宝钢污水处理工艺设计计算详细95分

精选优质文档-----倾情为你奉上/r/n精选优质文档-----倾情为你奉上/r/n专心---专注---专业/r/n专心---专注---专业/r/n精选优质文档-----倾情为你奉上/r/n专心---专注---专业/r/n一、各污水处理构筑物的计算/r/n1、/r/n集水井、格栅/r/n（1）/r/n车间的废水/r/n经/r/n管道流到污水处理站的集水井，集水井后设置人工清除格栅，拟选用回转式格栅除污机，因为处理水量教小，故选用设备宽度最小的一型，即HG-800回转式格栅除污机/r/n。集水井的长度设为2.0m，宽度设为1.0m，深度4m。/r/n粗格栅宽度为b/r/n1/r/n=80mm，n/r/n1/r/n=12个；粗格栅宽度为b/r/n2/r/n=30mm，n/r/n2/r/n=32个。/r/n粗格栅栅槽宽度：/r/nB/r/n1/r/n=S（/r/nn/r/n1/r/n-1）+b/r/nn/r/n1/r/n=0.0/r/n1/r/n×/r/n(12-1)+0.08/r/n×/r/n12/r/n=/r/n1.07m/r/n中格栅栅槽宽度：/r/nB/r/n2/r/n=S（/r/nn/r/n2/r/n-1）+b/r/nn/r/n2/r/n=0.0/r/n1/r/n×/r/n(/r/n3/r/n2-1)+0.0/r/n3/r/n×/r/n3/r/n2=/r/n1./r/n（2）通过格栅的水头损失：设栅条断面为锐边矩形断面/r/n/r/n/r/n①/r/nh/r/n1/r/n=/r/nβ/r/n（s/b）/r/n4/3/r/n（v/r/n2/r/n//r/n2g/r/n）sin/r/nа/r/nk/r/n=2.42(0.01/0.08)/r/n4/3/r/n（/r/n0.8/r/n2/r/n/2/r/n×/r/n9.8/r/n）sin/r/n(/r/n45/r/n°×/r/n3)/r/n=/r/n0.015m/r/n/r/n②/r/nh/r/n2/r/n=/r/nβ/r/n（s/b）/r/n4/3/r/n（v/r/n2/r/n//r/n2g/r/n）sin/r/nа/r/nk/r/n=2.42(0.01/0.03)/r/n4/3/r/n（0.8/r/n2/r/n/2/r/n×/r/n9.8/r/n）sin(/r/n45/r/n°×/r/n3)/r/n=/r/n0.039m/r/n（3）格栅前水深取/r/n0.4m/r/n粗格栅后槽总高：H/r/n1/r/n=h+h/r/n1/r/n+h/r/n2/r/n=0.4+0.015+0.3/r/n=/r/n0.715m/r/n;/r/n中格栅后槽总高：H/r/n2/r/n=/r/nh+h/r/n1/r/n+h/r/n2/r/n=0.4+0.039+0.3/r/n=/r/n0.739m/r/n;/r/n所以栅后槽总高取H/r/n2/r/n=0.739。/r/n（4）栅后槽总长度：/r/nа/r/n1/r/n取20/r/n°/r/n，/r/nB/r/n1/r/n取0.65。/r/n/r/n/r/n粗格栅：/r/nL=l/r/n1/r/n+l/r/n2/r/n+1.0+0.5+H/r/n1/r/n/tan/r/nа/r/n1/r/n=（B-B/r/n1/r/n）/(2/r/ntan/r/nа/r/n1/r/n)+/r/n（B-B/r/n1/r/n）/(2/r/ntan/r/nа/r/n1/r/n×/r/n2)+1.0+0.5+(/r/nh/r/n+h/r/n2/r/n)/tan/r/nа/r/n1/r/n=（/r/n1.07/r/n-/r/n0.65/r/n）/(2/r/ntan/r/n20/r/n°/r/n)+/r/n（/r/n1.07/r/n-/r/n0.65/r/n）/(2/r/ntan20/r/n°/r/n×/r/n2)+/r/n1.0+0.5+(/r/n/r/n0.4/r/n+/r/n0.3/r/n)/tan20/r/n°/r/n=/r/n4.29m/r/n。/r/n中/r/n格栅：/r/nL=l/r/n1/r/n+l/r/n2/r/n+1.0+0.5+H/r/n1/r/n/tan/r/nа/r/n1/r/n=（B-B/r/n1/r/n）/(2/r/ntan/r/nа/r/n1/r/n)+/r/n（B-B/r/n1/r/n）/(2/r/ntan/r/nа/r/n1/r/n×/r/n2)+1.0+0.5+/r/n(/r/nh/r/n+h/r/n2/r/n)/tan/r/nа/r/n1/r/n=（/r/n1.27/r/n-/r/n0.65/r/n）/(2/r/ntan20/r/n°/r/n)+/r/n（/r/n1.27/r/n-/r/n0.65/r/n）/(2/r/ntan20/r/n°×/r/n2)+/r/n1.0+0.5+(/r/n/r/n0.4/r/n+/r/n0.3/r/n)/tan20/r/n°/r/n=/r/n4.70m/r/n。/r/n（5）每日栅渣量：/r/nW=（Q/r/nmax/r/n×/r/nW/r/n1/r/n×/r/n86400）/(/r/n/r/nK/r/nz/r/n×/r/n1000)/r/n=（0.015/r/n×/r/n0.004/r/n×/r/n86400）/(/r/n/r/n1.3/r/n×/r/n1000)/r/n=/r/n0.040m/r/n3/r/n调节池/r/n（1）每日栅渣量调节池有效容积V/r/n：/r/n调节池时间间隔t=10h。/r/nV=/r/nQt=1000/24/r/n×/r/n10=/r/n417m/r/n3/r/n（2）调节池面积A:调节池有效水深H取5m，超高0.5m。/r/nA=V/H=417/5+/r/n83.4m/r/n2/r/n（3）调节池长度L:取调节池宽度为7m。/r/nL=84/7/r/n=/r/n12m/r/n。/r/n池的尺寸为：L/r/n×/r/nB/r/n×/r/nH=/r/n12/r/nm/r/n×/r/n7m/r/n×/r/n5.5m/r/n初沉池/r/n/r/n初沉池选用平流式沉淀池。/r/n沉淀池的沉淀时间t为1.0h，表面负荷q′为2.0/r/nm/r/n3/r/n/（/r/nm/r/n2/r/n·h），沉淀池的水平流速v取/r/n1.5/r/nmm/r/n/s。/r/n（1）池总表面积A：/r/nA=Q/r/n×/r/n3600/q/r/n=（1000/r/n×/r/n3600）/(24/r/n×/r/n60/r/n×/r/n60/r/n×/r/n2)/r/n=/r/n20.8m/r/n2/r/n取/r/n21m/r/n（2）沉淀部分有效水深：/r/n去沉淀时间1h。/r/nh/r/n2/r/n=q/r/n×/r/nt/r/n=2/r/n×/r/n1/r/n=/r/n2m/r/n。/r/n（3）沉淀部分有效容积：/r/nV/r/n1/r/n=A/r/n×/r/nh/r/n2/r/n=/r/n/r/n21/r/n×/r/n2/r/n=/r/n42m/r/n3/r/n（4）池长：/r/nL=/r/nv/r/nt/r/n×/r/n3.6/r/n=/r/n1/r/n.5/r/n×/r/n1/r/n×/r/n3.6/r/n=/r/n5.4/r/nm/r/n（5）池子总宽度：/r/nB=A/L/r/n=21//r/n5.4/r/n=/r/n3.9/r/nm/r/n。/r/n取/r/n4m/r/n（/r/n6）沉淀池的污泥量：/r/n/r/nW/r/n=Q(C/r/n1/r/n-C/r/n2/r/n)/r/n×/r/n100T/r/n÷γ÷/r/n(100-/r/nρ/r/n0/r/n)/r/n=1000(/r/n0.002/r/n-/r/n0.002/r/n×/r/n0./r/n5/r/n)/r/n×/r/n100/r/n×/r/n（4/24）/r/n÷/r/n1/r/n÷/r/n(100-99)/r/n=/r/n1/r/n2.52/r/n式中：Q/r/n—/r/n处理水的量，m/r/n3/r/n/d。/r/nC/r/n1/r/n/r/n—/r/n进水悬浮物浓度，t/m/r/n3/r/n。/r/nC/r/n2/r/n/r/n—/r/n出水悬浮物浓度，t/m/r/n3/r/n。/r/nT/r/n—/r/n两次清除污泥间隔(d)，取/r/n3/r/nh。/r/n/r/nγ/r/n—/r/n污泥密度，其值约为1t/m/r/n3/r/n。/r/n/r/nρ/r/n0/r/n—/r/n污泥含水率（％）。/r/n（/r/n7）池子总高度：/r/nH=h/r/n1/r/n+h/r/n2/r/n+h/r/n3/r/n+h/r/n4/r/n=0.3+2+0.6+2.4=/r/n5.3m/r/n。/r/n式中：h/r/n1/r/n/r/n—/r/n超高，取/r/n0.3m/r/n。/r/nh/r/n3/r/n—/r/n缓冲层高度，/r/n0.6m/r/n。/r/nh/r/n4/r/n/r/n—/r/n污泥部分高度，取/r/n2.4m/r/n。/r/n（/r/n8）污泥斗容积：/r/nV=1/3h/r/n4/r/n×/r/n[f/r/n1/r/n+f/r/n2/r/n+(f/r/n1/r/nf/r/n2/r/n)/r/n1/2/r/n]/r/n=1/3/r/n×/r/n2.4/r/n×/r/n[1/r/n7./r/n6+0./r/n3/r/n6+(1/r/n7./r/n6/r/n×/r/n0./r/n3/r/n6)/r/n1/2/r/n]/r/n=/r/n1/r/n6.38/r/nm/r/n3/r/nf/r/n1/r/n—/r/n斗上口面积（m/r/n2/r/n）/r/n，取/r/n4/r/nm/r/n×/r/n4/r/nf/r/n1/r/n—/r/n斗下口面积/r/n（m/r/n2/r/n）/r/n，取/r/n0./r/n6/r/nm/r/n×/r/n/r/nh/r/n4/r/n/r/n—/r/n污泥部分高度。/r/n（/r/n9/r/n）/r/n沉淀池总长度：/r/n/r/nL=0.5+0.3+9=/r/n9.8m/r/n。/r/n式中：0.5/r/n—/r/n流入口至挡板距离。/r/n0.3/r/n—/r/n流出口至挡板距离。/r/n4、/r/n接触氧化池/r/n/r/n生物接触氧化池一般不少于两座。/r/n设计进水资料：Q=/r/n1000m/r/n3/r/n/d/r/n，进水BOD/r/n5/r/n=8/r/n50/r/nmg/l，出水BOD/r/n5/r/n=/r/n212.15/r/nmg/L。/r/n（1/r/n）/r/n生物接触氧化池的有效容积V/r/n:/r/n取BOD/r/n——/r/n容积负荷为1.0kgBOD/m3.d。按公式：/r/n=/r/n=/r/n637.5m/r/n3/r/n。/r/n/r/n（2）/r/n生物接触氧化池的面积/r/n：/r/n/r/n设反应器有效水深H=/r/n3m/r/n，则接触氧化池的面积为/r/n因为池子有两座，所以池子的尺寸为2/r/n×/r/nL/r/n×/r/nB=2/r/n×/r/n11/r/nm/r/n×/r/n10m。/r/n（3）/r/n生物接触氧化池的总高度/r/nH/r/n0/r/n：/r/n/r/n式中：H/r/n——/r/n填料层高度，/r/n3m/r/n；/r/nh/r/n1/r/n——/r/n接触氧化池超高，/r/n0.5m/r/n；/r/nh/r/n2/r/n——/r/n填料上部稳定水深，/r/n0.5m/r/n；/r/nh/r/n3/r/n——/r/n填料层距池底高度，/r/n1.0m/r/n。/r/n（4）停留时间：/r/n/r/n（5）需氧量R/r/n：/r/n/r/nR=QSra′+VX/r/nb′/r/n/r/n式中/r/n：/r/na′——微生物氧化分解有机物过程中的需氧量，/r/n（本文取/r/n/r/n/r/n0./r/n75kgO/r/n2/r/n/kgBOD/r/n5/r/n)；/r/nb′——污泥自身氧化的需氧量，/r/n（本文取0.12/r/n）；/r/nSr——有机基质降解量，kg/d；/r/nX——MLSS，g/L（本文取/r/n4g/r/n/L）。/r/n/r/nR=a′/r/nQ（Sa-Se/r/n）/r/n+/r/nVX/r/nb′/r/n=0.75/r/n×/r/n1000/r/n×/r/n（850-212.5）/r/n÷/r/n1000+0.12/r/n×/r/n4/r/n×/r/n637.5/r/n=/r/n784.125kg/r/n/d/r/n=/r/n32.67kg/r/n/h。/r/n（6）供气量计算：/r/n出口处绝对压力：/r/n/r/nPa/r/n氧的转移效率（E）为30%/r/n，/r/n温度为/r/n20/r/n℃/r/n时，氧化池中的溶解氧饱和度为9.17mg/l，/r/n30/r/n温度为/r/n20/r/n℃/r/n/r/n/r/n/r/n/r/n/r/n/r/n=/r/n60.70/r/nkg/r/n式中：/r/n氧转移折算系数，（一般取0.8~0.85，取0.8）；/r/n/r/n—/r/n氧溶解折算系数，（一般取0.9~0.97，取0.9）；/r/n/r/n—/r/n密度，/r/n1.0kg/r/n/L；/r/n/r/n废水中实际溶解氧浓度，mg/l（一般取2mg/l）；/r/n/r/nR/r/n—/r/n需氧量。/r/n供气量为：/r/n/r/n（7）/r/n曝气器/r/n及空气管路的计算/r/n：/r/n本设计采用WZP中微孔曝气器，技术参数如下：/r/n曝气量：4/r/n-12m/r/n3/r/n服务面积：0.5/r/n-1.2m/r/n2/r/n氧利用率：在/r/n4米/r/n以上水深，标准状态下为30%～50%/r/n充氧能力：0.40-0.94kgO/r/n2/r/n/Kw.h/r/n充氧动力效率：7.05-11.74kgO2/Kw.h/r/n本设计取服务面积为/r/n0.7m/r/n2/r/n/个，则此池共需要曝气器为/r/n400/r/n每池设/r/n25/r/n根支管，管长1/r/n1m/r/n，曝气头间距0.5/r/n1/r/nm，每根支管设1/r/n6/r/n个曝气头，共/r/n4/r/n00个。每根支管所需空气量：/r/n反应池充气管管径：/r/n设空气干管流速/r/nV/r/n1/r/n=/r/n15m/r/n/s,/r/n支管流速/r/nv/r/n2/r/n=10m/s,/r/n小支管流速/r/nv/r/n3/r/n=5m/s/r/n干管直径：/r/n取DN/r/n150mm/r/n钢管/r/n校核：/r/n支管直径：/r/n取/r/nDN/r/n50/r/nmm/r/n钢管/r/n校核：/r/n（8）污泥产量计算：/r/n①/r/n由去除BOD产生的污泥：/r/n泥量：/r/n/r/n=0.6（0.85-0.212）/r/n×/r/n1000/r/n=/r/n382.8/r/nkg/r/n污泥含水率为98%，当含水率>95%时，取/r/n污泥产量：/r/n/r/n②/r/n由/r/n进水SS产生的污泥量/r/n：/r/n/r/n/r/n=/r/n24.5m/r/n3/r/n式中/r/n：/r/nCss/r/no/r/n、Css/r/ne/r/n——进、出水SS浓度，mg/L/r/n；/r/nρs——污水密度，/r/nt//r/n；/r/nρ/r/no—/r/n—污水含水率，%/r/n。/r/n由/r/n①/r/n、/r/n②/r/n得/r/n：Ws=19.14+24.5=43.64/r/n/r/nm/r/n3/r/n/d/r/n5、中沉池/r/n/r/n/r/n采用一个辐流式沉淀池，沉淀池的表面负荷取为1.0/r/n/(/r/n·h)，沉淀时间/r/n1.5/r/n/r/nh，污泥停留时间1.5h，池底坡度取0.0/r/n5,/r/n/r/n污泥区高度/r/n1.1/r/nm/r/n，，污泥斗高为/r/n2/r/nm/r/n，超高/r/n0.3m/r/n,缓冲层高度/r/n1m/r/n./r/n（1）沉淀部分水面面积：/r/nF=Q/nq/r/n’/r/n=1000/(24/r/n×/r/n1/r/n×/r/n1)/r/n=/r/n41.7m/r/n（2）池子直径：/r/nD=（/r/n4F/r/n÷π/r/n）/r/n1/2/r/n/r/n=（4/r/n×/r/n41.7/r/n÷/r/n3.14）/r/n1/2/r/n/r/n=/r/n7.3m/r/n取/r/n8m/r/n（3）/r/n沉淀部分有效水深：/r/n/r/nh/r/n2/r/n=q/r/n’/r/n×/r/nt/r/n=1/r/n×/r/n1.5/r/n=/r/n1.5/r/n（4）沉淀部分有效容积:/r/nV/r/n’/r/n=F/r/nh/r/n2/r/n=41.7/r/n×/r/n2/r/n=/r/n83.4m/r/n（5）污泥部分所需容积：/r/n/r/n二沉池所承纳的污泥量为接触氧化池所产生的污泥量。/r/n所以V=Ws=/r/n43.64m/r/n3/r/n（6）污泥斗容积：/r/n/r/nV/r/n1/r/n=/r/nπ/r/nh/r/n5/r/n÷/r/n3/r/n×/r/n(r/r/n1/r/n2/r/n+r/r/n1/r/nr/r/n2/r/n+r/r/n2/r/n2/r/n)/r/n=3.14/r/n×/r/n2/r/n÷/r/n3/r/n×/r/n(2/r/n2/r/n+2/r/n×/r/n1+1/r/n2/r/n)/r/n=/r/n14.65m/r/nh/r/n5/r/n—/r/n污泥斗高度，m；/r/nr/r/n1/r/n—/r/n污泥斗上部半径，取/r/n2m/r/n；/r/nr/r/n2/r/n—/r/n污泥斗下部半径，取/r/n1m/r/n。/r/n（7）/r/n污泥斗以上圆锥体部分污泥容积：/r/nV/r/n2/r/n=/r/nπ/r/nh/r/n4/r/n÷/r/n3/r/n×/r/n(R/r/n2/r/n+R/r/n1/r/nr/r/n1/r/n+r/r/n1/r/n2/r/n)/r/n=3.14/r/n×/r/n1.1/r/n÷/r/n3/r/n×/r/n(4/r/n2/r/n+4/r/n×/r/n2+2/r/n2/r/n)/r/n=/r/n32.24/r/nh/r/n4/r/n—/r/n圆锥体高度，m；/r/nR/r/n—/r/n池子半径，m。/r/n共可储存污泥体积为：V/r/n1/r/n+V/r/n2/r/n=14.65+32.24=46.89>43.64,足够。/r/n（8）沉淀池总高度：/r/nH=h/r/n1/r/n+h/r/n2/r/n+h/r/n3/r/n+h/r/n4/r/n+h/r/n5/r/n=0.3+/r/n1.5/r/n+1+/r/n1.1+2/r/n=/r/n5.9/r/n（9）沉淀池周边处的高度：/r/nh/r/n1/r/n+h/r/n2/r/n+h/r/n3/r/n=0.3+/r/n1.5/r/n+1.1/r/n=/r/n2.9/r/n（10）径深比核算：/r/nD/h2=8/1.5=6.5合格/r/n6、曝气生物滤池/r/n（1）/r/n曝气生物滤池尺寸的确定/r/n:/r/n在进行抱起生物滤池的计算时，首先需计算出滤池内滤料的体积，然后再计算其他部分尺寸滤料的体积可根据BOD容积负荷率/r/nNw/r/n按下式计算：/r/n/r/n式中/r/n设计参数：/r/nQ=1000/r/nm³/d；进水BOD=/r/n212.5/r/nmg/L，出水BOD=20mg/L/r/n取BOD—容积负荷为/r/n4/r/n.0kgBOD/m/r/n3/r/n.d。/r/n=1\*GB3/r/n①/r/n曝气生物滤池滤料体积：/r/n=/r/n48.12m/r/n=2\*GB3/r/n②/r/n滤池总面积：设滤层高H=/r/n3/r/nm/r/n=/r/n16.04m/r/n式中H——滤料层高度，m。/r/n一般滤料层高度H为2.5/r/n—/r/n4.5m，但这要根据工程的实际情况确定，本文中取3.0m。高度过高则所需鼓风机的风压较高，能耗较大；高度过低则所需鼓风机的风压较小，能耗也较低，但滤池总面积增大。/r/n考虑到单座滤池总面积过大会增加反冲洗的供水、供气量，同时不利于布水、布气的均匀，所以在滤池总面积过大时必须分格。一般来说，单格滤池截面积越小则其布水布气越均匀，反冲洗时的供水和供气量也越少，但单格滤池截面积越小则会使整个滤池的土建工程量增加，从而使土建工程投资增加。曝气生物滤池的结构一般可采用圆形、正方形或矩形可以采用公共壁，对于公共壁的正方形或矩形滤池，池形的长宽比对造价也有影响，正方形的周长比矩形要小，所以正方形滤池所需的建筑量最少，本文中建两个池体，单格滤池定为正方形池，则每个池体的面积为A′=/r/n8.02m/r/n2/r/n，取边长a=/r/n3/r/n.0m，则A=2×/r/n3/r/n×/r/n3/r/n=/r/n18/r/n(/r/nm/r/n2/r/n)。/r/n=3\*GB3/r/n③/r/n滤池总高度：/r/n式中：/r/nH/r/n—滤料层高度/r/n，取3/r/nm/r/n；/r/nh/r/n1/r/n—配水区高度/r/n，取/r/n1.2m/r/n；/r/nh/r/n2/r/n—承托层厚度/r/n，取/r/n0./r/n3/r/nh/r/n3/r/n—清水区高度/r/n，取/r/n1.0m/r/n；/r/nh/r/n4/r/n—曝气池超高/r/n，取/r/n0.5m/r/n；/r/nh/r/n5/r/n—承拖板厚度/r/n，/r/n0.1m/r/n。/r/n=3+1.2+0.3+1.0+0.5+0.1/r/n=/r/n6/r/n.1m/r/n=4\*GB3/r/n④/r/n停留时间/r/n式中/r/n：/r/n——滤料层的空隙率（一般取0.5）。/r/n（2）供气量的计算/r/n：/r/n/r/n/r/n生物膜耗费的溶解氧总量一般为1-3mg/l/r/n/r/n通过滤料层后的剩余溶解氧应保持在2-3mg/l/r/n/r/n这样要求污水在进入滤料层前的溶解氧为4-6mg/l左右/r/n需氧量：/r/n=0.8/r/n×/r/n1000/r/n×/r/n10/r/n-3/r/n×/r/n192.5+0.18/r/n×/r/n48.12/r/n×/r/n8/r/n=/r/n223.29kg/r/n/d/r/n=/r/n9.30kg/r/n/h/r/n实际需氧量：/r/n式中/r/n:/r/nα—/r/n氧的水质转移系数（本文取α值为0.5）；/r/nβ—/r/n饱和溶解氧修正系数（本文β值为0.9）；/r/nρ—/r/n修正系数（本文ρ值为1）；/r/n—/r/n最不利水温，℃（本文取/r/n30/r/n℃/r/n；/r/n—/r/n温/r/n(℃)时曝气装置在水下深度处至池液面的平均溶解氧/r/nmg/L/r/n，取9.17mg/L；/r/n—在水温/r/n(℃)时清水中的饱和溶解氧浓度，/r/nmg/L/r/n，取8.4mg/L；/r/n——滤池出水中的剩水溶解氧浓度，/r/nmg/L，取3.0mg/L。/r/n=/r/n29.5kg/r/n/h/r/n供气量/r/n:/r/n计算出曝气生物滤池实际需氧量/r/nRs/r/n后，还需换算成实际所需的空气量/r/nGs/r/n。/r/nGs/r/n与曝气装置和生物滤池的总体氧的利用率/r/nE/r/nA/r/n有关，按下式计算/r/n:/r/n/r/n在曝气生物滤池的运行过程中，曝气不仅提供微生物所需的溶解氧，还起到了强化滤料层的紊动，处境微生物膜的脱落和更新，防止滤料堵塞，有利于污水中的有机物和微生物代谢产物的扩散传递。同时对于上流生物滤池来说，由于空气的携带作用，使进水中的SS被带入滤床深处，对SS的截流起了生物过滤的作用。/r/n（/r/n3/r/n）/r/n供气系统：/r/n①/r/n曝气生物滤池的曝气类型为鼓风曝气，鼓风曝气系统由鼓风机、空气扩散装置（曝气器）和一系列连同的管道组成。鼓风曝气是采用曝气器在水中引入气泡的方式，经过扩散装置使空气形成不同尺寸的气泡，气泡在扩散装置出口形成，尺寸则取决于扩散装置的形成，气泡经过上升和随水循环流动，最后在液面处破裂。鼓风机将空气出送到安装在滤料层底部的扩散装置，这一过程中产生的氧向混合液中转移。/r/n本/r/n设计/r/n中采用专用单孔膜曝气器，每个滤池单孔曝气器的供气量为0.2/r/n—/r/n3/r/nm/r/n3/r/n/（个·/r/nh）/r/n，取曝气器供气量为0.25/r/nm/r/n3/r/n/（个·/r/nh/r/n），则所需曝气器数量/r/nn/r/n为：/r/n/r/n②/r/n空气管道的计算与设计/r/n/r/n空气管道系统是指从鼓风机的出口到空气扩散装置的空气管道，一般使用焊接钢管。小型废水处理站的空气管道系统一般为枝状，而大、中型污水处理厂则宜于连成环状，以保证安全供气。空气干管一般敷设在地面上，接入曝气生物滤池的空气管道应高出出水池水面/r/n0.5/r/nm/r/n以上，以免产生回水现象。空气干管、支管内的空气流速为10/r/n-/r/n15/r/nm/r/n/s/r/n，通向空气扩散装置的竖管、小支管为4/r/n本设计/r/n中空气干管中的空气流速/r/nv/r/n1/r/n取15/r/nm/s/r/n，空气支管中的空气流速/r/nv/r/n2/r/n取10/r/nm/s/r/n，小支管中的空气流速/r/nv/r/n3/r/n为4/r/n-/r/n5/r/nm/s。/r/n池体外干管管径/r/n，取/r/nDN/r/n1/r/n00/r/n无缝碳钢钢管；/r/n校核：/r/n池体内连接支管管径/r/n，取/r/nDN/r/n1/r/n00/r/n无缝钢管；/r/n校核：/r/n池体内小支管管径/r/n，取/r/nDN5/r/n0无缝钢管。/r/n校核：/r/n/r/n/r/n（/r/n4/r/n）/r/n配水系统和承托层：/r/n曝气生物滤池的配水系统一般采用小阻力配水系统，并根据反冲洗形式以采用滤头式、格删式、平板孔式较多。/r/n在本工程设计中，由于单格滤池的面积不是很大，进入滤池的废水比较容易布得均匀，所以配水系统与滤料承托板合建，采用钢制孔板形式。承托板采用100/r/nmm/r/n厚的钢板，钢制孔板开孔孔径/r/nd=10mm/r/n，孔中心间距30/r/nmm/r/n，均匀分布。/r/n由于滤料层采用粒径较小的陶粒做滤料，故不能直接装在钢制承托孔板上，所以在滤料层下部设置承托层。承托层选用鹅卵石，并按一定的级配布置，总高度为0.3/r/nm/r/n。/r/n（/r/n5/r/n）/r/n反冲洗系统计算/r/n:/r/n反冲洗系统在曝气生物滤池的运行中，生物膜渐渐增厚。膜的厚度一般应控制在300/r/n-/r/n400/r/num/r/n，此时生物膜新陈代谢能力强，出水水质好。当膜的厚度超过这一范围时，一方面氧的传递速率减小，导致溶解氧过低，影响微生物的繁殖，生物膜活性变差，同时又抑制丝状菌的生长，结果使去除能力降低，出水水质变坏，另一方面使传质速度减缓，有机物浓度过低，造成营养不足，生物膜难以形成。此外进水中的颗粒物质被截留在滤料深处的填料空隙中，同时生长的过量微生物也被聚集在滤料深处的填料空隙中，随着处理过程的持续运行，填料的空隙减小，一方面加大了滤池的水头损失，另一方面加大了对水流的剪切应力。在达到或接近滤池的设计流量时，当总的水头损失接近通过曝气生物滤池所必需的水头损失或出现截留物质穿透滤层时，曝气生物滤池应停止运行并进行反冲洗。/r/n曝气生物滤池与一般滤池的反冲洗方式大致相同，现阶段用于滤池反冲洗的工艺主要有单一水反冲洗和气-水联合反冲洗两种。本文中使用气-水联合反冲洗的方式。/r/n反冲洗是保证曝气生物滤池正常运行的关键，其目的是在较短的反冲洗时间内使滤料得到适当的清洗，恢复其截污功能，但也不能对滤料进行过分冲刷，以免冲洗掉滤池正常运行必要的生物膜.反冲洗的质量对出水水质、运行周期、运行状况的影响很大.采用气-水联合反冲洗的顺序通常为:先单独用气反冲洗，再气-水联合反冲洗，最后用清水反冲洗.整个反冲洗过程由计算机程序控制，通过计算机自动开启或关闭进出水管和空气管道上的自动阀门来实现/r/n。/r/na/r/n.反冲洗空气量/r/nQ/r/n气/r/n式中/r/n：/r/nS/r/n—需要冲洗的滤池面积，/r/nm/r/n2/r/n[/r/n2/r/n0/r/nm/r/n2/r/n——冲洗空气强度，/r/nL/(s/r/n·/r/nm/r/n2/r/n)。/r/nb.空气反冲洗管管径/r/nDN/r/n滤池布置两根空气反冲洗管，每根空气进气管空气量为/r/n1350/r/nm/r/n3/r/n/s/r/n，取气速/r/nv/r/n1/r/n为/r/n15/r/n则/r/n，选用/r/nDN/r/n=/r/n15/r/n0的无缝碳钢钢管。/r/nc.反冲洗用水/r/n式中/r/n:/r/nq2/r/n—反冲洗水强度，/r/nL/(m/r/n2/r/n·/r/ns)/r/n/r/n[一般取5.0~/r/n10/r/n/r/nL/r/n/(m/r/n2/r/n·/r/ns)/r/n，本文取/r/n8.0/r/n/r/nL/r/n/(m/r/nd.反冲洗水管管径/r/nDN/r/n’/r/n滤池布置两根反冲洗水管，每根水管的水量为/r/n288m/r/n3/r/n/h/r/n，取水速/r/nv/r/n2/r/n为/r/n20/r/nm/r/n则/r/n，选用/r/nDN/r/n=1/r/n00/r/n的无缝碳钢钢管。/r/ne.反冲洗水头/r/nH/r/n反冲洗水使用曝气生物滤池正常工作时出水，由水泵加压供给，反冲洗水头由下式计算：/r/n式中/r/n:/r/nH/r/n—反冲洗需要的水头，/r/nm/r/n；/r/nh/r/n0/r/n—冲洗排水槽与反冲洗排水池最低水位的高程差，/r/nm/r/n（本文取/r/n2.0/r/nm/r/nh/r/n1/r/n—反冲洗池与滤池见冲洗管道的沿程与局部水头损失之和，/r/nm/r/n（本文取/r/n1.5/r/nm/r/nh/r/n2/r/n—管式/r/n小/r/n阻力/r/n配/r/n水系统水头损失，/r/nm/r/n；/r/nh/r/n3/r/n—承托层水头损失，/r/nm/r/n；/r/nh/r/n4/r/n—过滤层在冲洗时的水头损失，/r/nm/r/n；/r/nh/r/n5/r/n—备用水头，/r/nm/r/n（一般取1.5~/r/n2.0/r/nm/r/nα/r/n—配备系统开孔比（25%）；/r/nμ/r/n—孔口流量系数（0.68）；/r/nH/r/na/r/n—承托层高度，/r/nm/r/n；/r/nρ/r/n1/r/n—滤料的密度，陶粒滤料=1.2/r/nt/m/r/n3/r/n；/r/nρ/r/n—水的密度，/r/nρ/r/n=1.0/r/n/r/nt/m/r/n3/r/n；/r/nm/r/n0/r/n—滤料膨胀前的空隙率，陶粒/r/nm/r/n0/r/n=0.55；/r/nH/r/nb/r/n—滤料层膨胀前的厚度，/r/nm/r/n。/r/n则：/r/n；/r/n；/r/n。/r/n所以/r/n：/r/n/r/n根据反冲洗流量和反冲洗水头选择两台型号为350/r/nQw-12/r/n的水泵（一/r/n用/r/n一/r/n备/r/n）。反冲洗排水经收集后，进入冲洗排水池，由潜水泵均匀地输送到预处理构筑物。/r/n（6）污泥产量的计算/r/n污泥由两部分组成，一部分为/r/n，另一部分为消化/r/n而产生的/r/n[14]/r/n。/r/na.由/r/nSS/r/n产生的污泥量/r/nW/r/n1/r/n（含水率99%）/r/nb./r/n消化/r/nBOD/r/n而产生的/r/nVSS/r/n量/r/nW/r/n2/r/n/r/n式中/r/n：/r/n/r/n污泥含水率为98%，当含水率大于95%时取密度为/r/n1000kg/r/n/m3。/r/n污泥产量：/r/n则：W=W/r/n1/r/n+W/r/n2/r/n=14.7+6.72=21.42m/r/n3/r/n/d/r/n二、污泥处理系统/r/n1、贮泥池的设计计算/r/n根据前面计算知，有/r/n以/r/n下构筑物排泥/r/n：/r/n初沉池/r/n/r/n/r/n/r/n65/r/n/r/n/r/n含水率/r/n=98/r/n%/r/n中沉池（接触氧化系统）/r/n43.64/r/n/r/n/r/n含水率/r/n=99%/r/nBAF/r/n生物曝气系统/r/n/r/n21/r/n./r/n42/r/n/r/n/r/n/r/n含水率/r/n=99%/r/n则污水处理系统总排泥量为/r/n。/r/n每天产生污泥的体积Qw/r/n=/r/n130/r/n.06/r/nm/r/n3/r/n,贮泥/r/n池的设计/r/n贮泥/r/n时间为/r/n1/r/n天，/r/n则贮泥/r/n池/r/n的体积应该大于/r/nQw/r/n。/r/n设/r/n贮泥/r/n池为矩形，/r/n贮泥/r/n池/r/n的尺寸为：L×B×H=/r/n8/r/n/r/nm/r/n×/r/n8/r/n/r/nm/r/n×/r/n2.5/r/nm/r/n2、浓缩池的设计计算/r/n本设计采用间歇/r/n式/r/n重力浓缩池/r/n，/r/n由于浓缩池的处理泥量较少，使得池子的体积也比较小，所以浓缩池可以不采用刮渣机。此外，上清液的回流不用采用出水堰，可以直接采用几根上清液的回流管道进行回流。上清液/r/n最后回流至调节池。此外，污泥浓缩池还设置了溢流管道，最后也是流入调节池中。由于二者都流入调节池，可以将两管道合并成一根。/r/n设计参数/r/n①/r/n入流污/r/n泥/r/n固体/r/n浓度：C/r/n0/r/n=/r/n2.0/r/nk/r/ng//r/nm/r/n3/r/n；/r/n污泥含水率/r/n:/r/nP/r/n1/r/n＝/r/n98%；/r/n②/r/n污泥总量/r/n(体积)为沉淀池和好氧池所产生的所有污泥之和为/r/n130.06/r/nm/r/n3/r/n//r/nd/r/n；/r/n③/r/n设计浓缩后含水率P/r/n2/r/n=97.0％；/r/n④/r/n浓缩池污泥固体：取/r/nG=/r/n4/r/n8/r/nkgSS/(m/r/n2/r/n.d)；/r/n/r/n=5\*GB3/r/n/r/n⑤/r/n污泥/r/n停留/r/n时间：T=/r/n1/r/n6/r/nh/r/n；/r/n/r/n⑥/r/n水力负荷/r/n取q=0.3kg/(m/r/n2/r/n·/r/nh)。/r/n（1）/r/n浓缩池表面积：/r/n①/r/n根据固体通量计算浓缩池的表面积/r/nA：/r/n/r/n式中：Q/r/nw/r/n--污泥量，m/r/n3/r/n/d/r/n；/r/nC/r/n0/r/n--污泥固体浓度，g/L/r/n；/r/nG--浓缩池污泥固体通量，kg/(m/r/n2/r/n·/r/nd)/r/n；/r/n/r/n②/r/n根据水力负荷计算浓缩池表面积/r/nA/r/n’/r/n：/r/n/r/n因为/r/nA/r/n’>/r/nA/r/n，故浓缩池的表面积应取/r/n18.06m/r/n2/r/n。/r/n（2）浓缩池直径：/r/n/r/n（3）/r/n浓缩池/r/n浓度污泥层的/r/n高度/r/n为/r/n：/r/n（4）/r/n污泥浓缩后的体积：/r/n/r/n/r/n式中：Qw/r/n--/r/n污泥浓缩前的体积，m3；/r/nQw′/r/n--/r/n污泥浓缩后的体积，m3；/r/nP1/r/n--/r/n污泥浓缩前的的含水率，％/r/nP2/r/n--/r/n污泥浓缩后的的含水率，％/r/n（5）/r/n污泥浓缩池的高度H/r/n1/r/n：/r/n超高取0.5/r/nm/r/n，缓冲层高取0.3/r/nm/r/n。底部直径/r/nD/r/n1/r/n=0.6m/r/n，圆锥倾角为55°，池底坡度造成的深度为0.04/r/nm/r/n。/r/n则/r/n圆锥高度为：/r/nt/r/n所以：/r/n（6）/r/n泥斗的体积为/r/n：/r/n式中/r/n：/r/n/r/n/r/nR/r/n—/r/n池体半径，即/r/nD/2；/r/n/r/n/r/nr/r/n—/r/n下底半径，即/r/nD/r/n1/r/n/2；/r/n圆柱体体积（不含超高/r/n部分）为：/r/n/r/n/r/n/r/n则浓缩池总体积为/r/n＞/r/n130.06/r/nm/r/n3/r/n，/r/n符合/r/n要求。/r/n/r/n图2-/r/n5/r/n污泥浓缩池计算草图/r/n污泥/r/n脱水系统/r/n（1）/r/n污泥脱水前的预处理/r/n:/r/n/r/n预处理的目的在于改善污泥脱水性能，提高脱水效果与脱水设备的生产/r/n/r/n能力，本/r/n设计/r/n采用化学调节法，投加（聚丙烯酰胺）调理污泥，投加量为5/10000，/r/n配成2%的溶液后投加。/r/n（2）/r/n污泥机械脱水/r/n:/r/n/r/n本/r/n设计/r/n中采用带式压滤法进行污泥脱水/r/n。/r/n设计参数/r/n：/r/n/r/n=1\*GB3/r/n/r/n①/r/n设计/r/n处理/r/n泥量/r/n为/r/n：Q/r/n1/r/n=/r/n86.71/r/nm/r/n3/r/n//r/ns/r/n；/r/n/r/n=2\*GB3/r/n/r/n②/r/n压滤前污泥含水率为97%；/r/n/r/n=3\*GB3/r/n/r/n③/r/n压滤后污泥含水率为7/r/n0/r/n%；/r/n/r/n=4\*GB3/r/n/r/n④/r/n压滤时间取T=/r/n3/r/nh/r/n。/r/n工艺流程：/r/n图2-/r/n6/r/n带式压滤脱水工艺流程图/r/n（3）/r/n设计计算/r/n:/r/n污泥体积/r/n：/r/n压滤后污泥含水率为7/r/n0/r/n%/r/n，则/r/n压滤后污泥体积/r/n为/r/n：/r/n/r/n/r/n/r/n/r/n/r/n式中：/r/n—压滤前污泥体积，/r/nm/r/n3/r/n//r/nd/r/n；/r/n/r/n/r/nV/r/n3/r/n—压滤后污泥体积，/r/nm/r/n3/r/n//r/nd/r/n；/r/n/r/n/r/nP/r/n2/r/n—压滤前污泥含水率，%；/r/n/r/n/r/nP/r/n3/r/n—压滤后污泥含水率，%/r/n；/r/n/r/n（4）/r/n机型选取/r/n:/r/n每天压滤机压滤时间为8/r/nh,则进泥量为8.67/r/n÷/r/n8=/r/n1.08m/r/n3/r/n//r/n则选择ZQWT/r/n—/r/n500型带式压滤机。/r/nZQWT/r/n—/r/n500型/r/n带式压滤机工作参数表/r/n滤带宽度（/r/nmm/r/n）/r/n5/r/n00/r/n处理/r/n量（/r/nm/r/n3/r/n//r/nh/r/n）/r/n0.5/r/n～/r/n3/r/n驱动/r/n电机功率（/r/nkw/r/n）/r/n0.75/r/n空压机/r/n功率（/r/nkw/r/n）/r/n1./r/n5/r/n进/r/n浆浓度/r/n（%）/r/n3/r/n～/r/n8/r/n出浆浓度/r/n（%）/r/n30/r/n～/r/n45/r/n主观外形尺寸/r/n（/r/nmm/r/n）/r/n5260/r/n×/r/n1080/r/n×/r/n2360/r/n重量（/r/nkg/r/n）/r/n20/r/n00/r/n带式压滤机采用一个班次（/r/nt=3h/r/n）连续运行，其余时间不运行，故采用扬程为/r/n9.4/r/nm/r/n，流量为/r/n30/r/nm/r/n3/r/n//r/n/r/nh/r/n的/r/n50ZD/r/n型泥浆泵两台（一备一用）。/r/n4、/r/n鼓风机房/r/n（1）/r/n鼓风机的选定与鼓风机房的设计/r/n鼓风曝气系统用鼓风机供应压缩空气，常用的有罗茨鼓风机和离心式鼓风机两种。罗茨鼓风机的气量小但噪声大，一般用于中、小型的污水处理级工业废水处理。离心式鼓风机的特点是气量大、噪声小、效率高、空气量容易控制，只要调节出气管上的控制阀门即可，适用于大、中型的污水处理厂。现在在一些大、中型的污水处理厂常用带变频器的变速率离心式鼓风机，可根据出水混合液中溶解氧的浓度自动调节风机启动台数和转速，节省能耗。/r/n在同一供气系统中，应尽量选用同一型号的鼓风机，一边与备品备件的采购。鼓风机的备用台数在工作鼓风机≦3时，备用1台；在工作鼓风机≧4台时，备用2台。在安装时，每台鼓风机应单设相应基础，基础间距应在1.5/r/n/r/nm/r/n以上。鼓风机应设双电源，以保证安全供电，供电设备的容量应按全部机组同时启动时的负荷设计。/r/n在进行鼓风机房的设计时，应采取防止噪声的措施，使其符合《工业企业厂界噪声标准》和《城市区域环境噪声标准》。/r/n（2）/r/n供气量/r/n据前计算，本处理流程需提供空气的处理构筑物及其供风量如下：/r/n接触氧化池/r/n：/r/n；/r/n曝气生物滤池/r/n：/r/n；/r/n曝气生物滤池反冲洗/r/n：/r/n。/r/n则/r/n鼓风机供风量=/r/n30.11/r/n+/r/n5.85/r/n=/r/n35.96/r/n（/r/n）=21/r/n57.6/r/n（/r/n）/r/n反冲洗鼓风机供风量=/r/n18/r/n=/r/n108/r/n0/r/n（3）/r/n鼓风机的选择/r/n①/r/n反应供气系统/r/n选用两台（一备一用）风量/r/n36/r/n，风压14.7/r/n的罗茨鼓风机。/r/n则可选/r/nRME-150，排气压力为9.8/r/nkpa/r/n,DN150/r/nmm,转速n=1500r/min的/r/n罗茨鼓风机/r/n。/r/n②/r/n反冲洗系统/r/n选用两台（一备一用）风量/r/n18/r/n，风压9.8/r/n的罗茨鼓风机。/r/n则可选RD-100，排气压力为9.8/r/nkpa/r/n,DN/r/n100/r/n/r/nmm/r/n,转速/r/nn/r/n=1750/r/nr/min/r/n的/r/n罗茨鼓风机/r/n。/r/n（4）/r/n鼓风机房的布置/r/n本/r/n设计/r/n中共设置4台鼓风机，鼓风机房建为：平面尺寸12/r/nm/r/n×/r/n5/r/nm/r/n，净高5/r/nm/r/n。/r/n5、/r/n加氯间及药剂仓库/r/n（1）/r/n加氯间/r/n本设计通过加氯消毒，加氯量为10/r/nmg/r/n/L,通过加氯机在进水管道内进行自动投加，进行管道混合，设计接触时间为15/r/nmin/r/n，池体为钢筋混凝土结构；每天的加氯量为：/r/n，/r/n接触池的容积为：/r/n，/r/n则接触池尺寸为：/r/n，其中保护高为0.3/r/nm/r/n。/r/n采用REGAL210加氯机，/r/n其加氯量为0-2/r/n/r/nkg/h/r/n，/r/n选用两台，一用一备。/r/n因为加氯量为1/r/n0/r/nkg/r/n//r/nd/r/n，贮存量按/r/n15/r/n天计，需储备氯量为：/r/n（2）/r/n药剂仓库/r/n药剂仓库和/r/n加药间/r/n合建，内设置/r/n絮凝剂/r/nPAC、pH值调整药剂（/r/nH/r/n2/r/nSO/r/n4/r/n、/r/nNaOH/r/n）、硫酸亚铁（/r/nFeSO/r/n4/r/n）、双氧水（/r/nH/r/n2/r/nO/r/n2/r/n）、P营养盐、/r/nPAM/r/n溶解及/r/n投加装置各/r/n1/r/n套（包括药剂溶解、溶液制备、溶液搅拌和计量投加等设备组成）/r/n，/r/n用于絮凝/r/n、厌氧反应水质调整/r/n和污泥调质反应/r/n池/r/n投药/r/n等/r/n。/r/n三、污水高程的设计计算/r/n各处理构筑物自身和构筑物之间的水头损失计算。/r/n（1）格栅的损失：/r/n自身损失：0.015+0.039=0.054/r/nm/r/n（2）格栅至调节池的损失：/r/n沿程损失：/r/nh/r/n沿/r/n=L/r/ni=10/r/n×/r/n0.01=/r/n0.1/r/n局部损失：h=/r/nξ/r/n=/r/n0.04/r/nm/r/n管道进出口总损失：0.2/r/nm/r/n合计：/r/n0.34/r/n（3）调节池的损失：/r/n跌落水头：/r/n0.05/r/n（4）调节池至初沉池的损失：/r/n沿程损失：/r/nh/r/n沿/r/n=L/r/ni/r/n=10/r/n×/r/n0.01=/r/n0.1/r/n局部损失：h=/r/nξ/r/n=/r/n0.04/r/nm/r/n管道进出口总损失：0.2/r/nm/r/n合计：/r/n0.34/r/n（5）初沉池的损失：/r/n自身损失：/r/n0.2/r/n（6）初沉池至接触池的损失：/r/n沿程损失：/r/nh/r/n沿/r/n=L/r/ni/r/n=10/r/n×/r/n0.01=/r/n0.1/r/n局部损失：h=/r/nξ/r/n=/r/n0.04/r/nm/r/n管道进出口总损失：0.2/r/nm/r/n合计：/r/n0.34/r/n（7）接触氧化池的损失：/r/n自身损失：0.25/r/nm/r/n（8）/r/n接触氧化池至二沉池：/r/n沿程损失：/r/nh/r/n沿/r/n=L/r/ni/r/n=/r/n2/r/n0/r/n×/r/n0.01=0./r/n2/r/nm/r/n局部损失：h=/r/nξ/r/n=/r/n0.04/r/nm/r/n管道进出口总损失：0.2/r/nm/r/n合计：/r/n0.44/r/n（9）二沉池的水头损失：/r/n自身损失：0.55/r/nm/r/n（10）二沉池至曝气生物滤池的损失：/r/n沿程损失：/r/nh/r/n沿/r/n=L/r/ni/r/n=/r/n2/r/n0/r/n×/r/n0.01=0./r/n2/r/nm/r/n局部损失：h=/r/nξ/r/n=/r/n0.04/r/nm/r/n管道进出口总损失：0.2/r/nm/r/n合计：/r/n0.44/r/n（11）曝气生物滤池的损失：/r/n自身损失：0.27/r/nm/r/n（12）曝气生物滤池至出口的损失：/r/n沿程损失：/r/nh/r/n沿/r/n=L/r/ni/r/n=/r/n5/r/n×/r/n0.01=0./r/n05/r/nm/r/n局部损失：h=/r/nξ/r/n=/r/n0.03/r/nm/r/n管道进出口总损失：0.2/r/nm/r/n合计：/r/n0.28/r/n表2-6：/r/n污水高程水力计算表/r/n序号/r/n管渠及构筑物/r/n设计流量/r/nQ/r/n（L/s）/r/n管渠设计参数/r/n水头损失/m/r/n水面标高/r/n（/r/nm/r/n）/r/nD/r/n(/r/nmm/r/n)/r/nI/r/n（%）/r/nV/r/n(/r/nm/r/n/s)/r/nL/r/n(/r/nm/r/n)/r/n沿程/r/n局部/r/n构筑物/r/n合计/r/n1/r/n出水口至/r/n曝气生物滤池/r/n11.57/r/n200/r/n0.01/r/n0.8/r/n5/r/n0.0/r/n5/r/n0.03/r/n0./r/n28/r/n2/r/n曝气生物滤池/r/n2.7/r/n2.7/r/n94.05/r/n3/r/n曝气生物滤池/r/n至/r/n二沉池/r/n11.57/r/n200/r/n0.01/r/n0.8/r/n20/r/n0./r/n2/r/n0.04/r/n0./r/n44/r/n4/r/n二沉池/r/n0./r/n55/r/n0./r/n55/r/n95.04/r/n5/r/n二沉池/r/n至/r/n接触氧化/r/n池/r/n11.57/r/n200/r/n0.01/r/n0.8/r/n20/r/n0./r/n2/r/n0.04/r/n0./r/n4/r/n4/r/n6/r/n接触氧化/r/n池/r/n0./r/n25/r/n0./r/n25/r/n95.73/r/n7/r/n接触氧化/r/n池至/r/n初沉/r/n池/r/n11.57/r/n200/r/n0./r/n0/r/n1/r/n0.8/r/n20/r/n0./r/n2/r/n0.04/r/n0./r/n34/r/n8/r/n初沉池/r/n0./r/n2/r/n0./r/n2/r/n96.27/r/n9/r/n初沉池/r/n至/r/n调节/r/n池/r/n11.57/r/n200/r/n0./r/n0/r/n1/r/n0.8/r/n1/r/n0/r/n0.1/r/n0./r/n04/r/n0./r/n34/r/n10/r/n调节/r/n池/r/n0./r/n05/r/n0./r/n05/r/n96.66/r/n11/r/n调节/r/n池至/r/n格栅/r/n11.57/r/n200/r/n0./r/n0/r/n1/r/n0.8/r/n10/r/n0.1/r/n0.04/r/n0.34/r/n12/r/n格栅间/r/n0.05/r/n4/r/n0.05/r/n4/r/n97.05/r/n五、污水处理厂工程概算/r/n（1）/r/n投资估算/r/n投资估算总共分三个部分进行计算：土建部分投资估算、设备部分投资估算和其他费用估算，其中每部分的估算都要根据具体情况来确定。/r/n/r/n表2-7：土建部分（万元）/r/n序号/r/n构筑物名称/r/n数量/r/n单价/r/n金额/r/n备注/r/n1/r/n格栅间/r/n30/r/n0.1//r/nm/r/n2/r/n3./r/n0/r/n砖混、半地下/r/n2/r/n调节池/r/n462/r/n0.06//r/nm/r/n3/r/n27./r/n8/r/n钢混、地下/r/n3/r/n初沉池/r/n114.48/r/n0.06//r/nm/r/n3/r/n6./r/n9/r/n钢混/r/n4/r/n接触氧化池/r/n1/r/n0.06/r/n//r/nm/r/n3/r/n66/r/n钢混/r/n5/r/n中/r/n沉/r/n池/r/n296.42/r/n0.06/r/n//r/nm/r/n3/r/n1/r/n7./r/n8/r/n钢混/r/n6/r/n曝气生物滤池/r/n97.84/r/n0.06/r/n//r/nm/r/n3/r/n5./r/n9/r/n钢混/r/n7/r/n接触池/r/n25/r/n0.06/r/n//r/nm/r/n3/r/n1.5/r/n钢混/r/n8/r/n加药间/r/n30/r/n0.1/r/n//r/nm/r/n2/r/n3/r/n砖混/r/n9/r/n鼓风机房/r/n60/r/n0.1/r/n//r/nm/r/n2/r/n6/r/n砖混/r/n1/r/n0/r/n集泥池/r/n160/r/n0.06/r/n//r/nm/r/n3/r/n9.6/r/n钢混/r/n1/r/n1/r/n污泥浓缩池/r/n167.64/r/n0.06/r/n//r/nm/r/n3/r/n10./r/n1/r/n钢混/r/n1/r/n2/r/n污泥脱水机房/r/n7/r/n0.1/r/n//r/nm/r/n2/r/n7/r/n砖混/r/n13/r/n清水池/r/n84/r/n0.06/r/n//r/nm/r/n3/r/n/r/n5.1/r/n钢混、地下/r/n14/r/n泵房/r/n30/r/n0.1/r/n//r/nm/r/n2/r/n3/r/n砖混、地上/r/n合计/r/n172.7/r/n13.3设备材料投资估算/r/n表2-8：/r/n主要设备/r/n材料估价（万元）/r/n序号/r/n名称/r/n规格/r/n数量/r/n金额（万元）/r/n备注/r/n单价/r/n合计/r/n1/r/n细/r/n格栅/r/nR/r/nS/r/nG/r/n-/r/n127/r/n1/r/n10/r/n1/r/n0/r/n2/r/n粗/r/n格栅/r/nRHG/r/n-/r/n107/r/n1/r/n10/r/n1/r/n0/r/n3/r/n曝气管/r/nABS管/r/n1900/r/n0.001/r/n1.9/r/n4/r/n罗茨鼓风机/r/nRD-100/r/n10/r/n3/r/n30/r/n5/r/n污水泵1/r/n250-LWP/r/n500-10-30/r/n4/r/n0.8/r/n4/r/n6/r/n污水泵2/r/n150-LWP/r/n300-7-15/r/n5/r/n0.6/r/n3/r/n7/r/n二氧化氯发生器/r/nSYCL/r/n-300C/r/n2/r/n3/r/n6/r/n8/r/n汽水分离器/r/n——/r/n3/r/n0.3/r/n0.9/r/n9/r/n污泥泵/r/n50QW/r/n42-9-2/r/n.2/r/n4/r/n0.7/r/n2.8/r/n1/r/n0/r/n管道阀门/r/n——/r/n——/r/n——/r/n10/r/n1/r/n1/r/n配电柜电缆/r/n——/r/n——/r/n——/r/n20/r/n1/r/n2/r/n流量计仪表/r/n——/r/n——/r/n——/r/n15/r/n1/r/n3/r/n钢管/r/n——/r/n——/r/n——/r/n5/r/n1/r/n4/r/n带式压滤机/r/n2/r/n2.5/r/n5/r/n1/r/n5/r/n弹性立体填料/r/n——/r/n60/r/n0.01//r/nm/r/n3/r/n6/r/n1/r/n6/r/n三相分离器/r/n玻璃钢防强腐蚀/r/n360/r/n0.05/r/n18/r/n17/r/n混凝沉淀搅拌机/r/nQWJ418-36-800-G/r/n2/r/n1.2/r/n2.4/r/n18/r/n曝气头/r/nYC-280/r/n3000/r/n套/r/n0.0003/T/r/n0.9/r/n19/r/n药剂费/r/n---/r/n0.5/r/n吨/r/n0.12/吨/r/n0.06/r/n合计/r/n150.96/r/n13.3总投资估算/r/n表2-9：/r/n投资/r/n估算/r/n汇总表/r/n（万元）/r/n序号/r/n项目名称/r/n总价(/r/n万/r/n元)/r/n备注/r/n1/r/n土建费/r/n用/r/n172.7/r/n2/r/n设备费/r/n用/r/n150.96/r/n3/r/n设备安装费/r/n用/r/n22.65/r/n（2）*