污水处理厂设计计算书软件

1、2021/11/11page. 1民治污水处理厂功能计算书一、前言 本计算书为针对东港溪流域潮万污水下水道系统之民治污水处理厂新建工程设计工作，所进行之处理厂各单元功能计算。本计算书共分十个单元进行计算，除前处理及进流抽水站采用尖峰小时流量为功能设计基准外，其余单元原则上采用最大日流量为功能设计基准。1.00平均日流量 =22,840 cmd =0.264 cms =6.03mgd最小日流量 = 平均日流量 x0.65=14,850 cmd最大日流量 = 平均日流量 x1.33=30,400 cmd尖峰小时流量= 平均日流量 x2.00=45,700 cmd2.00进流 bod5 =200.0

2、 mg/l进流 tss =200.0 mg/l进流 nh3-n =25.0mg/l进流 tp =8.0mg/l3.设计放流水水质出流 bod5 =20.0mg/l出流 tss =20.0mg/l出流 nh3-n =10.0mg/l出流 tp =4.0mg/l4.尖峰小时流量质量平衡计算结果2021/11/11page. 2(1) 污水部份污水名称流量tssbod5tpcmdkg/dmg/lkg/dmg/lkg/dmg/l进流污水45,7009,140200.09,140200.0365.68.0回流水合并3,2171,204.3547.6402.6183.147.521.6初沉池进流48,91

3、710,344211.59,543195.1413.18.4初沉池出流48,7634,13884.97,062144.8367.67.5二沉池出流48,095961.920.0327.06.824.00.5砂滤池出流45,805458.010.024.00.511.50.3浓缩机清洗水72.00.710.00.00.50.020.3脱水机清洗水96.01.010.00.10.50.020.3放流水45,637456.410.023.90.511.40.3浓缩滤液(回流)638.7275.9432.083.3130.417.226.9脱水滤液333.0524.31,57440.6122.0353

4、.91,062.6除磷单元出流水288.3424.51,47316.256.417.761.4(回流)砂滤反洗水(回流)2,290503.9220.0303.1132.312.65.5(2) 污泥部份污泥名称流量tssbod5tpcmdkg/dmg/lkg/dmg/lkg/dmg/l初沉污泥154.26,20740,2412,48116,08645.4294.6废弃活性污泥667.95,3438,0001,6642,492343.3513.9浓缩废弃活性污泥101.25,10050,3781,58115,618326.13,221化学污泥44.82,24850,20924.4544.4336.

5、27,510消化污泥255.511,30744,2584,06215,901371.51,454消化后污泥255.57,91530,981786.93,080371.51,454脱水污泥300.210,16233,848811.32,702707.72,357脱水污泥饼63.29,700153,453770.712,193353.95,5985.最大日流量质量平衡计算结果2021/11/11page. 3(1) 污水部份污水名称流量tssbod5tpcmdkg/dmg/lkg/dmg/lkg/dmg/l进流污水30,4006,080200.06,080200.0243.28.0回流水合并2,1

6、99802.0364.7268.2121.931.614.4初沉池进流32,5996,882211.16,348194.7274.88.4初沉池出流32,4962,75384.74,698144.6244.67.5二沉池出流32,052641.020.0218.06.816.00.5砂滤池出流30,526305.310.016.00.57.60.3浓缩机清洗水72.00.710.00.00.50.020.3脱水机清洗水96.01.010.00.10.50.020.3放流水30,358303.610.015.90.57.60.3浓缩滤液(回流)448.9183.7409.355.4123.411

7、.425.5脱水滤液253.7349.11,37627.0106.6235.4928.0除磷单元出流水223.9282.51,26210.848.311.852.6(回流)砂滤反洗水(回流)1,526335.8220.0202.0132.38.45.5(2) 污泥部份污泥名称流量tssbod5tpcmdkg/dmg/lkg/dmg/lkg/dmg/l初沉污泥102.64,12940,2411,65116,08530.2294.6废弃活性污泥444.23,5548,0001,1072,492228.3514.0浓缩废弃活性污泥67.33,39250,3781,05215,618216.93,22

8、1化学污泥29.81,49550,20916.2544.5223.67,509消化污泥169.97,52144,2582,70215,900247.11,454消化后污泥169.95,26530,980523.43,080247.11,454脱水污泥199.76,76033,848539.62,702470.82,357脱水污泥饼42.06,453153,453512.612,191235.45,5986.平均日流量质量平衡计算结果(1) 污水部份2021/11/11page. 4污水名称流量tssbod5tpcmdkg/dmg/lkg/dmg/lkg/dmg/l进流污水22,8404,568

9、200.04,568200.0182.78.0回流水合并1,696603.3274.3201.891.723.810.8初沉池进流24,5365,171210.84,770194.4206.58.4初沉池出流24,4592,06984.63,530144.3183.87.5二沉池出流24,125482.520.0164.16.812.10.5砂滤池出流22,976229.810.012.00.55.70.3浓缩机清洗水72.00.710.00.00.50.020.3脱水机清洗水96.01.010.00.10.50.020.3放流水22,808228.110.011.90.55.70.3浓缩滤液

10、(回流)355.1138.2389.241.6117.28.624.2脱水滤液214.5262.51,22420.394.7176.9824.7除磷单元出流水192.1212.41,1068.142.38.846.0(回流)砂滤反洗水(回流)1,149252.7220.0152.0132.36.35.5(2) 污泥部份污泥名称流量tssbod5tpcmdkg/dmg/lkg/dmg/lkg/dmg/l初沉污泥77.13,10340,2411,24016,08422.7294.6废弃活性污泥333.72,6698,000831.52,492171.5514.1浓缩废弃活性污泥50.62,5485

11、0,378789.915,618163.03,222化学污泥22.41,12450,20912.2544.7168.07,508消化污泥127.75,65144,2572,03015,900185.71,454消化后污泥127.73,95630,980393.23,079185.71,454脱水污泥150.15,07933,848405.42,701353.72,357脱水污泥饼31.64,848153,453385.112,189176.95,5982021/11/11page. 5二、前处理及污水抽水站1.设计条件粗栏污栅设计采用进流之尖峰小时流量：q = 45,700 cmd进流抽水泵、

12、细栏污栅及除砂池设计采用质量平衡之尖峰小时流量：q = 48,917 cmd2.设计粗拦污栅采用设计条件如下：(请参见 m&e table 9-2)尖峰流量时栅间流速3.00fps = 0.91m/s (0.6 0.99 m/s)平均流量时栅间流速2.00fps = 0.61m/s (0.6 0.99 m/s)最大水头损失0.50ft =0.15m ( 6 in)栅格间距0.2inchs =0.51cm(0.63 in)格栅厚度0.6inchs =1.52cm (0.20.6)选用拦污渠道数 2 (含一台备用)渠道宽度 1.0m，总操作长度1.00m (一台备用)有效空间 0.51cm

13、 /2.03cm =25.0%有效宽度 1.00 m x25% =0.25m尖峰流量时水深45,700 cmd /0.91m/s / 0.25m2.314 m选择渠道深度1.6m (水深水头损失水面上池深 )check: 如果抽水站湿井维持定水位操作, 则在平均流量时栅间流速22,840 cmd /2.31m/s / 0.25m0.457 m/s3.0选用泵浦数3 (外加一台备用)每台泵浦流量 48,917 cmd /3 16,306 cmd =0.19cms4.设计细拦污栅采用设计条件如下：(请参见 m&e table 9-2)最大进入流速3.00fps = 0.91m/s (0.6

14、 0.99 m/s)2021/11/11page. 6平均进入流速2.00fps = 0.61m/s (0.6 0.100 m/s)最大水头损失1.00ft =0.30m栅格间距0.25inches = 0.64 cm(0.63 in)格栅厚度0.2inches = 0.51 cm (0.20.6)拦污渠道数2 (含一台备用)渠道宽度1.2m，总操作长度1.20m有效空间0.64cm /1.14cm =55.6%有效宽度1.20m x55.6%=0.67m尖峰流量时水深48,917 cmd /0.91m/s / 0.67m0.929 m选择渠道深度1.6m (水深水头损失水面上池深 )chec

15、k:平均流量时水深24,536 cmd /0.61m/s / 0.67m0.699 m5.涡流式沉砂池(1)池体计算表面负荷120,000gpd/ft2(西图公司设计指引)4,884 cmd/m2需要面积48,917 cmd / 4,884 cmd/ m2 =10.02 m2选择使用池数2 每池所需面积 10.02m2 /2=5.01m2计算体积：水深 1.4 m,沉砂池直径 2.50m选择直径 3.0 m每池体积 10.18 m3除砂池总体积 10.18 m3 x2=20.36 m3每池负荷 48,917cmd /2=24,459 cmdcheck:各流量下停留时间：平均流量20.36m3

16、x1,440 min/d / 24,536 cmd1.2min最大流量20.36m3 x1,440 min/d / 32,599 cmd0.9min尖峰流量20.36m3 x1,440 min/d / 48,917 cmd2021/11/11page. 70.6min(2)砂浆泵浦选用采用设计条件如下：(西图公司设计指引)砂砾量2.5ft3/mg, 在平均流量下 =18.7m3/106m3或7.0ft3/mg ,在尖峰流量下 =52.4m3/106m3砂砾密度2,600 kg/m3平均流量时之砂砾量18.70 m3/106m3 x24,536cmd0.46cmd1,193 kg/d尖峰流量时砂

17、砾量52.36 m3/106 m3 x48,917cmd2.56cmd6,660 kg/d假设砂浆浓度=1%(西图公司设计指引)砂浆密度 (0.01/2,600 kg/m3 +0.99/1,000 kg/m3 ) -1=1,006kg/m3平均流量时砂浆重1,193 kg/d / 0.01=119,302kg/d尖峰流量时砂浆重6,660 kg/d / 0.01=665,984kg/d平均流量时砂浆体积119,302kg/d / 1,006kg/m3=119cmd尖峰流量时砂浆体积665,984kg/d / 1,006kg/m3=662cmd每一涡流式沉砂池选用2 台砂浆泵浦（一台备用）每台泵

18、浦流量662cmd /2pumps = 331cmd假设每台泵浦操作时间10.0min/hr则每台泵浦相对流量331cmd x60min / 10.0min1,986 cmd2021/11/11page. 8三、初沉池1.设计条件初沉池设计流量考虑平均日,最大日及尖峰小时流量：平均日流量q24,536 cmd最大日流量q32,599 cmd尖峰小时流量q48,917 cmd设计采用去除率如下：tss去除率 60%(一般为5070%,参见m&e section 9-6)bod5去除率28%(一般为2540%,参见m&e section 9-6)初沉污泥泵送以最大日流量设计，依质量

19、平衡计算结果其性质如下：q 102.6 cmdtss 4,129 kg/d = 40,241 mg/lbod51,651 kg/d = 16,085 mg/l2.设计初沉池(1)计算初沉池长度及宽度初沉池之溢流率设计值如下：在平均日流量下 32 48 cmd/m2(m & e table 9-7)，或 30 50 cmd/m2(qasim table 12-1)在最大日流量下 80 120 cmd/m2 (m & e table 9-7)，或 70 130 cmd/m2(qasim table 12-1)在尖峰时流量下 80 120 cmd/m2 (m & e tabl

20、e 9-7)，或 70 130 cmd/m2(qasim table 12-1)采用最大日流量时溢流率 (sor)50.0cmd/m2选用矩型沉淀池数4需要面积 32,599cmd /50.0 cmd/m2 651.98 m2假设长宽比5.0: 15 w x w=652.0 m2 /4得出宽度 w 5.7m，长度 28.5m选择宽度5.8m，长度 30.0m各池面积30.0m x5.8m =174.0 m22021/11/11page. 9总面积4x174.0 m2 =696.0 m2check:平均日流量时溢流率sor 24,536 cmd / 696.0m235.3cmd/m2okok !

21、 !最大日流量时溢流率sor 32,599 cmd / 696.0m246.8cmd/m2ok!ok!尖峰时流量溢流率sor 48,917 cmd / 696.0m270.3cmd/m2okok ! !平均日流量一池停用时溢流率sor 24,536 cmd /3 /174.0 m247.0cmd/m2okok ! !最大日流量一池停用时溢流率sor 32,599 cmd /3 /174.0 m262.5cmd/m2okok ! !尖峰时流量一池停用时溢流率sor 48,917 cmd /3 /174.0 m293.7cmd/m2okok ! !(2)计算初沉池深度初沉池池侧水深一般为 3 4.

22、6m (参见 m&e table 9-8)假设平均水深3.57m初沉池设计尺寸归纳如下(长 x 宽 x 水深)：30.0m x5.8m x3.57 m体积 3.6m x174.0m2 = 621.2 m3检查水平流速24,536cmd4x5.8m x3.57 m x1,4400.21m/min (better 0.3m/min) check:水力停留时间一般为1.52.5 hr (m&e table 9-7)，或1.02.0 hr (qasim section 12-3)平均日流量时水力停留时间621.2 m3 x4x2424,536 cmd2021/11/11page. 10

23、2.43hrokok ! !尖峰小时流量时水力停留时间621.2 m3 x4x2448,917 cmd1.22hrokok ! !(3)计算污泥量及污泥泵依最大日流量时初沉污泥量设计污泥泵假设初沉污泥浓度4.0%(412 %，m&e table 9-9)比重 1.006 kg/l污泥流量 102.6 cmd污泥 tss4,129 kg/day污泥 bod5 1,651 kg/day初沉池共计4池，每池选用污泥泵1台，两池另设一台备用，每台污泥泵每日使用时为4小时，则污泥泵容量102.6cmd /4台 /4hr6.4m3/hr共选用污泥泵6台(4)计算沉水式溢流管(submerged l

24、aunder)长度每池出水量(平均日流量)24,536 cmd /46,134 cmd沉水式溢流管负荷一般为小于 625 cmd/m (西图公司设计指引)取溢流管负荷320.0cmd/m则溢流管长度6,134 cmd / 320.0 cmd/m19.2m选用4根溢流管,每根长度为5.0mcheck:检查尖峰流量时溢流管负荷48,917 cmd/4 /20.0=611.5cmd/mok!ok!2021/11/11page. 11四、曝气池1.设计条件曝气池采用平均日流量作为设计基准，并配合检验尖峰小时流量时情形。依平均日质量平衡计算结果，初沉池出流水性质：q =24,459cmdtss =2,0

25、69kg/d =84.6mg/lbod5 =3,530kg/d =144.3mg/ltp =183.8kg/d =7.5mg/l依尖峰小时质量平衡计算结果，初沉池出流水性质：q =48,763cmdtss =4,138kg/d =84.9mg/lbod5 =7,062kg/d =144.8mg/ltp =367.6kg/d =7.5mg/l二沉池设计面积：二沉池面积1,257m2 =13,526ft22.计算结果摘要回流污泥(ras)q =3.95mgd =14,962cmd废弃污泥(was)q =287.5cmd =0.076mgdtss =2,300kg/dbod5 =2,002kg/d反

26、应槽出流水q =38,581cmdtss =3,107mg/l二沉池出流水q =23,331cmd =6.16mgdtss =20.0mg/l总非溶解性 bod5 6.7mg/l溶解性 bod5 1.8mg/l总磷0.5mg/l3.设计生物反应槽2021/11/11page. 12(1)原进流水水质特性基本假设(参考theory, design and operation of nutrient removal-activated sludge process一书)a.污染负荷平均日流量时：流量，qin，mgd6.4624,459 cmdbod5 ，lb/d7,777144.3mg/l总悬浮固

27、体物，tss，lb/d4,55884.6mg/l总凯氏氮，tkn，lb/d2,15640.0mg/l总磷，tp，lb/d404.97.5mg/l碱度，lb/d as caco310,779200.0mg/l硫化氢，lb/d53.91.0mg/l尖峰小时流量时：流量，qin，mgd12.8848,763 cmdbod5 ，lb/day15,560144.8mg/l总悬浮固体物，tss，lb/d9,11784.9mg/l总凯氏氮，tkn，lb/d4,29840.0mg/l总磷，tp，lb/d810.17.5mg/l碱度，lb/d as caco321,489200.0mg/l硫化氢，lb/d107

28、.41.0mg/lb.进流水质特性总 bod/bod5, r1 =1.47难分解性总凯氏氮(%), tkn1 =4.0难分解溶解性cod(%), cod1 =12.50总悬浮固体物(tss)挥发性固体物(vss) (%), vss175.0难分解之挥发性固体物(%), vss240.0volatile content of nonbiodegradable vss (%), vss390.0cod/vss , r21.42vss之氮含量 (%,n/vss), n1vss8.0vss之磷含量 (%,p/vss), p1vss1.0cod/bod之估计值, r32.21溶解性 bod5/总 bod

29、5之估计值 (%), r475初沉池中各污染物去除率：tss 去除率 (%),rtss60bod5,rbod = rtssx进流水tss/进流水bod5xvss1x(1-vss2)xr2/r1 =2021/11/11page. 13总凯氏氮,rtkn = rtss x 进流水 tss/ 进流水tkn x vss1 x n1vss =总磷,rtp = rtss x 进流水 tss/ 进流水tp x vss1 x p1vss =(2)曝气池中之生化反应机制常数及水质特性a.喜气槽max 20 =10.0day-1， formax 20 =1.04max t =8.42day-1ks =50.0mg

30、/lyg =0.73mg tss/mg bod5kd 20 =0.23day-1， for kd 20 =1.04kd t =0.19day-1挥发性tss (%),vss4 =90.0难分解性vss (%), vss5 =23.0vss之氧当量数 (mg cod/mg vss) , codvss =1.42vss中之氮含量 (%, n/vss) n2vss =12.0bod5/总磷 (mg bod5/mg tp-p), r5 =15.0b.硝化槽max t =0.28day-1kn =0.40mg-n/lkdo =1.30mg/lyn =0.15mg tss/mg no3kdn t =0.0

31、5day-1挥发性tss (%), vss6 =90.0vss中之氮含量 (%, n/vss), n3vss12.0vss中之磷含量 (%, p/vss), p3vss2.0硝化菌之 mcrt ,mcrtn4.3dayc.硝化作用单位需氧量(mg o2/mg no3 generated) =4.60碱度消耗量(mg as caco3/mg no3) =7.20d.脱硝作用单位需氧量 (mg o2/mg no3 denitrified) =2.86碱度产生量 (mg as caco3/mg no3) =3.60e.硫化氢氧化作用2021/11/11page. 14单位需氧量 (lb o2/lb

32、h2s) =2.00(3)操作参数由于设计一vip生物处理法所须考虑之设计参数相当多，除一般活性污泥法所常采用之mlss、f/m及hrt外，尚考虑硝化液回流率(nrcy)，厌气池回流率(arcy)，回流污泥(ras)等，西图公司以多年发展vip系统之经验，建议各参数之设计准则如下：f/m (kg tbod/kg mlvss-day)0.10.2srt (days)515mlss (mg/l)20003500hrt (hours)厌氧槽1.00缺氧槽1.00好氧槽4.010.0合计6.012.0ras (%)4080nrcy(%)100arcy(%)50100a.基本设计条件假设依据民治污水处理

33、厂的背景条件，假设各项操作参数如下。水中溶氧 =2.0mg/l细胞停留时间(mcrt) =10ph =7.20units水温 =15mlss =3,000mg/l好氧槽脱硝率anr =10废弃污泥浓度8,000mg/lnrcy =120b.反应槽体积计算依前述设计准则，假设好氧槽之hrt =6.0hours缺氧槽之hrt =1.0hours厌氧槽之hrt =1.0hours则可得好氧槽总体积 (aer vol)qin x taer6.46mgd x6.0hours1.62mganaanaanxanaanxanxare2021/11/11page. 15缺氧槽总体积 (anx vol)qin x

34、 tanx6.46mgd x1.0hours0.27mg厌氧槽总体积 (ana vol)qin x tana6.46mgd x1.0hours0.27mg已知初沉池出流水 =24,459cmdras = (qin x mlss - q2nd x bodout - qwas x was) / (was - mlss)=3.73mgd =14,122cmd总进流量24,459cmd +14,122cmd38,581cmd =10.19mgd选择反应槽池数 =4池选择反应槽水深 =6.0m已知各槽体之体积如下:总体积 (tot vol) 2.15mg =8,153 m3好氧槽总体积 (aer vol

35、) 1.62mg =6,115 m3厌氧槽总体积 (ana vol) 0.27mg =1,019 m3缺氧槽总体积 (anx vol) 0.27mg =1,019 m3选择四个反应槽总宽度32.0m每一反应槽宽度 =32.0 m /4=8.0 选择反应槽的渠道数 =1每一渠道宽度 =8.0 m /1=8.0每一反应槽之好氧槽长度 =6,115m3 /6.0m /8.0m /4 31.8m选择好氧槽之长度28.0m好氧槽每一分区长度28.0/4=7.0缺氧槽及厌氧槽长度1,019.1m3 /6.0m /4.0m /123.5m选择厌氧槽或缺氧槽之长度为3.5m每一反应槽总长度 =28.0m +3

36、.5m +3.5m +3.538.5manaanaanxanaanxanxare2021/11/11page. 16每一渠道长度 =38.5m /1=38.5m厌氧槽总体积 (ana vol)3.50m x4.00m x6.00m x121,008m3 =0.27mg缺氧槽总体积 (anx vol)3.50m x4.00m x6.00m x121,008m3 =0.27mg好氧槽总体积 (aer vol)7.00m x8.00m x6.00m x165,376m3 =1.42mg反应槽总体积 (tot vol)7,392m3 =1.95mgcheck :厌氧槽之hrtana vol/ qin

37、=0.99 hours缺氧槽之hrtanx vol/ qin =0.99 hours好氧槽之hrtaer vol/ qin =5.27 hours反应槽之总 hrt =7.25hoursmlss = (total tss x mcrt)/(8.34 x total vol) =3,107mg/l(其中total tss系指废弃污泥中之tss量，请见4.固体物产量)f/m = bod loading/ (tot vol x mlss ) =0.11缺氧槽之 f/m =0.81day-1好氧槽之 mcrtaer = (aer vol/tot vol) x mcrt =7.27c.脱氮计算脱氮速率常

38、数 (specific denitrification rate, sdrn) 系指单位时间之单位mlss所能去除之氮量，其计算式为：sdnr20 = 0.03 x f/m + 0.029 (在 20oc下)sdnrt = sdnr20 x 1.06 (t-20)因此本反应槽之sdnr15 =1.87mg/g/hrnox-n (mg/l)浓度计算:无脱硝反应时dno(1+mcrt x kdnt) x nitrifier tss/(qin x 8.34 x yn) = 20.2(其中 nitrifier tss 系指废弃污泥中由硝化反应产生之tss量,请见(4)固体物产量)2021/11/11p

39、age. 17考虑好氧槽脱硝反应时dn1(1- anr) x dno =18.2考虑缺氧槽脱硝反应时dn1 - sdnr x anx hrt x mlss / 1000 =12.4考虑回流nrcy时dn1 /(1+ ras/qin + nrcy/100) =8.3d.回流污泥量计算已知假设回流污泥浓度 =8,000mg/lras = (qin x mlss - q2nd x bodout - qwas x was) / (was - mlss)=3.95mgd =14,962cmdarea =13,526ft2sor =477.7 cmd/m2ras cap =3.60mgd = 19.4sl

40、r =12.4lb/sf-day =2.52kg/m2-hr(4)固体物产量，solids production (lb/d)a.初沉污泥，primary sludgetss = 进流水tss x rtss =6,834lb/d =3,107kg/dvss = 进流水tss x rtss x vss1 =5,126lb/d =2,330kg/d生物可分解性vss = 进流水tss x rtss x vss1 x (1-vss2) =3,075lb/d =1,398kg/db.废弃污泥，waste activated sludge (was)(a)进流之难分解固体物vssa= 进流水 tss x

41、 (1-rtss) x vss1 x vss2 =1,367lb/d =621.3kg/dtss = 进流水 tss x(1-rtss)x(1-vss1/vss3x(1-vss2) =2,278lb/d =1,036kg/d(b)好氧槽之固体物活性tss = 进流水 bod5 x (1-rbod)-qin x bodeff x 8.34) xyg /(mcrt + (1/mcrt+kdt) =1,849lb/d =840.4kg/d2021/11/11page. 18非活性tss = 活性tss x kdt x vss5 x mcrt = =823.5lb/d =374.3kg/d(c)硝化槽

42、tss = yn x (1- n3vss x vss6) x ( 进流水tkn x (1-rtkn)-vssa x n1vss - 好氧槽固体物 x vss4 x n2vss - qin x nh3eff x 8.34 -tkn x tkn1) /(mcrt x (1/mcrt+kdnt) =108.8lb/d =49.4kg/d总固体物，total tss =5,059lb/d = 2,300 kg/d净污泥产生率 = total tss / (进流bod5x(1- rbod)0.91lb tss/lb bod5 applied总 bod5 = 总固体物 / 净污泥产生率5,578lb/d

43、=2,535kg/d废弃污泥所含bod5 =总固体物 x 0.9 x 1.42 x 0.68 + 液体中所含 bod51,999kg/d +2.5kg/d2,002kg/d挥发性固体物比率 =(vssa+好氧槽固体物xvss4+硝化槽tssxvss6)/ (total tss)76.5%活性tss比率 = 活性tss / total tss =36.5%硝化槽污泥比率 = 硝化槽 tss / total tss =2.2%n-content = (vssa x n1vss+好氧槽固体物 x n2vss x vss4+硝化槽tss x vss6 x n3vss) / (硝化槽挥发性固体物比率 x

44、 total tss)10.6%，n/vssp-content = ( 进流水tp x(1-rtp)- qin x 出流水之tp) /(硝化槽挥发性固体物比率 x total tss)8.6%，p/vss(5)出流水水质预估水质项目平均日流量尖峰时流量bod5 (mg/l)难分解性6.77.6溶解性1.82.7tss (mg/l)，假设值20.020.02021/11/11page. 19tkn-n (mg/l)4.013.1nh3-n (mg/l)0.89.9nox-n (mg/l)12.47.9tn (mg/l)16.421.0total-p (mg/l)0.50.5alkalinity

45、(mg/l as caco3)82.6123.2note: residual alkalinity less than 50 mg/l as caco3 indicate need for supplemental alkalinity.附注 : bodeff=出流水之溶解性bod=ks x (1/mcrt+kdt)/(maxt-1/mcrt-kdt)=1.8mg/lnh3eff = 出流水之nh3=knx(1/mcrtaer+kdnt)/(maxt-1/mcrtaer-kdnt)=0.8mg/ltkneff = 出流水之tkn=nh3eff +进流水tkn x tkn1 / (qin x 8

46、.34) +(硝化槽之挥发性固体物比率 x n-content x 出流水tss) =4.0mg/lpeak nox possible =23.36max f/m =1.62srdn =2.72nox w/ sim denite =12.1nox based on denite =7.9nox based on recycle =7.54.空气需求量 理论需氧量为碳水化合物分解、硝化作用及硫化氢氧化各项需氧量之和，再扣除脱硝之释氧量，由下表计算： oxygen requirements (lb/day)item日平均值每日尖峰值(average)(diurnal peak)carbonaceo

47、us5,81711,695nitrogeneous5,0046,640denitrification credit1,1961,701h2s108215net9,73316,849carbonaceous oxygen demand1.04lb o2/lb bod5 applied2021/11/11page. 20total oxygen demand1.74lb o2/lb bod5 applieddiurnal peaking factor1.73理论需氧量(取每日尖峰值)tor =16,849lb/d =7,649kg/d依下式计算标准需氧量sor =toralpha x (beta

48、x cw x dc)- cl x theta (tw-20)c20 x dc其中：alpha=0.8dc=1.06beta =0.9cl=1.0cw =9.17c20 =9.17theta=1.024tw =20计算标准需氧量sor =7,649 /0.64=11,995kg/d传氧效率ote设为0.28空气密度为1.20kg/m3空气中氧含量为23%(重量比)计算空气量11,995kg/d0.28x1.20kg/m3x0.23x1,440105.6cmm各曝气池需要空气量105.6cmm /4=26.42021/11/11page. 212021/11/11page. 2228.3(参考th

49、eory, design and operation of nutrient removal-activated sludge2021/11/11page. 2319.011.32021/11/11page. 24天%anaanaanxanaanxanxare2021/11/11page. 25 mmmanaanaanxanaanxanxare2021/11/11page. 26okok ! !okok ! !okok ! !okok ! !okok ! !days脱氮速率常数 (specific denitrification rate, sdrn) 系指单位时间之单2021/11/11pa

50、ge. 272021/11/11page. 282021/11/11page. 29每日尖峰值(diurnal peak)lb o2/lb bod5 applied2021/11/11page. 30min/dcmmlb o2/lb bod5 applied2021/11/11page. 21五、二沉池1.设计条件二沉池采用平均日流量作为设计基准，并配合检验尖峰小时流量时情形。依前节曝气池计算结果，二沉池进流性质如下：进流水q =38,581 cmdtss =3,107 mg/ltp =183.8 kg/d回流污泥q =14,962 cmdtss =8,000 mg/l尖峰进流流量qp =62

51、,200 cmd依前节曝气池计算结果，废弃污泥性质如下：废弃污泥q =287.5 cmdtss =2,300 kg/dbod5 =2,002 kg/d出流水质依前节曝气池计算结果：总非溶解性 bod5 =6.7mg/l = 156.8 kg/d溶解性 bod5 =1.8mg/l =42.2kg/dtss =20.0mg/l = 466.6 kg/dtp =0.5mg/l =11.7kg/d2.设计二沉池以试误法解得二沉池出流水量=23,331 cmd假设 was 比重1.000 kg/lwas流量 2,300 kg/d x 1,000287.5 cmd8,000 mg/l x 1.000二沉池

52、出流水二沉池进流 ras was=38,581 cmd 14,962 cmd 287.5 cmd=23,331 cmd选择圆型二沉池数42021/11/11page. 22假设溢流率22m3/m2-d (typical 1632, m&e, table 10-12)假设堰负荷200m3/m-d (typical 125250, m&e, p.591)总面积出流量=23,331=1,061 m2溢流率22每池面积1,061=265.1 m24每池直径18.4m选择直径 d 20.0m假设深度3.6m总面积4x /4 x d2 1,257 m213,526 ft2每池出流量(平均日

53、) 23,331 cmd /4=5,833 cmd表面溢流率(sor) =18.6m3/m2-dokok ! !已知堰负荷200.0 cmd/m (125 - 250 cmd/m, m&e, p.591)堰长 x d =62.8m堰负荷92.8m3/m-dcheck:检查下列情况二沉池之固体负荷及溢流率(1)平均日流量a. 固体负荷 = 38,581 cmd x3,107 mg/l1,257 m2 x1,000=3.97kg/m2-hr (4.06.0 kg/m2-hr, m&e, table 10-12)b. 溢流率 =23,331 cmd /1,257m2= 18.57 c

54、md/m2 (1632, m&e, table 10-12)okok ! !(2)尖峰小时流量a.固体负荷62,200 cmd x3,106.54mg/l1,257 m2 x1,000=6.41kg/m2-hr (9.5 kg/m2-hr, m&e, table 10-12)okok ! !b.溢流率 47,238cmd /1,257 m2=37.59 cmd/m2 (4050, m&e, table 10-12)okok ! !(3)平均日流量于一池停机(维护状态)a.固体负荷38,581 cmd x 3,107 mg/l314.2 m2 x3x1,0002021/1

55、1/11page. 23=5.30kg/m2-hr (4.06.0 kg/m2-hr, m&e, table 10-12)okok ! !b.溢流率 23,331cmd314.2 m2 x3=24.76 cmd/m2 (1632, m&e, table 10-12)okok ! !(4)尖峰小时流量于一池停机时(紧急状态)a.固体负荷 =62,200 cmd x 3,107 mg/l314.2 m2 x3x1,000=8.54kg/m2-hr (9.5 kg/m2-hr, m&e, table 10-12)okok ! !b. 溢流率 =47,238 cmd314.2m

56、2 x3= 50.12 cmd/m2 (4050, m&e, table 10-12)okok ! !每一池体积 =3.6m x314.2m2 =1,131 m3(5)平均日流量时水力停留时间水力停留时间 1,131 m3 x4 /38,581 cmd x 24=2.81hrs(6)尖峰小时流量时水力停留时间水力停留时间 1,131 m3 x4 /62,200 cmd x 24=1.75hrs2021/11/11page. 24六、砂滤池1.设计条件根据质量平衡计算结果，砂滤池进流性质如下：最大日流量q32,052 cmdtss641.0 kg/d =20.0mg/lbod5 =218

57、.0 kg/d =6.8mg/l平均日流量q24,125 cmd依最大日流量质量平衡计算结果，砂滤池出流水质如下：tss303.6 kg/d =10.0mg/lbod5 =15.9kg/d =0.5mg/l2.设计砂滤池假设滤率3.0gpm/ft2176.0 m3/m2-d (117-350 m3/m2-d, m&e 11-5)计算所需滤池面积32,052 cmd / 176.0 m3/m2-d182.1 m2选择使用池数2池选择长度20.0m选择宽度5.0m长宽比4.0: 1总过滤面积2x20.0m x5.00m= 200.0 m22,153 ft2check:平均日流量实际滤率 2

58、4,125 /200.0 120.6 m3/m2-dokok ! !最大日流量实际滤率 32,052 /200.0 160.3 m3/m2-dokok ! !平均日流量一池停用实际滤率 24,125 /100.0 = 241.3 m3/m2-dokok ! !最大日流量一池停用实际滤率 32,052 /100.02021/11/11page. 25 = 320.5 m3/m2-dokok ! !3.计算出流水及反冲洗水水质假设出流水tss10.0mg/lbod5去除率50%反冲洗水需要 5%之过滤液1,526 cmd出流水q30,526 cmdtss 出流量 20.0mg/l 10.0mg/l

59、 = 10.0mg/l= 305.3 kg/d出流水bod5 = 6.8mg/l 6.3mg/l 0.5mg/l=16.0kg/d假设砂滤中并不累积bod5及tss，计算反洗水水质如下：tss335.8 kg/d =220.0 mg/lbod5 =202.0 kg/d =132.3 mg/l2021/11/11page. 26七、加氯消毒池1.设计条件依最大日流量质量平衡计算结果，消毒池进流性质如下：q30,526 cmd大肠菌数200,000count/ml依平均日流量质量平衡计算结果，消毒池平均日流量时进流量如下：q22,976 cmd设计放流水质：放流水标准中大肠菌数之规定2,000 c

60、ount/ml选择较安全之大肠菌数设计值1,000 count/ml2.设计加氯消毒池假设最大日流量时 dt =22.5min选择使用池数2池深：宽：长1.0:1.0:40.0池体积 =30,526 cmd /2 /1,440 min/d x22.5min238.5 m3深度 = (238.5 m3 /40.0) 1/3 = 1.81m选择深度 =2.0m宽度 =1.81选择宽度 =1.8m长度 =238.5 m3 /1.80m /1.80m = 73.6m选择长度 =70.0m消毒总体积2x2.0m x1.8m x70.0m504.0 m3平均日流量时停留时间504.0 m3 /30,526 cmd=23.8min选择出流渠道数 = 5每一渠道长度70.0m /5=14.0mcheck :平均日流量下停留时间31.6min2021/11/11pag