化学工程习题答案.pdf

5 0 00 5 3 0 0 11 3 0 0 43 7003 102 1160.5 2 1 1 21112 1 3 10 37.085 8.314(700273) (1)37.0850.5 9.27 1(12 0.5) o AAAAAB AAAAAA A A AA A AAA CPaABC wkgxcpyc yyxx pPa cm RTJ molKK cxmol m cm yx ol m o + = + =+= + = + = + ， ，求时的 ， ， 。 解： 3 0 0 0 3 1 0 1 0 3 4 (1)(1 0.5) 0.25 9.278.314(700273) 7.499 10 112 0.5 2 37.085 0.5 18.54 112 0.5 AA A AAA BAA B AA A A A l m yx y yx b cc x a pc RTmol mJ molKK cm y a x P = + = + = + + = ol m 1 0 0 44 0.50.260.03 0.50.03 0.94 0.5 0.5 10000.26 1000 10.879.286 46/28 / 9.286 0.854 10.87 0.854 0.909 0.94 ABB A AB B B A B B A ABC kg Akg Bkg AxYS x gg nmolnmol g molg mol n Y n Y S x + = = = = ，剩未反应，求 ， 解： 2 3 0 D 7231 00 3 0 00 000 0 45 1002.9 10 :4.972:1240030min 7500.50.7 4.97200 (1)(4.972) o A BAc A nA nAnA nAAnAAnAAnAA nAA ABCD TCrc mol ms nnwkgt kg mx q ABC qq qxqxqxqx qx + = = = + 混 ， ， ，求活塞流反应器V。 解： 设反应初始A的摩尔流量为 反应前 反应后 0 0 0 33 0 0 33 2400 1000 0.2395/ 116/24 3600 0.2395/0.50.479/ 4.972 0.4792.381/ 0.479/60/2.381/74/ 204.934/ 204.934/ 0.2732 10/ 750 10/ nA nB wT wT V A g mol s g mols qmol smol s qmol s qmol sg molmol sg mol g s qg s qm g m c = = = =+ = = s 33 0 0 33 0 0.5 00 22 00 00 0 73 33 0 3 0.479/ 1.735 10/ 0.2732 10/ 1 (1)1 1 1967 2.9 101.735 10 ()0.2732 10/(1967 1800) 1.029 /1.029/0.71 AA nA V xx AAA rAA AAAAA RV R qmol s mol m qms dxdxx tcc rkcxkcx s Vqttmss m VV = = = =+=+ = = 3 .47m 4 0 0 22 0 732 33 0 0.5 0 0 33 0 48 45 ()(1) 0.5 3934 2.9 101.753 10(1 0.5) 0.2732 1039341.08 4 13 45 1967 () 0.2732 1019670.54 AfAAf A AfAAf V A A A V xc x c rkcx s Vqm dx cs r Vqm = = = = = 同，改用全混流反应器，求V。 同，改用活塞流反应器，求V。 在相同 PFRCSTRIBR 操作条件下，所需反应器体积从小到大为 5 0 3 0 3 0 0 11 00 11 2 0 0 3 4 11 22 1101325627.2 1.7120/ ()0.7 1 101325 19.43/ 8.314627.2 A A VA A A x AA AA AA ABC ypPaTK kqmh STPx pPa cm RTJ molKK dxdx cc mkmo rk s c l + = = = = ol m = 二级不可逆反应 ，活塞流反应器 ， 求考虑或不考虑体积变化所需反应体积。 （ ）不考虑体积变化 0.7 2 0 0 0 3113 3131 0 3 0 0 0 1 (1)1 0.7 70.640.0196 1.70.01943/0.3 627.2 627.2 120275.54 273.2 275.54 0.01965.42 2 2 1 2 0.511 0.5 2 A x A AAA V V AAAAA A x xkcx sh mkmolskmol m TK qmhmh Vqm yxx d c = = = = = + =+= + = （ ）考虑体积变化 2 02 000 0 0 0.7 2 2 0 0 0.7 0 1 0.51 1 (1) 1 0.5 (1 0.5)1 2 0.51+0.5ln(1)0.5 1 2.251 1.5ln(1)0.25 1.7 0.019431 109.560.03 AAA xxx AAA AA AAA AA A A AA AA A AA A xdxx cdx rkcx cx k x x xx kcx x xx x s + = + + =+ =+ = （） 3 0 04 275.54 0.03048.40 V h Vqm= 6 0 0 0 0000 0.5 ,00,00 00 ,0 ,00 0 4 12 3 ,0.5 0.51.5 3 1 211 1 (1)(1)1.5 0.5 ()(1 1 ) 0min 1 A A IVVA AAAAA VVAAAVAV A x AA VAVA AVAVA A VA A APy yqqxk yxx qqyxqxq x dxdx tqcqc r qkc qx d q c t x c k = = =+= + =+=+= = = + = = 气相一级反应使用等温活塞流反应器， ，求及 。 解： 解得 0.50.5 00 ,0 1 1 (1) 1 ln2/0.0693 A A A VA A dx kxx qx x kt = + + = 7 2313 0 3331 0 3 111 10 222 00101 1 23 1 4 15 0.0174(min )7.14 7507.14 10min 120.25 (1)(1) 0.25 0.0174 7.14(1)7.14 10 AAA V AA A VAAAA A A rckmol mckmol m kg mqm m Vxx c qkcxkcx x x = = = = ， ，。 计算下列转化率各为多少？ （ ）串联 个的全混流反应器。 解： 2 11 1 2212 20 222 0022 2 22 3 2 33 1 2.2310 0.6218 0.6218 (1)0.0174 7.14(1) 0.25 2.231.14290 7.14 10 0.7985 2 10.2510.25 0.6218 AA A AAA A VAAA AA A A xx x Vxxx c qkcxx xx x mm x + = = = =+= = = 整理得 解得 整理得 解得 （ ） 个的全混流反应器后接 个的活塞流反应器。 由以上计算得 活塞流反应 22 11 2 00 22 0 2 02 0.6218 3 2 (1) 110.6218 10.0174 7.14 11 0.6218 0.25 7.14 10 0.8570 AA AA A xx AA AA xx AAA x AA AAA A dxdx cc rkcx xx kcxx x = = = = 器 整理并求解得 11 1 100 22 00 0 1 3 01 0 1 2212 20 222 0022 3 (1) 110.25 10.0174 7.14 17.14 10 0.8131 0.8131 (1)0.0174 7.14(1) 0.25 7.14 AA A xx AA AA AAA x AA AAA A AAA A VAAA dxdx cc rkcx xx kcxx x Vxxx c qkcxx = = = = = （ ）先活塞流后全混流反应器。 解： 解得 22 2 3 2 100 22 00 0 2 3 02 0 2 10 0.8779 4 (1) 110.25 2 10.0174 7.14 17.14 10 0.8969 AA A A xx AA AA AAA x AA AAA A x dxdx cc rkcx xx kcxx x = = = = 整理并求解得 （ ）2个活塞流反应器串联。 整理并求解得 8 11 11 0 1 00 00 0 0 0 0 4 18 0.2 0.1,0.01 100 ln(1) (1) ln(1) AA AA A xx AAA AA AAA nAA V A ARrcmol Lh cmol LLh ARmol h dxdxx cc rkcxk qx Vq ck = = = = 活塞流反应器。反应，。 反应器折旧及操作费为￥。 不回收，求生产最佳反应体积、进料 速率及转化率。 解：一级反应活塞流反应器体积 依题 1 1 0 0 00 0 2 0 100 ln(1) 0.010.50.5 ln(1)0.01 10010050 0.51 ln(1) 0.10.2 50 1 ln(1)0 1 1 ln(1)0.6821 1 nRnAA nAA nAnA A A A AAA A A AAA A AA A nA qqxmol h qx MVqq ck x x xxx xdM x dxxx x xx x qq = =+=+ =+= = + = = = = 意 总费用 总费用最低 解得 1 331 000 3 0 0 1 /100/0.6821146.6 /146.6/(0.1 10 )1.466 ln(1)ln(1 0.6821) 1.4668.40 0.2 50 1 ln(1) 50 1 ln(1 0.6821)1.57 100 0.6821 nRA VnAA nAA A A nRnRA xmol h qqcmh qx Vm ck M x qq x mol = = = = = 产品成本 ￥ 9 0 22 1 22 1.81.8 1 22 2.2 1 2 420 /4/ 22min (1) 1 1(2)10.6322(2)0.184min 2 1 3(1.8)10.5934(1.8)0.203min 2 1 5(2.2)0.166min 2 (2) 1(2)12(2)3(1.8)0 4(1.8)05(2.2)0 3 V tVq FeEe s FeEe s Ee s FEE FE = = = = = = = = = 全混流 活塞流 （ ）非理想流 00 0 (0)0( )1( )0 ( )1( )2min ( )1 FFE E t dttE t dtt Ed = = = = = 体 10 4-21 t c(t) c(t) F(t) E(t) E(t) tc(t) t2c(t) 0 0 0 0 0 0 0 0 5 2 2 0.0396040.0792080.00792110 50 10 6 8 0.1584160.2376240.02376270 650 15 12 20 0.39604 0.4752480.047525250 3350 20 12 32 0.6336630.4752480.047525490 8150 25 10 42 0.8316830.39604 0.039604740 14400 30 5 47 0.9306930.19802 0.019802890 18900 35 2 49 0.9702970.0792080.007921960 21350 40 1 50 0.9900990.0396040.00396 1000 22950 45 0.5 50.5 1 0.0198020.00198 1022.5 23962.5 50 0 50.5 1 0 0 1022.5 23962.5 50.5 t平均= 20.24752 离散度= 64.54269 离散度= 0.157436 0 0.2 0.4 0.6 0.8 1 1.2 02468101214 F(t) 10E(t) 0 0 2 222 0 t 0 2 2 t 22 ( ) 1022.5 20.25 s 50.5 ( ) ( ) 23962.5 20.2564.54 50.5 ( ) 64.54 0.1574 20.25 tc t t c t t c t t c t t = = = 11 () () 2 24 23 0 0 3 1 1 44 0 0 2 2 48 0 0 422 ( )16 exp( 4 ) 22 (1)16exp( 4 )16 4( 4)( 4) 16 2 00.5 ( 4) (2)(1)16 exp( 4 )41510.9084 (3)(2)16 exp( 4 )41910.9970 (4) t t t E ttt tt ttt dte Ftt dtete Ftt dtete = =+ = = + = = + = 多釜串 22232 00 3 422 0 2 2 2 2 22 0 0 ( )16exp( 4 ) 3 160.75 0.50.50.125 44 0.125/0.250.5 1/2/0.25 11 110.84 (1)(1 6 0.25) 5 t t t i A i A A A t E t dtttt dtt t ett t NttN x kt dx tc r = = = = = = = + = 联模型 （ ） 凝集流模型,间歇釜式反应器一级反应 0 0 0 4 00 1010 20 0 ln(1) (1) 1 ( )(1) 16 e 16 1 16e1e( 101) ( 10) 1 16/1000.84 AA xx AA A AA kt A ktt AA tt dxx c kcxk xe xx E t dtetdt tdtt = = = = = = = 12 () 13 21 S 22 S SSS 423 ,1.7 10 2.556.2 22.522.5 50.17 0.8333 0.60395.0325 1/0.199 111 0.186 tanh 33 424 2 1 P Pe A 21 1 ABDe Vks ADmms r cms = = + = = = = 内 内 内