CN103626352A - 一种达标污水深度处理及回用工艺及装置 - Google Patents
一种达标污水深度处理及回用工艺及装置 Download PDFInfo
- Publication number
- CN103626352A CN103626352A CN201210299842.2A CN201210299842A CN103626352A CN 103626352 A CN103626352 A CN 103626352A CN 201210299842 A CN201210299842 A CN 201210299842A CN 103626352 A CN103626352 A CN 103626352A
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- water
- filter
- ozone
- tank
- ultrafiltration
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- 239000010865 sewage Substances 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title abstract description 20
- 238000004064 recycling Methods 0.000 title abstract 3
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- CBENFWSGALASAD-UHFFFAOYSA-N ozone Chemical compound 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[O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 101
- 244000005700 microbiome Species 0.000 claims abstract description 57
- 238000006243 chemical reaction Methods 0.000 claims abstract description 42
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 39
- 238000001914 filtration Methods 0.000 claims description 63
- 238000000108 ultra-filtration Methods 0.000 claims description 57
- 239000000126 substance Substances 0.000 claims description 27
- 238000005273 aeration Methods 0.000 claims description 19
- 230000004907 flux Effects 0.000 claims description 17
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- VSCWAEJMTAWNJL-UHFFFAOYSA-K Aluminium chloride Chemical compound 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- 239000000758 substrate Substances 0.000 claims description 3
- 239000000725 suspension Substances 0.000 claims description 3
- 239000007787 solid Substances 0.000 abstract description 7
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound 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- 239000003208 petroleum Substances 0.000 description 8
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- 230000015556 catabolic process Effects 0.000 description 2
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Abstract
本发明涉及一种以石化达标污水为水源的深度处理及回用组合装置，其包括依次连接的气浮滤池、臭氧反应池、固定化微生物曝气生物滤池、V型滤池、超滤和反渗透。以及应用该装置深度处理及回用为循环水补给水的方法：污水首先进入气浮滤池，去除水中的油、轻质絮体及悬浮物；随后污水进入臭氧反应池，降解难降解有机物，提高污水可生化性；随后污水进入固定化微生物曝气生物滤池，去除水中的有机物和氨氮；随后污水进入V型滤池，去除水中的悬浮物及悬浮态有机物；滤池出水进入超滤，去除悬浮物及胶体态有机物；超滤出水进入反渗透，脱除盐分，最终出水至循环水补给水用水点。
Description
—种达标污水深度处理及回用工艺及装置技术领域
[0001] 本发明涉及一种石化企业达标污水深度处理及回用工艺技术，特别是采用气浮滤池-臭氧反应池(投加臭氧)-固定化微生物曝气生物滤池-V型滤池-超滤-反渗透组合工艺技术。
背景技术
[0002] 石化企业是用水大户，随着水资源日益匮乏，水源的供给已经成为限制企业扩产、增产的制约因素。为降低吨油水耗，确保企业可持续发展，将达标污水深度处理回用为循环水补给水，可带来一定的经济效益和环境效益。
[0003] 气浮滤池是溶气浮选池和综合滤料过滤池相结合的工艺。滤池除油、除悬浮物效果好，同时具有占地面积小、能耗低、处理效果好的特点。
[0004] 在臭氧反应池中投加臭氧，利用臭氧的强氧化性，将水中部分难生化降解的有机物氧化分解为小分子有机物，降低污水有机物负荷，并提高污水的可生化性。
[0005] 固定化微生物曝气生物滤池(G-BAF)工艺是由一种新型微生物降解有机物和脱氮的新工艺。该工艺利用基因工程的手段，对自然微生物进行了强化与变异而产生的硝化菌、亚硝化菌和反硝化菌可适应各种水质，应用先进的微生物固定化技术，将高效微生物菌群固定在大孔网状载体，使其生物负载量为传统工艺的3~10倍，能高效处理传统生物法难降解的有机物和氨氮。
[0006] V型滤池是快滤池的一种形式，因其进水槽形状呈V字形而得名，也叫均粒滤料滤池(滤料采用均质滤料)。V型滤池采用了气、水反冲洗兼表面扫洗的技术，能够实现节水、节能，且改善了滤池的过滤性能。
[0007] 超滤-反渗透双 膜工艺通过过滤和脱盐去除水中的悬浮物、胶体和溶解盐，出水满足循环水补给水的要求。
[0008] 石化企业达标污水相对于循环水补给水，悬浮物、油、有机污染物、氨氮、溶解性总固体含量超标，同时C/N较低，可生化性较差，不利于微生物的生长及有机物的降解。上述工艺在石化企业污水深度处理及回用工艺的应用中，对有机污染物和氨氮的处理效果不佳，超滤-反渗透双膜工艺易发生有机物和微生物污染，需研发针对石化企业达标污水水质特点的深度处理及回用工艺及装置。
发明内容
[0009] 本发明的目的在于克服固定化微生物曝气生物滤池、超滤-反渗透双膜工艺等单项工艺处理石化企业达标污水深度处理及回用工艺技术性和针对性的不足，提供一种包括气浮滤池、臭氧反应池、固定化微生物曝气生物滤池、V型滤池、超滤-反渗透双膜工艺的组合工艺及装置。与同类单项及常规组合工艺相比，该工艺可提高污水可生化降解性，实现有机物、氨氮、悬浮物和溶解性总固体的去除，同时延缓超滤-反渗透双膜工艺的有机物、微生物污染周期。[0010] 为实现上述目的，一方面，本发明提供一种石化企业达标污水深度处理及回用组合装置，其包括依次连接的气浮滤池1、臭氧反应池2、固定化微生物曝气生物滤池4、V型滤池5、滤后水箱9、超滤11、超滤水箱12、保安过滤器15、反渗透17。
[0011] 如上所述的装置，其中，该装置还包括臭氧发生装置3、曝气风机6、气洗风机7、滤池反洗水泵8、滤后水泵10、超滤反洗水泵13、超滤水泵14、保安过滤器15和高压泵16。
[0012] 其中，达标污水由气浮滤池I进水口进入，出水口与臭氧反应池2进水口连接，臭氧反应池2出水口与固定化微生物曝气生物滤池4进水口连接，固定化微生物曝气生物滤池4出水口与V型滤池5进水口连接，V型滤池5出水口与滤后水箱9进水口连接，滤后水箱9出水口与超滤11进水口连接，超滤11出水口与超滤水箱12进水口连接，超滤水箱12出水口与滤后水泵14进水口连接，滤后水泵14出水口与保安过滤器15进水口连接，保安过滤器15出水口与高压泵16出水口连接，高压泵16出水口与反渗透17连接。
[0013] 气浮滤池I上部为溶气气浮区，压缩空气经溶气罐后，由溶气释放器释放的气泡直径为10 u m。下部为滤料过滤区,填装石英砂滤料,石英砂粒径0.5mm~1.2mm,填料层有效高度为0.7m。气浮滤池进水前投加混凝剂，气浮滤池的出水采用虹吸出水，气浮滤池的反洗米用移动冲洗罩反洗。
[0014] 臭氧反应池2底部具有钛板曝气盘，曝气盘与具有流量调节功能的臭氧发生装置3连接；臭氧反应池内设置有导流板，将臭氧接触池分为3格，三格臭氧接触的气量比为5:3:2。臭氧反应池2顶部具有尾气出口，将未反应的臭氧气体收集后由臭氧分解系统处理，达标后外排。臭氧接 触池2的有效高度为6m，停留时间lh。
[0015] 固定化微生物曝气生物滤池4，采用高效悬浮大孔载体，通过分子设计，将高效微生物菌群固定在载体上。载体比表面积为100m2/m3，填料层厚度2.5米，微生物负载量20~40g/L。运行初期，填料内部投加变异菌和酶制剂，投加比例为4~IOg菌剂/L。固定化微生物曝气生物滤池4底部有曝气口、反洗口和气洗口，分别连接曝气风机6、气洗风机7和滤池反洗水泵8。
[0016] V型滤池5前投加混凝剂。
[0017] 超滤11过滤精度0.0311!11，通量不大于60171112*11。超滤设反洗口，与超滤反洗水泵13出水口连接。
[0018] 保安过滤器内置PP材质大通量滤芯,过滤精度5 ii m，单支滤芯过滤流量50m3/h。
[0019] 反渗透采用抗污染反渗透膜元件，一级二段排列，反渗透膜通量不大于20L/m2 *h。
[0020] 另一方面，本发明提供应用上述装置深度处理及回用石化达标废水的方案，其包括如下步骤:
[0021] a)石化达标污水至气浮滤池1，去除水中的油、轻质絮体及悬浮物。气浮滤池前投加聚合氯化铝和聚丙烯酰胺，投加浓度分别为5~10mg/L和lmg/L。气浮滤池滤速5~10m/h,水力停留时间0.5~Ih0
[0022] 其后，污水进入臭氧反应池2。臭氧发生装置3产生的臭氧经盘式曝气头进入臭氧接触池，污水在臭氧池反应内流动，与臭氧充分接触并反应。臭氧反应池2顶部具有尾气出口，将未反应的臭氧气体收集后由臭氧分解系统处理，达标后外排。臭氧投加比例为I~
1.5mg03/mg CODcr (需降解的)，臭氧接触时间为Ih。
[0023] b)污水由臭氧反应池2的出水口进入固定化微生物曝气生物滤池4进行有机物和氨氮的去除。填料载体外部溶解氧浓度控制在2~4mg/L，载体内部溶解氧浓度为0.5~2mg/L，pH值为6~8，温度为5~35°C，水力停留时间为I~1.5h。
[0024] c)污水由固定化微生物曝气生物滤池4出水口进入V型滤池5去除悬浮物，在V型滤池前投加聚合氯化铝，投加浓度为5~10mg/L。V型滤池滤速8~12m/h。
[0025] d) V型滤池5出水进入滤后水箱9，滤后水箱9出水进入滤后水泵10进水口。
[0026] e)滤后水泵10出水进入超滤11，超滤通量不大于60L/m2 *h,出水浊度≤0.1NTU0
[0027] f)超滤11出水进入超滤水箱12，超滤水箱12出水口连接超滤反洗水泵13入水口和超滤水泵14入水口。
[0028] g)超滤水泵14出水进入保安过滤器15。保安过滤器采用PP材质5 ii m精度的滤芯，更换周期3~6个月。
[0029] h)保安过滤器15出水进入高压泵16。
[0030] i)高压泵16出水进入反渗透17。反渗透运行通量不大于20L/m2 -h,反渗透脱盐率≥98%。
[0031] 如上所述的方法可进一步包括如下步骤:
[0032] i)滤后水池9出水经滤池反洗水泵8分别进入固定化微生物曝气生物滤池4和V型滤池5，同时气洗风机7出口分别连接固定化微生物曝气生物滤池4和V型滤池的气洗进口。通过气、水反洗完成反洗步骤，固定化微生物曝气生物滤池反冲洗周期为3~10天，V型滤池反冲洗周期12~24h。
[0033] k)超滤水池12出水经超滤反洗水泵13进入超滤11，完成超滤反洗，超滤反洗周其月30min。
[0034] 本发明针对石化达标污水的水质特点，提供一种深度处理及回用的装置和方法。其有益效果在于:
[0035] I)气浮滤池兼具除油、除悬浮态有机物、除悬浮物的功能，同时有效降低了后续臭氧接触池的臭氧反应负荷。
[0036] 2)臭氧接触池分为三格，臭氧接触气量逐格递减，有利于臭氧与污水的充分接触，有利于臭氧氧化污水中的难降解有机物，提高污水的可生化性；同时，臭氧接触池出水溶解氧浓度较高，有利于固定化微生物曝气生物滤池的反应。
[0037] 3)固定化微生物曝气生物滤池采用大孔载体，固定后的微生物不易流失、微生物负载量高、传质速度好；投加的高效变异菌和酶制剂，有效改善了普通曝气生物滤池微生物浓度低的问题。
[0038] 4) V型滤池可进一步去除固定化微生物曝气生物滤池出水含有的悬浮态有机物。
[0039] 5)本发明装置的自动化程度高、操作管理方便、系统适应性与实用性强。
[0040] 6)使用本发明提出的石化达标污水深度处理及回用方法，出水C0D&、B0D5、NH3-N、SS分别达到20~30mg/L、l~5mg/L、l~5mg/L和低于0.lmg/L。对水体中各污染物的去除效果为:C0D&去除率超过50%，BOD5超过60%、NH3-N的去除率超过90%、悬浮物SS的去除率约100%，溶解性总固体的去除率超过98%。石化达标污水水质满足中华人民共和国国家标准《污水综合排放标准》(GB8978-1996)中一级标准，出水水质满足中华人民共和国国家标准《工业循环冷却水处理设计规范》(GB50050-2007)中再生水水质要求。附图说明
[0041] 图1为本发明一种达标污水深度处理及回用工艺装置及流程图。
具体实施方式
[0042] 以下结合附图和具体实例对本发明进行进一步详细说明。
[0043] 如图1所示，在本发明的工艺中，达标污水深度处理及回用工艺装置主要包括:气浮滤池1、臭氧反应池2、臭氧发生装置3、固定化微生物曝气生物滤池4、V型滤池5、曝气风机6、气洗风机7、滤池反洗水泵8、滤后水箱9、滤后水泵10、超滤11、超滤水箱12、超滤反洗水泵13、超滤水泵14、保安过滤器15、高压泵16、反渗透17以及填料和管道等。 [0044] 其中，达标污水由气浮滤池I进水口进入，出水口与臭氧反应池2进水口连接，臭氧反应池2出水口与固定化微生物曝气生物滤池4进水口连接，固定化微生物曝气生物滤池4出水口与V型滤池5进水口连接，V型滤池5出水口与滤后水箱9进水口连接，滤后水箱9出水口与超滤11进水口连接，超滤11出水口与超滤水箱12进水口连接，超滤水箱12出水口与滤后水泵14进水口连接，滤后水泵14出水口与保安过滤器15进水口连接，保安过滤器15出水口与高压泵16出水口连接，高压泵16出水口与反渗透17连接。
[0045] 气浮滤池I上部为溶气气浮区，压缩空气经溶气罐后，由溶气释放器释放的气泡直径为10 u m。下部为滤料过滤区,填装石英砂滤料,石英砂粒径0.5mm~1.2mm,填料层有效高度为0.7m。气浮滤池进水前投加混凝剂，气浮滤池的出水采用虹吸出水，气浮滤池的反洗米用移动冲洗罩反洗。
[0046] 臭氧反应池2底部具有钛板曝气盘，曝气盘与具有流量调节功能的臭氧发生装置3连接；臭氧反应池内设置有导流板，将臭氧接触池分为3格，三格臭氧接触的气量比为5: 3: 2。臭氧反应池2顶部具有尾气出口，将未反应的臭氧气体收集后由臭氧分解系统处理，达标后外排。臭氧接触池2的有效高度为6m，臭氧投加比例为I~1.5mg03/mgCODcr (需降解的)，停留时间Ih。
[0047] 固定化微生物曝气生物滤池4，采用高效悬浮大孔载体，通过分子设计，将高效微生物菌群固定在载体上。载体比表面积为100m2/m3，填料层厚度2.5米，微生物负载量20~40g/L。运行初期，填料内部投加变异菌和酶制剂，投加菌剂比例为4~10g/L。固定化微生物曝气生物滤池4底部有曝气口、反洗口和气洗口，分别连接曝气风机6、气洗风机7和滤池反洗水泵8。
[0048] V型滤池5前投加混凝剂。
[0049] 超滤11过滤精度0.0311!11，通量不大于60171112*11。超滤设反洗口，与超滤反洗水泵13出水口连接。
[0050] 保安过滤器内置PP材质大通量滤芯,过滤精度5 ii m，单支滤芯过滤流量50m3/h。
[0051] 反渗透采用抗污染反渗透膜元件，一级二段排列，反渗透膜通量不大于20L/m2 -h,回收率不大于70%。
[0052] 如图1所示，其是本发明的石化达标污水深度处理及回用工艺的流程图，其应用了上述石化达标污水深度处理及回用装置，具体操作步骤如下:
[0053] (I)石化达标污水进入气浮滤池1，去除水中的油、轻质絮体及悬浮物。气浮滤池前投加聚合氯化铝和聚丙烯酰胺，投加浓度分别为5~10mg/L和lmg/L。气浮滤池滤速5~lOm/h,水力停留时间0.5~lh。气浮滤池反洗周期16~24h,每次反洗时间15min。
[0054] (2)气浮滤池I出水进入臭氧反应池2，臭氧发生装置3产生的臭氧经盘式曝气头进入臭氧反应池。臭氧反应池内设置有导流板，将臭氧接触池分为3格，三格臭氧接触的气量比为5: 3: 2。臭氧反应池2顶部具有尾气出口，将未反应的臭氧气体收集后由臭氧分解系统处理，达标后外排。臭氧接触池2的有效高度为6m，臭氧投加比例为I~1.5mg03/mgC0D&(需降解的)，停留时间lh。难降解有机物得到降解，同时污水的可生化性得到较大改善。[0055] (3)臭氧反应池2出水进入固定化微生物曝气生物滤池4。运行初期投加变异菌和酶制剂，投加菌剂比例为4~10g/L，对固定化微生物曝气生物滤池中的工程菌进行驯化，驯化步骤包括:培养初期固定化微生物曝气生物滤池的C0D&浓度在500~600mg/L，DO浓度控制在3~5mg/L,闷曝3~5天。随后，以达标污水进入固定化微生物曝气生物滤池,控制DO浓度在2~4mg/L，直至出水的有机物去除率达到30~40%，驯化步骤完成。
[0056] (4)固定化微生物曝气生物滤池4出水进入V型滤池5，去除悬浮物，在V型滤池前投加聚合氯化铝，投加浓度为5~10mg/L。V型滤池滤速8~12m/h。V型滤池反洗周期为16~24h,气洗-水洗时间约6min。
[0057] (5) V型滤池5出水进入滤后水箱9，滤后水箱9出水由滤后水泵10加压进入超滤
11。超滤截留胶体态有机物、悬浮物及微生物。超滤过滤孔径0.03iim，通量不大于60L/m2 • h，出水浊度≤0.1NTU0超滤反洗周期约30min，反洗时间约3min。
[0058] (6)超滤11出水进入超滤水箱12，超滤水箱12出水由超滤水泵14加压进入保安过滤器15。保安过滤器采用PP材质5 y m精度的滤芯，更换周期3~6个月。
[0059] (7)保安过滤器15出水进入高压泵16，高压泵16出水进入反渗透17。反渗透采用抗污染反渗透膜元件，一级二段排列，反渗透膜通量不大于20L/m2 • h，回收率不大于70%。
[0060]实例:
[0061] 原水为某石化企业炼油达标污水，水质满足中华人民共和国国家标准《污水综合排放标准》(GB8978-1996)中一级标准，应用本发明装置处理污水，运行初期向固定化微生物曝气生物滤池投加变异菌和酶制剂，投加比例为4~IOg菌剂/L，并进行驯化。培养初期控制固定化微生物曝气生物滤池C0D&浓度在500~600mg/L，DO浓度控制在3~5mg/L，闷曝3~5天后，以达标污水顺序进入污水深度处理及回用装置，实现整个工艺系统连续进出水。
[0062] 达标污水进入气浮滤池，去除水中的油、轻质絮体及悬浮物。气浮滤池前投加聚合氯化招和聚丙烯酰胺，投加浓度分别为5~10mg/L和lmg/L。气浮滤池滤速5~10m/h,水力停留时间0.5~lh。气浮滤池反洗周期16~24h,每次反洗时间15min。
[0063] 气浮滤池出水进入臭氧反应池，臭氧发生装置3产生的臭氧经盘式曝气头进入臭氧反应池。臭氧反应池内设置有导流板，将臭氧接触池分为3格，三格臭氧接触的气量比为5: 3: 2。臭氧反应池2顶部具有尾气出口，将未反应的臭氧气体收集后由臭氧分解系统处理，达标后外排。臭氧接触池2的有效高度为6m，臭氧投加比例为I~1.5mg03/mgC0D&(需降解的)，停留时间lh。难降解有机物得到降解，同时污水的可生化性得到较大改
盡
口 o
[0064] 臭氧反应池出水进入固定化微生物曝气生物滤池。控制DO浓度在2~4mg/L，载体内部溶解氧浓度为0.5~2mg/L，pH值为6~8，温度为5~35°C，水力停留时间为I~
1.5h。
[0065] 固定化微生物曝气生物滤池出水进入V型滤池，去除悬浮物，在V型滤池前投加聚合氯化铝，投加浓度为5~10mg/L。V型滤池滤速8~12m/h。V型滤池反洗周期为16~24h,气洗-水洗时间约6min。
[0066] V型滤池5出水进入滤后水箱，滤后水箱出水由滤后水泵加压进入超滤。超滤截留胶体态有机物、悬浮物及微生物。超滤过滤孔径0.03 u m,通量不大于60L/m2 • h,出水浊度(0.1NTUo超滤反洗周期约30min,反洗时间约3min。
[0067] 超滤出水进入超滤水箱，超滤水箱出水由超滤水泵加压进入保安过滤器。保安过滤器采用PP材质5 ii m精度的滤芯，更换周期3~6个月。
[0068] 保安过滤器出水进入高压泵，高压泵出水进入反渗透。反渗透采用抗污染反渗透膜元件，一级二段排列，反渗透膜通量不大于20L/m2 • h，回收率不大于70%。
[0069]经检测，进水 C0D&、BOD5, NH3-N, SS 和 TDS 分别在 50 ~60mg/L、8 ~10mg/L、8 ~10mg/L、50 ~60mg/L、800 ~1000mg/L，出水 C0DCr、B0D5、NH3_N、SS 和 TDS 维持在 25 ~30mg/L、2~5mg/L、l~3mg/L、0~0.lmg/L和16~20mg/L之间，各项指标平均去除率分别达到50%、50%、70%、99%和 9 8% 以上。
Claims (11)
1.一种达标污水深度处理及回用工艺及装置，其特征在于，其包括依次连接的气浮滤池(I)、臭氧反应池(2)、固定化微生物曝气生物滤池(4)、V型滤池(5)、滤后水箱(9)、超滤(11)、超滤水箱(12)、保安过滤器(15)、反渗透(17)。
2.如权利要求1所述的装置，其特征在于，所述装置还包括臭氧发生装置(3)、曝气风机(6)、气洗风机(7)、滤池反洗水泵(8)、滤后水泵(10)、超滤反洗水泵(13)、超滤水泵(14)、保安过滤器(15)和高压泵(16)。 其中，达标污水由气浮滤池(I)进水口进入，出水口与臭氧反应池(2)进水口连接，臭氧反应池(2)出水口与固定化微生物曝气生物滤池(4)进水口连接，固定化微生物曝气生物滤池⑷出水口与V型滤池(5)进水口连接，V型滤池(5)出水口与滤后水箱(9)进水口连接，滤后水箱(9)出水口与超滤(11)进水口连接，超滤(11)出水口与超滤水箱(12)进水口连接，超滤水箱(12)出水口与滤后水泵(14)进水口连接，滤后水泵(14)出水口与保安过滤器(15)进水口连接，保安过滤器(15)出水口与高压泵(16)出水口连接，高压泵(16)出水口与反渗透(17)连接。 固定化微生物曝气生物滤池(4)底部有曝气口、反洗口和气洗口，分别连接曝气风机(6)、气洗风机(7)和滤池反洗水泵(8)。 V型滤池(5)底部有反洗口和气洗口，分别连接气洗风机(7)和滤池反洗水泵(8)。 超滤(11)底部有反洗口，连接超滤反洗水泵(13)。
3.如权利要求2所述的装置，其特征在于，气浮滤池(I)上部为溶气气浮区由溶气释放器释放的气泡直径为10 V- m。滤料过滤区填装的石英砂粒径0.5mm~1.2mm,填料层有效高度为0.7m。
4.如权利要求2所述的装置，其特征在于，臭氧反应池(2)内设置有导流板，将臭氧接触池分为3格，三格臭氧接触的气量比为5: 3: 2。臭氧接触池(2)的有效高度为6m，臭氧投加比例为I~1.5mg03/mgC0DCr(需降解的)，停留时间Ih。
5.如权利要求2所述的装置，其特征在于，固定化微生物曝气生物滤池(4)，采用的高效悬浮大孔载体比表面积为100m2/m3，填料层厚度2.5米，微生物负载量20~40g/L。运行初期，填料内部投加变异菌和酶制剂，投加菌剂比例为4~10g/L。
6.如权利要求2所述的装置，其特征在于，超滤(11)过滤精度0.03 ym，通量不大于60L/m2 • ho超滤反洗周期约30min,反洗时间约3min。
7.如权利要求2所述的装置，其特征在于，保安过滤器(15)内置PP材质大通量滤芯，过滤精度5 u m,单支滤芯过滤流量50m3/h。
8.如权利要求2所述的装置，其特征在于，反渗透(17)采用抗污染反渗透膜元件，一级二段排列，反渗透膜通量不大于20L/m2 • h。
9.应用权利要求1~8中任一项所述装置深度处理及回用达标污水的方法，其特征在于，包含如下步骤:a.石化达标污水进入气浮滤池(I)，去除水中的油、轻质絮体及悬浮物。气浮滤池前投加聚合氯化铝和聚丙烯酰胺，投加浓度分别为5~10mg/L和lmg/L。气浮滤池滤速5~10m/h,水力停留时间0.5~lh。气浮滤池反洗周期16~24h,每次反洗时间15min ；b.其后，气浮滤池(I)出水进入臭氧反应池(2)，臭氧发生装置(3)产生的臭氧经盘式曝气头进入臭氧反应池。臭氧反应池内设置有导流板，将臭氧接触池分为3格，三格臭氧接触的气量比为5: 3: 2。臭氧反应池(2)顶部具有尾气出口，将未反应的臭氧气体收集后由臭氧分解系统处理，达标后外排。臭氧接触池(2)的有效高度为6m，臭氧投加比例为1~1.5mg03/mg COD&(需降解的)，停留时间lh。难降解有机物得到降解，同时污水的可生化性得到较大改善；c.臭氧反应池(2)出水进入固定化微生物曝气生物滤池(4)，控制DO浓度在2~4mg/L，载体内部溶解氧浓度为0.5~2mg/L，pH值为6~8，温度为5~35°C，水力停留时间为1~1.5h ；d.固定化微生物曝气生物滤池(4)出水进入V型滤池(5)去除悬浮物，在V型滤池前投加聚合氯化铝，投加浓度为5~10mg/L，V型滤池滤速8~12m/h。V型滤池反洗周期为16~24h，气洗-水洗时间约6min ；e.V型滤池(5)出水进入滤后水箱(9)，滤后水箱(9)出水由滤后水泵(10)加压进入超滤(11)，超滤截留胶体态有机物、悬浮物及微生物。超滤过滤孔径0.03 u m,通量不大于60L/m2 -h,出水浊度≤0.1NTU,超滤反洗周期约30min，反洗时间约3min ；f.超滤(11)出水进入超滤水箱(12)，超滤水箱(12)出水由超滤水泵(14)加压进入保安过滤器(15)，保安过滤器采用PP材质5 精度的滤芯，更换周期3~6个月；g.保安过滤器(15)出水进入高压泵(16)，高压泵(16)出水进入反渗透(17)，反渗透采用抗污染反渗透膜元件，一级二段排列，反渗透膜通量不大于20L/m2 *h，回收率不大于70%。
10.如权利要求9所述的方法，其特征在于，该方法进一步包括如下步骤:h.滤后水池(5)出水经滤池反洗水泵(8)从底部分别进入固定化微生物曝气生物滤池(4)和V型滤池(5)的反洗进水口，同时气洗风机(7)分别通过固定化微生物曝气生物滤池(4)和V型滤池(5)的反洗进气口进行充气，完成反冲洗步骤，固定化微生物曝气生物滤池(4)的反冲洗周期为3~10天，V型滤池(5)的反冲洗周期为12~24h。
11.如权利要求9所述的方法，其特征在于，该方法进一步包括如下步骤:1.运行初期，对所述固定化微生物曝气生物滤池(4)的工程菌进行驯化，驯化步骤包括:培养初期固定化微生物曝气生物滤池的C0D&浓度在500~600mg/L，DO浓度控制在3~5mg/L，闷曝3~5天。随后，以达标污水进入固定化微生物曝气生物滤池，控制DO浓度在2~4mg/L，直至出水的有机物去除率达到30~40%，驯化步骤完成。
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|---|---|---|---|---|
| CN103979689A (zh) * | 2014-05-29 | 2014-08-13 | 南京信息工程大学 | 一种利用微生物降解有机废水的装置及处理方法 |
| CN104150636A (zh) * | 2014-07-25 | 2014-11-19 | 张列宇 | 一种降低浊度强化膜分离污水纯化的装置和方法 |
| CN104529020A (zh) * | 2014-12-31 | 2015-04-22 | 浙江东洋环境工程有限公司 | 一种汽车饰件电镀废水处理系统 |
| CN105060650A (zh) * | 2015-08-25 | 2015-11-18 | 格蓝特环保工程(北京)有限公司 | 污水资源化处理方法 |
| CN105366769A (zh) * | 2014-08-25 | 2016-03-02 | 成都安捷宜康环保科技有限公司 | 利用双膜法治理城市污水的方法 |
| CN106430742A (zh) * | 2016-12-15 | 2017-02-22 | 南京中船绿洲环保有限公司 | 一种石油压裂液废水预处理方法 |
| CN108136293A (zh) * | 2015-08-10 | 2018-06-08 | 水技术国际有限责任公司 | 用于在反渗透膜中减轻生物结垢的方法和设备 |
| WO2018115500A1 (fr) * | 2016-12-22 | 2018-06-28 | Suez International | Installation et procede pour le traitement de l'eau |
| CN111762965A (zh) * | 2020-06-30 | 2020-10-13 | 烟台南山学院 | 一种石油化工废水深度处理回收利用方法 |
| CN111847795A (zh) * | 2020-07-31 | 2020-10-30 | 新疆中泰创新技术研究院有限责任公司 | Pta中水的回用处理系统及方法 |
| CN112744982A (zh) * | 2020-12-25 | 2021-05-04 | 西华师范大学 | 一种基于反渗透技术的水处理系统及其处理方法 |
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Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103979689A (zh) * | 2014-05-29 | 2014-08-13 | 南京信息工程大学 | 一种利用微生物降解有机废水的装置及处理方法 |
| CN103979689B (zh) * | 2014-05-29 | 2016-02-24 | 南京信息工程大学 | 一种利用微生物降解有机废水的装置及处理方法 |
| CN104150636B (zh) * | 2014-07-25 | 2016-01-20 | 张列宇 | 一种降低浊度强化膜分离污水纯化的装置和方法 |
| CN104150636A (zh) * | 2014-07-25 | 2014-11-19 | 张列宇 | 一种降低浊度强化膜分离污水纯化的装置和方法 |
| CN105366769A (zh) * | 2014-08-25 | 2016-03-02 | 成都安捷宜康环保科技有限公司 | 利用双膜法治理城市污水的方法 |
| CN104529020A (zh) * | 2014-12-31 | 2015-04-22 | 浙江东洋环境工程有限公司 | 一种汽车饰件电镀废水处理系统 |
| CN108136293A (zh) * | 2015-08-10 | 2018-06-08 | 水技术国际有限责任公司 | 用于在反渗透膜中减轻生物结垢的方法和设备 |
| CN105060650A (zh) * | 2015-08-25 | 2015-11-18 | 格蓝特环保工程(北京)有限公司 | 污水资源化处理方法 |
| CN106430742A (zh) * | 2016-12-15 | 2017-02-22 | 南京中船绿洲环保有限公司 | 一种石油压裂液废水预处理方法 |
| WO2018115500A1 (fr) * | 2016-12-22 | 2018-06-28 | Suez International | Installation et procede pour le traitement de l'eau |
| FR3061169A1 (fr) * | 2016-12-22 | 2018-06-29 | Suez International | Installation et procede pour le traitement de l'eau |
| CN111762965A (zh) * | 2020-06-30 | 2020-10-13 | 烟台南山学院 | 一种石油化工废水深度处理回收利用方法 |
| CN111847795A (zh) * | 2020-07-31 | 2020-10-30 | 新疆中泰创新技术研究院有限责任公司 | Pta中水的回用处理系统及方法 |
| CN112744982A (zh) * | 2020-12-25 | 2021-05-04 | 西华师范大学 | 一种基于反渗透技术的水处理系统及其处理方法 |
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