造纸废水处理（sbr)毕业设计论文 49页

摘要本设计的内容为某造纸厂废水处理工艺设计。造纸厂废水的特点是：所产生的废水悬浮物浓度较高，且有机物浓度也较高。设计中的主要构筑物有格栅、沉砂池、SBR池、絮凝反应器、以及污泥浓缩池。SBR工艺是本次设计的核心。SBR工艺是活性污泥法的变形，由于其具有自动化程度高，抗冲击能力强、池形简单、具有脱氮降磷效果、不产生污泥膨胀等特点，因此SBR处理工艺在小型污水处理设施中应用较广泛。经过该工艺处理后的出水水质达到造纸废水排放标准GB3544－2001一级排放标准。本设计需要选择几种造纸厂废水处理的工艺，并对其进行比较，确定造纸厂废水处理工艺并确定废水处理工艺流程图；并对各种构筑物进行了详细的设计计算，同时也对废水处理工艺进行了工程预算。设计采用AutoCAD软件绘制工艺流程中各构筑物的详图、平面布置图、高程图。关键词:造纸工业废水；SBR；污泥浓缩44nAbstractThecontentofpapermillwastewatertreatmentprocesswasdesigned.Papermillwastewaterhasthefollowingcharacteristics:wastewatergeneratedbythehighconcentrationofsuspendedsolid,andhigherconcentrationsoforganicmatter.SBRprocessisthecoreofthisdesign.SBRisactivatedsludgeprocessofdeformation,owingtoitshighdegreeofautomation,impactresistanceandstrong,simple-shapedpool,withnitrogenandphosphorusdowneffect,noexpansionofsludge,andothercharacteristics,SBRprocessinthesmallsewagetreatmentFacilitiesinthewiderapplication.AfterthetreatmentofeffluentqualityofthepaperindustrytoachievenationalwaterpollutantdischargestandardsGB3544－2001levelemissionstandards.Theneedtoselectthedesignofseveralofthepapermillwastewatertreatmentprocess,anditscomparisontodeterminepapermillwastewatertreatmentprocessandtoidentifywaste-watertreatmentprocessmapsofvariousstructuresandcarriedoutadetaileddesign,butalsoonWastewatertreatmenttechnologyoftheprojectbudget.AutoCADsoftwaredesignusesmappingprocesslayoutplans,elevationmaps,alldealingwithstructures’drawing.Keywords:papermillwastewater;SBR;sludgethickening44n目录第一章绪论------------------------------------------------------11.1前言----------------------------------------------------------11.2造纸厂废水的特点、水量及水质-----------------------------------11.2.1造纸厂废水的特点------------------------------------------11.2.2造纸厂废水水量--------------------------------------------11.2.3造纸厂废水水质--------------------------------------------21.3排放标准------------------------------------------------------21.3.1废水水质排放标准------------------------------------------21.3.2收纳水体--------------------------------------------------21.4设计任务及依据------------------------------------------------21.4.1设计任务--------------------------------------------------21.4.2计依据----------------------------------------------------21.5废水处理工程运行过程中应遵循的原则----------------------------3第二章SBR生化处理工艺的简介--------------------------42.1SBR工艺概况---------------------------------------------------42.1.1SBR简介---------------------------------------------------42.1.2SBR工艺原理-----------------------------------------------42.1.3SBR工艺流程-----------------------------------------------52.1.4SBR的适用范围---------------------------------------------52.2与其他工艺比较分析--------------------------------------------62.3SBR工艺的优缺点-----------------------------------------------62.3.1SBR工艺的特点---------------------------------------------62.3.2SBR工艺的优点---------------------------------------------72.3.3SBR工艺的缺点---------------------------------------------72.4造纸厂废水处理工艺--------------------------------------------72.4.1造纸厂废水处理工艺流程------------------------------------72.4.2废水处理工艺流程图----------------------------------------82.4.3造纸厂废水工艺流程描述------------------------------------8第三章废水处理构筑物的设计---------------------------93.1原始设计参数--------------------------------------------------93.2格栅----------------------------------------------------------93.2.1设计说明--------------------------------------------------93.2.2设计参数-------------------------------------------------103.2.3设计计算-------------------------------------------------103.3污水提升泵房-------------------------------------------------1244n3.4泵后细格栅---------------------------------------------------123.5曝气沉砂池---------------------------------------------------133.5.1设计说明-------------------------------------------------133.5.2设计参数-------------------------------------------------143.5.3设计计算-------------------------------------------------143.6鼓风机房-----------------------------------------------------153.7SBR反应池----------------------------------------------------163.7.1设计说明-------------------------------------------------163.7.2SBR反应池容积计算---------------------------------------183.7.3SBR反应池运行时间与水位控制-----------------------------203.7.4排水管管径-----------------------------------------------203.7.5排泥量及排泥系统-----------------------------------------203.7.6需氧量及曝气系统设计计算---------------------------------213.7.7空气管计算-----------------------------------------------233.7.8滗水器---------------------------------------------------243.8絮凝反应池---------------------------------------------------243.8.1设计说明-------------------------------------------------243.8.2设计参数-------------------------------------------------253.8.3设计计算-------------------------------------------------253.9滤池---------------------------------------------------------273.9.1设计说明-------------------------------------------------273.9.2设计参数-------------------------------------------------283.9.3设计计算-------------------------------------------------283.10接触消毒池--------------------------------------------------293.10.1设计说明------------------------------------------------293.10.2设计参数------------------------------------------------303.10.3设计计算------------------------------------------------303.11污泥处理系统------------------------------------------------303.11.1污泥水分去除的意义和方法--------------------------------303.11.2各部分尺寸计算------------------------------------------313.11.3堆肥----------------------------------------------------34第四章投资估算--------------------------------------354.1土建部分投资估算---------------------------------------------354.2设备部分投资估算---------------------------------------------354.3其他费用-----------------------------------------------------364.4项目总投资---------------------------------------------------36第五章环境保护--------------------------------------385.1施工过程中对环境影响及对策-----------------------------------385.1.1对交通的影响及缓解措施-----------------------------------3844n5.1.2扬尘的影响-----------------------------------------------385.1.3噪声的影响-----------------------------------------------385.1.4生活垃圾的影响-------------------------------------------395.1.5弃土的影响及对策-----------------------------------------395.1.6对地下水的影响-------------------------------------------395.2项目建成后的环境影响及对策-----------------------------------395.2.1臭味对环境的影响及缓解措施-------------------------------39结语-------------------------------------------------40致谢-------------------------------------------------41参考文献---------------------------------------------4244n第一章绪论１.１造纸废水的概况水是生命的源泉，它与人类的生产和生活息息相关。然而占地球水量四分之三的海水，我们是不能大规模使用的，只能使用占地球水量不到四分之一的淡水资源。但是，水环境中的淡水资源很少，仅占总量的2.53%，而目前能供人类直接取用的淡水资源仅占0.22%。我国是一个极大的“贫水国”，人均拥有水量不到世界人均的1／4。而造纸工业要用大量的水进行输送、洗涤、分散纤维和冷却等。因此，它对环境影响最大的是水质污染，其次才是大气污染，臭氧和废料。它不仅是我国造纸工业污染防治的首要问题，而且是全国工业废水进行达标处理的首要问题。废水中含有大量有机物，排放后在微生物的作用下发生氧化分解，在此过程中，大量消耗水中的溶解氧，当耗氧速度大于从水表面溶解空气中氧的速度时，就会造成水中缺氧，此时厌氧微生物却在缺氧状态下大量繁殖，使水变质。若用这种废水灌溉农田，会引起植物根部腐烂，影响农作物生长。同时废水中含有无机盐和有害物质，以及来自木质素的色素，天长日久的积累会使土地变成盐碱化，土壤结构受到破坏，农业减产。SBR工艺是把进水、曝气、沉淀三个过程在一个池子中完成。一般由多个池子构成一组，各池工作状态轮流变换运行，单池由滗水器间歇出水，故又称为序批式活性污泥法。SBR工艺将传统的曝气池、沉淀池由空间上的分布改为时间上的分布，形成一体化的集约构筑物，并利于实现紧凑的模块布置，最大的优点是节省占地。另外，可以减少污泥回流量，有节能效果。典型的SBR工艺沉淀时停止进水，静止沉淀可以获得较高的沉淀效率和较好的水质。本次设计选择SBR工艺作为造纸厂废水的处理工艺方案。44n１.2造纸厂废水的特点、水量及水质1.2.1造纸厂废水的特点造纸厂所产生的废水特点：悬浮物浓度较高，且有机物浓度较高。1.2.2造纸厂废水水量本次设计的废水量为100000m3/d，每天运行24小时，则每小时处理水量为4166.67m3/h。1.2.3废水水质主要水质指标见下表表1-1进水水质Table1-1influentwastewaterquality项目进水水质(mg/L)BOD5CODcrSS40012006001.3排放标准1.3.1废水水质排放标准针对该造纸厂废水进行废水处理工程设计，要求主体工艺采用SBR工艺，处理后的出水水质按照国家造纸工业水污染物排放标准GB3544－2001一级排放标准。表1-2GB3544－2001一级排放标准Table1-2GB3544－2001astandard项目出水水质(mg/L)BOD5CODcrSS10030701.3.2受纳水体污水经过处理后排入市政废水管网1．4设计任务及依据1.4.1设计任务本设计方案的编制范围是造纸厂废水处理工艺，处理能力为10万m344n/d,内容包括处理工艺的确定、各构筑物的设计计算、设备选型、平面布置、高程计算、经济技术分析。完成总平面布置图、剖面图、一个主要构筑物的详图。1.4.2设计依据（1）根据环保部门的要求。（2）根据设计任务书批文和设计委托书。（3）依据给排水设计手册。（4）依据排放标准GB3544－2001一级标准。1.5废水处理工程运行过程中应遵循的原则应该在保证污水处理效果的同时，正确处理城市、工业、农业等各方面的用水关系，合理安排水资源的综合利用，节约用地，节约劳动力，考虑污水处理厂的发展前景，尽量采用处理效果好的先进工艺，同时合理设计、合理布局，做到技术可行、经济合理。44n第二章SBR生化处理工艺的简介2.1SBR工艺概况2.1.1SBR简介SBR（序批式活性污泥法）工艺早在1914年即已开发，但由于当时监测手段落后，并没有得到推广应用。1979年美国的L.Irvine对SBR工艺进行了深入的研究，并于1980年在印第安那州的Culver改进并投产了一个SBR污水处理厂。此后随着计算机监控技术、各种新型不堵塞曝气器和软件技术的出现，同时也由于开发了在线溶解氧测定仪、水位计等精度高并且对过程控制比较经济的水质检测仪表，污水处理厂的运行管理逐渐实现了自动化，加之SBR具有均化水质、工艺简单，处理效果稳定，耐冲击负荷力强，出水质好，操作灵活、占地面积少等优点而成为包括美、德、日、澳、加等在内的许多工业发达国家竞相研究和开发的热门工艺[1]。SBR工艺（seriesbatchreactor）全称为序批式间歇反应器。是近年来发展起来的新的活性污泥法工艺。该工艺由一个或多个SBR池组成，通过程序化控制进水、反应、沉淀、排水和闲置五个阶段，来完成对废水的生化处理。在SBR中发生的生化反应过程是典型的非稳态过程，底物和微生物浓度的变化在空间上呈完全混合状态，在时间上则呈理想推流状态。SBR工艺可充分利用兼性菌的作用，通过控制曝气量，可在同一反应器内程序地进行缺氧-厌氧-好氧过程，这是SBR工艺的重要特征。SBR工艺在处理高浓度有机废水方面具有优越性，该工艺流程短，装置结构简单，不易发生污泥膨胀，耐负荷冲击能力强，运行费用较低。2.1.2SBR工艺原理SBR法的设施是由曝气装置、上清液排出装置（滗水器），以及其他附属设备组成的反应器。SBR对有机物的去除机理为：在反应器内预先培养驯化一定量的活性微生物（活性污泥），当废水进入反应器与活性污泥混合接触并有氧存在时，微生物利用废水中的有机物进行新陈代谢，将有机污染物转化为CO2、H244nO等无机物，同时，微生物细胞增殖，最后将微生物细胞物质（活性污泥）与水沉淀分离，废水得到处理。该工艺将传统的曝气池、沉淀池由空间上的分布改为时间上的分布，形成一体化的集约构筑物，并利于实现紧凑的模块布置，最大的优点是节省占地。另外，可以减少污泥回流量，有节能效果。典型的SBR工艺沉淀时停止进水，静止沉淀可以获得较高的沉淀效率和较好的水质。2.1.3SBR工艺流程SBR法的一般流程图消毒剂↓污水→沉砂池→SBR→接触地→排水↓污泥浓缩→消化→脱水→污泥处理2.1.4SBR的适用范围SBR系统进一步拓宽了活性污泥的使用范围。就近期的技术条件，SBR系统更适合以下情况：（1）中小城镇生活污水和厂矿企业的工业废水，尤其是间歇排放和流量变化较大的地方。（2）需要较高出水水质的地方，如风景游览区、湖泊和港湾等，不但要去除有机物，还要求出水中除磷脱氮，防止河湖富营养化。（3）水资源紧缺的地方。SBR系统可在生物处理后进行物化处理，不需要增加设施，便于水的回收利用。（4）用地紧张的地方。（5）对已建连续流污水处理厂的改造等。（6）非常适合处理小水量，间歇排放的工业废水与分散点源污染的治理。近期来随着SBR工艺的发展，特别是连续进水、连续出水方案的改进，使SBR工艺以应用于大中心污水处理厂。44n2.2与其他工艺比较分析（1）传统活性污泥法传统活性污泥法，又称推流式活性污泥法，它是依据污水的自净作用发展而来的。污水在经过沉砂、初沉等工序进行一级处理后，进入推流式曝气池，在曝气和水力条件下，曝气池中的水均匀地流动，污水从入口流向出口，前端液流不与后端液流混合。在曝气池中，污水中的有机物绝大部分被微生物吸附、氧化分解，生成无机物，然后进入沉淀池。在这个过程中，随着环境的变化，生物反应速度是变化的，F/M值也是不断变化的，微生物群的量和质不断地变动，后行污泥的吸附、絮凝、稳定作用不断的变化，其沉降-浓缩性能与不断地变化[2]。（2）SBR工艺是活性污泥法的变形，由于其具有自动化程度高，抗冲击能力强、池形简单、具有脱氮降磷效果、不产生污泥膨胀等特点，因此在小型的工业污水处理中应用是较为合理的，因此SBR处理工艺在小型污水处理设施中应用较广泛。（3）接触氧化法是工业废水中采用较多的好氧处理工艺，原因是该工艺克服了传统活性污泥法的缺点，具有抗冲击能力强、负荷高、运行稳定，出水水质好等特点，且一次性投资及占地面积小，运行管理方便，在工程中得到较多的推广及应用。综合分析各种好氧处理工艺，采用SBR法治理此类废水是合理可行的。SBR池出水进入中间水池，经机械纤维过滤器后，出水后达标排放。2.3SBR工艺的优缺点2.3.1SBR工艺的特点（1）采用了SBR生化处理工艺，使得污水在此得到较高的处理。（2）本工艺曝气设备具有高效，氧利用率高，运行稳定，曝气均匀的特点。（3）本工艺流程有较大的灵活性、稳定性和可操作性。（4）本工艺流程没有二次污染，污泥进行干化处理后，干泥饼可直接外运填理，实现了清洁生产和文明生产的工艺。44n2.3.2SBR工艺的优点SBR工艺是一种简易、快速且低耗的废水生物处理工艺。SBR其本身特有的优点如下：（1）不设初沉池、二沉池、污泥回流系统。调节池投资省，占地面积小，维护管理方便。（2）曝气时间短，处理效率高。（3）出水水质好，在完全混合池中，采用专用的滗水器排水装置。（4）耐冲击负荷能力强：在曝气阶段是完全混合反应器；SBR法中可调节排水与进水的比例。（5）可脱氮除磷。（6）适应性强，运行灵活，运行费用低。2.3.3SBR法的缺点（1）连续进水时，对于单一SBR反应器需要较大的调节池。（2）对于多个SBR反应器，其进水和排水的阀门自动切换频繁。（3）无法达到大型污水处理项目的连续进水、出水的要求。（4）设备的闲置率较高。（5）污水提升水头损失较大。（6）如果需要后处理，则需要较大容积的调节池。2.4.造纸厂废水处理工艺2.4.1造纸厂废水处理工艺流程本设计方案由下列系统构成：预处理系统：格栅、污水提升泵房、泵后细格栅、沉砂池；废水处理部分：SBR池、鼓风机房、絮凝反应器、滤池、接触消毒池；污泥处理部分：集泥井、污泥浓缩池、污泥贮柜、污泥脱水机房、污泥棚；44n2.4.2废水处理工艺流程图(1)废水处理部分产生的废水→格栅→污水提升泵→泵后细格栅→沉砂池→SBR池→鼓风机房↓出水达标排放←接触消毒池←滤池←絮凝反应器(2)污泥处理部分污泥、沉渣→集泥井→污泥浓缩池→污泥贮柜→污泥脱水机房→泥饼外运2.4.3造纸厂废水工艺流程描述（1）废水处理部分产生的污水先进入格栅池，在格栅池中去除了大的悬浮杂物，然后进入污水提升泵后，进入泵后细格栅，处理的废水进入沉砂池，去除水中密度较大的无机颗粒。沉砂池出水进入SBR池，然后进入鼓风机房，接着进入化学絮凝沉降装置。主要是去除水中细小悬浮物、漂浮物以及胶体物质，悬浮物去除率可达90%。化学絮凝沉降装置出水后进入滤池，进行消毒。本工艺处理能力大，污泥生成量少，运行中不会产生污泥膨胀，能够保证出水水质的稳定，无需污泥回流，由于该工艺兼有活性污泥和生物膜法两者的优点，且一次性投资及占地面积小，运行管理方便，在工程中得到较多的推广及应用。（2）污泥处理部分化学絮凝沉降装置沉渣和SBR池排泥进入污泥浓缩池，浓缩后由泵提升到干化场自然干化，定期外运。44n第三章废水处理构筑物的设计3.1原始设计参数原水水量Q＝100000m³/d=4166.7m³d取流量总变化系数为KZ=设计流量Qmax=Kz·Q=1.241.157=1.43m³/s3.2格栅3.2.1设计说明格栅一般斜置在进水泵站之前，主要对水泵起保护作用，截去生活水中较大的悬浮物，它本身的水流阻力并不大，水头损失只有几厘米，阻力主要产生于筛余物堵塞栅条，一般当格栅的水头损失达到10~15厘米时就该清洗。格栅按形状可分为平面格栅和曲面格栅两种，按格栅栅条间隙可分为粗格栅（50~100mm），中格栅（10~40mm），细格栅（3~10mm）三种。根据清洗方法，格栅和筛网都可设计成人工清渣和机械清渣两类，当污染物量大时，一般应采用机械清渣，以减少人工劳动量。本设计栅渣量大于0.2m3/d,栅渣量与地区特点，格栅的间隙大小，污水流量以及下水道系统的类型等因素有关，在无当地资料时，可采用：(1)格栅间隙16~25mm，处理0.10-0.05栅渣/103m3污水(2)格栅间隙30~50mm，处理0.03-0.01栅渣/103m3污水栅渣的含水率一般为80%，容重约为960kg/m3。栅条的断面形状有圆形、锐边矩形、迎水面为半圆形的矩形、迎水面背水面均为半圆的矩形几种。而其中迎水面为半圆形的矩形的栅条具有强度高，阻力损失小的优点[3]。44n3.2.2设计参数（1）变化系数:平均日流量：=100000=4166.7=1.157()（2）最大日流量：=1.244166.7=5166.7()=1.43()（3-1）（3）设过栅流速：=0.8m/s(取0.6~1.0m/s)（4）通过格栅的水头损失(取0.08~0.25)（5）栅前水深：h=0.4(取0.3~0.5m)（6）格栅安装倾角：(取~)（7）机械清渣设备：采用链条式格栅除污机3.2.3设计计算(1)中格栅（2个）格栅间隙数n==46个Qmax——最大废水设计流量m3/s——格栅安装倾角~取h——栅前水深mb——栅条间隙宽度取30mm——过栅流速m/s验算平均水量流速=0.80m/s符合(0.65~1.0)（2）栅渠尺寸B2=s(n-1)+nb=0.02(46-1)+0.0346=2.28(m)=8cm圆整取B2=2.5cm44ns——栅条宽度取0.02mB2——格栅宽度mB1===1.5(m)(3-2)B1——进水渠宽m栅钱扩大段L1==1.37(m)(3-3)——渐宽部分的展开角，一般采用20º栅后收缩段（m）栅条总长度+0.5+(3-4)=1.37+0.5++1.0+0.67=3.94(m)h2——栅前渠道超高，采用0.3m（3）水通过格栅的水头损失设栅条断面为瑞边矩形断面k=3(3-5)==0.12(m)(4)栅渣量（总）W==(m³/d)44nW1取NC—400型机械格栅三台。3.3污水提升泵房根据污水流量，泵房设计为L×B=10×10m。提升泵选型：采用LXB型螺旋泵型号：LXB-1100螺旋外径D：1100mm转速：48r/min流量Q：875m3/h提升高度：5m功率：15Kw购买6台，5台工作，1台备用。3.4泵后细格栅（4个）公式计算同上（1）格栅间隙数n==138(个)(3-6)其中b取5mm取0.9m/sh取0.4m反带验算得=1.0m/s符合(0.6―1.0m/s)栅渠尺寸B2=s(n-1)+nb=0.01×(138-1)+0.005×138=2.06(m)圆整2.0m栅条宽度s取0.01m进水渠宽B1==0.80(m)栅前扩大段44nL1==1.04(m)取30º栅后收缩段L2=0.5L1=0.52栅条总长度L=L1+0.5++1.0+L2=1.04+0.5++1.0+0.52=3.52（m）(3)水通过格栅的水头损失设栅条断面为圆形断面=1.83(3-7)=0.50m（4）每日栅渣量W：W=在b=5mm情况下，设栅渣量为0.05m³/10³污水W==4.98＞0.2(m³/d)采用机械清渣选用NC—300型机械格栅三台。3.5曝气沉砂池3.5.1设计说明44n沉砂池有4种：平流式、竖流式、曝气式、钟式和多尔式。普通平流沉砂池的主要缺点是沉砂中含有15%的有机物，使沉砂的后续处理难度增加。采用曝气沉砂池可以克服这一缺点[4]。3.5.2设计参数（1）旋流速度应保持：0.25~0.3m/s。（2）水平流速为0.06~0.12m/s。（3）最大流量时停留时间为1~3min。（4）有效水深应为2~3m，宽深比一般采用1~2。（5）长宽比可达5，当池长比池宽大得多时，应考虑设置横向挡板。（6）1m3污水的曝气量为0.2m3空气。（7）空气扩散装置设在池的一侧，距池底约0.6~0.9m,送气管应设置调节气量的闸门。（8）池子的形状应尽可能不产生偏流或死角，在集砂槽附近可安装纵向挡板。（9）池子的进口和出口布置应防止发生短路，进水方向应与池中旋流方向一致，出水方向应与进水方向垂直，并宜考虑设置挡板。（10）池内应考虑设消泡装置[5]。3.5.3设计计算（1）池子总有效容积（V）设t=2min，则V=Qmax﹒t﹒60=1.43×2×60=171.6(m³)（2）水流断面积（A）设ν1=0.1m/s（水平流速），则A===14.3(m²)（3）池总宽度（B）设h2=2.5m（设计有效水深），则B==5.72(m)（4）每格池子宽度（b）设n=2格，则b==3.0(m)（5）池子（L）44nL==12(m)（6）每小时所需空气量（q）设d=0.2m³/m³（1m³污水所需空气量），则Q=d﹒Qmax﹒3600=0.2×1.43×3600=1029.6(m³/h)（7）沉砂室所需容积（V）设T=2d（清除沉砂的间隔时间），则(3-8)式中，X——城市污水沉砂量[(污水)]取30Kz——生活污水流量总变化系数（8）每个沉砂斗容积（V0）设每一分格有2个沉砂斗，则（9）沉砂斗各部分尺寸设斗底宽，斗壁与水平面的倾角为斗高，沉砂斗上口宽：最终定沉砂斗容积（3-9）=（10）沉砂室高度（h）采用重力排砂，设池底坡度为0.06，坡向砂斗，则，（11）池总高度(H)设超高=0.3m,则3.6鼓风机房鼓风机房要给曝气沉砂池和SBR池供气，选用TS系列罗茨鼓风机。选用TSD-150型鼓风机三台，工作两台，备用一台。44n设备参数：流量20.40m3/min升压44.1kPa配套电机型号Y200L-4功率30kW转速1220r/min机组最大重量730kg设计鼓风机房占地LB=2010=200m2。3.7SBR反应池3.7.1设计说明设计方法有两种：负荷设计法和动力设计法[6]，本工艺采用负荷设计法。根据工艺流程论证，SBR法具有比其他好氧处理法效果好，占地面积小，投资省的特点，因而选用SBR法。SBR是序批式间歇活性污泥法的简称。该工艺由按一定时间顺序间歇操作运行的反应器组成。其运行操作在空间上是按序排列、间歇的。污水连续按顺序进入每个池，SBR反应器的运行操作在时间上也是按次序排列的。SBR工艺的一个完整的操作过程，也就是每个间歇反应器在处理废水时的操作过程，包括进水期、反应期、沉淀期、排水排泥期、闲置期五个阶段，如图4-1。这种操作周期是周而复始进行的，以达到不断进行污水处理的目的。对于单个的SBR反应器来说,在时间上的有效控制和变换，即达到多种功能的要求，非常灵活[21]。进水期反应期沉淀期排水期闲置期图4-1SBR工艺操作过程44n（1）SBR工艺特点①工程简单，造价低；②时间上有理想推流式反应器的特性；③运行方式灵活，脱N除P效果好；④良好的污泥沉降性能；⑤对进水水质水量波动适应性好；⑥易于维护管理。（2）SBR工艺操作过程①进水期进水期是反应池接纳污水的过程。由于充水开始是上个周期的闲置期，所以此时反应器中剩有高浓度的活性污泥混合液，这也就相当于活性污泥法中污泥回流作用。SBR工艺间歇进水，即在每个运行周期之初在一个较短时间内将污水投入反应器，待污水到达一定位置停止进水后进行下一步操作。因此，充水期的SBR池相当于一个变容反应器。混合液基质浓度随水量增加而加大。充水过程中逐步完成吸附、氧化作用。SBR充水过程，不仅水位提高，而且进行着重要的生化反应。充水期间可进行曝气、搅拌或静止。曝气方式包括非限制曝气（边曝气边充水）、限制曝气（充完水曝气）半限制曝气（充水后期曝气）。②反应期在反应阶段，活性污泥微生物周期性地处于高浓度、低浓度的基质环境中，反应器相应地形成厌氧—缺氧—好氧的交替过程。虽然SBR反应器内的混合液呈完全混合状态，但在时间序列上是一个理想的推流式反应器装置。SBR反应器的浓度阶梯是按时间序列变化的。能提高处理效率，抗冲击负荷，防止污泥膨胀。③沉淀期44n相当于传统活性污泥法中的二次沉淀池，停止曝气搅拌后，污泥絮体靠重力沉降和上清液分离。本身作为沉淀池，避免了泥水混合液流经管道，也避免了使刚刚形成絮体的活性污泥破碎。此外，SBR活性污泥是在静止时沉降而不是在一定流速下沉降的，所以受干扰小，沉降时间短，效率高。④排水期活性污泥大部分为下周期回流使用，过剩污泥进行排放，一般这部分污泥仅占总污泥的30%左右，污水排出，进入下道工序。⑤闲置期作用是通过搅拌、曝气或静止使其中微生物恢复其活性，并起反硝化作用而进行脱水。3.7.2SBR反应池容积计算处理要求:表4-1进出水质Table4-1influent/outwastewaterquality项目进水水质(mg/L)出水水质(mg/L)BOD5CODcrSS40012006001003070设计处理流量(3-10)=1/3设SBR运行每一周期时间为8h，进水1.0h，反应(曝气)（4.0~5.0h）取4h，沉淀2.0h，排水（0.5h~1.0h）取1h。周期数:SBR处理污泥负荷设计为Ns=0.4kgBOD5/(kgMLSS﹒d)根据运行周期时间安排和自动控制特点，SBR反应池设置6个。（1）污泥量计算SBR反应池所需污泥量为=[kg(干)]44n=100（t）设计沉淀后污泥的SVI（污泥容积指数）=90ml/g，（SBR工艺中一般取80~150）SVI在100以下沉降性能良好[7]。则污泥体积为：VS=1.2·SVI·MLSS=1.2×90×10-3×100000=10800(m3)(2)SBR反应容积SBR反应池容积式中——代谢反应所需污泥容积——反应池换水容积（进水容积）——保护容积=，则单池污泥容积为则V=1800+4166.7+=5966.7+(3)SBR反应池构造尺寸SBR反应池为满足运行灵活及设备安装需要，设计为长方形，一端为进水区，另一端为出水区。SBR反应池单池平面（净）尺寸为5025（长比宽在~）水深为5.0m池深5.5m单池容积为=50255=6250()则保护容积为=283.3m36个池总容积44n3.7.3SBR反应池运行时间与水位控制SBR池总水深5.0m,按平均流量考虑，则进水前水深为3.2m，进水结束后5.0m,排水时水深5.0m,排水结束后3.2m。5.0m水深中，换水水深为1.8m,存泥水深2.0m,保护水深1.2m,保护水深的设置是为避免排水时对沉淀及排泥的影响。进水开始与结束由水位控制，曝气开始由水位和时间控制，曝气结束由时间控制，沉淀开始与结束由时间控制，排水开始由时间控制，排水结束由水位控制。3.7.4排水口高度和排水管管径(1)排水口高度为保证每次换水=4166.7的水量及时快速排出，以及排水装置运行的需要，排水口应在反应池最低水位之下约0.5~0.7，设计排水口在最高水位之下2.5。(2)排水管管径每池设自动排水装置一套，出水口一个，排水管1根；固定设于SBR墙上。排水管管径DN1000。设排水管排水平均流速为1.5，则排水量为：则每周期（平均流量时）所需排水时间为：3.7.5排泥量及排泥系统(1)SBR产泥量SBR的剩余污泥主要来自微生物代谢的增值污泥，还有很少部分由进水悬浮物沉淀形成[8]。SBR生物代谢产泥量为（3-11）44n式中:——微生物代谢增系数，kgVSS/kgBOD;——微生物自身氧化率，l/d根据生活污泥性质，参考类似经验数据，设=0.70，=0.05,则有：假定排泥含水率为98%，则排泥量为(3-12)=（P=98%）或（P=99.25%）考虑一定安全系数，则每天排泥量为2200m3/d。(2)排泥系统剩余污泥在重力作用下通过污泥管路排入集泥井。3.7.6需氧量及曝气系统设计计算(1)需氧量计算SBR反应池需氧量计算式为（3-13）式中:——微生物代谢有机物需氧率，kg/kg——微生物自氧需氧率，l/d——去除的BOD5(kg/m3)=经查有关资料表，取=0.50，=0.190,需氧量为：=29250（kg/O2/d）44n=1218.75(kgO2/h)(2)供气量计算设计采用塑料SX-1型空气扩散器，敷设SBR反应池池底，淹没深度H=4.5m。SX-1型空气扩散器的氧转移效率为EA=8%。查表知20℃，30℃时溶解氧饱和度分别为=9.17mg/L，=7.63mg/L空气扩散器出口处的绝对压力Pb为：=空气离开曝气池时，氧的百分比为曝气池中溶解氧平均饱和度为：（按最不利温度条件计算）（3-14）=水温20℃时曝气池中溶解氧平均饱和度为：20℃时脱氧清水充氧量为：（3-15）式中:——污水中杂质影响修正系数，取0.8(0.78~0.99)——污水含盐量影响修正系数，取0.9(0.9~0.97)——混合液溶解氧浓度，取c=4.0最小为2——气压修正系数==1曝气池中溶解氧在最大流量时不低于2.0mg/L,即取Cj=2.0，则计算得：44n=SBR反应池供气量为:每立方污水供气量为:(m3空气/m3污水)——反应池进水容积()去除每千克BOD5的供气量为:(m3O2/kgBOD5)3.7.7空气管计算空气管的平面布置如图3-5所示。鼓风机房出来的空气供气干管，在相邻两SBR池的隔墙上设两根供气支管，为6个SBR池供气。在每根支管上设25条配气竖管，为SBR池配气，六池共六根供气支管，150条配气管竖管。每条配气管安装SX-I扩散器26个，每池共650个扩散器，全池共3900个扩散器。每个扩散器的服务面积为：1250m2/650个=1.9m2/个空气支管供气量为：1.25——安全系数由于SBR反应池交替运行，六根空气支管不同时供气，故空气干管供气量亦为m3/min。选用SX-I型盆形曝气器，氧转移效率6~9%，氧动力效率1.5~2.2kg/(kW44nh),供气量20~25m3/h,服务面积1~2m2/个。3.7.8滗水器现在的SBR工艺一般都采用滗水器排水。滗水器排水过程中能随水位的下降而下降，使排出的上清液始终是上层清液。为防止水面浮渣进入滗水器被排走，滗水器排水口一般都淹没在水下一定深度[9]。目前SBR使用的滗水器主要有旋转式滗水器，套筒式滗水器和虹吸式滗水器三种。本工艺采用旋转式滗水器。旋转式滗水器属于有动力式滗水器，应用广泛，适合大型污水处理厂使用。本工艺采用XB-1800型旋转式滗水器。3.8絮凝反应池（竖直往复式隔板反应池）3.8.1设计说明深度处理包括混凝、澄清、过滤、活性炭吸附、臭氧氧化、反渗透等，其目的是去除二级处理水中的悬浮物（SS），溶解性有机物（BOD），N，P等污染物质，以满足水环境标准，防止封闭式水域富营养化和污水再利用的水质要求。混凝的基本原理：向污水中投入某种化学药剂（常称之为混凝剂），使在水中难以沉淀的胶体状悬浮颗粒或乳状污染物失去稳定后，由于互相碰撞而聚集或聚合、搭接而形成较大的颗粒或絮状物，从而使污染物更易于自然下沉或上浮而被除去。混凝剂可降低污水的浊度、色度，除去多种高分子物质、有机物、某些重金属毒物和放射性物质[10]。在水处理中，凝聚是指脱稳的胶粒相互聚集为较大颗粒的过程。絮凝则指未经脱稳的胶体也可聚结成较大的颗粒现象。混凝则包括凝聚与絮凝两种过程。凝聚是瞬时的，只需将化学药剂扩散到全部水中即可。絮凝则与凝聚作用不同，它需要较长的时间去完成。但一般情况下两者也不好绝然分开。因此我们把能凝聚与絮凝作用的药剂统称为混凝剂。絮凝通常在絮凝池内，以机械或水力等方式造成颗粒碰撞机会，形成易于沉淀或上浮的絮体，最终达到与水分离的目的，反应时间t在1030min之间。用于水处理的混凝剂要求44n混凝效果好，对人类健康无害，价廉易得，使用方便，本工艺选择明矾。3.8.2设计参数（1）廊道内流速采用6档（经验数据）（2）反应时间T=20min（3）池内平均水深H1=2.4m，超高H2=0.3m（4）反应池采用钢筋混凝土及砖组合结构，外用水泥砂浆抹面，粗糙系数n=0.0133.8.3设计计算（1）总容积（2）分为2池，每池净平面面积（3）池长池子宽度B按沉淀池宽采用30（4）隔板间距（按廊道内流速不同分为6档）(3-16)取44n（5）水头损失按廊道内的不同流速分成6段计算前5段内水流转弯数均为3，则前5段各段廊道长度为(3-17)(3-18)44n可见可省略絮凝池总水头损失3.9滤池（普通快滤池）3.9.1设计说明过滤是利用过滤材料分离污水中杂质的一种技术，有时用作污水的预处理，有时用作最终处理，出水供循环使用或重复利用。在污水深度处理技术中，普遍采用过滤技术。根据材料不同，过滤可分为多孔材料过滤和颗粒材料过滤两类。过滤过程是一个包含多种作用的复杂过程。完成过滤工艺的处理构筑物称为滤池。在污水处理中，颗粒材料过滤，主要用于去除悬浮和胶体杂质，特别是用重力沉淀法不能有效去除的微小颗粒以及细菌。颗粒材料过滤对污水中的BOD，COD等也有一定的去除效果[11]。滤池的种类虽然很多，但其基本构造是相似的，在污水深度处理中使用的各种滤池都是在普通快滤池的基础上加以改进而来的，普通快滤池外部由滤池池体、进水管、出水管、冲洗水排出管等管道及其附件组成；滤池内部由冲洗水排出槽、进水渠、滤料层、垫料层排水系统组成。普通快滤池可以用单层滤料、双层滤料和三层滤料。双层滤料滤池的工作效果较好，一般底层用粒径0.5~1.2的石英砂，高50044n，上层用陶粒或无烟煤，粒径为0.8~1.8，层高300~500。滤速8~10；反冲洗强度为15~16，延时8~10。3.9.2设计参数（1）滤速取10m/h（2）冲洗强度=13~16L/(m2﹒s)（3）冲洗时间20（4）停留时间1（5）滤池工作时间243.9.3设计计算(1）滤池面积及尺寸采用滤池数6个，每个滤池面积为71.43m2，设计滤池长宽比L/B=1.5。（2）承托层高度采用0.45，滤料层高度，无烟煤层为450，石英砂层为300，总高度750，滤料上水深H3采用1.5，超高H4采用0.3，滤板高度H5采用0.12。滤池总高度H1+H2+H3+H4+H5=3.12(m)（3）滤池反冲洗水头损失①管式大阻力配水系水头损失：——冲洗强度44n——配水系统开孔比——孔口流量系数②经砾石支承层水头损失计算如下：③滤料层水头损失及富余水头为：h4=2m④反冲洗水泵扬程：3.10接触消毒池3.10.1设计说明城市污水经过一级或二级处理后，水质改善，细菌含量也大幅度减少，但其绝对值仍很可观，并有存在病源菌的可能。因此，污水排入水体前应进行消毒，特别是医院、生物制品以及屠宰场等有致病菌污染的污水，更应严格消毒。目前，用消毒剂消毒能产生有害物质，影响人们的身体健康已广为人知，氯化是当今消毒采用的普遍方法。氯与水中有机物作用，同时有氧化和取代作用，前者促使去除有机物或称降解有机物，而后者则是氯与有机物结合，氯取代后形成的卤化物是有致突变或致癌活性的。所以，目前污水消毒一是要控制恰当的投剂量，二是采用其他消毒剂代替液氯或游离氯，以减少有害物的生成。消毒设备应按连续工作设置。消毒设备的工作时间、消毒剂代替液氯或游离氯，以减少有害物的生成。消毒设备应按连续工作设置，消毒设备的工作时间、消毒剂投加量，可根据所排放水体的卫生要求及季节条件掌握。一般在水源的上游、旅游日、夏季应严格连续消毒，其他情况时可视排出水质及环境要求，经有关单位同意，采用间断消毒或酌减消毒剂投量。44n目前常用的污水消毒剂是液氯，其次是漂白粉、臭氧、次氯酸钠、氯片、氯氨、二氧化氯和紫外线等。其中液氯效果可靠、投配设备简单、投量准确、价格便宜。其他消毒剂如漂白粉投量不准确，溶解调制不便。臭氧投资大，成本高，设备管理复杂。其他几种消毒剂也有很明显的缺点，所以目前液氯仍然是消毒剂首选。3.10.2设计参数（1）水力停留时间T=0.5h（2）设计投氯量一般为3.0~5.0mg/l本工艺取最大投氯量为3.10.3设计计算（1）设计消毒池一座，池体容积设消毒池池长L=35m，有3格，每格池宽b=5.0m，长宽比L/b=7.0。设有效水深H1=4m，接触消毒池总宽B=nb=3×5=15.0m，实际消毒池容积。满足有效停留时间的要求。（2）加氯量的计算最大投氯量为则每日投加氯量为：=20.8(kg/d)选用贮氯量为500kg的液氯钢瓶，每日加氯量1瓶，共贮用15瓶，选用加氯机两台。（3）混合装置在消毒池第一格和第二格起端设置混合搅拌机两台。选用JBK-2200框式调速搅拌机，搅拌直径2200mm，高2000mm，电动机功率4.0kW。接触消毒池设计为纵向折流反应池。在第一格每隔7设纵向垂直扩流板，第二格每隔11.67设垂直折流板，第三格不设。3.11污泥处理系统3.11.1污泥水分去除的意义和方法44n污水处理厂的污泥是由液体和固体两部分组成的悬浮液。污泥处理最重要的步骤就是分离污泥中的水分以减少污泥体积，否则其他污泥处理步骤必须承担过量不必要的污泥体积负荷。污泥中的水分和污泥固体颗粒是紧密结合在一起的，一般按照污泥水的存在形式可分为外部水和内部水，其中外部水包括孔隙水、附着水、毛细水、吸附水。污泥颗粒间的孔隙水占污泥水分的绝大部分（一般约为70%~80%），其与污泥颗粒之间的结合力相对较小，一般通过浓缩在重力的作用下即可分离。附着水（污泥颗粒表面上的水膜）和毛细水（约10%~22%）与污泥颗粒之间的结合力强，则需要借助外力，比如采用机械脱水装置进行分离。吸附水（5%~8%，含内部水）则由于非常牢固的吸附在污泥颗粒表面上，通常只能采用干燥或者焚烧的方法来去除。内部水必须事先破坏细胞，将内部水变成外部水后，才能被分离。3.11.2各部分尺寸计算（1）集泥井①集泥井容积的计算:产泥量根据前面计算所知，有以下构筑物排泥。SBR反应池1300m3/dP=99%则每日的总排泥为V=1300（m3）考虑构筑物的每日排泥量为1300，需在2.0内抽完，集泥井容积定为污泥泵提升流量的10的体积：②集泥井尺寸的计算设有效泥深为5m，平面面积59m2，设计尺寸LB=96.5=30m2，集泥井为地下式，池顶加盖，有潜污泵抽送污泥，池底相对标高-5.5m，最高泥位-0.5m，最低泥位-5.0m。③污泥提升泵的选择选择GMP型自吸式离心泵马力：20kW相数：3极数：444n型号：GMP-320-150口径：150mm质量：110kg流量：180m3/h最大流量：222m3/h扬程：17.5m最高扬程：24.0m选用六台，两台备用；（2）污泥浓缩池降低污泥中的含水率，可以采用污泥浓缩的方法来降低污泥中的含水率，减少污泥体积，能够减少池容积和处理所需的投药量，减小用于输送污泥的管道和泵类的尺寸。具有一定规模的污水处理工程中常用的污泥浓缩方法主要有重力浓缩.溶气气浮浓缩和离心浓缩[12]。根据需要选用间歇式重力浓缩池。①设计说明运行周期22h，其中进泥2.0h，浓缩15.0h，排水和排泥3.0h，闲置2.0h。浓缩前污泥量为1300m3，含水率p=99.0%。②设计计算a)容积计算浓缩15.0h后，污泥含水率为96.5%，则浓缩后污泥体积为则污泥浓缩池所需要的容积应不小于371.43+1300=1671.43m3b)工艺构造尺寸设计污泥浓缩池4个，单池容积不应小于417.9m3，取420m3。设计平面尺寸为4×(8×8)m2，则净面积为256m2。设计浓缩池上部柱体高度为5.0m，其中泥深为4.0m，柱体部分污泥容积为320m3。浓缩池下部为锥斗，上口尺寸(8×8)m2，下口尺寸为(1×1)m2，锥斗高为，则污泥斗容积为44n。污泥浓缩池总容积为320+389.3=709.3＞417.9m3满足要求。③排水和排泥a)排水浓缩后池内上清液利用重力排放，由站区溢流管道排入调节池。浓缩池设4根排水管于池壁，管径DN100mm。于浓缩池最高水位处置一根，向下每隔1.0m、0.6m、0.4m处设置一根排水管，下面三根安装蝶阀。b)排泥浓缩后污泥泵抽送污泥贮柜。污泥泵抽升流量123.8m3/h。浓缩池最低泥位-0.5m,污泥贮柜最高泥位为5.5m，则污泥泵所需静扬程为6.0m。④设备选择选用CP(T)-55.5-100型沉水式污泥泵1台，购买2台，使用1台，备用1台，该泵工作流量Qb为135m3/h，扬程Hb为8m为，转速n=1450r/min，电动机功率N=5.5kW，质量W=150kg。（3）污泥贮柜浓缩后需排出污泥123.81m3/d，污泥贮柜容积应，设污泥贮柜为ф6m，H为5.0m，则贮泥有效容积为，可满足污泥贮存要求。（4）污泥脱水机房①污泥产量经过浓缩处理后，产生含水量为96.5%的干污泥123.81m3/d。②污泥脱水机根据所需处理污泥量，选用DYQ300型带式压滤机1台，购买2台，使用1台，备用1台。该脱水机参数：处理量22m3/h，滤带有效宽度3000mm，滤带运行速度0.5~4.0，主机功率1.5kW，外型尺寸6.4×3.5×2.0，设备质量6500kg。③干污泥饼体积V设泥饼的含水率为75%（5）污泥棚44n堆放浓缩后的污泥,设计污泥厚度为4m,覆盖面积：即占地面积取150m2。3.11.3堆肥污泥堆肥是农业利用的有效途径。堆肥方法有污泥单独堆肥和污泥与城市垃圾混合堆肥两种。其基本原理是，污泥堆肥一般采用好氧条件下，利用嗜温菌和嗜热菌的作用，分解污泥中有机物质并杀灭传染病菌、寄生虫卵与病毒，提高污泥肥分。污泥堆肥一般应添加膨胀剂。堆肥可分为两个阶段，即一级堆肥阶段与二级堆肥阶段。一级堆肥阶段可分为3个过程：发热、高温消毒及腐熟。堆肥初期为发热过程：在强制通风条件下，堆肥中有机物开始分解，嗜温菌迅速成长，堆肥温度上升至约45~55℃；高温消毒过程：有机物分解所释放的能量，一部分合成新细胞，一部分使堆肥的温度继续上升可达55~70℃，此时嗜温菌受到抑制，嗜热菌繁殖，病原菌、寄生虫卵与病毒被杀灭，由于大部分有机物已被氧化分解，需氧量逐渐减少，温度开始回落；腐熟过程：温度降至40℃左右，堆肥基本完成。一级堆肥阶段约耗时7~9d，在堆肥仓内完成。二级堆肥阶段：一级堆肥完成后，停止强制通风，采用自然堆放方式，使进一步熟化、干燥、成粒。堆肥成熟的标志是物料呈黑褐色，无臭味，手感松散，颗粒均匀，蚊蝇不繁殖，病原菌、寄生虫卵、病毒以及植物种子菌被杀灭，符合我国卫生部颁发的《高温堆肥的卫生评价标准》[13]。44n第四章投资估算4.1土建部分投资估算土建部分投资估算见表4-1表4-1土建部分投资估算（单位：元）Table4-1acivilengineeringpartoftheinvestmentestimate序号名称规格(m)数量体积(m3)单价(元∕m3)总价1曝气沉砂池12×5.72×3.31226.51240090604.82SBR池50×25×5.51687540027500003絮凝反应池9.6×30×2.72777.64006220804滤池2.7×8.45×3.12171.182840028473.125接触消毒池35×15×4121004008400006污泥浓缩池4×641256400102400合计4433557.924.2设备部分投资估算设备部分估算见表4-2表4-2设计部分估算见Table4-2equipmentinvestmentestimation序号名称规格(m)数量单价（元）总价1格栅污水提升泵NC—400型机械格栅3300090002污水提升泵房LXB—1100型螺旋泵6（1备用）3000150003泵后细格栅NC—300型机械格栅3300090004滗水器XB—1800型旋转式滗水器1300030005鼓风机房TSD—150型鼓风机2（1备用）300030006污泥提升泵GMP型自吸式离心泵6（2备用）3000120007污泥脱水机DYQ300型带式压滤机13000300044n合计为54000直接费用为：4433557.92+54000=4487557.92≈448.8（万）4.3间接费用间接费用是指一些在施工过程中，使设备就位，和能够正常运行而消耗的费用。具体明细见表4-3。表4-3间接费用表Table4-3Overheadcostform序号费用名称价格（元）备注1设计费41600直接费用×5%2施工费83200直接费用×10%3调试验收费33300直接费用×4%4运输费41600直接费用×5%5安装费33300直接费用×4%6管理、税金106500总和的10%7合计344000间接费用合计为：34.4万元。费用总计为直接费用与间接费用之和：448.8+34.4=483.2万元。4.4运行费用①人工费本系统只需管理人员及操作工3人，每人每月工资为1200元，则处理每吨水的人工费为：3×1200/30/600=0.2元；②电费各用电器消耗电功率的显示表，见表4-4。表4-4电费表Table4-4Electricitychargesform名称功率（kw）数量（台）使用率（%）日耗电量（kw/h）NC—4001.135039.6LXB—11007.5550450NC—3004350144XB—1800TSD—1501115013244nGMP54100480DYQ300315036合计1461.6本系统总装机容量为115kw，其平均每小时连续运行功率为57kw，每日耗电量为57×24=1368kw；则处理每吨水的电费为：1368×0.60/600=1.37元。①药剂费约为0.7元/吨；②折旧费按使用年限为20年记，1342800/20/360/600=0.31元/吨；合计每吨水的处理费用为：0.13+1.37+0.7+0.31=2.51元44n第五章环境保护5.1施工过程中对环境影响及对策5.1.1对交通的影响及缓解措施在工程建设期间由于截流干管的铺设而增加的交通量，从而使交通变得拥挤或混乱，易造成交通事故。这种影响随着工程的建设而消失。工程建设将不可避免的与一些道路交叉。道路的开挖将严重的影响该地的交通。建设单位在制定实施方案时应充分考虑，对于交通繁忙的道路要设临时便道，并要求施工分段进行。在可能短的时间完成工作。对于交通特别繁忙的道路要避让高峰时间。挖出的泥土除作为回填土，要及时运走，堆土应尽可能少占道路，以保证开挖道路的交通运行。5.1.2扬尘的影响工程施工期间，挖掘的泥土通常堆放在施工现场，短则几个星期，长则数月。堆土裸露干旱风致，以至车辆过往，满天尘土，使大气中悬浮颗粒物含量骤增，施工扬尘使附近建筑物、植物等蒙上厚厚的一层尘土，使邻近的居家蒙上一层泥土，给居住区环境带来了污染。为了减少工程扬尘对周围环境的影响，建议施工中遇到连续的晴天又起风的情况下，对其土表面洒一些水。工程承包者应按照弃土处理要求，及时运走弃土。5.1.3噪声的影响污水处理厂施工期间的噪声主要来自施工机械和建筑材料运输，车辆马达的轰鸣喇叭的喧闹声。特别是在晚间，施工的噪声将产生严重的扰民问题，影响临近居民的工作和休息。为了减少施工对居民的影响，工程在距民舍200m的区域内不许在晚上十一时至次日上午六时内施工，同时应在施工设备和方法中加以考虑，应尽量采用低噪音的措施，同时也可在工地周围或居民住的地区设立临时的声障装置，以保证周围居民的环境质量。44n5.1.4生活垃圾的影响工程施工时，施工人员的食宿将会在工作区内。这些临时食宿的水电以及生活废弃物如没有做出妥善的安排，将会产生严重的后果，影响环境卫生。5.1.5弃土的影响及对策施工期间将产生许多弃土，这些弃土在运输过程中都可能产生影响。弃土处置地不明确或无规则乱放，将影响土地利用、河流流畅，破坏自然生态环境，影响城市的建设和整洁。工程建设单位应会同有关部门，为本工程的弃土指定处置计划，弃土的出路主要用于建路，小区建设等。分散与建设工地的弃土运输计划，将与有关部门联系，经他们采取措施处理后继续施工。5.1.6对地下水的影响工程建设不会对地下承压含水层的水流、水量以及水质等方面产生影响。5.2项目建成后的环境影响及对策污水处理厂本身是一个环境保护项目，它建成后将对改善地区环境和水体水质产生很大的作用，但它作为一个企业，也要有三废排除，虽然数量不大，但也会对周围环境产生一定的影响，为此也不容忽视。本工程针对环境影响采取了缓解措施。5.2.1臭味对环境的影响及缓解措施由于污水处理厂内很多污水处理设备均为敞开式的水池，所以污水的臭味散发在大气中，势必影响到周围的环境。污水处理设施下风向100m范围内，其臭味对人的感觉影响明显，在300m则闻不到臭味。污水处理厂建成运行后对厂外300m之内居民产生一定的影响。由于国内的经济技术标准限制，不可能也不必要对厂内散发气味的场所封闭，并收集有恶臭的进行统一处理。本设计采用最常规的做法即为绿化带隔离的办法在场区内种树和花草，有效地减缓厂区气味对周围环境的影响。44n总结（1）本设计是对某造纸厂废水处理工艺的设计，比较了几种工艺的优缺点，决定采用SBR工艺。（2）针对造纸厂废水的水质水量特点，参考国内外各种造纸厂处理相关废水的处理方法及技术，最后选择了SBR工艺。该方法对污水的处理比较彻底，效果较好；处理效率高，该方法对废水的水质水量变化适应能力强；废水的处理成本比较低并且建设和运行费用比较低。（3）该工艺将传统的曝气池、沉淀池由空间上的分布改为时间上的分布，形成一体化的集约构筑物，并利于实现紧凑的模块布置，最大的优点是节省占地。另外，可以减少污泥回流量，有节能效果。（4）在设计过程中，参看了大量的废水处理设计的相关资料，使得本设计考虑问题较全面，设计的可操作性较高。（5）处理后的废水达到造纸废水排放标准GB3544－2001中的一级标准。该设计总体项目投资省，污水处理成本较低，具有较高的经济可行性。44n致谢本设计任务重，加上本人的知识水平有限，缺乏实践工作方面的经验，所以在设计过程中存在着错误和不足的地方，敬请各位老师和同学们给予批评和修正。在这次的设计过程中，将我的所学知识进行了有效的重组整合，也让我了解了什么是具体的工程设计，以及设计中所必须注意的具体事项，同时也培养了我发现问题、解决问题的具体能力，这为我将来走向具体的工作岗位做了充分的锻炼和准备。经过几个月的不懈努力，我的毕业设计终于完稿了，在此过程中，得到了张老师的悉心指导。在此感谢张志生老师，同时也向在这次设计中给予我帮助的同学们表示深深的感谢!最后感谢各位领导和老师在百忙之中对本设计所做的精心评阅和指正。44n参考文献[1]上海市政工程设计研究院.给水排水工程快速设计手册.专用机械.第二版.北京：中国建筑工业出版社，1996.[2]中国市政工程西南设计院.给水排水工程快速设计手册.常用资料.第一版.北京：中国建筑工业出版社，1995.[3]上海市政工程设计研究院.给水排水.工程快速设计手册.技术经济.第二版.北京：中国建筑工业出版社，1996.[4]谢水波，余健.现代给水排水工程设计.第一版.湖南：湖南大学出版社，2000.[5]王金全.给水排水管道设计.第一版.北京：中国铁道出版社，1997.[6]丁亚兰.国内外废水处理工程设计实例.第二版.北京：化学工业出版社，1998.[7]许泽美，唐建国，周彤.水工业工程设计手册废水处理及再用.第一版.北京：中国建筑工业出版社，2002.[8]罗固源.水污染物化控制原理与技术.第一版.北京：化学工业出版社，2003.[9]于尔捷，张杰.给水排水工程快速设计手册2.第一版.北京：中国建筑工业出版社，1996.[10]王洪臣，扬向平.城市污水处理厂运行控制与维护管理.第一版.北京：科学出版社，1999.[11]张锡辉，刘勇弟.废水生物处理.第二版.北京：化学工业出版社，2003.[12]严道岸.实用环境工程手册.第一版.北京：化学工业出版社，2002.[13]段文义，李压峰.流体力学.第一版.沈阳：东北大学出版社，2001.[14]谢嘉.水污染控制原理.第一版.四川：四川大学出版社，1994.[15]卜秋平，曾科.城市污水处理厂的建设与管理.第一版.北京：化学工业出版社，2002.[16]张希衡.水污染控制工程.第一版.北京：化学工业出版社，1992.[17]张智，张勤，郭士权，扬文玲.给水排水工程专业毕业设计指南.第一版.北京：中国水利水电出版社，2001.[18]扬岳平，徐新华，刘传富.废水处理工程及实力分析.第一版.北京：化学工业出版社，1996.[19]徐新华，宋爽.工业废水中专项污染物处理手册.第二版.北京：化学工业出版社，1994.[20]高俊发，王社平.污水处理厂工艺设计手册.第三版.北京：化学工业出版社，2000.[21]dwardS.Rubin,CliffI.Davidson.IntroductiontoEngineering&theEnvironment.北京：清华大学出版社，2002，12-16.44n内部资料，请勿外传！9JWKffwvG#tYM*Jg&6a*CZ7H$dq8KqqfHVZFedswSyXTy#&QA9wkxFyeQ^!djs#XuyUP2kNXpRWXmA&UE9aQ@Gn8xp$R#͑Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5ux^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmUE9aQ@Gn8xp$R#͑Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5ux^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z8vG#tYM*Jg&6a*CZ7H$dq8KqqfHVZFedswSyXTy#&QA9wkxFyeQ^!djs#XuyUP2kNXpRWXmA&UE9aQ@Gn8xp$R#͑Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^G89AmUE9aQ@Gn8xp$R#͑Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5ux^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z8vG#tYM*Jg&6a*CZ7H$dq8KqqfHVZFedswSyXTy#&QA9wkxFyeQ^!djs#XuyUP2kNXpRWXmA&UE9aQ@Gn8xp$R#͑Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5ux^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmUE9aQ@Gn8xp$R#͑Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5ux^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNuGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5ux^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$U*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89Amv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5ux^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9C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