第一章习题1有一反应在间歇反应器中进行,经过8min后,反应物转化掉80%,经过18min后,转化掉90%,求表达此反应的动力学方程式。解2AAmin18A0min8A0AAA0dd219.019.0181)(218.018.081)(11kctckckcxxckt为假设正确,动力学方程2在间歇搅拌槽式反应器中,用醋酸与丁醇生产醋酸丁酯,反应式为:SRBAOHHCOOCCHOHHCCOOHCH2943SOH94342反应物配比为:A(mol):B(mol)=1:4.97,反应在100℃下进行。A转化率达50%需要时间为24.6min,辅助生产时间为30min,每天生产2400kg醋酸丁酯(忽略分离损失),计算反应器体积。混合物密度为750kg·m-3,反应器装填系数为0.75。解13313111111i1.2m0.750.8949总体积反应0.8949m0.910.9834有效体积反应0.91hr6054.6折合54.6min3024.6总生产时间hr0.9834m750737.5换算成体积流量hr737.5kg634.1103.4总投料量hr634.1kg744.97724.1B4.97:1B:Ahr103.4kg601.724折算成质hr1.724kmol0.50.862的投料量A,则50%转化率hr0.862kmol116100hr100kg2400/24R1167460MSRBA器器投料量则量流量产量3反应(CH3CO)2O+H2O→2CH3COOH在间歇反应器中15℃下进行。已知一次加入反应物料50kg,其中(CH3CO)2O的浓度为216mol·m-3,物料密度为1050kg·m-3。反应为拟一级反应,速率常数为k=5.708×107exp(−E/RT)min-1,E=49.82kJ·mol-1。求xA=0.8时,在等温操作下的反应时间。解min6.308.011ln05252.0111ln1min05252.0)288314.849820exp(10708.5A17xktk4在555K及0.3MPa下,在平推流管式反应器中进行气相反应A→P,已知2进料中含A30%(摩尔分数),其余为惰性物料,加料流量为6.3mol·s-1,动力学方程式为−rA=0.27cAmol·m-3s-1为了达到95%转化率,试求:(1)所需空速为多少?(2)反应器容积大小?解1R000VNO30R111V95.00AA95.00AAA01330s131.0075.11013.015.5553.015.2730969.0m075.110.110969.0s09.010.11s10.1195.011ln27.01127.0ddsm0969.030015.555314.8103.6VppTTVSVVSxxrxcV标准空速为:5反应A+B→R+S,已知VR=0.001m3,物料进料速率V0=0.5×10-3m3min-1,cA0=cB0=5mol·m3,动力学方程式为−rA=kcAcB,其中k=100m3kmol-1min-1。求:(1)反应在平推流反应器中进行时出口转化率为多少?(2)欲用全混流反应器得到相同的出口转化率,反应器体积应多大?(3)若全混流反应器体积VR=0.001m3,可达到的转化率为多少?已知k=1m3kmol-1hr-1,cB0=3kmol·m-3,cA饱和=0.02kmol·m-3,水溶液流量为10m3hr-1。解3(1)平推流5.00005.051.0001.0111111)111(1)1(d10A0RAfAf0A02AA0A0RAfVkcVxxkcxxkcVVx(2)全混流3330R2BAAA0AAA00Rm1024105.040025.01000025.0005.0VVckcccrccVV(3)VR=0.001m3时可达到的转化率3820.0111005.0100105.0m001.01A2AA2AA33R2A20AAA0BAAA0AAA00RxxxxxVxkcxcckcccrccVV4第二章习题1.平行液相反应A→PrP=1A→RrR=2cAA→SrS=cA2已知cA0=2kmol·m-3,cAf=0.2kmol·m-3,求下列反应器中,cP最大为多少?(1)平推流反应器;(2)全混流反应器;(3)两相同体积的全混流反应器串联,cA1=1kmol·m-3。解3-A0AfA2AAf0ApPAPAfA0p2A2AASRPPPmkmol5.02112.011)1(1)1(1d)1(1)(d1PFRFor)1(1211A0Af0AAfccccccSccSccScccrrrrScccc3-22AfAfA0AfA0pPmkmol25.1)2.01(1)2.02()1(1)()(CSTRForcccccSc53-22P2AfA1P1A1A0Pmkmol81.056.025.0)2.01(1)2.01()11(1)12()()(SeriesinCSTRFortwoSccSccc2.自催化反应A+P→2P的速率方程为:−rA=kcAcP,k=lm3kmol-1min-1,原料组成为含A13%,含P1%(摩尔百分数),且cA0+cP0=lkmol·m-3,出口流中cP=0.9kmol·m-3,计算采用下列各种反应器时的空间时间(τ=VR/V0)。(1)平推流反应器;(2)全混流反应器;(3)平推流与全混流反应器的最佳组合;(4)全混流反应器与一分离器的最佳组合。解AA2A0AA0AA0PAAAfAin3A0)1()1(9.00714.0141m1kmolxxkcxcxkcckcrxxcmin76.40714.010714.09.019.0ln11111ln1d11111d1dPFRForAinAinAfAfA0AA0AAAAA0AAA0AfAinAfAinAfAinxxxxkcxxxkcxxxkcrxcxxxxxxmin2.99.09.010714.09.01111CSTRForAfAf20AAinAf0Axxkcxxc6min91.320.271.120.25.015.09.019.0lnmkmol5.0)1(min71.15.0)5.01(0714.05.0111)1(15.00210dd,1PFRCSTRFor2123A1A0A1A11AAinAf0A1A1AAAAAxccxxxxkcxxxrrr,,有令的极值点相同与由于min71.15.0)5.01(0714.05.0111)1(15.0,0ddCSTRForA1A1AinAfA01AAAxxxxkcxxr分离器7第三章习题1.有一有效容积VR=1m3,送入液体的流量为1.8m3hr-1的反应器,现用脉冲示踪法测得其出口液体中示踪剂质量浓度变化关系为:t/min01020304050607080c/kg·m-3036543210求其停留时间分布规律,即F(t),E(t),t,2t解示踪法求停留时间分布规律t/minc/kg·m-3∑cF(t)E(t)t·ct2c000000010330.1250.01253030020690.37500.02501202400305140.58330.02081504500404180.750.01671606400503210.8750.01251507500602230.95830.00831207200701241.00.0042704900800241.0000∑24803320022222tmin2.27233.332433200min33.3324800tcctctct82.请将习题一中停留时间分布规律用对比时间θ作变量,求F(θ),E(θ),,2θ。解min33.335.110R0R22t2θVVVVttEEtFFt3.在习题一的反应器中进行A→D反应,已知cA0=25mol·m-3,动力学方程为−rA=0.05cAmol·m-3min-1,请分别用:(1)凝集流模型;(2)多级混合槽模型;(3)平推流模型;(4)全混流模型。计算出口物料中A组分的转化率。解(1)凝集流模型t/minc/kg·m-3∑cF(t)ktccexp0000010330.1250.11890.0758220690.3750.22620.091979305140.58330.17930.04649404180.750.13650.02256503210.8750.09740.01026602230.95830.06170.00415701241.00.02940.00126800241.00∑240.25257475.0exp1Aktccx(2)多级混合槽模型:7556.008.433.33005.011111108.41245.008.4A22θ2θNNkxNN(3)PFR模型:8111.033.3311ln201d201d05.01dmin33.33AA0AA0AA0AAA00RAAAxxxxxxrxcVVxxx(4)CSTR模型:106250.033.33120105.0min33.33AAAAA0AA0AfAA00RxxxxcxcrccVV4.用题一的条件,采用轴向扩散模型,计算其Pe值与出口物料中A组分的转化率。解7578.02422.012993.63976.1exp3976.112993.63976.1exp3976.112993.6exp3976.1412Peexp12Peexp12Peexp413976.1993.633.3305.041Pe41993.6PePePeexp11Pe2245.012222A222θxkttt试差得闭式边界条件满足闭5.设E(θ)、F(θ)分别为某流动反应器的停留时间分布密度函数和停留时间分布函数,θ为对比时间。(1)若反应器为PFR,试求:11(a)F(1),(b)E(1),(c)F(0.8),(d)E(0.8),(e)E(1.2)(2)若反应器为CSTR,试求:(a)F(1),(b)E(1),(c)F(0.8),(d)E(0.8),(e)E(1.2)(3)若反应器为一非理想流动反应器,试求(a)F(∞),(b)F(0),(c)E(∞),(d)d0F,(e)d0E解(1)对PFR,F(1)=1,E(1)=∞,F(0.8)=0,E(0.8)=0,E(1.2)=0(2)3012.02.14494.08.03679.015507.018.06321.0111CSTR2.18.018.01eEeEeEeFeFeEeF