CN101234836B - 一种垃圾渗滤液处理工艺 - Google Patents
一种垃圾渗滤液处理工艺 Download PDFInfo
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- CN101234836B CN101234836B CN2008100693809A CN200810069380A CN101234836B CN 101234836 B CN101234836 B CN 101234836B CN 2008100693809 A CN2008100693809 A CN 2008100693809A CN 200810069380 A CN200810069380 A CN 200810069380A CN 101234836 B CN101234836 B CN 101234836B
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- water
- aeration tank
- tank
- compatibility pool
- oxygen compatibility
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- 238000000034 methods Methods 0.000 title claims description 25
- 239000010813 municipal solid wastes Substances 0.000 title claims description 20
- 239000011901 water Substances 0.000 claims abstract description 92
- 239000010802 sludge Substances 0.000 claims abstract description 30
- 238000006243 chemical reactions Methods 0.000 claims abstract description 20
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 239000002699 waste materials Substances 0.000 claims abstract description 6
- 238000005273 aeration Methods 0.000 claims description 45
- MYMOFIZGZYHOMD-UHFFFAOYSA-N oxygen Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 34
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- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 claims description 29
- 238000000108 ultra-filtration Methods 0.000 claims description 22
- 239000010865 sewage Substances 0.000 claims description 21
- 238000001223 reverse osmosis Methods 0.000 claims description 17
- 230000005484 gravity Effects 0.000 claims description 14
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- 239000007788 liquids Substances 0.000 claims description 14
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- 238000005516 engineering processes Methods 0.000 abstract description 13
- 238000002306 biochemical methods Methods 0.000 abstract description 2
- 239000000149 chemical water pollutants Substances 0.000 abstract 4
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound 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Abstract
本发明公开了一种垃圾渗滤液处理工艺，预处理、上流式污泥床反应、硝化反硝化反应、泥水分离、膜处理步骤，该工艺综合运用物理和生化方法对垃圾渗滤液进行处理，大大降低渗滤液处理的成本，同时大幅度提升出水水质，广泛用于垃圾处理厂的垃圾渗滤液处理。
Description
一种垃圾渗滤液处理工艺
技术领域
[0001] 本发明涉及垃圾处理技术领域，尤其是涉及一种垃圾渗滤液处理工艺。 背景技术
[0002] 城市垃圾渗滤液是一种成分复杂的高浓度有机废水，若不加处理而直接排入环 境，会造成严重的环境污染。与一般城市污水不同，垃圾渗滤液的BOD5和CODcr浓度高、 金属含量高、水质水量变化大、氨氮的含量高，微生物营养元素比例失调等。在我国，随着 城市人口的增加、城市规模的扩大和居民生活水平的提高，我国城市生活垃圾的产量在急 剧增加，根据我国垃圾处理无害化、减量化、资源化的原则，将有一大批生活垃圾焚烧发电 厂得到新建，而垃圾渗滤液是否能够处理达标排放是垃圾焚烧发电厂面临的一个严峻的难 题。垃圾渗滤液作为一种高浓度有机废水，其处理近几年得到了广大研究人员的关注，进行 了大量的试验研究，并取得了不少成果。但是目前的处理工艺还存在着一些缺陷，主要表现 在两个方面：
[0003] 1)渗滤液高浓度氨氮的问题
[0004] 高浓度的氨氮是渗滤液的水质特征之一，根据垃圾处理方式和垃圾成分的不同， 渗滤液氨氮浓度一般从数十至几千mg/L不等。
[0005] 与城市污水相比，垃圾渗滤液的氨氮浓度高出数十至数百倍。一方面，由于高浓度 的氨氮对生物处理系统有一定的抑制作用；另一方面，由于高浓度的氨氮造成渗滤液中的 C/N比失调，生物脱氮难以进行，导致最终出水难以达标排放。
[0006] 因此，在高氨氮浓度渗滤液处理工艺流程中，一般采用先氨吹脱，再进行生物处理 的工艺流程。目前氨吹脱的主要形式有曝气池、吹脱塔和精馏塔。国内用得最多的是前两 种形式，曝气池吹脱法由于气液接触面积小，吹脱效率低，不适用于高氨氮渗滤液的处理， 采用吹脱塔的吹脱法虽然具有较高的去除效率，但具有投资运行成本高，脱氨尾气难以治 理的缺点。以深圳下坪为例，氨吹脱部分的建设投资占总投资的30%左右，运行成本占总处 理成本的70%以上。这主要是由于在运行过程中，吹脱前必须将渗滤液pH调至11左右， 吹脱后为了满足生化的需要，需将PH回调至中性，因此在运行过程中需加大量的酸碱调整 PH，为了提供一定的气液接触面积，还需要风机提供足够的风量以满足一定的气液比，造成 了渗滤液处理成本的偏高。
[0007] 另外，空气吹脱法对于年平均气温较低的地区，存在低温条件下吹脱无法正常运 行和冬季吹脱塔结冰的问题，在我国北方地区，其应用受到一定的限制。
[0008] 采用汽提的方式虽然可以较好的解决氨氮的去除问题，但由于需要提高渗滤液的 水温，其处理成本仍然较高。
[0009] 2)部分有机物难以生物降解的问题
[0010] 虽然渗滤液的可生化性较好，但是光靠生物处理也很难将之处理至二级甚至一级 标准以下，一般来讲，渗滤液的COD中将近有500〜600mg/L无法用生物处理的方式处理。 在当今世界范围内，生活垃圾渗滤液处理技术研究者已达成共识：从生态及经济效益双赢的角度考虑，生化工艺是渗滤液处理过程中不可省略的预处理阶段，但仅仅依靠生化阶段 无法满足严格的出水要求，必须与其他工艺进行合理优化组合。
发明内容
[0011] 有鉴于此，本发明的目的是提供一种垃圾渗滤液处理工艺，在现有技术的基础上 进行创新改造，综合运用物理和生化方法对垃圾渗滤液进行处理，大大降低渗滤液处理的 成本，同时大幅度提升出水水质。
[0012] 本发明的垃圾渗滤液处理工艺，包括以下步骤：
[0013] a.预处理
[0014] 将垃圾渗滤液加压送入格栅沉砂池进行预处理除去较大的悬浮物、漂浮物、纤维 物质和其它较大的固体颗粒物质；经过预处理的污水自流进入调节池；
[0015] b.上流式污泥床反应
[0016] 调节池的出水由水泵泵入UASB反应器以除去大部分CODcr和BOD5,泵入前对废水 进行升温，使UASB反应器水温保持30°C -35 °C，UASB反应器的出水自流进入中间池，中间 池的回流污水从UASB反应器厌氧污泥床底部回流进入UASB，中间池的回流水水量是UASB 进水量的5-6倍；
[0017] c.硝化反硝化反应
[0018] 中间池的出水由水泵泵入兼氧池，污水在泵入兼氧池前降温至25V -30°C，兼氧 池内的污水由搅拌器充分搅拌以进行反硝化反应，兼氧池的出水自流进入曝气池；
[0019] 污水在曝气池内进行硝化反应，硝化反应过程中PH值控制在7-8，曝气池采用 微孔曝气提供空气或者纯氧，穿孔曝气搅拌以加强泥水混合，经过硝化反应的回流污水进 入兼氧池，从曝气池回流进入兼氧池的回流水的水量是由兼氧池直流进入曝气池水量的 21-25 倍；
[0020] d.泥水分离
[0021] 曝气池出水自流进入沉淀池，在该沉淀池进行初次泥水分离，分离后的上清液自 流进入膜处理系统，分离出的回流污泥至兼氧池及曝气池，以保证曝气池中保持足够的污 泥浓度进行微生物接种，污泥回流量是曝气池进水量的1. 5-4倍；剩余污泥泵入污泥浓缩 池进行再次泥水分离；
[0022] 经污泥浓缩池浓缩后的污泥加压送入离心式污泥脱水机脱水，污泥浓缩池上清液 和脱水机产生的废液回流至调节池；
[0023] e.膜处理
[0024] d步骤中沉淀池首次分离出的上清液首先加压进入超滤膜处理系统进行过滤，超 滤膜采用管式陶瓷超滤膜；
[0025] 超滤膜处理系统回收的浓液回流至调节池，超滤膜处理系统过滤之后产生的清液 进入反渗透膜处理系统进行反渗透处理，反渗透膜处理系统的反渗透膜采用聚酰胺类复合膜。
[0026] 进一步，从中间池的回流水水量是UASB进水量的5. 7倍；c步骤中，从曝气池回流 进入兼氧池的回流水的水量是由兼氧池直流进入曝气池水量的23倍；
[0027] 进一步，b步骤中，使UASB反应器水温保持35°C ;c步骤中，硝化反[0028] 应过程PH值控制在7. 5 ;d步骤中，污泥回流量是曝气池进水量的3倍；
[0029] e步骤中管式陶瓷超滤膜膜孔径为0. 05 μ m。
[0030] 本发明的有益效果是：与现有技术相比，本发明的垃圾渗滤液处理工艺，综合现有 技术的优点并在现有技术的基础之上进行技术创新，采用生化段处理和膜处理相结合的处 理方式，同时优化了工艺参数，生化段处理即所述的b上流式污泥床反应和c硝化反硝化处 理。本发明的渗滤液处理工艺优点是：
[0031] 1、采用该工艺的系统能处理高指标的污水，特别是高氨氮指标的垃圾渗滤液，原 水指标如下表：
[0032] 原水水质指标
[0034] 2、采用该工艺的系统出水水质可达到并优于《污水综合排放标准》（GB8978-1996) 一级标准指标值；
[0035] 3、未采用传统的氨吹脱塔，仅依靠生物脱氨即硝化_反硝化处理技术可使生化段 出水NHa-N指标稳定达标，使处理成本大大降低；
[0036] 4、采用超滤（UF) +反渗透（RO)深度处理即所述的膜处理工艺，可将生化段未降解 的有机物大部分截留。
[0037] 可见，采用本发明进行垃圾渗滤液处理，能使处理高指标污水特别是报氨氮浓度 的污水的处理成本大大降低，出水水质大幅提高，具有巨大的实用价值和社会价值。
附图说明
[0038] 下面结合附图和实施例对本发明作进一步描述。
[0039] 附图为本发明的工艺流程框图。
具体实施方式
[0040] 本发明成功应用于重庆同兴垃圾焚烧发电厂的垃圾渗漏液的处理，如图所示，本 发明的工艺实施时，整个系统主要包括沉砂池1、调节池2、UASB反应器3、中间池4、兼氧池 5、曝气池6、沉淀池7、超滤膜处理系统8、反渗透膜处理系统9、污泥浓缩池10和离心式污 泥脱水机11。在调节池2和UASB反应器3之间设置有换热器，调节池2的出水由水泵泵入 UASB反应器3之前由该换热器通过蒸汽进行升温，使UASB反应器内水的温度保持在35 °C。 在中间池4和兼氧池5之间设置也设置有换热系统，中间池4的出水由水泵泵入兼氧池5 之前由换热系统进行降温至25°C -30°C。经污泥浓缩池10浓缩后的污泥在加压送入离心 式污泥脱水机之前加入絮凝剂PAM。其中，在各构筑物建造时，若以沉砂池1底部为垂直方 向的坐标零点，则调节池2的底部坐标为-2. 5m，顶部坐标为3. 15m ；UASB反应器3底部坐 标-3. 5m，顶部坐标为8. 5m ；中间池4底部坐标_3. 5m，顶部坐标1. 5m ；兼氧池5、曝气池6 和沉淀池Ί的底部坐标为-3. 0m，顶部坐标为4. Om ；污泥浓缩池底部坐标为-1. 7m，顶部坐 标为2. Om ；沉砂池1的出水到调节池2的出水口垂直方向坐标为4. 962m,UASB反应器3出 水到中间池4的出水口垂直方向坐标为7. 4m，兼氧池5出水到曝气池6的出水口垂直方向 坐标为3. 6m,曝气池6出水到的沉淀池7出水口垂直方向坐标为3. 5m，沉淀池7出水到超滤膜处理系统8的出水口垂直方向坐标为3. 0m。
[0041] 使用时，垃圾贮坑内的垃圾渗滤液利用废水管加压进入沉砂池1进行预处理，沉 砂池1为格栅沉砂池，废水在该池中去除较大的悬浮物、漂浮物、纤维物质和固体颗粒物 质，以减轻后续处理构筑物的负荷，保证后续处理的正常运行。经过预处理后的污水自流 进入调节池2，进行水质、水量调节，而后泵入UASB反应器3。UASB反应即上流式污泥床反 应工艺可以去除63% CODcr, 50-70% BOD5，经过UASB反应器3三相分离后产生的沼气导入 垃圾坑处理（焚烧炉检修时就地燃烧处理），混合液自流进入中间池4。中间池4的污水从 UASB反应器3厌氧污泥床底部回流进入UASB反应器3，中间池的回流水水量是UASB进水 量的5. 7倍，以保证UASB反应器的上流速度。中间池4内的废水泵入兼氧池5，兼氧池5底 部设有水下搅拌器，使污水充分搅拌水解，而后自流进曝气池6，废水中的有机物在曝气池 6中的高活性好氧微生物的作用下充分硝化反应，硝化反应过程中PH值控制在7. 5，PH值 过低不利于进行硝化降解，可以加入适量NaOH调节PH值；曝气池采用微孔曝气提供溶解 氧，穿孔曝气搅拌以加强泥水混合；在曝气池6中硝化后的废水需要回流进入兼氧池5，从 曝气池6回流进入兼氧池5的水量是由兼氧池5直流进入曝气池6水量的23倍，从而完成 硝化-反硝化生物脱氮过程。之后废水由曝气池6自流进入沉淀池7，在该池中进行首次泥 水分离，分离后的上清液自流进入超滤膜处理系统8的进水罐，沉淀池7产出的污泥回流至 兼氧池5及曝气池6，污泥回流量是曝气池进水量的3倍；剩余污泥泵入污泥浓缩池10进 行再次泥水分离；经污泥浓缩池10浓缩后的污泥加压送入离心式污泥脱水机10脱水，污泥 浓缩池10上清液和离心式污泥脱水机10产生的废液回流至调节池，离心污泥脱水机产生 的泥饼运至厂内焚烧炉焚烧处理。
[0042] 经过生化处理的废水经过沉淀池7分离后的清液进入膜处理系统，膜处理系统包 括超滤膜处理系统8和反渗透膜处理系统9，超滤膜处理系统8采用管式陶瓷超滤膜（UF 膜）和错流过滤方式，该管式陶瓷超滤膜内外表面为致密层，层面密布微孔，中间是多孔支 撑层，通过该超滤膜将经过生化处理后的垃圾渗滤液大部分的悬浮物截留住以确保后续反 渗透处理的顺利进行，超滤膜处理系统8回收的浓液带着活性污泥直接回流至调节池2。超 滤膜处理系统8过滤之后产生的清液进入反渗透膜处理系统9进行反渗透处理，反渗透膜 处理系统9的反渗透膜（RO膜）采用聚酰胺类复合膜，具体使用陶氏BW30-400FR膜元件。 UF膜和RO膜定期进行使用盐酸清洗。
[0043] 重庆同兴垃圾焚烧发电厂的垃圾渗漏液经过生化处理和膜处理后的废水中各项 污染物指标达到《污水综合排放标准》（GB8978-1996) —级标准的要求。具体指标如下表：
[0044] 生化处理效果对比
[0045]
[0046] 生化处理后的膜处理进水C0D& ( 1500，出水C0D& ( 100 ；去除率达94%。
[0047] 同时，该工艺流程结合了现有技术的优点并在现有技术的基础之上进行技术创 新，大大降低了处理成本，具体运行费（300T/d处理量）用见下表：
[0048] 动力、水、药剂消耗量分析
[0049]
[0050] 本设计污水处理系统定员5人，成本分析见下表：
[0051] 污水处理系统运行成本分析[0052]
[0053] 重庆同兴垃圾焚烧发电厂的垃圾渗漏液项目，每年可为该厂节约工业水10. 8万 吨，仅此一项就可以为该厂每年节约水费30-40万元。
[0054] 综上，同兴渗滤液处理系统工艺具有以下优点：
[0055] 1、采用该工艺的系统能处理高指标的污水，特别是高氨氮指标的垃圾渗滤液，原 水指标如下表：
[0056] 原水水质指标
[0058] 2、采用该工艺的系统出水水质可达到并优于《污水综合排放标准》 (GB8978-1996) 一级标准指标值；
[0059] 3、未采用传统的氨吹脱塔，仅依靠生物脱氨即硝化、反硝化处理技术可使生化段 出水NH3-N指标稳定达标，使处理成本大大降低；
[0060] 4、采用超滤（UF) +反渗透（RO)深度处理即所述的膜处理工艺，可将生化段未降解的有机物大部分截留。
[0061] 最后说明的是，以上实施例仅用以说明本发明的技术方案而非限制，本领域普通 技术人员对本发明的技术方案所做的修改或者等同替换，只要不脱离本发明技术方案的精 神和范围，均应涵盖在本发明的权利要求范围当中。
Claims (3)
- 一种垃圾渗滤液处理工艺，包括以下步骤： a.预处理 将垃圾渗滤液加压送入格栅沉砂池进行预处理除去较大的悬浮物、漂浮物、纤维物质和其它较大的固体颗粒物质；经过预处理的污水自流进入调节池； b.上流式污泥床反应 调节池的出水由水泵泵入UASB反应器以除去大部分CODcr和BOD5，泵入前对废水进行升温，使UASB反应器水温保持30℃‑35℃，UASB反应器的出水自流进入中间池，中间池的回流污水从UASB反应器厌氧污泥床底部进入UASB，中间池的回流水水量是UASB进水量的5‑6倍； c.硝化反硝化反应 中间池的出水由水泵泵入兼氧池，污水在泵入兼氧池前降温至25℃‑30℃，兼氧池内的污水由搅拌器充分搅拌以进行反硝化反应，兼氧池的出水自流进入曝气池； 污水在曝气池内进行硝化反应，硝化反应过程中PH值控制在7‑8，曝气池采用微孔曝气提供空气或者纯氧，穿孔曝气搅拌以加强泥水混合，经过硝化反应的回流污水进入兼氧池，从曝气池回流进入兼氧池的回流水的水量是由兼氧池直流进入曝气池水量的21‑25倍； d.泥水分离 曝气池出水自流进入沉淀池，在该沉淀池进行初次泥水分离，分离后的上清液自流进入膜处理系统，分离出的回流污泥进入兼氧池及曝气池，以保证曝气池中保持足够的污泥浓度进行微生物接种，污泥回流量是曝气池进水量的1.5‑4倍；剩余污泥泵入污泥浓缩池进行再次泥水分离； 经污泥浓缩池浓缩后的污泥加压送入离心式污泥脱水机脱水，污泥浓缩池上清液和脱水机产生的废液回流至调节池； e.膜处理 d步骤中沉淀池首次分离出的上清液首先加压进入超滤膜处理系统进行过滤，超滤膜采用管式陶瓷超滤膜； 超滤膜处理系统回收的浓液回流至调节池，超滤膜处理系统过滤之后产生的清液进入反渗透膜处理系统进行反渗透处理，反渗透膜处理系统的反渗透膜采用聚酰胺类复合膜。
- 2.根据权利要求1所述的垃圾渗滤液处理工艺，其特征在于，b步骤中，从中间池的回 流水水量是UASB进水量的5. 7倍；c步骤中，从曝气池回流进入兼氧池的回流水的水量是 由兼氧池直流进入曝气池水量的23倍。
- 3.根据权利要求1或2所述的垃圾渗滤液处理工艺，其特征在于，b步骤中，使UASB反 应器水温保持35°C ；c步骤中，硝化反应过程PH值控制在7. 5 ；d步骤中，污泥回流量是曝气 池进水量的3倍；e步骤中管式陶瓷超滤膜膜孔径为0. 05 μ m。
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| CN108285240A (zh) * | 2017-12-27 | 2018-07-17 | 武汉天源环保股份有限公司 | 满足冷却塔回用水要求的生活垃圾焚烧厂渗滤液处理方法 |
| CN108264193A (zh) * | 2017-12-27 | 2018-07-10 | 武汉天源环保股份有限公司 | 一种提高生活垃圾焚烧厂渗滤液出水量的处理方法 |
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| GB2344815A (en) * | 1998-12-14 | 2000-06-21 | County Environmental Services | Landfill leachate treatment |
| US6398958B1 (en) * | 2000-03-08 | 2002-06-04 | Waste Management, Inc. | Facultative landfill bioreactor |
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