化工原理课程设计甲苯,二甲苯

课程设计说明书设计题目：双组份连续精馏筛板塔的设计学院、系：专业班级：学生姓名：指导教师：成绩：20年月日目录TOC\o"1-5"\h\z\o"CurrentDocument"第一部分工艺设计计算4\o"CurrentDocument"1.1物料衡算：4\o"CurrentDocument"1.2塔顶温度、塔底温度及最小回流比的计算：5\o"CurrentDocument"1.3确定最佳操作回流比与塔板层数：6\o"CurrentDocument"1.3.1列相平衡关系式：6\o"CurrentDocument"1.3.2列操作线方程：7\o"CurrentDocument"1.3.3由塔顶向下逐板计算精馏段的汽、液相组成:7\o"CurrentDocument"1.3.4由进料口向下逐板计算提馏段的汽、液相组成:7\o"CurrentDocument"1.3.5逐板法计算塔板层数：7\o"CurrentDocument"1.3.6对上表塔板数列表：14\o"CurrentDocument"1.3.7绘制R-Nt曲线，确定最佳操作回流比及最佳理论板数：14\o"CurrentDocument"1.3.8查取塔板效率：14\o"CurrentDocument"1.3.9计算全塔理论板数：15第二部分设备设计计算152.1塔板结构计算：（设计塔顶第一块板）152.1.1计算塔顶实际的汽液相体积流量：15\o"CurrentDocument"2.1.2选取塔板间距Ht:162.1.3计算液泛速度Uf（Umax）:16\o"CurrentDocument"2.1.4空塔气速：16\o"CurrentDocument"2.1.5选取溢流方式及堰长同塔径的比值lw/D:172.1.6计算塔径：17\o"CurrentDocument"2.1.7计算塔径圆整后的实际气速：172.1.8在D=1.8m时，塔板结构尺寸：17\o"CurrentDocument"2.2溢流堰高度七及堰上液层高度h^的确定18\o"CurrentDocument"2.3板面筛孔布置的设计18\o"CurrentDocument"2.3.1选取筛孔直径d0=5mm。18\o"CurrentDocument"2.3.2计算开孔区面积Aa：182.3.3开孔率182.3.4开孔面积：18\o"CurrentDocument"2.4水力学性能参数计算及校核19\o"CurrentDocument"2.4.1液沫夹带分率的检验192.4.2塔板压降19\o"CurrentDocument"2.4.3液面落差的校验：20\o"CurrentDocument"2.4.4塔板漏液状况的校验20\o"CurrentDocument"2.4.5降液管液泛情况的校验：20\o"CurrentDocument"2.4.6液体在降液管内停留时间的校验：21\o"CurrentDocument"2.5塔板负荷性能图21\o"CurrentDocument"2.5.1负荷性能图21\o"CurrentDocument"2.5.2操作性能的评定：23\o"CurrentDocument"2.6筛板设计计算的主要结果：24第三部分结束语26化工原理课程设计I.原始数据设计题目：双组分连续精馏筛板塔的设计原料处理量：1.45X104kg/h原料组成：组分名称甲苯二甲苯组成（质量分率）0.440.56分离要求：（1）：馏出液中低沸点组分的含量不低于0.985（质量分率）。（2）：馏出液中低沸点组分的收率不低于0.99（质量分率）。操作条件：（1）：操作压力：常压。（2）：进料及回流状态：泡点液体。II.设计计算1第一部分工艺设计1.1物料衡算:甲苯的摩尔质量：MA=92kg/kmol二甲苯的摩尔质量：Mb=106kg/kmol原料液摩尔分率:F0.4751塔顶产品摩尔分率:D=0.9870原料液摩尔分率:F0.4751塔顶产品摩尔分率:D=0.9870原料液的平均摩尔质量：M=0.4751X92+(1—0.4751)X106=99.3486kg/kmol1.45x104物料衡算原料处理量:=145.95kmol/h99.3486D-xDF-x物料衡算原料处理量:D-xDF-xFD=69.55kmol/h总物料衡算：F=D+W塔顶易挥发组分回收率:=0.99DX°，9870=0.99145.95x0.4751・•・w=f-D=145.8979—69.5268=Fxf=DxD+%145.95乂。.4751=693。.987。+76*..・常二°.°°911.2塔顶温度、塔底温度及最小回流比的计算:Fxf=DxD+%1.2.1确定操作压力：塔顶压力：760mmHg塔底压力：760mmHg+28x100/13.6mmHO=965.8824mmHg21.2.2计算塔顶温度（露点温度）根据塔顶压力及塔顶汽相组成用试差法计算塔顶温度。其中甲苯、二甲苯的饱和蒸气压由安托因方程计算。•设'顶=111.27。°由lgPA。6.9531344t__+219.4顶2.8885得P。=773.6149mmHgA由l由lgPA。6.9531344t__+219.4顶2.8885得P。=773.6149mmHgA由lgPB。7.000-1463t__+214.7顶2.5119得P。=324.9802mmHgBkAP0=P_773.6149=1.0179760x=Ia_0.9870_0.9696AkA1.0179xB324.9802760=0.4276-0.98700.42760.03040Zx.-1|=|0.9696+0.03040-1|=0<£=0.0004...'顶=111.27°假设正确，为所求露点温度。「•a=里=773.5149=2.3805顶P0324.98021.2.3计算塔底温度（泡点温度）根据塔底压力及塔底残液组成用试差法计算塔底温度。其中甲苯、二甲苯的饱和蒸气压由安托因方程计算。•(1)设'底=149.28°

由lgP0A13446.953t+219.4底=3.3076得P。由lgP0A13446.953t+219.4底=3.3076得P。=2030.3094mmHgA由lgP0B7.000-一1463一t+214.7底=2.9805得P。=956.1992mmHgB2030.3094965.8824=2.1020956.1992965.8824=0.9900yA=xA•kA=0.0091x2.1020=0.01913yB=XB•kB=l—0.0091)x0.9900=0.9810Zy,-1|=0.01913+0.9810-1|=0.00013<£=0.0004...'底=149.28。°假设正确，为所求泡点温度。=2.1233.P0=2.1233・・a==底P0956.1992B...a=.\,a顶•a广=J2.3805x2.1233=2.24821.2.4计算最小回流比Rmin：q=1x=七=0.4751y=]+°j=0.6704e=X^=0.9870-0.6704=1.6211miny-x0.6704-0.47511.3确定最佳操作回流比与塔板层数:1.3.1列相平衡关系式:X=fyn)=Lna—k—1为2.2482-1.2482y1.3.2列操作线方程:精馏段：y=火x+Xd。+1R+1nR+1提馏段：y=L+Fx-―-—x(L=R*D)m+1L+F-WmL+F-W-1.3.3由塔顶向下逐板计算精馏段的汽、液相组成:由y1=xD，根据平衡关系计算x1，由操作关系计算y2，由平衡关系计算x2，…由平衡关系计算xn，当xnWxF时，则n-1即为精馏段的理论板数。1.3.4由进料口向下逐板计算提馆段的汽、液相组成:由x1=xn，根据操作关系计算)2，由平衡关系计算x2，由操作关系计算y3,…由平衡关系计算xm，当xmWxw时，则m即为提馏段的理论板数。1.3.5逐板法计算塔板层数：由R=(1.1-2.0)Rmin范围内，步长为O.IRmin，逐次增大操作回流比，按上述2-4步计算，具体计算结果如下表：R=1.1Rmin=1.782精馏段：n=1y=0.987x=0.9712n=2y=0.9769x=0.9495n=3y=0.963x=0.9205n=4y=0.9444x=0.8831n=5y=0.9204x=0.8372n=6y=0.891x=0.7843n=7y=0.8572x=0.7275n=8y=0.8208x=0.6708n=9y=0.7845x=0.6182n=10y=0.7508x=0.5727n=11y=0.7216x=0.5355n=12y=0.6978x=0.5067n=13y=0.6793x=0.4851n=14y=0.6655x=0.4695提馏段：m=0x=0.4751m=ly=0.6591x=0.4624m=2y=0.6414x=0.4431m=3y=0.6145x=0.4149m=4y=0.5751x=0.3758m=5y=0.5206x=0.3257m=6y=0.4507x=0.2674m=7y=0.3694x=0.2067m=8y=0.2847x=0.1504m=9y=0.2062x=0.1036m=10y=0.1409x=0.068m=lly=0.0913x=0.0428m=12y=0.0561x=0.0258m=13y=0.0324x=0.0147m=14y=0.0169x=0.0076n=23（不包括塔釜）TV=13TV=13（不包括塔釜）T精提（2）R=l.2Rmin=1.944精馅段：n=ly=0.987x=0.9712n=2y=0.9766x=0.9489n=3y=0.9618x=0.918n=4y=0.9414x=0.8772n=5y=0.9145x=0.8263n=6y=0.8809x=0.7669n=7y=0.8417x=0.7028n=8y=0.7993x=0.6392n=9y=0.7573x=0.5812n=10y=0.719x=0.5323n=lly=0.6867x=0.4937n=12y=0.6613x=0.4648提馅段：m=0x=0.4751m=ly=0.649x=0.4513m=2y=0.6163x=0.4167m=3y=0.5688x=0.3698m=4y=0.5044x=0.3116m=5y=0.4245x=0.2471m=6y=0.3359x=0.1837m=7y=0.2488x=0.1284m=8y=0.1729x=0.0851m=9y=0.1135x=0.0539m=10y=0.0706x=0.0327m=lly=0.0415x=0.0189m=12y=0.0226x=0.0102m=13y=0.0106x=0.0047N广23（不包括塔釜）N精=11N提=12（不包括塔釜）（3）R=1.3Rmin=2.106精馏段：n=1y=0.987x=0.9712n=2y=0.9763x=0.9483n=3y=0.9608x=0.916n=4y=0.9389x=0.8724n=5y=0.9093x=0.8168n=6y=0.8716x=0.7512n=7y=0.8271x=0.6803n=8y=0.779x=0.6106n=9y=0.7318x=0.5483n=10y=0.6895x=0.4969n=11y=0.6547x=0.4575提馏段：m=0x=0.4751m=1y=0.6399x=0.4415m=2y=0.5944x=0.3946m=3y=0.5309x=0.3349m=4y=0.4501x=0.2669m=5y=0.3581x=0.1988m=6y=0.2659x=0.1388m=7y=0.1847x=0.0915m=8y=0.1206x=0.0575m=9y=0.0746x=0.0346m=10y=0.0436x=0.0199m=11y=0.0237x=0.0107m=12y=0.0113x=0.0051Nt=21（不包括塔釜）N精=10N提=11（不包括塔釜）（4）R=1.4Rmin=2.268精馏段：n=1y=0.987x=0.9712n=2y=0.976x=0.9476n=3y=0.9597x=0.9137n=4y=0.9361x=0.867n=5y=0.9037x=0.8067n=6y=0.8619x=0.7352n=7y=0.8123x=0.6581n=8y=0.7587x=0.5831n=9y=0.7067x=0.5173n=10y=0.661x=0.4645提馅段：m=0x=0.4751m=ly=0.6317x=0.4328m=2y=0.5752x=0.3759m=3y=0.4992x=0.3072m=4y=0.4074x=0.2342m=5y=0.3099x=0.1665m=6y=0.2194x=0.1111m=7y=0.1454x=0.0704m=8y=0.091x=0.0426m=9y=0.0539x=0.0247m=10y=0.0299x=0.0135m=lly=0.015x=0.0067N=19（不包括塔釜）N=9N=10（不包括塔釜）T精提（5）R=l.5Rmin=2.43精馅段：n=ly=0.987x=0.9712n=2y=0.9758x=0.9472n=3y=0.9588x=0.9119n=4y=0.9338x=0.8625n=5y=0.8988x=0.798n=6y=0.8531x=0.7209n=7y=0.7985x=0.638n=8y=0.7397x=0.5583n=9y=0.6833x=0.4897n=10y=0.6347x=0.436提馅段：m=0x=0.4751m=ly=0.6243x=0.425m=2y=0.5582x=0.3598m=3y=0.4721x=0.2846m=4y=0.3728x=0.2091m=5y=0.2732x=0.1433m=6y=0.1863x=0.0924m=7y=0.1191x=0.0567m=8y=0.0719x=0.0333m=9y=0.0411x=0.0187m=10y=0.0218x=0.0098m=lly=0.01x=0.0045N广19（不包括塔釜）N精=9N提=10（不包括塔釜）（6）R=1.6Rmin=2.592精馏段：n=1y=0.987x=0.9712n=2y=0.9756x=0.9468n=3y=0.958x=0.9103n=4y=0.9317x=0.8585n=5y=0.8943x=0.7901n=6y=0.8449x=0.7079n=7y=0.7856x=0.6198n=8y=0.722x=0.536n=9y=0.6616x=0.4652提馏段：m=0x=0.4751m=1y=0.6176x=0.4181m=2y=0.5432x=0.346m=3y=0.449x=0.2661m=4y=0.3447x=0.1896m=5y=0.2448x=0.126m=6y=0.1617x=0.079m=7y=0.1004x=0.0473m=8y=0.059x=0.0271m=9y=0.0326x=0.0148m=10y=0.0165x=0.0074Nt=17（不包括塔釜）N精=8N提=9（不包括塔釜）（7）R=1.7Rmin=2.754精馏段：n=1y=0.987x=0.9712n=2y=0.9754x=0.9463n=3y=0.9571x=0.9085n=4y=0.9294x=0.8541n=5y=0.8895x=0.7817n=6y=0.8364x=0.6946n=7y=0.7725x=0.6017n=8y=0.7043x=0.5145n=9y=0.6404x=0.442提馏段：m=0x=0.4751m=1y=0.6115x=0.4118m=2y=0.5296x=0.3337m=3y=0.4287x=0.2503m=4y=0.3209x=0.1737m=5y=0.2219x=0.1126m=6y=0.1429x=0.069m=7y=0.0865x=0.0404m=8y=0.0496x=0.0227m=9y=0.0267x=0.0121m=10y=0.013x=0.0058N丁=17（不包括塔釜）N精=8N提=9（不包括塔釜）（8）R=1.8Rmin=2.916精馏段：n=1y=0.987x=0.9712n=2y=0.9752x=0.9459n=3y=0.9564x=0.907n=4y=0.9274x=0.8504n=5y=0.8853x=0.7744n=6y=0.8287x=0.6827n=7y=0.7604x=0.5854n=8y=0.688x=0.4952n=9y=0.6208x=0.4214提馏段：m=0x=0.4751m=1y=0.6058x=0.406m=2y=0.5173x=0.3228m=3y=0.4108x=0.2367m=4y=0.3005x=0.1604m=5y=0.2028x=0.1017m=6y=0.1277x=0.0611m=7y=0.0757x=0.0352m=8y=0.0425x=0.0194m=9y=0.0223x=0.01m=10y=0.0103x=0.0046Nt=16（不包括塔釜）N精=8N提=8（不包括塔釜）（9）R=1.9Rmin=3.078精馏段：n=1y=0.987x=0.9712n=2y=0.9751x=0.9457n=3y=0.9558x=0.9058n=4y=0.9257x=0.8471n=5y=0.8814x=0.7678n=6y=0.8216x=0.672n=7y=0.7492x=0.5706n=8y=0.6727x=0.4776n=9y=0.6025x=0.4027提馏段：m=0x=0.4751m=1y=0.6006x=0.4008m=2y=0.5063x=0.3133m=3y=0.3952x=0.2252m=4y=0.2834x=0.1496m=5y=0.1874x=0.093m=6y=0.1156x=0.0549m=7y=0.0672x=0.0311m=8y=0.037x=0.0168m=9y=0.0189x=0.0085N丁=16（不包括塔釜）N精=8N提=8（不包括塔釜）（10）R=2Rmin=3.24精馏段：n=1y=0.987x=0.9712n=2y=0.9749x=0.9453n=3y=0.9551x=0.9044n=4y=0.9239x=0.8438n=5y=0.8776x=0.7613n=6y=0.8145x=0.6614n=7y=0.7382x=0.5564n=8y=0.658x=0.4612提馏段：m=0x=0.4751m=1y=0.5958x=0.396m=2y=0.4962x=0.3047m=3y=0.3813x=0.2152m=4y=0.2686x=0.1404m=5y=0.1744x=0.0859m=6y=0.1058x=0.05m=7y=0.0606x=0.0279m=8y=0.0328x=0.0149m=9y=0.0164x=0.0074Nt=15（不包括塔釜）N精=7N提=8（不包括塔釜）

1.3.6对上表塔板数列表:R=nRmin1.11.21.31.41.51.61.71.81.92.0精馏段1311109988887提馏段131211101099988N（不含釜）262321191917171716151.3.7绘制R-Nt曲线，确定最佳操作回流比及最佳理论板数:本题取回流比R=1.4Rm.n=1.3x1.62=2.268NT=19（不包括塔釜）N精=9N提=10（不包括塔釜）1.3.8查取塔板效率:111.27+111.27+149.282=130.275°c日甲苯=日20+（鲁）（七—20）=0.2000nt(不含釜nt(不含釜)eT取N实=33块2第二部分结构设计日二甲苯=日20+(告)^—2°)=Q2238U=£xLX=xLX+(1-x)LXLiiF甲苯F二甲苯Xl=°.4751x°.20°+V—0.475Ux0.2238=°.2125Et=0.49x0-245=°.49x22482x0.2125—°-245=0.58721.3.9计算全塔理论板数:19=32.360.58722.1塔板结构计算：（设计塔顶第一块板）2.1.1计算塔顶实际的汽液相体积流量:对于液相：pl甲苯=P20+(铮)(t—20)=761.15Kg/m3Pi二甲苯=p20+(|t)(t—20)=767.51Kg/m3液相密度计算：p=px+p(1—x)=761.15x0.9712+767.51x(1—0.9712)LL甲苯1L二甲苯1・.・Pl=761.33Kg/m3汽相密度计算：M=0.9870X92+(1—0.987)X106=92.182kg/kmolPM101.325x92.182RT顶)=2.92248.PM101.325x92.182RT顶)=2.92248.314x073.15+111.27)Kg/m3塔顶气相体积流量:Vl=RDM/pl=2.268x69.55x92.182/761.33=19.0991m3/hVG=(R+1)DM/pG=(2.268+1)x69.55x92.182/2.9224=7169.4468ms/h2.1.2选取塔板间距ht:选取塔板间距H=0.45mT计算液汽动能参数C：液气动能参数:V\p19.0991.'761.33―^XI—L=■VG\，PG7169.4468E2.9224=0.04430查史密斯关联图，查得汽相负荷参数C=0.08420液体表面张力的计算：。甲苯=气+（净（一20）=盅郊0.113x（BWORWdyn心。二甲苯=气。+(笠)(七-20)=28.99-0.109x(130.275-20)=16.9700dyne/cb=Z。热=16.0689x0.4751+16.97x(1-0.4751)=16.5419dyne/cmi「，b、八no.(16.54191=C(——)0.2=0.084x0.2=0.080872.1.3计算液泛速度七(u):U=C-PL-PG=0.08087x；761.33-2.9224=1.3028m/sFA,'p2.9224G2.1.4空塔气速：取安全系数为0.7，则空塔气速UG=0.7U广0.7x1.3028=0.9120m/s2.1.5选取溢流方式及堰长同塔径的比值//d:选用单溢流弓形降液管，取lw/D=0.7。查弓形降液管的参数图，查取降液管面积同塔截面积的比值勺/A=0.088，及降液管宽度同塔径的比值W/D=0.14。2.1.6计算塔径：V-G-UV-G-UG7169.44680.9120x3600=2.1838m2截塔面积：A=X_A/A)=2.183%_0.088)=2.3945m2塔径:D=青=塔径:D=青=.'4x2.3945=1.7461m按标准塔径圆整后D=1.8m。2.1.7计算塔径圆整后的实际气速:,兀-兀一A=—D2=—x1.82=2.543m244A。=A(1_AJA)=2.543x(1_0.088)=2.3196m2VG7169.44682.3196x3600=0.8586m/sVG7169.44682.3196x3600=0.8586m/s液泛分率：匕=0.8586=0.6590m/s在(0.6〜0.8)范围内u1.3028F2.1.8在D=1・8m时，塔板结构尺寸:堰长：l=0.7D=0.7x1.8=1.26m降液管宽度：W广0.14D=0.14x1.8=0.252m

降液管面积：气=0.088A=0.088x2.543=0.2238m22.2溢流堰高度"及堰上液层高度h的确定选取溢流堰高度h=50mm=0.05m查取液流收缩系数图，得液流收缩系数E=1.021(vV3选用平直堰，堰上液层高度h=0.0028Et=0.017m=17mm°w"lw)h=h+h=50+17=67mm2.3板面筛孔布置的设计：2.3.1选取筛孔直径d0=5mm。筛孔按正三角形排列，孔中心距/孔径二3,孔中心距t=3d°=3X5=15mm选塔板厚度t^=3.5mm(碳钢板)W=50mmW=70mm2.3.2计算开孔区面积A.a•A=A-2A,-21W-2(D-2W,)W=2.543—2X0.2238—2X1.26X0.07—2X(1.7461—2X0.252)X0.05=1.7948m22.3.3开孔率甲A

Q=—oAA

Q=—oAa=0.907(%TIt)=0.907X=0.1008=10.08%A二QA=0.1008X1.7948=0.1811m2

气体通过筛孔的流速：U=匕二—=10.9967m/oA0.1811x3600/so孔个数N==0.1811=9223个土d2lx0.00524o42.4水力学性能参数计算及校核2.4.1液沫夹带分率的检验0.057b0.057x14.20420.91200.45—2.5x0.0670.057b0.057x14.20420.91200.45—2.5x0.067=0.01295kg液/kg气<0.1kg液/kg气故在本设计液沫夹带量e在允许范围内。G2.4.2塔板压降2.4.2.1干板压降由d=5mmt=3.5由d=5mmt得孔流系数C0=0.792g"C2g"C>o2.4.2.2液层静压降12x9.81(10.9967)2、0.8087/x2.9224=0.03617m761.33查充气系数关联图，得充气系数P=0.62。h^=^h^=^(h+h2.4.2.3液层表面张力压降4x10-3b)=0.62X0.067=0.04154m液柱hbPLgd。2.4.2.4单板总压降4x10-3x敏5419=0.001772m761.33x9.81x0.005AH=AH=h+hL+h2.4.3液面落差的校验：b=D^^W-=1.8+1.26=1.53mh=2.5(h+h)=2.5x0.067=0.1675m22fwowT=D-2Wd=1.8-2x0.252=1.296匕=0.3090x10-3N•身m-2PL=761.33Kg/m3Vl=19.0991m3/h00476(b+4〃2』‘匕匚=.(by)3pl(1.53+4x0.1675)2x0.3090x10-3x19.0991x1.296=0.0476x(1.53x0.1675)3x761.33=0.000137=0.000137<§=0.01886忽略2.4.4塔板漏液状况的校验1）产生漏液的干板压降h'=0.0050+0.05（h+h）=0.00835m2）工作状态下稳定系数k10.3617)I—

"0.00835)=6.5816>1.5故不会产生严重漏液。稳定系数k10.3617)I—

"0.00835)=6.5816>1.52.4.5降液管液泛情况的校验:2.4.5.1选取降液管下缘至下层塔板的距离h0=20mm：则降液管下缘缝隙通道的截面积A广h/l=0.02X1.26=0.0252m22.4.5.2液体流出降液管的阻力损失h:d=0.006280m1.39(V=1.39~g了^8Tx119.0991/3600]2"0.0252)=0.006280m2.4.5.3计算降液管内的清液层高度H及泡沫层高度h':ad=AH+h+h+A+hHd=0.07948+0.050+0.017+0.000137+0.006280=0.1529m液柱甲苯一二甲苯物系属一般物系，取4=0.5,H01529则*-="=0.3058m2.4.5.4校核:Ht+h=0.45+0.05=0.5m故在本设计中不会发生液泛现象。2.4.6液体在降液管内停留时间的校验:3600H%=3600x0.1529x0.2238=6＞吴t=广'.SSL故降液管设计合理。19.09912.5塔板负荷性能图2.5.1负荷性能图2.5.1.1过量液沫夹带线Ht-2.5hw+0.0028EI8812x2.3196x16.541913.20.45-2.50.05+0.0028x1.0211"1.26/¥3二15965.37-300.9578匕232.5.1.2最小气相负荷线VG=15946CAcA*

择GJ0.5Ao0.0056+0.13h+0.0028Ew0.5=15946x0.81(761.33A0.512.9224)x0.18110.0056+0.130.05+0.0028x1.021-0.001559二37754.77\,'0.010541+0.0003186匕232.5.1.3最大液相负荷线匕=1200HdA^=1200X0.1529X0.2238=41.06282.5.1.4最小液相负荷线(6V；(6a32匕=[&]2・匕=[28xi021)x1.26=3.83112.5.1.5降液管液泛线A,=0.02L=0.0252Vg=15946C0.5Ao0.5Ht-(0.5+P)h-G+P)x(V0.0028E-lllA23-0.142*

l3600A、Vg=15946C0.5Ao0.5Ht-(0.5+P)h-G+P)x(V0.0028E-lllA23-0.142*

l3600A、2da0.52.5.2操作性能的评定:2.5.2.1本设计的操作条件为「19.0991"匕,匕二7169.4468叫在负荷性能图上作出操作点P（匕，匕），连接OP，即作出操作线。2.5.2.2根据操作线同负荷性能图的交点及设计工作点的坐标，计算下列参数:根据负荷性能图及操作线的交点，可以看出从图上读出：匕=16744.09m3/,匕.二3837.03m3^,V=10.4960m3,；L,min/h匕V=10.4960m3,；L,min/h按汽相负荷计算：K=匕皿=16744。9=4.3638m3/hT，GVG.3837.03V458027按液相负何计算：K=Ex==4.3638m3/ht，lV10.4960L,minB.设计工作点的安定系数（设计负荷对极限之比）：V1674409对汽相负荷上限：K=—ax=二=2.4505A,GV6832.8516G对汽相负荷下限：K侦二土=6832'516=1.7808A，Gv3837.03G,min对液相负荷上限：K=匕4=45.8