CN102603128A - 一种垃圾渗滤液深度处理回用方法 - Google Patents
一种垃圾渗滤液深度处理回用方法 Download PDFInfo
- Publication number
- CN102603128A CN102603128A CN2012100984694A CN201210098469A CN102603128A CN 102603128 A CN102603128 A CN 102603128A CN 2012100984694 A CN2012100984694 A CN 2012100984694A CN 201210098469 A CN201210098469 A CN 201210098469A CN 102603128 A CN102603128 A CN 102603128A
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- treatment
- reclamation
- percolate
- water outlet
- advanced treatment
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- 239000000149 chemical water pollutant Substances 0.000 title abstract description 7
- 238000004064 recycling Methods 0.000 title abstract description 6
- 238000001728 nano-filtration Methods 0.000 claims abstract description 31
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 26
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 21
- OKTJSMMVPCPJKN-UHFFFAOYSA-N carbon Chemical compound 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- 238000006731 degradation reaction Methods 0.000 claims description 3
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group 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- -1 nitrogen phosphorus Chemical compound 0.000 description 6
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound 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[Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N carbon dioxide Chemical compound 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[Na] KEAYESYHFKHZAL-UHFFFAOYSA-N 0.000 description 1
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- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
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Abstract
本发明涉及一种垃圾渗滤液深度处理回用方法。所述方法包括以下步骤:(1)对垃圾渗滤液进行厌氧处理;(2)对步骤(1)厌氧处理所得到的出水进行好氧处理,好氧处理的出水再进行超滤;(3)对步骤(2)超滤所得到的出水进行纳滤;(4)对步骤(3)所得到的纳滤出水进行反渗透处理,得到回用出水。本发明的优点在于:(1)有机污染物去除率达98%以上,并确保了后续系统的稳定运行;(2)脱氮率达98%以上,利用垃圾渗滤液原液作补充碳源,节省了运行成本;(3)处理后的污水满足回用标准,避免二次污染。
Description
一种垃圾渗滤液深度处理回用方法
技术领域
[0001] 本发明涉及垃圾渗滤液处理领域,具体地,本发明涉及一种垃圾渗滤液深度处理回用方法。
背景技术
[0002]目前,我国城市生活垃圾的处理主要采用填埋技术或焚烧技术,无论在填埋或焚烧处理过程中都会产生垃圾渗滤液。垃圾渗滤液中C0D&浓度约6000-70000mg/L,NH3-N浓度约1000-2500mg/L,同时含有大量溶解性固体(钠、钙、氯化物、硫酸盐等),是一种水质水量变化大、微生物营养元素比例失调、成分极其复杂、污染物浓度高的有机废水,并伴有极重的腐败臭味,如不妥善处理,会对周围的水体和土壤造成严重污染,对周边人民群众的身体健康产生严重威胁。
[0003] 随着社会的进步与发展,环境容量逐渐减小,环境承载力逐渐降低及随经济的发展带来的水资源的日益短缺,迫切要求开发污水资源化技术。目前垃圾渗滤液资源化利用所采用的主流工艺为生化处理+深度处理,现有技术中有采用厌氧处理+好氧处理+反渗透的污水处理工艺,通过所述工艺方法可以大部分去除渗滤液中的固体和有机污染物以及氮磷等元素;另外还有利用反硝化-硝化的组合工艺对垃圾渗滤液进行处理,该工艺提高了对垃圾渗滤液中氨氮和总氮的去除率,具有较好的效果,但是上述两种方法中通过生物处理和深度处理后仅能达到1996年制定的污水排放标准(GB8978-1996)和2002年制定的出水回用标准(GB/T18920-2002),处理后得到的出水均达不到《城市污水再生利用工业用水水质标准》(GB/T19923-2005)的要求。
[0004] 为了要达到渗滤液深度处理后回用,必须综合考虑渗滤液中高浓度有机污染物的去除,氨氮、总氮的去除,盐分的去除以及系统可能产生的二次污染物的去除等问题,需要对目前的工艺作进一步的改进才有可能实现这一目的。
发明内容
[0005] 针对现有工艺的不足,本发明旨在提供一种垃圾渗滤液的深度处理回用工艺,解决国内垃圾渗滤液单纯依靠生物处理方法不能达标排放,而使用其他处理方法运行不稳定的难题,使出水能达到资源回用的标准。此外,综合考虑了纳滤及反渗透膜系统产生浓水的处理方案,避免了出水二次污染的问题。
[0006] 本发明所述的垃圾渗滤液深度处理回用方法包括以下步骤:
[0007] (I)对垃圾渗滤液进行厌氧处理,去除大部分有机物;
[0008] (2)对步骤(I)厌氧处理所得到的出水进行好氧处理,降解有机物同时脱除各种含氮物质,好氧处理的出水再进行超滤,实现固液分离;
[0009] (3)对步骤(2)超滤所得到的出水进行纳滤,脱除剩余的有机物;
[0010] (4)对步骤(3)所得到的纳滤出水进行反渗透处理,得到回用出水。
[0011] 优选地,所述步骤(2)好氧处理包括以下子步骤:[0012] (2-1)对步骤(I)厌氧处理所得到的出水进行反硝化处理;
[0013] (2-2)对步骤(2-1)反硝化处理所得到的出水进行硝化处理;
[0014] (2-3)对步骤(2-2)硝化处理所得到的出水进行强化脱氨处理,所述强化脱氨为后置反硝化。
[0015] 优选地,所述步骤(2)中超滤得到的浓水返回到步骤(2-1)的反硝化处理液中。
[0016] 优选地,所述步骤(2-3)的后置反硝化处理中加入垃圾渗滤液原液作为外加碳源。
[0017] 优选地,所述外加碳源与硝态氮的浓度(mg/L)比为2. 5-3. 5 : I。
[0018] 优选地,所述步骤(2-2)硝化处理时进行连续鼓风曝气,控制DO为2_5mg/L。
[0019] 优选地,所述步骤(2-2)硝化处理时控制污泥浓度为7-10g/L。
[0020] 优选地,所述步骤(4)反渗透处理选用海水淡化膜。
[0021] 优选地,所述步骤(3)纳滤得到的浓水和步骤(4)的反渗透得到的浓水进行混凝和高级氧化处理,得到的出水进行回用。
[0022] 本发明所提供的方法采用膜生物反应器对垃圾渗滤液进行好氧处理,考虑了反渗透膜产生浓水的处理,并在相关工艺上做了优化,整体提高对有机污染物、氨氮、总氮和盐分的去除率,具体地,本发明的方法首先将垃圾渗滤液进行厌氧处理,去除大部分有机污染物;然后进行好氧处理,优选采用膜生物反应器,去除大部分氨氮、总氮及剩余有机污染物; 采用纳滤系统,截留渗滤液中的大分子、难降解有机污染物及二价以上金属离子,采用反渗透系统,截留部分总氮和盐分,确保出水满足回用要求,并考虑了纳滤、反渗透系统产生浓水的处理。
[0023] 本发明涉及一种垃圾渗滤液深度处理回用方法,本发明的方法采用厌氧+好氧+ 纳滤+反渗透技术,处理后出水水质可以达到《城市污水再生利用工业用水水质标准》(GB/ T19923-2005)的要求,用于工厂冷却水的补给用水。浓水经混凝和高级氧化处理后回用,完全实现了资源的合理配置和循环利用。
[0024] 本发明所述方法的优点在于:
[0025] (I)采用新型高效厌氧反应器,有机污染物去除率达85 %以上,并确保了后续系统的稳定运行;
[0026] (2)采用膜生物反应器,脱氮率达95%以上,利用垃圾渗滤液原液作补充碳源,节省了运行成本;
[0027] (3)纳滤系统浓水部分回流至纳滤进水,提高纳滤系统产水率至80%以上;
[0028] (4)反渗透系统脱盐率99%以上;
[0029] (5)浓水经处理后回用,避免二次污染。
附图说明
[0030] 图I为本发明的垃圾渗滤液深度处理方法流程图;
[0031] 图2为本发明优选的垃圾渗滤液深度处理方法流程图。
具体实施方式
[0032] 在下文的描述中,给出了大量具体的细节以便提供对本发明更为彻底的理解。然而,对于本领域技术人员来说显而易见的是,本发明可以无需一个或多个这些细节而得以实施。在其他的例子中,为了避免与本发明发生混淆,对于本领域公知的一些技术特征未进行描述。
[0033] 本发明所述的方法主要包括以下步骤:厌氧处理、好氧处理、纳滤系统处理和反渗透系统处理,如图I和图2所示,具体实施方式为:
[0034] (I)厌氧处理:本发明渗滤液首先进入厌氧系统进行处理,去除大部分有机物。
[0035] 在该步骤中选用UASB (上流式厌氧污泥床反应器),污水自下而上通过UASB,反应器底部有一个高浓度、高活性的污泥床,污水中的大部分有机污染物在此间经过厌氧发酵降解为甲烷和二氧化碳,因水流和气泡的搅动,污泥床之上有一个污泥悬浮层。反应器上部设有三相分离器,用以分离沼气、净化后污水和污泥颗粒,沼气自反应器顶部导出;污泥颗粒自动滑落沉降至反应器底部的污泥床;净化后污水从澄清区出水。
[0036] 作为优选,为了达到更好的效果本发明对现有UASB反应器进行了改进,通过在反应器底部的中间位置设置柱形布水器,在柱形布水器的上下两层分别连接布水支管,布水支管按圆周均匀分布,布水支管末端连接反射器,将进水均匀布设在反应器底部。另外,在反应器中上部还设置有内循环集水管,将经厌氧处理后的渗滤液收集后通过内循环水泵与反应器进水管相连,与进水一起均匀分布在反应器底部,维持反应器的上升流速。此外,通过将反应器底部设计成污泥斗形式,便于污泥的收集及污泥均匀排出,避免局部出现沉积。 反应器底部设置成污泥斗形式后,避免反应器底部受力不均,在污泥斗的直边均匀开孔,使泥水混合物进入污泥斗两边的空容,采用水力承重法解决反应器底部受力不均问题,进一步的改进在在专利号为201220081068. 3的申请中有所描述。工作时内循环水通过反应器中上部的集水管汇集后由内循环水泵输送至反应器的进水总管,与进水混合一起进入反应器底部的柱形布水器,废水进入柱形布水器后,由于布水器内水位上升,废水先后进入分布在布水器的上下两层布水支管,两层布水支管均按圆周90度布置,废水通过布水支管进入锥形反射器,与反应器底部的污泥充分接触、混合,污泥中的微生物降解废水中的有机污染物产生沼气,气、水、泥的混合液上升至三相分离器内,气体进入集气室排出,污泥和水进入沉淀室在重力作用下泥、水分离,污泥沿斜壁返回反应区,上清液从沉淀区上部排走,实现水力停留时间和污泥停留时间分离,维持了反应器内较高的污泥浓度和较长的污泥龄。改进后的反应器底部进水布水更均匀,底部排泥也更均匀畅通,经厌氧处理,使部分有机物和固体悬浮物被截留或分解。采用新型高效厌氧反应器,有机污染物去除率达85%以上,并确保了后续系统的稳定运行。
[0037] (2)好氧处理:好氧处理中生化处理段采用“反硝化-硝化-强化脱氮”工艺,作为优选,好氧处理中采用膜生物反应器,脱氮率达95%以上。
[0038] 反硝化:首先,厌氧系统出水首先进入反硝化池,在缺氧环境下,微生物(如厌氧细菌)将回流硝化液中的硝态氮和亚硝态氮还原成氮气排出,达到生物脱氮的目的;作为进一步的优选,本发明中将超滤步骤得到的滤液浓缩液返回到反硝化池进一步脱氮。
[0039] 硝化:经反硝化池后的渗滤液进入硝化池进行硝化反应,在该步骤中将有机氮和氨态氮在氨化菌、亚硝化菌和硝酸菌的作用下将氮最终转化为硝态氮,在该步骤中DO值的控制非常关键,溶解氧的水平过低使活性污泥活性降低,会抑制生物对有机物的降解,产生污泥膨胀,但是溶解氧过高会加速消耗污水中的有机物,使微生物因缺乏营养而引起活性污泥的老化,长期过高的溶解氧会降低活性污泥的絮凝性能和吸附能力,增加能耗,在本发明的硝化池内连续射流鼓风曝气,控制DO在2-5mg/L之间,作为优选,将DO控制在
3. 2-4. 8mg/L,在该优选范围内效果更好,其氨氮转化为硝态氮的效率更高,使后置反硝化步骤中TN去除率进一步提高,作为进一步优选,DO控制在3. 5-4. 6mg/L,其TN去除率进更高效果更好;污泥浓度控制在7〜10g/L,优选7. 5-9. 5g/L,在所述优选范围内,污泥的活化效率增强,有机污染物降解率提高,同时对超滤过程中膜的污染也进一步降低,综合效益增强,作为进一步的优选,所述污泥浓度为8. 0-9. Og/L。
[0040] 强化脱氮:硝化后的废水进入强化脱氮系统,即后置反硝化,在后置反硝化中加入外加碳源以获得较高的TN去除率,作为优先,在本发明中选用渗滤液原液作为外加碳源进行添加,在所述后置反硝化池中,外加有机碳源在污水处理中起着重要的作用,它是细菌代谢的必要物质和能量来源,同时也是异养好氧菌和反硝化细菌的电子供体提供者,在一定范围内,有机碳源越充分,C/N(碳源与硝态氮浓度比:浓度-mg/L)值越高,反硝化获得的碳源越充足,反硝化越充分,TN(水中各种形态无机和有机氮的总量)的去除率也越高,但是当C/N值超过一定的比例时,TN的去除率不多,反而会增加运营成本,在本发明中控制碳源与硝态氮浓度比在2. 5-3. 5 : 1,在该范围内能提供足够的碳源,能使含氮化合物比较充分的降解,优选为2. 8-3. 2 : 1,更优选3. 0-3. I : 1,在该优选范围内,硝态氮能更多的被分解为氮气脱除,TN去除率进一步提高,而且节省了运行成本。
[0041] 超滤:强化脱氮后出水进入超滤系统,作为优选,超滤可以采用浸没式超滤膜系统,但是在本发明中不局限于浸没式超滤膜,平板式、管式、气提式超滤膜均可以实现本发明的目的,去除剩余有机污染物,超滤膜过滤后产生的浓缩液回流至反硝化系统,作进一步脱氮处理。
[0042] 在好氧处理阶段选用膜生物反应器,膜生物反应器优选浸没式超滤膜,膜生物反应器具有膜处理技术和生物处理技术的优点,超滤膜截留活性污泥混合液中微生物絮体和较大分子有机物,使之停留在反应器内,使反应器内获得高生物浓度,并延长有机固体停留时间,极大地提高了微生物对有机物的氧化率;同时,经超滤膜处理后,出水质量高,为后面的纳滤和反渗透提供了保障,再经过纳滤和反渗透处理后能达到回用的标准。
[0043] (3)纳滤:超滤系统出水进入纳滤膜系统,利用纳滤设备去除二价或多价离子及分子量介于200〜1000之间的有机物,对反渗透系统起到保护作用。
[0044] 作为优选,为防止纳滤膜系统结垢,延长清洗周期,在纳滤进水管路上增加管道混合器以投加盐酸和阻垢剂,在纳滤高压泵和循环泵的压力推动下,二价离子及其他污染物被有效截留,尤其对于二价或多价离子及分子量介于200〜1000之间的有机物具有更好的脱除效果。
[0045] 作为进一步的优选,纳滤产生的浓缩液部分通过高压循环水泵回流至纳滤进水端,以提高纳滤系统产水率,通过浓缩液回流可以使纳滤产水率达80%以上,纳滤系统同时作为反渗透系统的保护,确保反渗透进水符合要求。
[0046] (4)反渗透:纳滤出水进入反渗透系统进行脱盐处理,浓缩液排放至浓水贮池待处理,反渗透出水达到《城市污水再生利用工业用水水质标准》(GB/T 19923-2005)。
[0047] 作为优选,本发明反渗透系统采用海水淡化膜,以确保系统最终的脱盐效果,海水淡化膜的脱盐率达99%以上,所述海水淡化膜是一类具有高脱盐率,耐腐蚀、耐高压、抗污染的反渗透膜,反渗透膜主要分低能耗反渗透膜、抗污染反渗透膜和海水淡化膜,本发明中优选海水淡化膜,经海水淡化膜处理后的出水中无机盐离子、含氮化合物以及有机污染物的含量进一步降低,其效果均优于其他反渗透膜,处理得到的出水完全符合GB/T 19923-2005 的要求。
[0048] (5)纳滤系统及反渗透系统产生的浓水采用“混凝+高级氧化”处理后回用:纳滤和反渗透浓水经混凝沉淀和高级氧化后,去除绝大部分金属离子和部分有机物后回用,避免二次污染。
[0049] 应用此工艺进行渗滤液的深度处理,投加药剂量较少,污泥产生量少,电耗低,自动化程度高,运行稳定,最终处理后出水水质可以达到《城市污水再生利用工业用水水质标准》(GB/T19923-2005)标准,用于工厂冷却水的补给用水,从而实现资源的再次利用。垃圾渗滤液处理前后的水质数据见表I。
[0050] 表I垃圾渗滤液处理前后的水质数据
[0051]
[0052] 本发明已经通过上述实施例进行了说明,但应当理解的是,上述实施例只是用于举例和说明的目的,而非意在将本发明限制于所描述的实施例范围内。此外本领域技术人员可以理解的是,本发明并不局限于上述实施例,根据本发明的教导还可以做出更多种的变型和修改,这些变型和修改均落在本发明所要求保护的范围以内。本发明的保护范围由附属的权利要求书及其等效范围所界定。
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Claims (13)
1. 一种垃圾渗滤液深度处理回用方法,所述方法包括以下步骤:(1)对垃圾渗滤液进行厌氧处理;(2)对步骤(I)厌氧处理所得到的出水进行好氧处理,好氧处理的出水再进行超滤;(3)对步骤(2)超滤所得到的出水进行纳滤;(4)对步骤(3)所得到的纳滤出水进行反渗透处理,得到回用出水。
2.根据权利要求I所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤(I)的厌氧处理用于去除大部分有机物。
3.根据权利要求I所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤(2)的好氧处理用于降解有机物同时脱除各种含氮物质,超滤处理用于实现固液分离。
4.根据权利要求I所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤(3)纳滤用于脱除剩余的有机物。
5.根据权利要求I所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤(4)的反渗透处理用于去除剩余离子,得到回用出水。
6.根据权利要求I所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤(2)好氧处理包括以下步骤:(2-1)对步骤(I)厌氧处理所得到的出水进行反硝化处理;(2-2)对步骤(2-1)反硝化处理所得到的出水进行硝化处理;(2-3)对步骤(2-2)硝化处理所得到的出水进行强化脱氨处理,所述强化脱氨处理为后置反硝化。
7.根据权利要求6所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤(2)中超滤得到的浓水返回到步骤(2-1)的反硝化处理液中。
8.根据权利要求6所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤(2-3) 的后置反硝化处理中加入垃圾渗滤液原液作为外加碳源。
9.根据权利要求8所述的垃圾渗滤液深度处理回用方法,其特征在于,所述外加碳源与硝态氮的浓度比为2. 5-3. 5 : I。
10.根据权利要求6或9所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤 (2-2)硝化处理时进行连续鼓风曝气,控制DO值为2-5mg/L。
11.根据权利要求10所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤 (2-2)硝化处理时控制污泥浓度为7-10g/L。
12.根据权利要求I所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤(4) 反渗透处理选用海水淡化膜。
13.根据权利要求I所述的垃圾渗滤液深度处理回用方法,其特征在于,所述步骤(3) 纳滤得到的浓水和步骤(4)的反渗透得到的浓水进行混凝和高级氧化处理,得到的出水进行回用。
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