卧式天然气分离器工艺计算程序(new)(除液器)

一、工艺委托参数：工作压力P'w：1.3Mpa工作温度：25℃处理气量：200000m3/d液相密度：800kg/m3天然气组分：(Vi%)C1C2C3iC4nC4iC590.765.071.2700.470nC5C6C7N2CO2H2O0.070.1701.620.480.09二、基本参数的确定：1.天然气组分数据：组分百分比Vi(%)分子量(mi)临界压力Pci(Mpa)临界温度Tci(℃)C190.7616.0434.544-82.57C25.0730.074.81632.27C31.2744.0974.19496.67iC4058.1243.6134.97nC40.4758.1243.747152.03iC5072.1513.337187.28nC50.0772.1513.325196.5C60.1786.1782.973234.28C70100.2052.7267.11N21.6228.0133.355-146.89CO20.4844.017.28831.06H2O0.0918.01521.833374.222.天然气分子量M：17.796673.天然气相对密度△g：0.6144414.临界压力Pc:4.630762Mpa5.临界温度T'c：-72.7201℃=200.2799K6.工作温度：t=25℃Tw=t+273=298K7.工作压力Pw:P'w=1.3MPa0.38750.24820.19911.00091大气压下的定压比热Cpi(卡/克.℃)0.52660.40970.38810.38640.38720.38670.38270.3883卧式天然气分离器工艺计算M=∑yimi=△g=M/28.964=Pc=∑Pciyi=T'c=∑yiTci=Pw=P'w+0.1=1.4Mpa(绝）8.对比压力Pr：Pr=Pw/Pc=0.3023269.对比温度Tr：Tr=Tw/T'c=1.48791810.压缩因子Z：Z=1+(0.34Tr-0.6)Pr=0.97154911.1大气压下定压比热C0p：C0pi=∑yiCpi=0.512266(卡/克.℃)C0p=C0piM=9.116635(卡/克.℃)12.标准状态下大气压Ps:Ps=0.1MPa13.标准状态下温度Ts:(To=20℃或0℃）To=20℃Ts=To+273=293K14.标准状态下空气密度ρa(Ts=20℃时取1.205；Ts=0℃时取1.293):ρa=1.205kg/m315.标准状态下气体密度ρgs:ρgs=ρa△g=0.740401kg/m316.分离条件下气体密度ρg:ρg=ρgsPwTs/(PSTwZ)=10.49016kg/m317.分离条件下气体动力粘度μg:x=2.57+0.2781△g+1063.6/Tw=6.310004y=1.11+0.04x=1.3624c=2.415(7.77+0.1844△g)Tw1.5x10-4/(122.4+377.58△g+1.8Tw)=0.01099434μg=cexp[x(ρg/1000)y]=0.011135mPa.s18.液相密度ρ1：ρ1=800kg/m319.阿基米德准数Ar:Ar=d3(ρ1-ρg)gρg/μg2=654.640420.油滴沉降状态处于过渡区，雷诺数Re:Re=0.153Ar0.714=15.6789721.液滴沉降高度与容器直径之比η:η=h/D=0.522.油滴匀速沉降速度ω0:ω0=μgRe/dρg=0.166424m/s23.容器长度与直径之比L/D：3~524.分离器允许气体流速ωgh:ωgh=0.49(3~5)ω0/η=0.489288~0.815479m/s三、分离器外形尺寸的确定：1.处理气量Qgs：200000m3/d2.载荷波动系数β：1.23.气相面积与分离器横截面积之比n:n=[(2η-1)(1-(2η-1)2)1/2+arcsin(2η-1)]/π+1/2=0.54.分离器直径D：D=(1/260)[(QgsPsTwZβ)/(nωghPwTs))]1/2=1.012064~0.78394108m5.分离器实际外形尺寸：直径D=1.2m长度L=8m四、网垫除雾器计算：1.分离条件下气体的实际处理量Qg:Qg=QgsTwPsZ/(PwTs)=14116.11m3/d2.网垫除雾器的气体流速ωg:ωg=K[(ρ1-ρg)/ρg]0.5=0.928264m3/s3.网垫面积A:A=Qg/(86400ωg)=0.176007m24.丝网单丝直径D0:0.00015m5.斯托克斯准数St:St=d2ρ1ωg/(18μgD0)=2.470116.单丝的捕集效率η:查图3-27η=0.787.捕雾效率E:0.988.网垫比表面积a:590m2/m39.除雾器网垫厚度H:H=-3πln(1-E)/(2aη)=0.040059m10.丝网除雾器直径Ds：Ds=(4A/π)1/2=0.473511m实际取值：Ds=m五、分离器进出口管确定：1.进口管气体流速V1:V1=20m/s2.出口管气体流速V2:V2=15m/s3.进口管直径确定d1:d1=103[4Qg/(πV1)]1/2=101.986mm4.进口管直径确定d2:d2=103[4Qg/(πV2)]1/2=117.7633mm进口管实际取值：DN=mm出口管实际取值：DN=mm六、安全阀的计算：1.安全阀的安全泄放量Ws：Ws=Qgρg/24=6170.012kg/h2.分离器设计压力P:P=0.4MPa3.安全阀出口侧压力（绝）P0：P0=0.1Mpa4.安全阀开启压力Pz：Pz=P=0.4Mpa5.安全阀排放压力(绝）Pd：Pd=1.1P+0.1=0.54Mpa6.气体绝热系数k：Cpi0=∑yiCpi=0.512266Cp0=Cpi0M=9.116635查图2-27△Cp=0.07Cp=Cp0+△Cp=9.186635查图2-29Cp-Cv=2Cv=Cp-5=7.186635k=Cp/Cv=1.2782947.临界条件：P0/Pd=0.185185(2/(k+1))k/(k-1)=0.54968114条件判别：属于：临界状态8.气体特性系数C：C=520[k(2/(k+1))(k+1)/(k-1)]1/2=344.9209169.安全阀额定泄放系数K:K=0.6510.安全阀排放面积A：A=WS/(7.6x10-2CKPd(M/ZTw)1/2=2704.686mm211.安全阀数量N：N=2个12.安全阀喉径d0：d0=(4A/（N*π))1/2=41.50578mm结论：安全阀选用A44Y-16C公称直径DN100数量：2个N2CO2C1C2C3C4C5C61.620.4890.765.071.270.470.070.17H2S0.09