日产5万立方米造纸废水处理工艺设计 29页

'吉林化工学院毕业设计成绩课程设计题目5万m3/d造纸废水处理工艺设计课程名称：环境与生物工程学院院（系、部）：环境工程系29 吉林化工学院毕业设计目录第1部分设计任务书……………………………………………………………41.1题目名称……………………………………………………………………41.2设计资料……………………………………………………………………41.3设计内容……………………………………………………………………4第2部分污水处理流程说明……………………………………………………52.1关于造纸废水处理……………………………………………………………52.2造纸废水处理的研究方案……………………………………………………52.3工艺确定……………………………………………………………………82.4处理工艺流程图………………………………………………………………82.5污泥处理方案的确定…………………………………………………………9第3部分处理主要构筑物设计…………………………………………………113.1格栅……………………………………………………………………113.2集水井……………………………………………………………………113.3沉砂池……………………………………………………………………113.4升流式厌氧污泥反应床(UASB)………………………………………………113.5曝气池……………………………………………………………………113.6二沉池………………………………………………………………………113.7污泥浓缩池……………………………………………………………………123.8带式压滤机……………………………………………………………………12第4部分工艺计算……………………………………………………………134.1格栅………………………………………………………………………1329 吉林化工学院毕业设计4.2集水池………………………………………………………………………154.3沉砂池……………………………………………………………………154.4UASB……………………………………………………………………174.5曝气池……………………………………………………………………204.6二沉池……………………………………………………………………224.7污泥量计算…………………………………………………………………244.8污泥浓缩池设………………………………………………………………24第5部分设备一览表……………………………………………………26结束语…………………………………………………………………………27参考文献………………………………………………………………………28第1部分设计任务书29 吉林化工学院毕业设计1.1题目名称：5万m3/d造纸废水处理工艺设计1.2设计资料1、废水进水水量：Q=5万m3/d；2、废水进水水质：水质指标单位数量CODBOD5SSPHmg/Lmg/Lmg/L≤2000≤600≤90093、处理后出水水质要求：污水处理后出水排入Ⅳ类水体，即：水质指标单位数量CODBOD5SSPHmg/Lmg/Lmg/L150602006-9[1][2][3]4、气象水文资料：东北地区；冰冻深度1.7m；主导风向为东南风。1.3设计内容1、设计方案及设计计算；2、撰写设计计算说明书；3、画图（2张A1号----CAD图）；包括：1张工艺流程图，1张主体构筑物剖面图。第2部分污水处理工艺流程说明29 吉林化工学院毕业设计2．1关于造纸废水处理造纸企业是废水排放大户，也是环境污染的主要行业，我国2002年制浆造纸工业污染排放量约占全国污染排放总量的10%以上，排放污水中的化学耗氧量(COD)约占全国排放总量的35.3%，居于第一位。因此造纸废水的治理早已成为我国工业污染防治的焦点、热点和难点。如何按照科学发展观协调解决好造纸工业的原料与环境问题，使我国造纸工业走持续发展之路，是经济与社会发展的必然要求。造纸工业是能耗、物耗高，对环境污染严重的行业之一，其污染特性是废水排放量大，其中COD、悬浮物（SS）含量高，造纸废水的处理方法很多，归纳起来主要有物理处理法、化学处理法、生物处理法以及这3种方法的组合。鉴于目前造纸废水危害较大且治理难度比较大，2．2造纸废水处理的研究方案在实际和理论研究中一些比较常见的对于造纸废水的处理工艺有以下几种：a.气浮-接触氧化工艺，流程如下：b.混凝沉淀-A/O工艺，流程如下：29 吉林化工学院毕业设计a.水解酸化—好氧生物工艺，流程如下：b.CASS工艺，流程如下：高浓度水→调节池→水解酸化池→CASS池→出29 吉林化工学院毕业设计a.混凝气浮-A/O工艺，流程如下：29 吉林化工学院毕业设计2.3工艺确定因为本次处理的是造纸废水，属于高浓度有机废水，COD,BOD值较高，但是又由于不涉及到N,P的处理，所以只需使处理过程中的COD,BOD,SS达到排放标准即可。不需要太复杂的工艺，所以选择UASB和活性污泥法处理。UASB工艺可以去除80%[4]左右的COD和BOD.并且UASB无需设初沉池。活性污泥法的去除效率是90%[5]左右。这样处理后的水质就可以达到排放标准了。2.4处理工艺流程图29 吉林化工学院毕业设计出水进水格栅集水井沉砂池UASB曝气池二沉池污泥浓缩池污泥运出2.5污泥处理方案的确定产生污泥的地方主要是初沉池和二沉池，污泥处理工艺路线有：路线一：污泥—浓缩—脱水—最终处置路线二：污泥—浓缩—自然干化—堆肥—最终处置路线三：污泥—浓缩—机械脱水—干燥焚烧—最终处置路线四：污泥—浓缩—消化—最终处置污泥处理的方案比较见表2-3表2-3污泥处理方案比较[6]方案费用特点适用条件路线一根据所选的构筑物及设备决定以脱水为主要处理主体适于一般污泥的处理路线二较低以堆肥农用为主当污泥符合农用肥料条件及附近有农、林、牧或蔬菜基地时可以考虑采用路线三费用较高以干燥焚烧为主污泥不适于进行消化处理，或不符和农用条件，或受污水处理厂用地面积的限制以消化处理为主体29 吉林化工学院毕业设计路线四费用随消化处理的构筑物决定适于污泥中有机物含量较高的污泥污泥处理工艺路线确定本设计为50000m3/d的流量，流量不算太大，产生污泥不多，修建污泥消化池费用较高，不经济；污泥干燥焚烧需要脱去更多的水，费用也会很高；堆肥需要的场地较大，且费时，不合理。最后确定的污泥工艺路线为路线一。污泥浓缩方法的确定污泥浓缩的方法[5]力浓缩、气浮浓缩、离心浓缩。重力浓缩需要的费用较低；气浮浓缩需要通入空气，消耗能量，运行费用较高；离心浓缩是利用机械脱水，费用也较高。最后选用的浓缩的方法为重力浓缩。2）污泥脱水的方法的确定污泥脱水的方法有：自然干化和机械脱水。自然干化的脱水方法易受外界条件的影响，速度较慢，占用面积大，甚至还有臭味。所以最后选用的脱水的方法为机械脱水。3）污泥最终处置的方法的确定污泥最终处置的方法[1]埋、直接卫生填埋、堆肥、工业利用。29 吉林化工学院毕业设计第3部分处理主要构筑物设计3.1格栅格栅作为废水处的第一道工序，是用一组平行的刚性栅条制成的框架,可以用它拦截水中的大块漂浮物。格栅通常倾斜架设在其它处理构筑物之前或泵站集水池进口处的渠道中，以防漂浮物阻塞构筑物的孔道、闸门和管道或损坏水泵等机械设备。因此，格栅起着净化水质和保护设备的双重作用。所以在进入初沉池之前设置格栅间。纸浆污水中含有一定量的漂浮物及大颗粒悬浮物，一旦进入水泵或管道，必将发生堵塞现象，为防止堵塞，保护水泵及污水处理系统的稳定运行，特设置格栅一道，去除这些物质。3.2集水井集水井是设置在格栅之后的集水系统，是为了方便污水的提升以及缓冲污水的流量变化3.3沉砂池沉砂池主要用于去除污水中粒径大于0.2mm，密度连2.65t/m3的砂粒，以保护管道、阀门等设施免受磨损和阻塞。一般情况下，在污水中会含有相当数量的砂粒等杂质。设置沉砂池可以避免后续处理构筑物和机械设备的磨损，，减少管渠和处理构筑物产生沉积，避免重力排泥困难，防止对生物处理系统和污泥处理系统运行的干扰。常用的沉砂池有平流式、竖流式沉砂池、曝气沉砂池和旋流式沉砂池。本设计采用曝气沉砂池。3.4升流式厌氧污泥反应床（UASB）升流式厌氧生物反应器（UASB），其基本原理是：反应器主体分为上下两个区域，即反应区和气、液、固三相分离区，在下部的反应区内是沉淀性能良好的厌氧污泥床；高浓度有机废水通过布水系统进入反应器底部，向上流过厌氧污泥床，与厌氧污泥充分接触反应，有机物被转化为甲烷和二氧化碳，气、液、固由顶部三相分离器分离。出水COD的去除率可达到90%以上，容积负荷5—10kgCOD/（m3.d），分离后的沼气可作为能源利用3.5曝气池在曝气沉淀池内，污水和活性污泥混合，充分接触，污水中的可生物降解的物质被微生物代谢和利用，最后变为无机物，达到去除污染物的目的，最后泥水在外部的沉淀池内进行泥水分离，上清夜由出水堰排出，下面的泥部分排出池体，剩下的通过回流缝回流，进入曝气池，再次利用。3.6二沉池29 吉林化工学院毕业设计二沉池内实现泥水分离，污泥通过重力沉淀作用向下沉淀。上清液完全达标排放。一般在设计沉淀池时，选用平流式和辅流式沉淀池。为了使沉淀池内水流更稳、进出水配水更均匀、存排泥更方便，本设计采用流辐流式二次沉淀池。采用采用中心处进水，池中心出排泥，周边出水。3.7污泥浓缩池污泥浓缩池的主要作用为：污泥浓缩可使污泥初步减容，使其体积减少为原来的几分之一，从而为后续处理和处置带来方便3．8带式压滤机污泥脱水、干化的作用是去除污泥中的大量水分，从而缩小其体积，减轻其重量。经过脱水、干化处理，污泥含水率能从96%左右降到60%～80%左右，其体积降为原体积的1/10～1/5，有利于运输和后继处理。因此，国内外均比较重视污泥的脱水、干化技术。多数国家普遍采用的脱水机械为板框式压滤机、带式压滤机和离心机。污泥脱水中板框压滤机由于过滤能力较低，劳动强度大，操作管理复杂等因素，不是理想选择。带式压滤机具有能连续或间歇生产、操作管理简单、附属设备较少等优点，在国内外应用广泛。本设计采用带式压滤机，污泥含水率能降至80%左右，体积已大大缩小，脱水后污泥可以直接外用。29 吉林化工学院毕业设计第4部分工艺计算4.1格栅格栅是一种最简单的过滤设备，也是最常用的拦污设备。一般置于进水渠道上或泵站集水池的进口处，主要去除污水中较大的悬浮物或漂浮物。(1)格栅间隙数n[7]Qmax—最大设计流量，m3/s；α—格栅倾角，度（°）；b—栅条间隙，m;h—栅前水深，m;v—污水的过栅流速，m/sQmax=1.2×Q/24×3600=1.2×50000/24×3600=0.695m3/s设h=0.4m，过栅流速ν=0.9m/s，栅条间隙宽度b=0.01m，倾角α=60°n=0.695×sin60°1/2/0.01×0.4×0.9=179.7为安全考虑，取n=190个(2)格栅槽宽度BB=S(n-1)+bnS—栅条宽度，m;取S=0.01mB=0.01(190-1)+0.01×190=3.79m;(3)通过格栅的水头损失h2ho—计算水头损失，m；g—重力加速度，m/s2k—格栅受污物堵塞使水头损失增大的倍数，一般取3；ζ—阻力系数；设栅条断面为锐边矩形断面，则β=2.42h0=2.42×(0.01/0.01)4/3×(0.92/2×9.81)×sin60°=0.086mh2=3×0.086=0.258m(4)栅后槽总高度HH=h+h1+h2h1—栅前渠超高，一般取0.3mH=0.4+0.3+0.258=0.96m29 吉林化工学院毕业设计(5)栅槽总长度LL1—进水渠渐宽部分的长度，m；L2—栅槽与出水渠连接处渐窄部分长度，m；B1—进水渠宽，m；α1—进水渐宽部分的展开角，一般取20°取B1=3.0m，则进水渠内流速为Qmax/(B1×h1)=0.695/(3.0×0.3)=0.77m/s;在0.4～0.9m/s之间，符合要求。L1=(3.79-3.0)/2×tan20°=1.106mL2=1.106/2=0.553H=0.3+0.4=0.7mL=1.106+0.553+1.0+0.5+0.7/tan60°=3.564m(6)每日栅渣量WW—每日栅渣量，m3/d；W1—单位体积污水栅渣量，m3/10m3污水；一般取0.1～0.01，细格栅取大值，粗格栅取小值；KZ—污水流量总变化系数。当栅渣间距b=10㎜时，W1=0.1，Kz=1.3W=86400×0.695×0.07/1000×1.3=3.23m3/d＞0.2m3/d宜采用机械清渣计算草图[8]：29 吉林化工学院毕业设计图14.2集水井集水井的设计以自流1h不溢流为限，即水力停留时间（HRT）为1h；水流量Q=50000m3/d=2100m3/h。1.集水井的整容积的计算V=Q×h=2100×1=2100m3式中：h——水力停留时间，h；Q——水流量，m3/h；V——集水井体积，m3。2.集水井尺寸设计计算考虑到建设成本及设计水位，集水井的深度H取5m。集水井的面积S=V/H=420㎡。集水井的设计为圆形，所以可计算的直径D为23.13m。集水井设计尺寸为：高H=5m，直径D=23.13m。4.3沉砂池选择平流式沉砂池，共选两组，每组两格，则Qmax===0.29(m3/s)设沉砂池中最大流速vmax=0.3m/s，最大流量时停留时间t=50s。1.沉砂池长度（L）L=vmaxt=0.3×50=15(m)2.水流断面面积（A）29 吉林化工学院毕业设计A===0.97(m2)3.池总宽度（B）设n=2格，每格宽b=0.8mB=nb=2×0.8=1.6(m)4.有效水深（h2）h2===0.61(m)5.沉砂斗所需容积（V）设T=2d，则V===1.93(m3)6.每个沉砂斗容积（V0）设每一分格有两个沉砂斗，则V0==0.48(m3)7.沉砂斗各部分尺寸设斗底宽a1=0.5m,斗壁与水平面的倾角为55°，斗高h=0.35m，沉砂斗上口宽：a=+a1=+0.5=1.0(m)8.沉砂室高度（h）采用重力排砂，设池底坡度为0.01，坡向砂斗，则29 吉林化工学院毕业设计h=h+0.02l2=0.35+0.01×2.65=0.38(m)(l2为砂粒密度)9.池总高度（H）设超高h1=0.3m则H=h1+h2+h=0.3+0.79+0.38=1.47(m)10.验证最小流速Vmin在最小流量时只用一格工作（n1=1）Vmin===0.45(m/s)>0.15(m/s)4.4UASB1.UASB反应器容积的确定[9]本设计采用容积负荷法确立其容积V,容积负荷取8.5kgCOD/(m3.d)V=QS0/NVV—反应器的有效容积(m3)S0—进水有机物浓度(gCOD/L)V=50000*1.4/8.5=8235.3m3取有效容积系数为0.8,则实际体积为10293.75m32.主要构造尺寸的确定UASB反应器采用圆形池子，布水均匀，处理效果好。取水力负荷q1=0.6m3/（m2·d）反应器表面积A=Q/q1=2100/0.6=3500m2反应器高度H=V/A=8235.3/3500=2.35m取H=2.5m采用4座UASB反应器，则直径为：取D=35m则实际横截面积A2=3.14D2/4=961.6m2实际表面水力负荷q1=Q/4A2=2100/4*961.6=0.546q1在0.5—1.5m/h之间，符合设计要求。3配水系数设计本系数设计为圆形布水器，每个UASB反应器设200个布水点，采用连续均匀进水。①参数每个池子的流量：Q=Q1/4=2100/4=525m3/h②圆环直径计算：每个孔口服务面积a=A2/18=525/200=2.625㎡a在1—3m2之间，符合要求。可设4个圆环，最里面的圆环设12个孔口，中间设24和48个孔口，最外面设116个孔口。29 吉林化工学院毕业设计③内圈12个孔口设计服务面积：S1=12a=12×2.63㎡=31,.56㎡折合为服务区圆点直径:D1=(4S1/π)½=20.m用此直径作一虚圆，在该虚圆内等分面积处设计实圆环，其上布12个孔口。则圆的直径计算如下：则d1=(2S1/π)½=4.5m④中圈24个孔口设计服务面积：S2=24a=63.1㎡折合服务圆直径为D2=[4（S1+S2）/π]½=11m中间圆环的直径如下：π(D2²-d2²)/4=S2/2则d2=9m⑤中圈48个孔口设计服务面积：S3=48a=126.2㎡折合为服务圆直径：D3=[4（S1+S2+S3）/π]½=16.77m则外圆环的直径d3计算如下：π(D3²-d3²)/4=S3/2则d3=14.17m⑥外圈116个孔口设计服务面积：S4=116a=305.08㎡；折合为服务圆直径：D4=[4（S1+S2+S3+S4）/π]½=26m则外圆环的直径d3计算如下：π(D4²-d4²)/4=S4/2；；；则d4=21.9m计算草图如下：(4)三相分离器的设计①设计说明三相分离器主要具有气，液，固三相分离的功能。一般设在沉淀区的下部。三相分离器是UASB反应器污水厌氧处理工艺的主要特点之一，它同时具有传统废水生物处理工艺中的二沉池与污泥回流及气体收集的功能，因而三相分离器的合理设计是保证UASB反应器正常有效运行的一个重要内容。三相分离器的设计主要包括沉淀区，回流缝，气液分离器的设计。②沉淀区设计29 吉林化工学院毕业设计三相分离器的沉淀区设计同二次沉淀池的设计相似，主要是考虑沉淀区的面积和水深。面积根据废水水量和表面负荷来决定。由于沉淀区的厌氧污泥及有机物还可以发生一定的生化反应，产生少量气体，这对固液分离器不利，故设计时应满足以下要求：a.沉淀区水力表面负荷≤1.0m/h。b.沉淀器斜壁角度约为500，使污泥不致积聚，尽快落入反应区内。c.进入沉淀区前，沉淀槽底缝隙的流速≤2m/h。d.总沉淀水深应≥1.5m。e.水力停留时间介于1.5—2h。如果以上条件均能满足，则可达到良好的分离效果。沉淀器（集气罩）斜壁倾角=500沉淀区面积A=πD²/4=122.7㎡,表面水力负荷：q=Q/A=208/(2×122.7)=0.85<1.0,符合要求。③回流缝设计‘取h1=0.3m，h2=0.5m,h3=1.5m,如图所示：，式中：b1------下三角集气罩水平宽度，m。θ------下三角集气罩斜面的水平夹角。H3------下三角集气罩的垂直高度，m。b1==1.26m；；；；b2=D-2b1=6.2－2×1.26=3.68mA.下三角集气罩之间的污泥回流逢中混合液的上升流速V1可用下式计算：V1=Q1/S1；；；；；；式中：Q1----反应器中废水流量，m3/h；S1---下三角形集气罩回流逢面积，m2；29 吉林化工学院毕业设计V1=4Q1/2πb2²=1.96m/h；；V1<2m/s,符合设计要求B.上下三角形集气罩之间回流逢中流速(V2)可用下式计算：V2=Q1/S2，式中：Q1----------反应器中废水流量，m3/h；S2----------上三角形集气罩回流逢之间面积，m2；取回流逢宽CD=1.2m,上集气罩下底宽CF=6.0m；则DH=CD×sin50°=0.92mDE=2DH+CF=2×0.92+6.0=7.84mS2=π(CF+DE)CD/2=26.07m2则V2=Q1/S2=41.7/26.07=1.60m/h净水的μ,故取μ=0.02g/cm·s由斯托克斯工式可得气体上升速度为：；Vb==9.58m/h；；Va=V2=1.60m/h；则Vb/Va=5.9,BC/AB=1.87/1.81=1.03；；>,故满足设计要求。4.5曝气池采用完全混合式曝气法。设计两个曝气池，每个池子的流量（按平均流量计算）为Q单=Q/2=50000/2=25000m3/d每个池子设5个廊道。(1)水处理成都计算根据要求，处理效率为：η＝[(600-60)/600]*%=90%（2）曝气池的计算按BOD——污泥负荷法计算。29 吉林化工学院毕业设计1）BOD——污泥负荷率的确定。拟采用的BOD——污泥负荷率为Ns=0.3kgBOD5/（kgMLSSd）。2）确定混合液的污泥浓度（X）。根据已定的Ns确定相应的SVI值应在100-150之间，取值120。则Xr=取回流比R=0.5.则X=3）确定曝气池容积。V=QSr/NsX=(50000*180)/(0.3*3300)=9090.9≈9091m34）单池个部分尺寸计算。设计2组曝气池，每组容积为V单=V/2=9091/2=4545.5m3，取V单=4545m3取曝气池深h=4.5m，则每组池子的面积为F=4545/4.5=1010m3取池宽b=8m，B/h=8/4.5=1.78，介于1-2之间，符合规定，扩散装置设在廊道的一侧。池长L=F/B=1010/8=126.25m；L/B=126.25/8=15.8>10，符合规定满足要求。设2廊道式曝气池，单廊道长L1=L/2=126.25/2=63.13m，在50-70m之间，合理。取超高0.5m，则总高度为H=0.5+h=0.5+4.5=5m（3）剩余污泥的计算。干污泥量W=aQSr-bVXv=0.5*50000*0.18-0.07*9091*0.75*3.3=2925kg/d=121.9kg/h式中：a——污泥增值系数，0.5-0.7b——污泥自身氧化率，0.04-0.1Xv——挥发性悬浮固体浓度MLVSS（kg/m3），Xv=fX=0.75X湿污泥量Q=W/fXr=2925/(0.75*10)=390m^3/d（4）曝气系统的计算曝气池混合液需氧量W=a＇QSr+b＇VXv=0.42*50000*0.18+0.15*9091*0.75*3.3=3375kg/d=140.6kg/h29 吉林化工学院毕业设计式中：a’——氧化每公斤BOD需氧公斤数（kgO2/kgBOD），0.42-0.53b’——污泥自身氧化需氧率（kgO2/MLVSSd），0.11-0.188每日去除的BOD5的量BOD5=QSr=50000*0.18=9000m3去除每公斤BOD5的需氧量△O2=R/BOD5=3375/9000=0.375kgO2/kgBOD5（5）计算曝气池内平均溶解氧饱和度。采用网状膜型微孔空气扩散器，敷设于曝气池底部，据池底0.2m，计算温度为30℃（6）计算鼓风曝气池20℃时脱氧清水的需氧量。R0=RCsb(t)/a[BpC-C]1.024^T-20=3375*10.6/0.85[0.95*1*8.79-2]=5228kg/d=217.8kg/h（7）供气量Gs=Ro/0.3Ea*100=217.8/0.3*100=7260kg/h4.6二沉池二沉池主要是处理出水的悬浮物，经过二沉池后出水的SS达到了设计所规定的出水指标。本次设计采用辐流式沉淀池。1.有关设计参数取值1)水力表面负荷q一般在1.0～1.5m3/m2·h，设计取1.1m3/m2·h。29 吉林化工学院毕业设计1)沉淀个数n=1，沉淀时间T=3h。2)沉淀池超高取h1取0.3m。3)缓冲层高度h3取0.5m。4)刮泥板高度h5取0.5m。5)污泥回流比R取0.5。6)稳流筒中流速v筒一般0.02～0.03m/s，设计取0.03m/s。2.二沉池尺寸计算1)池表面积A计算A=Q/q=50000/（24×1.1）=1894m22)池直径D计算D=2（A/π）1/2=2（1894/3.14）1/2=49.12m设计采用中心传动式刮泥机。3)部分有效水深h2计算h2=q×T=1.1×3=3.3m式中：q——水力表面负荷，m3/m2·h；T——沉淀时间，h。3.沉淀部分有效容积计算V=πD2×h2/4=3.14×49.12^2×3.3/4=6250m34.沉淀池底坡落差h4计算设池底坡度i=0.05。h4=i×（D/2－2）=0.05×（49.12/2－2）=1.128m5.沉淀池周边（有效）水深H0计算H0=h2+h3+h5=3.3+0.5+0.5=4.3m式中：h2——部分有效水深，m；h3——缓冲层高度，m；h5——刮泥板高度，m。6.沉淀池总高度计算H=H0+h4+h1=4.3+1.128+0.3=5.73m二沉池对废水中污染物有一定的去除率，但由于废水在经过生物接触氧化处理后已经可达标排放，所以不予考虑，因此，上述的设计可对本次课题所设定的废水进行处理并达标排放。29 吉林化工学院毕业设计4.7污泥量计算初沉迟污泥量的确定剩余污泥产量总污泥量4.8污泥浓缩池设计1作用污泥浓缩池的主要作用为：污泥浓缩可使污泥初步减容，使其体积减少为原来的几分之一，从而为后续处理和处置带来方便。2设计规定连续流污泥浓缩池可采用沉淀池形式，一般为竖流式或辐流式；污泥浓缩池面积应该按污泥沉淀曲线实验数据决定的污泥固体负荷来进行计算，当无污泥沉淀曲线数据时可根据污泥种类，污泥中有机物的含量采用经验数据设计；连续式污泥浓缩池，一般采用圆形竖流或辐流沉淀池的形式。污泥室容积，应该根据排泥方法和两次排泥时间间隔而定，浓缩池较少时可采用竖流式浓缩池，一般不设刮泥机，沉淀池按浓缩分离出来的污水流量进行设计。当农村习惯采用湿污泥作肥料时，污泥的浓缩与储存可采用间歇式湿污泥池；1）浓缩池面积A29 吉林化工学院毕业设计2）浓缩池直径D：设计采用8个圆形辐流池单池面积为：浓缩池直径为：3）浓缩池深度为：浓缩池工作部分有效水深为超高取h1=0.3；缓冲层高h3=0.3；浓缩池设机械刮泥机，池底坡度；污泥斗底部直径，上底直径；池底坡度造成的深度为：污泥斗高：污泥浓缩池的总深度为：第5部分设备一览表序号名称规格数量设计参数备注29 吉林化工学院毕业设计1格栅L×B3.6m×38m1座设计水量：Qmax=2100m3/h格栅倾角：a=60°栅前水深：h=0.4m2集水井H=5mD=23.3m2座Q=2100m3/h3沉沙池L×B×H15m×1.6m×1.5m两组四格Q=2100m3/h停留50s每格两个沉沙斗斗底宽a=0.5m斗壁与水平面的倾角为55°斗高h=0.35m上口宽a=1.0m4UASBH=2.5mD=35m4座Q=2100m3/h5曝气池L×B×H126.3×8×2座5个廊道6二沉池H=5.7mD=49m1座沉淀时间T=3h池底坡落差h=1.13m7污泥浓缩池H=4.5mD=48m8座泥斗底部D=1m上底D2=7.4m泥斗高h=1.2m坡底造成的深度为0.2m结束语29 吉林化工学院毕业设计两周的课程设计结束了,通过本次的课程设计我学到了很多,对排水工程的相关设计计算和CAD制图有了一定的加强。本次设计时间比较仓促,同时自己对相关专业知识的了解程度还不够透彻，漏洞之处不可避免，但为我们以后的毕业设计打下了良好的基础，也为我们以后走向工作岗位起到一定的帮助最后，感谢指导老师廉老师的悉心指导和同学的帮助使我顺利完成本次的设计参考文献：1.《污水综合排放标准》GB8978-19962.《给水排水设计手册》（第五册）中国建筑工业出版社3.《室外排水设计规范》中华人民共和国国家标准上海市建设委员会主编4.张自杰.排水工程（下册）[M].北京:中国建筑工业出版社，2005.29 吉林化工学院毕业设计5.《水污染控制工程》高廷耀等主编高等教育出版社20026.黄惠芳,覃宏刚.采用厌氧-生物接触氧化工艺处理屠宰废水[J].广西轻工业，2005,4(89):15-18.1.韩洪军.污水处理构筑物设计与计算.第一版.哈尔滨:哈尔滨工业大学出版社，2002，2038.《给水排水制图标准》GBT50106-20019.张希衡.废水厌氧生物处理工程[M].北京:中国环境科学出版社,1996.10张兢人.采用厌氧-好氧工艺处理制浆废水,既保护环境又节能降耗[J].福建造纸信息,2009内部资料仅供参考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^vR9CpbK!zn%Mz849Gx^Gjqv^$U*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz84!z89Amv^$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$vSTT#&ksv*3tnGK8!z89AmYWv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$U*3tnGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9&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!z89AmYWpazadNuGK8!z89AmYWpazadNu##KN&MuWFA5uxY7JnD6YWRrWwc^vR9CpbK!zn%Mz849Gx^Gjqv^$UE9wEwZ#Qc@UE%&qYp@Eh5pDx2zVkum&gTXRm6X4NGpP$vSTT#&ksv*3tnGK8!z89AmYWpazadNu##KN&MuWFA5ux^Gjqv^$UE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吉林化工学院毕业设计29'