CN104986899B - 高浓度氨氮废水氨吹脱及资源化处理系统及处理方法 - Google Patents
高浓度氨氮废水氨吹脱及资源化处理系统及处理方法 Download PDFInfo
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- CN104986899B CN104986899B CN201510452491.8A CN201510452491A CN104986899B CN 104986899 B CN104986899 B CN 104986899B CN 201510452491 A CN201510452491 A CN 201510452491A CN 104986899 B CN104986899 B CN 104986899B
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N ammonia Chemical compound data:image/svg+xml;base64,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 data:image/svg+xml;base64,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 N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 144
- 239000002351 wastewater Substances 0.000 title claims abstract description 64
- 238000005273 aeration Methods 0.000 title claims abstract description 55
- 238000004064 recycling Methods 0.000 title claims abstract description 50
- 238000003672 processing method Methods 0.000 title claims abstract description 7
- 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 56
- 238000011084 recovery Methods 0.000 claims abstract description 37
- 239000002918 waste heat Substances 0.000 claims abstract description 32
- 239000002912 waste gas Substances 0.000 claims abstract description 13
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound 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- VHUUQVKOLVNVRT-UHFFFAOYSA-N ammonium hydroxide Chemical compound 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[NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 3
- 229910052757 nitrogen Inorganic materials 0.000 claims description 3
- 238000003756 stirring Methods 0.000 claims description 3
- 238000004781 supercooling Methods 0.000 claims description 3
- 239000002253 acid Substances 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 claims description 2
- CVTZKFWZDBJAHE-UHFFFAOYSA-N [N].N Chemical compound 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[N].N CVTZKFWZDBJAHE-UHFFFAOYSA-N 0.000 description 6
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 3
- BFNBIHQBYMNNAN-UHFFFAOYSA-N Ammonium sulfate Chemical compound 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N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 description 2
- 229910052921 ammonium sulfate Inorganic materials 0.000 description 2
- 235000011130 ammonium sulphate Nutrition 0.000 description 2
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
本发明公开了一种高浓度氨氮废水氨吹脱及资源化处理系统，包括依次连接的预处理单元、氨吹脱单元和后处理单元，所述的氨吹脱单元上设有进水口、出水口和废气出口，所述的废气出口与一资源化单元相连，所述的后处理单元包括依次连接的第二中间水池、pH回调池、出水池，所述的出水池上连接有余热回收单元，所述的第二中间水池的入口与所述出水口相连。本发明的目的是提供一种通过高温吹脱高浓度氨氮废水并对吹脱氨气进行回收利用的高浓度氨氮废水氨吹脱及资源化处理系统，以及一种高浓度氨氮废水氨吹脱及资源化处理方法。
Description
高浓度氨氮废水氨吹脱及资源化处理系统及处理方法
技术领域
[0001] 本发明涉及高浓度氨氮废水处理技术领域，特别是一种高浓度氨氮废水氨吹脱及 资源化处理系统以及一种高浓度氨氮废水氨吹脱及资源化处理方法。
背景技术
[0002] 由于高浓度氨氮废水(如垃圾渗滤液、化工废水等)对环境危害大，并难于处理，为 满足公众对环境质量不断提高的要求，国家对氨氮制订了越来越严格的排放标准，开发经 济、高效的脱氮技术已成为水污染工程领域的重点和热点。
[0003] 近几年来，国内外对氨氮废水处理方面开展了较多的研究。虽然许多方法都能有 效去除氨氮，但真正用于高浓度有机废水处理的只有少数几种。在高浓度氨氮废水行业，特 别是垃圾渗滤液处理行业，氨氮高达3〇〇〇mg/L以上，目前可用的预处理方法有氨吹脱、汽提 以及化学法(MAP)等。化学法(MAP)由于费用太高，在高浓度氨氮废水行业很少采用;汽提方 法由于需要蒸汽，在没有蒸汽来源的地方，需要建设锅炉，建设程序和费用高，运行成本也 高，因此受限较多。传统的氨吹脱方法，采用空气将氨转移到气相后，存在二次污染的问题； 而且吹脱后的气量大，往往采用硫酸吸收;即便是采用硫酸吸收生成硫酸铵，也存在着硫酸 铵处理处置难的问题，使用条件有一定的局限性。
[0004] 在此情况下，本发明采用改进型的氨吹脱系统，采用高温吹脱，极大的减少了吹脱 气体的产量;且增加吹脱气体的吸收系统，将气相的氨进行回收，最终生成销量广泛、且有 经济效益的氨水。从而解决了传统氨吹脱系统存在的种种弊端，避免了二次污染，降低了运 行成本，扩大了应用范围。
[0005] 此外，本发明充分利用废热、余热等低成本热源对高浓度有机废水进行升温，并采 用多种热量回收系统对系统的热量进行回收利用，使整个系统的运行成本进一步降低，从 而使本技术的推广性和应用型更加广泛。
发明内容
[0006] 本发明的目的是提供一种通过高温吹脱高浓度氨氮废水并对吹脱氨气进行回收 利用的高浓度氨氮废水氨吹脱及资源化处理系统，以及一种高浓度氨氮废水氨吹脱及资源 化处理方法。
[0007] 本发明提供的技术方案为：一种高浓度氨氮废水氨吹脱及资源化处理系统，包括 依次连接的预处理单元、氨吹脱单元和后处理单元，所述的预处理单元用于调节废水pH值 并沉淀废水中杂质，所述的氨吹脱单元上设有进水口、出水口和废气出口，所述的废气出口 与一资源化单元相连，所述的后处理单元包括依次连接的第二中间水池、pH回调池、出水 池，所述的出水池上连接有余热回收单元，所述的第二中间水池的入口与所述出水口相连， 所述的进水口与预处理单元的出口连接;所述的资源化单元包括氨气回收装置，所述的氨 气回收装置上设有用于冷却氨气回收装置内的液体的冷却装置，该冷却装置用于冷却氨气 回收装置内的液体，所述的氨气回收装置上设有排液口、进气口和排气口，所述的进气口与 所述废气出口相连，所述的排气口与大气相连。
[0008] 在上述的高浓度氨氮废水氨吹脱及资源化处理系统中，所述的预处理单元包括依 次连接的进水池、pH调整池、混凝池、沉淀池、第一中间水池，所述的第一中间水池的出口与 所述氨吹脱单元的进水口相连。
[0009] 在上述的高浓度氨氮废水氨吹脱及资源化处理系统中，所述的氨吹脱单元包括氨 吹脱塔，所述的进水口、出水口和废气出口设置在氨吹脱塔上，所述的氨吹脱塔上设有加热 装置，所述的加热装置与所述余热回收单元相连，所述的氨吹脱塔内设有曝气系统，所述的 曝气系统与鼓风机连接，所述的氨吹脱塔上设有pH计、超声波液位计、温控计、压力表，所述 的氨吹脱塔和资源化单元之间设有水雾分离器。
[0010] 在上述的高浓度氨氮废水氨吹脱及资源化处理系统中，所述的余热回收单元包括 与出水池连接的第一余热回收装置和用于回收厂区内生产余热的第二余热回收装置，所述 的第一余热回收装置和第二余热回收装置分别连接至所述的加热装置。
[0011] 在上述的高浓度氨氮废水氨吹脱及资源化处理系统中，所述的pH调整池、混凝池、 pH回调池内均设有搅拌装置，所述的pH调整池上设有加碱装置，所述的pH回调池上设有加 酸装置，所述的混凝池上设有混凝剂加药装置。
[0012] 在上述的高浓度氨氮废水氨吹脱及资源化处理系统中，所述的氨气回收装置包括 依次连接的氨吸收塔、硫酸吸收塔，所述的进气口设置在氨吸收塔上，所述的排液口设置在 氨吸收塔上，所述的排气口设置在硫酸吸收塔上。
[0013] 在上述的高浓度氨氮废水氨吹脱及资源化处理系统中，所述的氨吸收塔上连接有 水循环泵，所述的硫酸吸收塔上设有硫酸循环泵。
[0014] 在上述的高浓度氨氮废水氨吹脱及资源化处理系统中，所述的氨吹脱塔内设有防 干烧装置。
[0015] 本发明还公开了一种采用上述的处理系统的高浓度氨氮废水氨吹脱及资源化处 理方法，包括如下步骤：
[0016] 步骤1:通过预处理单元调节废水pH值并沉淀废水中杂质；
[0017] 步骤2:将经步骤1处理后的废水加入到氨吹脱单元中，分离其中的氨气;其中，氨 气进入氨气回收装置回收；
[0018] 步骤3:将经步骤2处理后的废水加入到后处理单元中调节pH值，并回收废水中的 热量，回收的热量返回到步骤2中，作为氨吹脱单元的部分热源。
[0019] 在上述的高浓度氨氮废水氨吹脱及资源化处理方法中，
[0020] 所述的步骤1包括：
[0021] S1:所处理的高浓度氨氮废水进入进水池，搅拌混匀进行均化水质；
[0022] S2:进水池出水经提升进入pH调整池内，投加碱调节，进行搅拌，使废水pH达到10-11;
[0023] S3: pH调整池出水进入混凝池，投加混凝剂进行加药搅拌；
[0024] S4:混凝池出水进入沉淀池进行混凝沉淀；
[0025] S5:沉淀池出水自流进入第一中间水池，进行中间提升；
[0026] 所述的步骤2包括：
[0027] S6:第一中间水池的出水提升至氨吹脱塔，通过与余热回收单元连接的加热装置 将废水加热升温至40〜90°C;并投加脱氮剂吹脱氨气至资源化单元；
[0028] S7:废水中的氨氮在达到排放标准要求的设计值后，停止加热和吹脱;氨吹脱塔出 水快速排水并自流进入第二中间水池进行中间提升；
[0029] S10:氨吹脱塔吹脱尾气经过冷却装置进行冷却降温，冷却后的氨吹脱塔吹脱尾气 进入氨气回收装置，回收制成质量浓度为5%以上的稀氨水，尾气达标排放
[0030] 所述的步骤3包括：
[0031] S8:第二中间水池出水提升至pH回调池，通过投加硫酸进行pH回调，pH回调到6-9;
[0032] S9:pH回调池出水自流进入出水池，在余热回收单元的作用下进行热交换回收热 量，出水池的水经过换热后出水排放。
[0033] 本发明在采用上述技术方案后，其具有的有益效果为：
[0034] 由上述提供的技术方案可以看出，本发明实施方式的处理系统，通过进水池、pH调 整池、混凝池、沉淀池、中间水池1、加药系统、氨吹脱系统、中间水池2、pH回调池、出水池、氨 气回收装置、加热系统、余热回收系统、冷却系统有机组合对高浓度氨氮废水进行处理，有 效去除水中的氨氮，使出水低于预定限值;并通过资源化系统实现了吹脱氨气的回收利用， 该方法工艺流程简单、处理效果稳定、运行费用较低、回收率高。
附图说明
[0035]图1是本发明实施例1和2的流程方框图；
[0036]图2是本发明实施例1和2的氨吹脱单元的结构示意图；
[0037]图3是本发明实施例1和2的资源化单元的结构示意图。
具体实施方式
[0038] 下面结合具体实施方式，对本发明的技术方案作进一步的详细说明，但不构成对 本发明的任何限制。
[0039] 实施例1:
[0040]如图1、图2和图3所示，一种高浓度氨氮废水氨吹脱及资源化处理系统，包括依次 连接的预处理单元1、氨吹脱单元2和后处理单元3,所述的预处理单元1用于调节废水pH值 并沉淀废水中杂质，所述的氨吹脱单元2上设有进水口、出水口和废气出口，所述的废气出 口与一资源化单元4相连，所述的后处理单元3包括依次连接的第二中间水池31、pH回调池 32、出水池33，所述的出水池33上连接有余热回收单元5，所述的第二中间水池31与出水口 相连，所述的进水口与预处理单元1的出口连接;所述的资源化单元4包括氨气回收装置41， 所述的氨气回收装置41上设有用于冷却氨气回收装置41内的液体的冷却装置46,该冷却装 置46用于冷却氨气回收装置41内的液体，所述的氨气回收装置41上设有排液口、进气口和 排气口，所述的进气口与废气出口相连，所述的排气口与大气相连，所述的预处理单元1包 括依次连接的进水池ll、pH调整池12、混凝池13、沉淀池14、第一中间水池15,所述的第一中 间水池15的出口与所述氨吹脱单元2的进水口相连，所述的氨吹脱单元2包括鼓风机21、氨 吹脱塔22、曝气系统23、pH计24、超声波液位计25、温控计26、压力表27、水雾分离器28、加热 装置29,具体来说，所述的氨吹脱塔22上设有加热装置29,所述的加热装置29与余热回收单 元5相连，必要地，本加热装置29还与外界的供热系统30相连，用以在余热回收单元5供热不 足的时候，通过外界的供热系统30相连，所述的氨吹脱塔22内设有曝气系统23,所述的曝气 系统23与鼓风机21连接，所述的氨吹脱塔22上设有pH计24、超声波液位计25、温控计26、压 力表27,所述的氨吹脱塔22和资源化单元4之间设有水雾分离器28。所述的余热回收单元5 包括与出水池33连接的第一余热回收装置和用于回收厂区内生产余热的第二余热回收装 置。所述的pH调整池12、混凝池13、pH回调池32内均设有搅拌装置，所述的pH调整池12上设 有加碱装置，所述的pH回调池32上设有加酸装置，所述的混凝池13上设有混凝剂加药装置， 所述的氨气回收装置41包括依次连接的氨吸收塔42、硫酸吸收塔43,所述的进气口设置在 氨吸收塔42上，所述的排液口设置在氨吸收塔42上，所述的排气口设置在硫酸吸收塔43上， 所述的氨吸收塔上连接有水循环栗44,所述的硫酸吸收塔43上设有硫酸循环泵45。具体到 本实施例中，氨吸收塔42的数量为3个，为串联，硫酸吸收塔43的数量为两个，为串联。经过 硫酸吸收塔43吸收后的溶液进入硫酸铵储罐46。
[0041] 在本实施例中，所述的氨吹脱塔22内设有防干烧装置。
[0042] 本实施例的处理系统能够通过氨吸收塔有效的吸收氨吹脱塔吹脱的氨气，提高废 气回收效率，通过余热回收装置回收余热能够有效的能量能力回收效率。
[0043] 实施例2:
[0044] 如图1-3所示，本实施例的方法采用实施例1的系统，具体来说：
[0045] 步骤1:通过预处理单元调节废水pH值并沉淀废水中杂质；
[0046] 所述的步骤1包括：
[0047] S1:所处理的高浓度氨氮废水进入进水池11，搅拌混匀进行均化水质；
[0048] S2:进水池出水经提升进入pH调整池12内，投加碱调节，进行搅拌，使废水pH达到 10-11；
[0049] S3: pH调整池出水进入混凝池13，投加混凝剂进行加药搅拌；
[0050] S4:混凝池13出水进入沉淀池14进行混凝沉淀；
[0051] S5:沉淀池出水自流进入第一中间水池15，进行中间提升；
[0052] 步骤2:将经步骤1处理后的废水加入到氨吹脱单元2中，分离其中的氨气;其中，氨 气进入氨气回收装置41回收；
[0053] 所述的步骤2具体包括：
[0054] S6:第一中间水池的出水提升至氨吹脱塔22，通过与余热回收单元5连接的加热装 置29将废水加热升温至40〜90°C ;并投加脱氮剂吹脱氨气至资源化单元4;
[0055] S7:废水中的氨氮在达到排放标准要求的设计值后，停止加热和吹脱;氨吹脱塔22 出水快速排水并自流进入第二中间水池31进行中间提升；
[0056] S10:氨吹脱塔22吹脱尾气经过冷却装置46进行冷却降温，冷却后的氨吹脱塔22吹 脱尾气进入氨气回收装置41，回收制成质量浓度为5%以上的稀氨水，尾气达标排放；
[0057] 步骤3:将经步骤2处理后的废水加入到后处理单元3中调节pH值，并回收废水中的 热量，回收的热量返回到步骤2中，作为氨吹脱单元的部分热源。
[0058] 所述的步骤3包括：
[0059] S8:第二中间水池31出水提升至pH回调池32，通过投加硫酸进行pH回调，pH回调到 6-9；
[0060] S9: pH回调池32出水自流进入出水池33，在余热回收单元5的作用下进行热交换回 收热量，出水池3 3的水经过换热后出水排放。
[0061]采用本实施例的方法有效去除水中的氨氮，使出水低于预定限值;并通过资源化 系统实现了吹脱氨气的回收利用，该方法工艺流程简单、处理效果稳定、运行费用较低、回 收率高。
[0062]上述实施例为本发明较佳的实施方式，但本发明的实施方式并不受上述实施例的 限制，其^的任何未背离本发明的精神实质与原理下所作的改变、修饰、替代、组合、简化， 均应为等補置换方式，都包含在本发_保护范围之内。
Claims (9)
1. 一种高浓度氨氮废水氨吹脱及资源化处理系统，包括依次连接的预处理单元（1)、氨 吹脱单元(2)和后处理单元(3)，其特征在于:所述的氨吹脱单元(2)上设有进水口、出水口 和废气出口，所述的废气出口与一资源化单元(4)相连，所述的后处理单元(3)包括依次连 接的第二中间水池(31)、pH回调池(32)、出水池(33)，所述的出水池(33)上连接有余热回收 单元(5)，所述的第二中间水池(31)的入口与所述出水口相连，所述的进水口与预处理单元 (1)的出口连接;所述的资源化单元(4)包括氨气回收装置(41)，所述的氨气回收装置(41) 上设有冷却装置(46)，所述的氨气回收装置(41)上设有排液口、进气口和排气口，所述的进 气口与所述废气出口相连，所述的排气口与大气相连;所述的氨吹脱单元⑵包括氨吹脱塔 (22)，所述的进水口、出水口和废气出口设置在氨吹脱塔(22)上，所述的氨吹脱塔(22)上设 有加热装置(29)，所述的加热装置(29)与所述余热回收单元(5)相连，所述的氨吹脱塔(22) 内设有曝气系统(23)，所述的曝气系统(23)与一鼓风机(21)连接，所述的氨吹脱塔(22) i： 设有pH计(24)、超声波液位计(25)、温控计(26)、压力表(27)，所述的氨吹脱塔(22)和资源 化单元⑷之间设有水雾分离器(28)。
2. 根据权利要求1所述的高浓度氨氮废水氨吹脱及资源化处理系统，其特征在于:所述 的预处理单元⑴包括依次连接的进水池（11)、pH调整池（12)、混凝池（13)、沉淀池（14)、第 一中间水池(15)，所述的第一中间水池(15)的出口与所述氨吹脱单元(2)的进水口相连。
3. 根据权利要求1所述的高浓度氨氮废水氨吹脱及资源化处理系统，其特征在于:所述 的余热回收单元⑸包括与出水池(33)连接的第一余热回收装置和用于回收厂区内生产余 热的第二余热回收装置，所述的第一余热回收装置和第二余热回收装置分别连接至所述的 加热装置(29)。
4. 根据权利要求2所述的高浓度氨氮废水氨吹脱及资源化处理系统，其特征在于:所述 的pH调整池（12)、混凝池（13)、pH回调池(32)内均设有搅拌装置，所述的pH调整池（12)上设 有加碱装置，所述的pH回调池(32)上设有加酸装置，所述的混凝池（13)上设有混凝剂加药 装置。
5. 根据权利要求1至4中任意一项所述的高浓度氨氮废水氨吹脱及资源化处理系统，其 特征在于:所述的氨气回收装置(41)包括依次连接的氨吸收塔(42)、硫酸吸收塔(43)，所述 的进气口设置在氨吸收塔(42)上，所述的排液口设置在氨吸收塔(42)上，所述的排气口设 置在硫酸吸收塔(43)上。
6.根据权利要求5所述的高浓度氨氮废水氨吹脱及资源化处理系统，其特征在于:所述 的氨吸收塔(42)上连接有水循环泵(44)，所述的硫酸吸收塔(43)上设有硫酸循环泵(45)。
7. 根据权利要求1所述的高浓度氨氮废水氨吹脱及资源化处理系统，其特征在于:所述 的氨吹脱塔(22)内设有防干烧装置。
8. —种应用于如权利要求1所述的处理系统的高浓度氨氮废水氨吹脱及资源化处理方 法，其特征在于:包括如下步骤： 步骤1:通过预处理单元⑴调节废水pH值并沉淀废水中杂质； 步骤2:将经步骤1处理后的废水加入到氨吹脱单元(2)中，分离其中的氨气;其中，氨气 进入氨气回收装置(41)回收； 步骤3:将经步骤2处理后的废水加入到后处理单元(3)中调节pH值，并回收废水中的热 量，回收的热量返回到步骤2中，作为氨吹脱单元⑵的部分热源。
9.根据权利要求8所述的高浓度氨氮废水氨吹脱及资源化处理方法，其特征在于:所述 的步骤1包括： S1:所处理的高浓度氨氮废水进入进水池（11)，搅拌混匀进行均化水质； S2:进水池（11)出水经提升进入pH调整池（12)内，投加碱调节，进行搅拌，使废水pH达 到10-11; S3:pH调整池（12)出水进入混凝池（13)，投加混凝剂进行加药搅拌； S4:混凝池（13)出水进入沉淀池（14)进行混凝沉淀； S5:沉淀池（14)出水自流进入第一中间水池（15)，进行中间提升； 所述的步骤2包括： S6:第一中间水池（15)的出水提升至氨吹脱塔(22)，通过与余热回收单元⑸连接的加 热装置(29)将废水加热升温至40〜9(TC ;并投加脱氮剂吹脱氨气至资源化单元⑷； S7:废水中的氨氮在达到排放标准要求的设计值后，停止加热和吹脱;氨吹脱塔(22)出 水快速排水并自流进入第二中间水池(31)进行中间提升； S10:氨吹脱塔(22)吹脱尾气经过冷却装置(46)进行冷却降温，冷却后的氨吹脱塔(22) 吹脱尾气进入氨气回收装置(41)，回收制成质量浓度为5%以上的稀氨水，尾气达标排放； 所述的步骤3包括： S8:第二中间水池(31)出水提升至pH回调池(32)，通过投加硫酸进行PH回调，PH回调到 6-9; S9:pH回调池(32)出水自流进入出水池(33)，在余热回收单元(5)的作用下进行热交换 回收热量，出水池(33)的水经过换热后出水排放。
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