硝化能力，也使好氧池的氧化分解能力提高。
Description
技术领域
[0001] 本发明涉及一种去除污水总氮的处理系统和处理方法，适合总氮比较高的污水的处理。
背景技术
[0002] 传统的废水生化脱氮系统包括调节池、厌氧池、好氧池和沉淀池，废水依次经过上述池进行生化处理，上述处理系统和处理方法可实现部分总氮去除，而排水标准低的企业所排放的废水中总氮浓度较高，上述方法处理效果不理想，处理后的总氮超标。
[
发明内容
[0003] 本发明所要解决的一个技术问题是:提供一种去除污水总氮的处理系统，该处理系统利用将沉淀池中的污泥回流至缺氧池和好氧池，将好氧池中处理后的泥水混合液回流至缺氧池中，从而提高了缺氧池的反硝化能力，也使好氧池的氧化分解能力提高。
[0004] 本发明所要解决的另一个技术问题是:提供一种去除污水总氮的处理方法，该处理方法将沉淀池中沉淀的污泥回流至缺氧池和好氧池以增加生物菌种和碳元素，好氧池中的泥水混合液回流至缺氧池中，提高缺氧池的反硝化能力。
[0005] 为解决上述技术问题，本发明的技术方案是:一种去除污水总氮的处理系统，包括调节池、缺氧池、好氧池和沉淀池，所述调节池的出水口与缺氧池的进水口之间通过输送管道连通，所述缺氧池的出水口与好氧池的进水口之间管道连通，所述好氧池的出水口与沉淀池的进水口通过管道连通，沉淀池的出水口与排放水槽连通，沉淀池的出泥口与污泥池连通，所述处理系统还包括第一回流输送管路和第二回流输送管路，所述第一回流输送管路一端伸入沉淀池的污泥层，另一端分别与缺氧池和好氧池连通;所述第二回流输送管路一端与好氧池的出水口连通，另一端与缺氧池连通。
[0006] 作为一种优选的方案，所述第一回流输送管路包括第一回流输送主管和两条第一回流输送分管，所述第一回流输送主管的一端分别与两条第一回流输送分管连通，另一端伸入沉淀池的污泥层，所述第一回流输送主管上设置污泥输送动力装置。
[0007]作为一种优选的方案，所述污泥输送动力装置包括污泥回流栗，该污泥回流栗的入口和出口连接于第一回流输送主管上。
[0008] 作为一种优选的方案，所述污泥输送动力装置为空气提升器，该空气提升器包括一个空气管，该空气管一端伸入沉淀池中且与第一回流输送主管的端部配合，该空气管与压缩空气动力源连接。
[0009]作为一种优选的方案，所述第二回流输送管路包括第二回流输送管道，该第二回流输送管道一端插入好氧池的池底，另一端伸入缺氧池中，所述第二回流输送管道连接有空气提升器。
[0010] 作为一种优选的方案，所述处理系统还包括厌氧池，该厌氧池的进水口与调节池的出水口连通，该厌氧池的出水口与缺氧池的进水口连通。
[0011]作为一种优选的方案，所述处理系统还包括碳源储罐，该碳源储罐内储存有为缺氧池补充碳的碳源，所述碳源储罐的出料口通过碳源添加管道与缺氧池连通，该碳源添加管道上设置有输送栗和流量计。
[0012] 采用了上述技术方案后，本发明的效果是:由于所述处理系统还包括第一回流输送管路和第二回流输送管路，所述第一回流输送管路一端伸入沉淀池的污泥层，另一端分别与缺氧池和好氧池连通;所述第二回流输送管路一端与好氧池的出水口连通，另一端与缺氧池连通。因此，沉淀池的污泥通过第一回流输送管路进入到缺氧池和好氧池中，为两个池提供了生物菌种，而好氧池中的泥水混合液又通过第二回流输送管路回流至缺氧池中，该泥水混合液为缺氧池提供电子受体和部分的碳元素，提高了反硝化的作用。
[0013] 又由于所述处理系统还包括碳源储罐，该碳源储罐内储存有为缺氧池3补充碳的碳源，所述碳源储罐的出料口通过碳源添加管道与缺氧池连通，该碳源添加管道上设置有输送栗和流量计。该碳源储罐可以选择性补充碳源，使缺氧池中的碳氮的比值稳定在一个合适的范围，反硝化效果达到最优化。
[0014] 另外本发明还公开了一种去除污水总氮的处理方法，其包括以下步骤:
[0015] A、将污水收集至调节池进行水质均质；
[0016] B、将调节池的污水送至缺氧池中进行处理，控制缺氧池中的溶解氧小于0.5mg/L，pH值为7-8之间，反应停留时间6小时以上，温度控制在25-35度，反应过程中持续利用搅拌机持续搅拌，每立方水搅拌机功率在8-12W;若污水中有机氮浓度非常高，则污水先进厌氧池处理，厌氧池的出水再进缺氧池;厌氧池中pH值为6.5-8.5之间，停留时间12小时以上，温度30-35度;
[0017] C、经缺氧池中反应后的污水进入到好氧池中进行生化反应，好氧池中具有好氧微生物及好氧型细菌，好氧池控制溶解氧2_4mg/L，pH值为6.5-9，反应停留时间为12-18小时，污泥泥龄10天以上；；
[0018] D、经好氧池处理后的出水一部分进入到沉淀池中沉淀，另一部分回流至缺氧池中，回流比100-200%;
[0019] E、废水在沉淀池中沉淀2-3小时，上清液排放，沉淀后的污泥一部分送至污泥池中，另一部分回流至缺氧池和好氧池中，总回流比100-200%，且缺氧池和好氧池的污泥回流量相同。
[0020] 优选的，所述缺氧池还连接有碳源补充系统，当缺氧池的进水低于C:N=4:1时，碳源补充系统启动为缺氧池补充碳元素。
[0021] 优选的，沉淀池污泥总回流比在100-160 %之间，好氧池的回流比在150-200 %之间。
[0022] 采用了上述技术方案后，本发明的效果是:该处理方法创造了良好的厌氧条件以分解有机氮，加强缺氧池中的泥水混合强度，利用沉淀池中的泥适当补充碳源，提高了缺氧池的反硝化效果，同时在保证好氧池硝化完全的情况下可实现氨氮、总氮去除率大大提高。
附图说明
[0023]下面结合附图和实施例对本发明进一步说明。
[0024]图1是本发明实施例的结构示意图；
[0025] 附图中:1.调节池;2.好氧池;3.厌氧池;4.碳源储罐;5.碳沉淀池;6.污泥池;7.搅拌装置;8.第二回流输送管道;9.第一回流输送主管；1.碳源添加管道；11.输送栗；12.第一回流输送分管;13.缺氧池。
具体实施方式
[0026] 下面通过具体实施例对本发明作进一步的详细描述。
[0027] 实施例1
[0028] 如图1所示，一种去除污水总氮的处理系统，包括调节池1、厌氧池3、缺氧池13，好氧池2和碳沉淀池5，所述调节池I的出水口与厌氧池3的进水口之间通过输送管道连通，所述厌氧池3的出水口与缺氧池13的进水口连通，缺氧池13的出水口与好氧池2的进水口之间管道连通，所述好氧池2的出水口与碳沉淀池5的进水口通过管道连通，碳沉淀池5的出水口与排放水槽连通，碳沉淀池5的出泥口与污泥池6连通，同时，调节池I的出水口还与缺氧池13的进水口连通，所述处理系统还包括第一回流输送管路和第二回流输送管路，所述第一回流输送管路一端伸入碳沉淀池5的污泥层，另一端分别与缺氧池13和好氧池2连通;所述第二回流输送管路一端与好氧池2的出水口连通，另一端与缺氧池13连通。所述缺氧池13中具有搅拌装置7，该搅拌装置7包括搅拌轴和搅拌叶片，该搅拌轴由电机驱动。
[0029] 所述第一回流输送管路包括第一回流输送主管9和两条第一回流输送分管12，所述第一回流输送主管9的一端分别与两条第一回流输送分管12连通，另一端伸入碳沉淀池5的污泥层，所述第一回流输送主管9上设置污泥输送动力装置。
[0030] 其中，污泥输送动力装置有两种方案，一种方案包括污泥回流栗，该污泥回流栗的入口和出口连接于第一回流输送主管9上，直接利用污泥回流栗的动力将碳沉淀池5中的污泥抽入到好氧池2和缺氧池13中，这样需要增加栗的采购成本以及电费。
[0031] 而另一种方案是所述污泥输送动力装置为空气提升器，该空气提升器包括一个空气管，该空气管一端伸入碳沉淀池5中且与第一回流输送主管9的端部配合，该空气管与压缩空气动力源连接，该压缩空气动力源可以采用好氧池2中的曝气系统中的风力，在曝气系统的管道接个三通，连接空气管，将风送入到第一回流输送主管9的端部，利用风力使污泥提升。
[0032]同样，所述第二回流输送管路包括第二回流输送管道8，该第二回流输送管道8—端插入好氧池2的池底，另一端伸入缺氧池13中，所述第二回流输送管道8连接有空气提升器。该空气提升器和前述的结构一致。利用风力提升可以降低成本。
[0033] 所述处理系统还包括碳源储罐4，该碳源储罐4内储存有为缺氧池13补充碳的碳源，所述碳源储罐4的出料口通过碳源添加管道10与厌氧池3连通，该碳源添加管道10上设置有输送栗11和流量计。当厌缺氧池13的进水的碳氮比低于设定值使开启输送栗11将碳源送入缺氧池13中，该碳源可以选用甲醇。在污水中的有机氮的浓度非常高时，污水先进入到厌氧池3中反应，厌氧池3内设配水装置、大流量循环栗及三相分离系统。厌氧池3将部分有机氮转为氨态氮，实现氨化过程，并将难降解有机物分解为易降解有机物，提高碳源，利于后道除氮。而若污水的有机氮的含量不高时可以直接进入到缺氧池13中反应。
[0034] 实施例2
[0035] 一种去除污水总氮的处理方法，其包括以下步骤:
[0036] A、将污水收集至调节池I进行水质均质；
[0037] B、将调节池I的污水送至缺氧池13中进行处理，控制缺氧池13中的溶解氧为
0.5mg/L，pH值为7，反应停留时间6小时，温度控制在25度，反应过程中持续利用搅拌机持续搅拌，每立方水搅拌机功率在8W;
[0038] C、经缺氧池13中反应后的污水进入到好氧池2中进行生化反应，好氧池2中具有好氧微生物及好氧型细菌，好氧池2控制溶解氧2mg/L，pH值为6.5，反应停留时间为12小时，污泥泥龄10天以上；
[0039] D、经好氧池2处理后的出水一部分进入到碳沉淀池5中沉淀，另一部分回流至缺氧池13中，回流比100 %，停留反应时间为24小时；
[0040] E、废水在碳沉淀池5中沉淀2小时，上清液排放，沉淀后的污泥一部分送至污泥池6中，另一部分回流至缺氧池13和好氧池2中，总回流比100%，且缺氧池13和好氧池2的污泥回流量相同，各占50%。
[0041] 所述缺氧池13还连接有碳源补充系统，当缺氧池13的进水低于C:N = 4:1时，碳源补充系统启动为缺氧池13补充碳元素，该碳源选用甲醛进行补充，缺氧池13的进水定期抽检检查C: N，当低于4:1补充碳源。
[0042] 该处理方法的去除总氮的原理是:在缺氧池13中由于污水有机物浓度很高，微生物处于缺氧状态，此时微生物为兼性微生物，它们将污水中的有机氨转化分解为NH3-N，同时利用有机碳作为电子供体，将N0-2-N、N0-3-N转化为N2，而且还利用部分有机碳源和NH3-N合成新的细胞物质。所以缺氧池13不仅具有一定的有机物去功能，减轻后续好氧池2的有机负荷，以利于硝化作用的进行，而且依靠原水中存在的较高浓度有机物，完成反硝化作用，最终消除氮的富营养化污染，而好氧池2的泥水混合液部分回流到缺氧池13，为缺氧池13提供了更多的电子受体，提高了反硝化作用，最终消除氮污染。
[0043] 而在好氧池2中，由于有机物浓度已大幅度降低，但仍有一定量的有机物及较高的NH3-N存在。为了使有机物得到进一步氧化分解，同时在碳化作用处于完成情况下硝化作用能顺利进行，在好氧池2设置了好氧微生物及硝化菌。其中好氧微生物将有机物分解成CO2和H2O;硝化菌利用有机物分解产生的无机碳或空气中的CO2作为营养源，将污水中的NH-3-N转化成 N0-2-N、N0-3-N。
[0044] 经过该方法处理后的污水，原来调节池I的出水CODo为2000mg/L,氨氮150mg/L，总氮220mg/L，处理后的总氮从220降至12mg/L，去除95%左右的总氮。氨氮出水2mg/L。
[0045] 实施例3
[0046] 该实施例与实施例1的处理方法基本相同，只是其中的一些处理参数有所改变。
[0047] 步骤B中，将调节池I的污水送至缺氧池13之间先进入到厌氧池3中反应，厌氧池中pH值为6.5-8.5之间，停留时间12小时以上，温度30-35度;然后再将厌氧池中的污水送入缺氧池13中进行处理，控制缺氧池13中的溶解氧0.4mg/L，pH值为8之间，反应停留时间24小时，温度控制在35度，反应过程中持续利用搅拌机持续搅拌，每立方水搅拌机功率在12W;
[0048] 步骤C中，经缺氧池13中反应后的污水进入到好氧池2中进行生化反应，好氧池2中具有好氧微生物及好氧型细菌，好氧池2控制溶解氧4mg/L，pH值为9，反应停留时间为18小时；
[0049] D、经好氧池2处理后的出水一部分进入到碳沉淀池5中沉淀，另一部分回流至缺氧池13中，回流比200 %，停留反应时间为36小时；
[0050] E、废水在碳沉淀池5中沉淀3小时，上清液排放，沉淀后的污泥一部分送至污泥池6中，另一部分回流至缺氧池13和好氧池2中，总回流比200%，且缺氧池13和好氧池2的污泥回流量相同。
[0051] 优选的，所述缺氧池13还连接有碳源补充系统，当缺氧池13的进水低于C:N = 4:1时，碳源补充系统启动为缺氧池13补充碳元素。
[0052] 该方法处理后的出水总氮从220降至10mg/L，去除95%左右的总氮。氨氮出水Img/L0
[0053] 实施例4
[0054] 该实施例与实施例1的处理方法基本相同，只是其中的一些处理参数有所改变。
[0055] 步骤B中，将调节池I的污水送至缺氧池13中进行处理，控制缺氧池13中的溶解氧
0.4mg/L，pH值为8之间，反应停留时间20小时，温度控制在30度，反应过程中持续利用搅拌机持续搅拌，每立方水搅拌机功率在I Off;
[0056] 步骤C中，经缺氧池13中反应后的污水进入到好氧池2中进行生化反应，好氧池2中具有好氧微生物及好氧型细菌，好氧池2控制溶解氧3mg/L，pH值为8，反应停留时间为16小时；
[0057] D、经好氧池2处理后的出水一部分进入到碳沉淀池5中沉淀，另一部分回流至缺氧池13中，回流比150%;
[0058] E、废水在碳沉淀池5中沉淀3小时，上清液排放，沉淀后的污泥一部分送至污泥池6中，另一部分回流至缺氧池13和好氧池2中，总回流比160%，且缺氧池13和好氧池2的污泥回流量相同。
[0059] 优选的，所述缺氧池13还连接有碳源补充系统，当缺氧池13的进水低于C:N = 4:1时，碳源补充系统启动为缺氧池13补充碳元素。
[0060] 该方法处理后的出水总氮从220降至10.5mg/L，去除95 %左右的总氮。氨氮出水1.2mg/L。
[0061] 实施例5
[0062] 该实施例与实施例1的处理方法基本相同，只是其中的一些处理参数有所改变。
[0063] 步骤B中，将调节池I的污水送至缺氧池13中进行处理，控制缺氧池13中的溶解氧
0.4mg/L，pH值为7之间，反应停留时间26小时，温度控制在30度，反应过程中持续利用搅拌机持续搅拌，每立方水搅拌机功率在11W;
[0064] 步骤C中，经缺氧池13中反应后的污水进入到好氧池2中进行生化反应，好氧池2中具有好氧微生物及好氧型细菌，好氧池2控制溶解氧4mg/L，pH值为8，反应停留时间为18;
[0065] D、经好氧池2处理后的出水一部分进入到碳沉淀池5中沉淀，另一部分回流至缺氧池13中，回流比190%;
[0066] E、废水在碳沉淀池5中沉淀3小时，上清液排放，沉淀后的污泥一部分送至污泥池6中，另一部分回流至缺氧池13和好氧池2中，总回流比170%，且缺氧池13和好氧池2的污泥回流量相同。
[0067] 优选的，所述缺氧池13还连接有碳源补充系统，当缺氧池13的进水低于C:N = 4:1时，碳源补充系统启动为缺氧池13补充碳元素。
[0068] 该方法处理后的出水总氮从2 2 O降至9 m g / L，去除9 5 %以上的总氮。氨氮出水0.9mg/L0
[0069]以上所述实施例仅是对本发明的优选实施方式的描述，不作为对本发明范围的限定，在不脱离本发明设计精神的基础上，对本发明技术方案作出的各种变形和改造，均应落入本发明的权利要求书确定的保护范围内。
Claims (3)
1.一种去除污水总氮的处理方法，其包括以下步骤: A、将污水收集至调节池进行水质均质； B、将调节池的污水送至缺氧池中进行处理，控制缺氧池中的溶解氧小于0.5mg/L，pH值为7-8之间，反应停留时间6小时以上，温度控制在25-35度，反应过程中持续利用搅拌机持续搅拌，每立方水搅拌机功率在8-12W;若污水中有机氮浓度非常高，则污水先进厌氧池处理，厌氧池的出水再进缺氧池；厌氧池中PH值为6.5-8.5之间，停留时间12小时以上，温度30-35度； C、经缺氧池中反应后的污水进入到好氧池中进行生化反应，好氧池中具有好氧微生物及好氧型细菌，好氧池控制溶解氧2_4mg/L，pH值为6.5-9，反应停留时间为12-18小时，污泥泥龄10天以上； D、经好氧池处理后的出水一部分进入到沉淀池中沉淀，另一部分回流至缺氧池中，回流比 100-200%; E、废水在沉淀池中沉淀2-3小时，上清液排放，沉淀后的污泥一部分送至污泥池中，另一部分回流至缺氧池和好氧池中，总回流比100-200%，且缺氧池和好氧池的污泥回流量相同。
2.如权利要求1所述的一种去除污水总氮的处理方法，其特征在于:所述缺氧池还连接有碳源补充系统，当缺氧池的进水低于C:N = 4:1时，碳源补充系统启动为缺氧池补充碳元素。
3.如权利要求2所述的一种去除污水总氮的处理方法，其特征在于:沉淀池污泥总回流比在100-160%之间，好氧池的回流比在150-200%之间。
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