双室浮阴床双室阳床计算书阳光

锅炉补给水处理系统工艺计算,,,,,,,

序号,名称,符号,单位,计算公式,来源,结果,

水质资料,,,,,,,

阳离子,,,,,,,

1,Na+,,me/l,,99,4.30,23

2,K+,,mg/l,,1.26,0.03,39

3,Ca2+,,me/l,,6.84,0.34,20

4,Mg2+,,me/l,,7.68,0.64,12

5,Fe2+,,mg/l,,0.03,0.00,28

6,Fe3+,,mg/l,,,0.00,19

合计,,,mg.eq/l,,,5.32,

,,,,,,5.54,配平

阴离子,,,,,,,

1,Cl-,,me/l,,19.1,0.54,35.5

2,SO42-,,mg/l,,66.7,1.39,48

3,NO3-,,mg/l,,0.01,0.00,62

4,HCO3-,,me/l,,194.3,3.19,61

5,CO32-,,mg/l,,5.9,0.20,30

6,NO2-,,mg/l,,0,0.00,46

7,SiO2,,mg/l,,13.7,0.23,60

合计,,,mg.eq/l,,,5.54,

,,,,,,5.54,配平

其它,,,,,,,

1,,,mg/l,,,14,

2,悬浮物,,mg/l,,,47.2,

3,总溶解固形物,,mg/l,,,57,

4,电导率（25℃）,,mg/l,,,6.75,

5,PH,,mg/l,,,9.2,

6,SiO2,,mg/l,,,3.4,

,CODMn,,,,,,

,,,,,,,,

,,,,,,,,

,,,,,,,,

,,,,,,,,

,水处理系统工艺计算,,,,,,

,一、混合床的计算,,,,,,

,系统总处理水量,Q出,,,,800,

,采用交换器台数,,,,,4,

,单台系统出力,q1,吨/时,,,200.00,

,运行流速,v,米/时,,设计取值,50,

,交换器工作台数,n,,,,1,

,1台交换器工作面积,f,米2,f=Q/（v*n）,,4.00,

,交换器直径,d,米,d=1.13√f,,2.26,

,选择交换器直径,d,米,,,2.5,

,实际交换器工作面积,f,,,根据选型实际工作面积,4.91,

,实际正常过滤速度,v,米/时,v=Q1/nf,,40.76,

,一台交换器需树脂体积,,米3,,,,

,阳树脂层装载高度,Hzh,米,,,0.5,

,001X7阳树脂,V1,米3,V1=fHzh,,2.5,

,阴树脂层装载高度,Hzh,米,,,1,

,201X7阴树脂,V1,米3,V1=fHzh,,4.9,

,每周期交换器工作时间,,小时,,,,

,进水中需除去离子总含量,CJ,毫克当量/升,,运行经验数据,0.1,

,阴树脂工作交换容量,EG,克当量/米3,,,250,

,按阳树脂计算,T,小时,T=V1*EG/（Q1*CJ）,,61,

,阳树脂工作交换容量,EG,克当量/升,,,500,

,按阴树脂计算,T,小时,T=V1*EG/（Q1*CJ）,,61,

,反洗流速,v,米/时,,设计取值（阳树脂15米/时，阴树脂6~10米/时）,10,

,反洗时间,t,分,,设计取值,15,

,反洗水量,qF,米3,qF=vft/60,,12.3,

,再生剂的当量（NaOH）,N,克/克当量,,,40,

,再生剂倍率,n,,,查表,5,

,交换器再生用NaOH量,G,公斤,G=V1EGNn/1000,,245.3,

,工业产品中再生剂的含量,ε,%,,,40%,

,折成工业产品的用量,GG,公斤,GG=G/ε,,613.3,

,需4%NaOH量为,GX,公斤,Gx=G/ε,,6132.81,

,稀释40%碱耗水量,qx,米3,qx=(GX-GG)/1000,,5.5,

,4%NaOH溶液的密度,ρ,,,,1.03,

,进碱流速,ν,米/小时,,查表,5,

,进碱时间,t,分,t=60GX/(1000ρfv),,14.6,

,正洗水比耗,α,米3/米3树脂,,强碱性树脂,12,

,正洗阴树脂用水量,qz,米3,qz=αV1,,58.9,

,再生剂的当量（HCl）,N,克/克当量,,,36.5,

,再生剂倍率,n,,,查表,5,

,交换器再生用HCl量,G,公斤,G=V1EGNn/1000,,223.8,需2.5%量为稀释30%碱耗水量

,工业产品中再生剂的含量,ε,%,,,30%,

,折成工业产品的用量,GG,公斤,GG=G/ε,,746.16,

,需4%HCl量为,GX,公斤,Gx=G/ε,,5596.19,

,稀释30%HCl的耗水量,qx,米3,qx=(GX-GG),,4.9,

,4%HCl溶液的密度,ρ,,,,1.02,

,进酸流速,ν,米/小时,,查表,5,

,进酸时间,t,分,t=60GX/(1000ρfv),,13.4,

,正洗水比耗,α,米3/米3树脂,,强酸性树脂,6,

,正洗阳树脂用水量,qz,米3,qz=αV1,,14.7,

,交换器总耗水量,q,米3,q=qF+(qX+qz)酸+(qX+qZ)碱,,384.92,交换器自耗水量：反洗、正洗、稀释

,交换器平均每小时耗水量,q',米3/小时,q'=q/(T+4),,5.89,加入阴离子交换器出力中

,,,,,,,,

,二、双室浮动阴离子交换器的计算,,,,,,

,双室阴离子交换器进水水量,Q2,吨/时,,,805.89,

,运行滤速,v,米/小时,,设计取值,25,

,交换器工作台数,n,,,,5,

,1台交换器工作面积,f,米2,f=Q/（v*n）,,6.45,

,交换器直径,d,米,d=1.13√f,,2.87,

,选择交换器直径,d,米,,,2.8,

,实际交换器工作面积,f,米2,,,6.1,

,实际过滤速度,v,米/小时,v=Q1/（n*f）,,26.06,

,进水中强酸阴离子总含量,cj,毫克当量/升,cj=SO42-+Cl-+NO3-,根据水源水质指标,1.93,

,进水中弱酸阴离子总含量,cj',毫克当量/升,cj'=+HCO3-+HSiO3-+DN,根据水源水质指标,,

,,,,,除碳后残存CO2=5mg/l,0.34,DN=0.50毫克当量/升

,混凝剂用量,DN,,,,0,

,1台交换器一个周期强酸阴离子交换容量,C,克当量,C=Q1CJT/n,,6168.87,

,每周期交换器工作时间,T,小时,,再生时间为4小时,20,

,1台交换器需弱碱阴树脂体积,V1,米,V1=C/EG,,6.17,

,弱碱阴树脂工作交换容量,EG,克当量/米3,,,1000,

,1台交换器中弱碱阴树脂树脂层高度,HZH,米,HZH=V1/f,,1.00,

,,,,,,,,

,1台交换器一个周期弱酸阴离子交换容量,C,克当量,C=Q1CJ'T/n,,1102.36,

,每周期交换器工作时间,T,,,再生时间为4小时,20,

,1台交换器需强碱阴树脂体积,V1,米,V1=C/EG,,5.51,

,修正值,V1',,V1'=1.15*V1,"为防止漏硅酸根,阴树脂需",6.34,

,,,,,"15%的富裕量,所以取系数1.15",,

,强碱阴树脂工作交换容量,EG,克当量/米3,,,200,

,交换器中强碱阴树脂树脂层高度,HZH,米,HZH=V1/f,,1.03,

,,,,,,,,

,1台交换器反洗水量,qF,米3,qF=vft/60,,15.35,

,反洗流速,v,米/小时,,DL/T5068-1996表F.2,10,

,反洗时间,t,分,,DL/T5068-1996表F.2,15,

,1台交换器再生NaOH用量,G,公斤,G=CNn/1000,,872.55,

,再生剂的当量,N,,,,40,

,再生剂倍率,n,,,,3,

,折成工业产品用量,GG,公斤,GG=G/ε,,2181.37,

,工业产品中再生剂的含量,ε,,,,40%,

,需4%NaOH量为,GX,公斤,,,21813.71,

,稀释40%碱耗水量,qX,公斤,,,19632.34,

,转换成体积,,米3,qX/1000,,19.63,

,进碱时间,t,分,t=60GX/(1000ρfv),,51.7,

,40%NaOH密度,ρ,kg/m3,,,1.03,

,进碱流速,v,米/小时,,,4,

,1台交换器正洗用水量,qZ,米3,qz=αV1,,37.52,

,1台交换器正洗水比耗,α,米3/米3树脂,,强碱性树脂,3,

,1台交换器耗水量,q,米3,q=qZ+qX+qF,,72.50,

,阴离子交换器总耗水量,q＇,米3,,,362.52,

,交换器平均每小时耗水量,q',米3/小时,q'=q/(T+4),,15.11,

,,,,,,,,

,三、除碳器的计算,,,,,,

,进水中CO2含量,（CO2）1,毫克/升,（CO2）1=44[HCO3-]+,,153.14,

,,,,22[CO32-]+0.268[HCO3-]3,,,

,进入除碳器的水量,Q3,米3/小时,q=Q1+nq'阴+nq'混床,,838.67,

,除碳器工作台数,n,,,,3,

,1台除碳器工作面积,f,米2,f=q/(b*n),,4.66,

,淋水密度,b,米3/米2.小时,,设计取值,60,

,除碳器直径,d,米,d=1.13√f,,2.44,

,选择除碳器直径,d,米,,选用d=1.5米定型设计设备,2.50,

,除碳器实际工作面积,f,米2,,,4.89,

,填料层高度,H,米,H=R㏑[（CO2）1/（CO2）2],,2.01,

,传质单元高度,R,,,选用d50塑料多面空心球,0.588,

,,,,,水温30。,,

,出水中CO2含量,（CO2）2,毫克/升,,,5,

,1台需填料层体积,V1,米3,V1=fH,,9.85,

,鼓风机的计算风量,QF,米3/小时,QF=KWEαq/n,,5870.71,

,,KWE,,,按水温30度,0.7,

,每处理1米3水需空气量,α,米3/米3树脂,,,30,

,风压,HF,毫米水柱,HF=30H+40,填料层阻力按25mmX25mmX3mm,100.36,

,,,,,瓷环的2/3计算,,

,,,,,,,,

,四、浮动阳离子交换器的计算,,,,,,

,进水中硬度阳离子的总含量,CJ,毫克当量/升,CJ=Ca2++Mg2+,,0.98,

,,,,,,,,

,进水中其它阳离子的总含量,CJ',毫克当量/升,CJ'=K++Na+,,4.34,

,,,,,,,,

,1台交换器一个周期弱碱离子交换容量,C,克当量,C=qTCJ/n,,17842.46,

,交换器工作台数,n,,,,5,

,进入阳离子交换器的水量,q,米3小时,,,838.67,

,运行周期,T,小时,,,20,

,1台交换器需弱酸阳树脂体积,V1,米3,V1=C/EG,,19.82,

,阳树脂工作交换容量,EG,克当量/米3,,,900,

,交换器中弱酸阳树脂层高度,HZH,米,HZH=V1/f,,2.81,

,交换器尺寸,,,为适应树脂装载体积，选用定型设备,,,

,选择交换器直径,d,米,,,3.00,

,实际工作面积,f,米2,,,7.0,

,实际1台交换器过滤速度,v,米/小时,v=q/（f*n）,,23.80,

,反洗水量,qF,米3,qF=vft/60,,17.62,

,反洗流速,v,米/小时,,,10,

,反洗时间,t,分,,,15,

,1台交换器再生用HCl量,G,公斤,G=V1EGNn/1000,,976.87,

,再生剂的当量,N,,,,36.5,

,再生剂倍率,n,,,,1.5,

,折成工业产品的用量,GG,公斤,GG=G/ε,,3256.25,

,工业产品中再生剂的含量,ε,%,,,30%,

,需4%HCl量为,GX,公斤,Gx=G/ε,,24421.86,

,稀释30%HCl耗水量,qx,公斤,qx=GX-GG,,21165.61,

,换算成体积,,米3,,,21.17,

,进HCl时间,t,分,t=60GX/(1000ρfv),,40.8,

,30%HCl密度,ρ,kg/m3,,,1.02,

,进酸流速,v,米/小时,,,5,

,1台交换器正洗用水量,qZ,米3,qZ=αV1,,39.65,

,1台交换器正洗水比耗,α,米3/米3树脂,,,2,

,1台交换器耗水量,q,米3,q=qF+qX+qz,,78.44,

,阳离子交换器总耗水量,q',米3,,,392.18,

,交换器平均每小时耗水量,q',米3/小时,q'=q/(T+4),,16.34,加入阴离子交换器出力中

,,,,,,,,

,离子交换总进水量,Q,米3/小时,,,855.01,

,,,,,,,,

,无阀滤池,,,,,,

,设备出力和台数,,,,,,

,,,,,,,,

,水力加速澄清池,,,,,,

,设备出力和台数,,,,,,

,,,,,,,,

,预沉池,,,,,,

,设备出力和台数,,,,,,

,,,,,,,,

,水箱,,,,,,

,清水箱,,,,,,

,中间水箱,,,,,,

,除盐水箱,,,,,,

,,,,,,,,

,药液贮存槽(罐)和计量箱,,,,,,

,盐酸储存槽,,,,,,

,再生混合床,,,,,,

,30%HCl10天用量,,公斤,GH=10GG,,29846.35,

,混床耗HCL折成工业产品的用量,GG,公斤,GG=nG/ε,,2984.6,注意一个周期的时间

,再生阳离子交换器30%HCl10天用量,GYA,公斤,GYA=10GG,,195374.89,注意一个周期的时间

,阳床耗HCL工业产品的用量,GG,公斤,GG=nG/ε,,16281.24,一周期

,10天共用HCl体积,V,米3,V=GH+GYA/(1000ρ),,195.8,

,30%HCL密度,ρ,千克/米3,,,1.15,

,碱液贮存槽,,,,,,

,再生混合床30%NaOH10天用量,GH,公斤,GH=10GG,,24531.3,

,混床耗NAOH折成工业产品的用量,GG,公斤,GG=G/ε,,2453.1,

,再生阴离子交换器30%NaOH10天用量,GYI,公斤,GYI=10GG,,109068.53,

,阴床耗NAOH折成工业产品用量,GG,公斤,GG=G/ε,,10906.85,

,10天共用体积,V,