连续或间歇进水的SBR工艺反应池的工程设计计算

连续或间歇进水的SBR工艺反应池的工程设计计算,,,,,,,,,,,,,,,,,

计算项目：10000m3/d城市污水处理工程多方案比较,,,,,,,,计算人：,,,,,,,,,

,,,,(2005/08),,,,,,,,,,,,,

序号,计算项目,符号,单位,举例数据,方案1,方案2,方案3,计算公式或备注,,,,,,,,,

"本计算表格是本公司根据天津市市政设计研究院周雹和中国市政工程华北设计研究院周丹两位给排水专家联合发表的《推荐一种新的SBR工艺设计计算方法》论文（详见《给水排水》2005年第4期）编制的，该计算方法借鉴了德国ATV标准A131E《单段活性污泥污水处理厂的设计》（2000年版）和日本下水道事业团主编的《序批式活性污泥法设计指南》（1990年版），结合了近年来国内诸多SBR工艺的设计经验，可谓是完善化的SBR工艺的简便计算方法。计算表格更加彻底地量化了两位专家的设计思想，表格中的“举例数据”栏是上述论文数据,建议不要删除，方案1、方案2、方案3的项目设计数据可以删除。",,,,,,,,,,,,,,,,,

1,外部条件,,,论文原例,选用HLB型滗水器,选用浮筒式滗水器,选用旋转式滗水器,,,,,,,,,,

1.1,设计规模,Q,m3/d,50000,10000,10000,10000,,,,,,,,,,

1.2,日变化系数,Kd,,1.17,1.2,1.2,1.2,,,,,,,,,,

1.3,总变化系数,KT,,1.38,1.42,1.42,1.42,,,,,,,,,,

1.4,进水BOD5,Lj,mg/L,150,185,185,185,,,,,,,,,,

1.5,进水CODCr,Cj,mg/L,330,300,300,300,,,,,,,,,,

1.6,进水SS,Sj,mg/L,200,183,183,183,,,,,,,,,,

1.7,进水TN,Nj,mg/L,35,34,34,34,,,,,,,,,,

1.8,出水BOD5,Lch,mg/L,20,20,20,20,,,,,,,,,,

1.9,出水CODCr,Cch,mg/L,100,100,100,100,,,,,,,,,,

1.10,出水SS,Sch,mg/L,20,20,20,20,,,,,,,,,,

1.11,出水TN,Nch,mg/L,15,15,15,15,,,,,,,,,,

1.12,设计最低水温,T,℃,10,12,12,12,按最低温度计算池容和曝气量以满足冬季需要,,,,,,,,,

1.13,污泥指数,SVI,mL/g,150,160,160,160,按《污泥指数取值》附表取值,,,,,,,,,

2,选定参数,,,,,,,,,,,,,,,,

2.1,周期时长,TC,h,6,6,6,6,一个完整周期的时间,,,,,,,,,

2.2,周期数,N,次/天,4,4,4,4,每天单池最多运行周期次数,,,,,,,,,

2.3,反应时间,TF,h,4,4,4,4,仅指反应池反应阶段的时间,,,,,,,,,

2.4,沉淀时间,Ts,h,1,1,1,1,仅指沉淀池(亦反应池)沉淀阶段的时间,,,,,,,,,

2.5,滗水时间,Tch,h,1,1,1,1,仅指沉淀池(亦反应池)滗水阶段的时间,,,,,,,,,

2.6,池水深度,H,m,5,4.5,4.5,4.5,本表以池底顶面标高为±0.000为相对高程基准,,,,,,,,,

2.7,安全高度,Hf,m,0.7,0.1,0.5,0.8,"预留堰口至污泥界面的高度,以防止污泥被带出",,,,,,,,,

2.8,保护层水深,Hp,m,0.25,0.3,0.8,0.1,"堰口淹没深度,以防止浮渣被带出",,,,,,,,,

3,计算污泥量,,,,,,,,,,,,,,,,

3.1,设计水量,Qd,m3/d,58500,12000,12000,12000,Qd=KdQ,,,,,,,,,

3.2,好氧泥龄,θCN,d,7.4,8.0,8.0,8.0,"θCN=3.4F·1.10315-T其中：BOD5<1200kg/d,F=1.8;BOD5≥6000kg/d,F=1.45)",,,,,,,,,

3.3',反应泥龄试算值,θ'CF,d,11.0,10.0,10.0,10.0,θ'CF=θCN/(1-2.9Nd/(0.75Lj*OVc'),,,,,,,,,

,,,,,,,,式中：Nd=Nj-0.05(Lj-Lch)-NCH,,,,,,,,,

,,,,,,,,OVc'=0.56+0.15·1.072T-15/(0.67/θCN+0.17·1.072T-15),,,,,,,,,

3.3,反应泥龄,θCF,d,11.0,10.1,10.1,10.1,OVc=0.56+0.15·1.072T-15/(1/θ'CF+0.17·1.072T-15),,,,,,,,,

3.4,缺氧泥龄,θCD,d,3.6,2.1,2.1,2.1,θCD=θCF-θCN,,,,,,,,,

3.5,总泥龄,θC,d,16.5,15.1,15.1,15.1,θC=θCF·TC/TF,,,,,,,,,

3.6,污泥产率系数,Y,kgSS/kgBOD5,1.148,0.945,0.945,0.945,Y=K(0.75+0.6Sj/Lj-0.8*0.17*0.75θCF1.072T-15/(1+0.17θCF1.072T-15);其中：K=0.9~0.95,,,,,,,,,

3.7,反应池污泥总量,ST,kg,144133.5191,28246,28246,28246,ST=QdθCY(Lj-Lch)/1000,,,,,,,,,

4,计算反应池池容,,,,,,,,,,,,,,,,

4.1,给定最高日最高时流量,Qh,m3/h,2880,556,556,556,,,,,,,,,,

4.2,实际沉淀时间,T's,h,1.83,1.83,1.83,1.83,T's=Ts+Tch-1/6,,,,,,,,,

4.3,反应池池容(间歇进水),V,m3,49137,8342,10403,9443,V=STSVI{Hf+Hp+[(Hf+Hp)2+62400QhHT's/(STSVI·N)]1/2}/(1300T's),,,,,,,,,

,反应池池容(连续进水),V,m3,45773,7688,9781,8803,V=STSVI{Hf+Hp+[(Hf+Hp)2+62400QhHT's·(1-Tch/Tc)/(STSVI·N)]1/2}/(1300T's),,,,,,,,,

,,,,,,,,,,,,,,,,,,

5,其他参数,,,,,,,,,,,,,,,,

5.1,缺氧反应时段,TD,h,1.3,0.8,0.8,0.8,TD=TF/(1+θCN/θCD),,,,,,,,,

5.2,好氧反应时段,TO,h,2.7,3.2,3.2,3.2,TO=TF-TD,,,,,,,,,

5.3,间歇进水滗水深度,ΔH,m,1.76,1.80,1.44,1.59,ΔH=24Qh·H/(N·V),,,,,,,,,

,连续进水滗水深度,ΔH,m,1.57,1.63,1.28,1.42,ΔH=24Qh·H/(N·V)·(1-Tch/TC),,,,,,,,,

5.4,高水位时污泥浓度,NWT,g/L,2.93,3.39,2.72,2.99,NWT=ST/V,,,,,,,,,

5.5,低水位时污泥浓度,NWL,g/L,4.52,5.64,4.00,4.63,"NWL=ST·H/(V·HL),指刚进水时曝气混合的浓度",,,,,,,,,

5.6,污泥负荷,FW,kgBOD5/kgMLSS·d,0.091,0.118,0.118,0.118,FW=Lj/[θCY(Lj-Lch)]·TC/TF,,,,,,,,,

5.7,水力停留时间,t,h,20.2,16.7,20.8,18.9,t=24V/Qd,,,,,,,,,

5.8,间歇进水方式池数选择,n,格,6,3,3,3,尽可能同时满足：（1）n≥2,,,,,,,,,

,,,,,,,,（2）n=k1TC,,,,,,,,,

,,,,,,,,（3）n=k2Tc/Tch,,,,,,,,,

,,,,,,,,（4）n=k3Tc/To,,,,,,,,,

5.9,单池容积,Vi,m3,8189,2781,3468,3148,Vi=V/n,,,,,,,,,

5.10,单池面积,Fi,m2,1638,618,771,699,Fi=Vi/H,,,,,,,,,

5.11,单池贮水容积,ΔVi,m3,2880,1112,1112,1112,ΔVi=Vi·ΔH/H,,,,,,,,,

5.12,计算最低水位,HL,m,3.24,2.70,3.06,2.91,HL=H-ΔH,,,,,,,,,

5.13,计算最低泥位,Hs,m,2.29,2.30,1.76,2.01,Hs=H-Hp-ΔH-Hf,,,,,,,,,

5.14,单池宽度,B,m,16.5,14.40,16.00,15.30,按方形池分割方案：B=(Fi/n)1/2,,,,,,,,,

5.15,单池长度,L,m,99.1,42.90,48.20,45.70,L=Fi/B,,,,,,,,,

5.16,方形池实际总面积,As,m2,9827,1853,2314,2098,"As=nBL,未考虑隔墙面积",,,,,,,,,

5.17,方形池实际总体积,Vs,m3,56999,9452,11799,10698,"Vs=As·Hz,未考虑隔墙体积",,,,,,,,,

5.18,池子超高,H1,m,0.8,0.6,0.6,0.6,H1取0.6~0.8m,,,,,,,,,

5.19,池子总深度,HZ,m,5.8,5.1,5.1,5.1,Hz=H+H1,,,,,,,,,

5.20,单池进水流量,Qj,m3/h,1440,556,556,556,Qj=ΔVi/2，进水时间按2h计算,,,,,,,,,

5.21,单池设滗水器台数,nb,台,1,1,1,1,,,,,,,,,,

5.22,单台滗水器流量,Qb,m3/h,2880,1112,1112,1112,Qb=ΔVi/(nb·Tch),,,,,,,,,

5.23,排水沟沟底比池底高,H0,m,1.20,2.210,2.210,2.210,根据工程条件确定排水沟沟底高程后即得到H0,,,,,,,,,

5.24,排水终了前排水沟水深,δ,m,0.60,0.050,0.050,0.180,根据排水沟坡度和滗水流量计算确定,,,,,,,,,

5.25,最大水头,Hmax,m,3.20,2.240,2.240,2.110,Hmax=H-H0-δ(沟底比池底低时:Hmax=H+H0-δ),,,,,,,,,

5.26,最小水头,Hmin,m,1.4,0.440,0.797,0.520,Hmin=Hmax-ΔH,,,,,,,,,

5.27,单台滗水器流量要求,Qa,m3/h,3168,1223,1223,1223,"Qa=(1+10%)Qb,按规定设备能力富裕10%",,,,,,,,,

5.28,滗水器选型,Mod,,HLB1223-0.44-1.8/4.5-500PA,,FT1223,XB1223,HLB、FT、XB分别代表浮动式、浮筒式、旋转式的滗水器,,,,,,,,,

,,,,,,,,,,论文例子：6池运行状态排布图,,,,,,,

6,生物选择器与回流,,,,,,,按反应池与沉淀池合建方式（一体化池）,,,甲,乙,丙,丁,戊,己,

6.1,占反应池体积之比,P,%,21.8%,14.0%,14.0%,14.0%,P=100θCD/θC,,1,进水,,,,,,

6.2,生物选择器单池体积,V1,m3,1789,389,485,440,V1=P·Vi,,2,进水,,,,,,

6.3,生物选择器单池长度,L1,m,21.7,6.00,6.74,6.39,L1=P·L，宽度与反应池相同,,3,,进水,,,,,

6.4,回流比,R,%,30%,30%,30%,30%,可根据工艺的差异选取恰当的回流比,,4,,进水,,,,,

6.5,回流时间,TR,h,2.0,2.0,2.0,2.0,指每周期运转时间，一般与进水时间相同,,5,,,进水,,,,

6.6,回流泵设计流量,QR,m3/s,0.06,0.023,0.023,0.023,QR=R*Qj/(3600·TR),,6,,,进水,,,,

6.7,回流泵设计扬程,HR,mH2O,6.0,5.5,5.5,5.5,需经阻力计算确定,,7,进水,,,进水,,,

6.8,回流泵同时运行台数,nR,台,1,1,1,1,指单池运行台数,,8,进水,,,进水,,,

6.9,回流泵备用台数,nR1,台,0,0,0,0,指单池备用台数,,9,,进水,,,进水,,

6.10,单台回流泵设计流量,QR1,m3/s,0.060,0.023,0.023,0.023,QR1=QR/nR,,10,,进水,,,进水,,

6.11,回流泵有效功率,Nc,kW,3.5,1.2,1.2,1.2,Nc=1000QR1*HR/102,,11,,,进水,,,进水,曝气

6.12,回流泵综合效率,ηZ,%,68.0%,61.5%,61.5%,61.5%,将泵效率和电机效率相乘得到综合效率,,12,,,进水,,,进水,曝气

6.13,回流泵需配电机功率,Nb,kW,5.2,2.0,2.0,2.0,Nb=Nc/ηZ,,13,进水,,,进水,,,曝气

6.14,回流泵配电机额定功率,Ne,kW,5.5,2.2,2.2,2.2,按电机产品功率参数选择或与回流泵配套购置,,14,进水,,,进水,,,曝气

7,剩余污泥与排出,,,,,,,,,15,,进水,,,进水,,沉淀

7.1,污泥增值系数,a,,0.7,0.7,0.7,0.7,0.5~0.7,,16,,进水,,,进水,,滗水

7.2,污泥自身氧化率,b,,0.04,0.04,0.04,0.04,0.04~0.1,,17,,,进水,,,进水,曝气

7.3,每天污泥净产量,SGw,kg/d,8731,1871,1871,1871,SGw=ST/θC,,18,,,进水,,,进水,曝气

7.4,去除每千克BOD产泥量,x,kg/kgBOD,0.262,0.361,0.361,0.361,x=a-b/Fw,,19,进水,,,进水,,,曝气

7.5,剩余污泥排出浓度,NW1,g/L,8.0,8.0,8.0,8.0,根据污泥性质确定,,20,进水,,,进水,,,曝气

7.6,每天排剩余污泥体积,VSG,m3/d,1091,234,234,234,VSG=SGw/NW1,,21,,进水,,,进水,,沉淀

7.7,单池周期排泥体积,Vsi,m3,45,19,19,19,Vsi=VSG/(n·N),,22,,进水,,,进水,,滗水

7.8,每次排泥时间,Tp,min,10,10.0,10.0,10.0,一般在排水后期排泥,,23,,,进水,,,进水,曝气

7.9,剩余污泥泵设计流量,Qs,m3/s,0.076,0.032,0.032,0.032,Qs=Vsi/(60Tp),,24,,,进水,,,进水,曝气

7.10,剩余污泥泵设计扬程,Hs,mH2O,9.0,8.0,8.0,8.0,需经阻力计算确定,,次1,进水,,,进水,,,曝气

7.11,剩余污泥泵选用台数,ns,台,1,1,1,1,指单池运行台数,,次2,进水,,,进水,,,曝气

7.12,单台泵设计流量,Qs1,m3/s,0.076,0.032,0.032,0.032,Qs1=Qs/ns,,次3,,进水,,,进水,,沉淀

7.13,剩余污泥泵有效功率,Nc,kW,6.7,2.5,2.5,2.5,Nc=1000Qs1*Hs/102,,次4,,进水,,,进水,,滗水

7.14,剩余污泥泵综合效率,ηZ,%,74.1%,68.4%,68.4%,68.4%,将泵效率和电机效率相乘得到综合效率,,次5,,,进水,,,进水,曝气

7.15,剩余泵需配电机功率,Nb,kW,9.0,3.7,3.7,3.7,Nb=Nc/ηZ,,次6,,,进水,,,进水,曝气

7.16,剩余泵配电机额定功率,Ne,kW,11,4.0,4.0,4.0,按电机产品功率参数选择或与回流泵配套购置,,次7,进水,,,进水,,,曝气

8,耗氧量计算,,,,,,,,,次8,进水,,,进水,,,曝气

8.1,每天去除BOD的量,BOD,kg/d,7605,1980,1980,1980,BOD=Qd(Lj-Lch)/1000,,次9,,进水,,,进水,,沉淀

8.2,碳的氧当量,a,,1.466,1.466,1.466,1.466,根据污水性质试验确定，或参照同类项目取值,,次10,,进水,,,进水,,滗水

8.3,每天去除总氮的量,NH,kg/d,1170,228,228,228,,,,,,,,,,

8.4,活性污泥含氮量,P,%,12.5%,12.5%,12.5%,12.5%,,,3池运行状态排布图,,,,,,,

8.5,氨氮的氧当量,b,,4.6,4.6,4.6,4.6,根据污水性质试验确定，或参照同类项目取值,,,甲,乙,丙,,,,

8.6,细菌细胞的氧当量,c,,1.42,1.42,1.42,1.42,,,1,进水,,,,,,

8.7,反消化回收氧系数,d,,2.90,2.90,2.90,2.90,,,2,进水,,,,,,

8.8,反消化氨氮量,NO,kg/d,0,0,0,0,不考虑反消化回收的氧,,3,,进水,,,,,

8.9,每天排出的活性污泥量,Vss,kg/d,1992,714,714,714,Vss=x·BOD,,4,,进水,,,,,

8.10,设计需氧量,AOR,kg/d,12556,2527,2527,2527,AOR=a·BOD+b·NH-(c+p·b)Vss-d·NO,,5,,,进水,曝气,,,

8.11,去除每千克BOD耗氧量,Ro,kg/kgBOD,1.65,1.28,1.28,1.28,Ro=AOR/BOD,,6,,,进水,曝气,,,

8.12,折算为20℃标准供气量,,,,,,,,,7,进水,,,曝气,,,

8.13,曝气器氧转移效率,E,%,20%,20%,20%,20%,,,8,进水,,,曝气,,,

8.14,气泡离开水面的氧百分比,Ot,%,17.5%,17.5%,17.5%,17.5%,Ot=21(1-E)/[79+21(1-E)],,9,,进水,,沉淀,,,

8.15,曝气器的安装高度,H1,m,0.50,0.50,0.50,0.50,,,10,,进水,,滗水,,,

8.16,当地大气压,P0,Pa,101300,101300,101300,101300,,,11,,,进水,曝气,,,

8.17,曝气器的绝对压力,Pb,Pa,145400,140500,140500,140500,Pb=P0+9800(H-H1),,12,,,进水,曝气,,,

8.18,设计最低水温下氧饱和度,Cs,mg/L,11.20,10.78,10.78,10.78,根据《含氧量与温度关系》表选取或插值法求取,,13,进水,,,曝气,,,

8.19,氧的平均浓度,Csm,mg/L,12.71,11.98,11.98,11.98,Csm=Cs(Pb/202600+100Ot/42),,14,进水,,,曝气,,,

,20℃下的氧平均浓度,Csm(T0),mg/L,10.33,10.11,10.11,10.11,Csm=9.1(Pb/202600+100Ot/42),,15,,进水,,沉淀,,,

8.20,表面活性剂的影响系数,k1,,0.85,0.85,0.85,0.85,选取范围：0.8~0.85,,16,,进水,,滗水,,,

8.21,含盐量的影响系数,k2,,0.90,0.90,0.90,0.90,选取范围：0.9~0.97,,17,,,进水,曝气,,,

8.22,当地大气压的影响系数,k3,,1.00,1.00,1.00,1.00,当地大气压与标准大气压的比值,,18,,,进水,曝气,,,

8.23,污水实际溶解氧浓度,Cl,mg/L,2.00,2.00,2.00,2.00,一般要求的DO值,,19,进水,,,曝气,,,

8.24,标准供气量换算系数,K,,1.57,1.59,1.59,1.59,"K=Csm(T0)/{1.02(T-T0)k1[k2k3Csm(T)-Cl]},T0=20℃",,20,进水,,,曝气,,,

8.25,标准供气量,SOR,kgO2/d,19699,4011,4011,4011,SOR=K·AOR,,21,,进水,,沉淀,,,

8.26,标准供气量,Gs,m3/d,328320,66848,66848,66848,Gs=SOR/(0.3E)，换算为空气量,,22,,进水,,滗水,,,

8.27,气水比,,,5.61,5.57,5.57,5.57,"Gs/Qd,一般要求大于3",,23,,,进水,曝气,,,

8.28,去除每千克BOD供气量,Vo,m3/kg,43.2,33.8,33.8,33.8,Vo=Gs/BOD,,24,,,进水,曝气,,,

9,曝气设备选择,,,,,,,,,,,,,曝气,,,

9.1,鼓风曝气设备选择,,,,,,,,,,,,,曝气,,,

9.1.1,每天曝气的总时间,Tb,h,96,48,48,48,Tb=N·n·TF,,,,,,沉淀,,,

9.1.2,单池最大曝气量,Qb,m3/h,3420,1393,1393,1393,Qb=Gs/Tb,,,,,,滗水,,,

9.1.3,单只曝气器曝气量,Qj,m3/h·个,3.0,3.0,3.0,3.0,,,,,,,,,,

9.1.4,单只曝气器服务面积,Fj,m2/个,0.7,0.7,0.7,0.7,,,,,,,,,,

9.1.5,按曝气量选单池数量,na1,个,1425,580,580,580,na1=Qb/(0.8Qj)，考虑20%富裕量,,,,,,,,,

9.1.6,按服务面积选单池数量,na2,个,3250,1226,1529,1388,na2=Fi/(0.72Fj)，无曝气盲区时利用率为72%,,,,,,,,,

9.1.7,实际单池选取曝气器数量,na,个,3250,1226,1529,1388,"MAX(na1,na2)",,,,,,,,,

9.1.8,实际选用曝气器总数,nz,个,19500,3678,4587,4164,,,,,,,,,,

9.1.9,最多同时曝气的池数,nb,座,4,2,2,2,排列如右图示,,,,,,,,,

9.1.10,最大曝气量,Qmax,m3/h,13680,2785,2785,2785,Qmax=nb·Qb,,,,,,,,,

9.1.11,曝气管网阻力损失,h,m,1.20,1.20,1.20,1.20,根据供气管路和曝气器计算确定,,,,,,,,,

9.1.12,曝气管网漏风系数,k4,,0.10,0.10,0.10,0.10,k4=0.05~0.1,,,,,,,,,

9.1.13,曝气设备的风压,∑h,m,6.20,5.70,5.70,5.70,∑h=H+h,,,,,,,,,

9.1.14,鼓风机计算风量,Qk,m3/h,15048,3064,3064,3064,Qk=Qmax(1+k4),,,,,,,,,

9.1.15,鼓风机运行台数,nb,台,6,2,2,2,,,,,,,,,,

9.1.16,鼓风机备用台数,nc,台,2,1,1,1,,,,,,,,,,

9.1.17,单台鼓风机计算风量,Qj,m3/h,2508,1532,1532,1532,Qj=Qk/nb,,,,,,,,,

9.1.18,单台鼓风机有效功率,Nj,kW,42.33,23.77,23.77,23.77,Nj=9.8Qj·H/3600,,,,,,,,,

9.1.19,总效率,e,%,0.69,0.63,0.63,0.63,将鼓风机效率和电机效率相乘得到综合效率,,,,,,,,,

9.1.20,配套电机计算功率,Nd,kW,61.68,37.73,37.73,