(完整版)化工原理课后答案

1、 p p p 101.3130绝表ap p p 231.375表绝a U 3p gh gh0p gR gm013.610 9.810.459009.810.8360037.27063.252974Pa kPa 9m 33 4 : :m q 9183116479kg/hsVq9/3600u 10.69m/sV0.785d0.7850.06822G u 0.6918311263.4kg/m2 s11 3.5 :16479kg/h ms2q9/u 21.27m/sV0.785d0.05222du u ( ) 0.69( ) 1.27m/s22121d2G u 1.271831 2325.4kg/m2

2、 s22 11ppZ g u Z g uW121222 2 212f12f1( 120)9.81 2.09m233 Z g u W Z g 121e2fp12e2fW 212e2fmsu 222.0) 1622e2 u f1hm 3 p3311pp1212f1pZ g 21f12 : V22334s26.39m3/h33AB efees11ppu Z u Z h22A2g2gAABBppAB15310 p 11009.81(79)3BBa Bm 33）Vu s2p sa 0.05 999.7 2 2W 0.052fh W /g 1.475mffP W 14465.7Pffa 33qu Vd24

3、12:11pp121e2f: We2fll u 22W 18.42J /ed22fsskg/m s z 。 1211ppZ g u1212fp:2f0.1061.5 由0.002 0.026d2个lu22W ( )(0.026d2fpZ ( W )/g (2f19.8111ppA22AABBfp，ABAB2则有ed2ABf） 64 du32( )lll2ee2dAB0.04 900 09.81d22AB32l l )323010 (503020)3e883.2 u 0.7850.04m2243411pp12211AA1pA21ApA12AAu p BB） ；）V0s0020.69.81998.

4、2)0.610.022998.2m33sh1面，高位槽液面为221 22121e2f: Wefl lWu2而ed2fV3ms0.785ds20.02J0.052fJe13面，在13p 1p 1 u Z g u Z g W121323 2 213fZ u Z 1.5,u 1.19m/s1133Wl 120 1.192 u 0.025.66J /2d 20.052fp p 1 u Z g W132323f1.19221.59.815.6621.023J /kgp p 21.0239.8120.6kPa13 和和，30q3600u 12.166mVs0.7850.072d2143036000.785

5、0.052u 4.246ms211ppu Z H u Z121222 2g 2g gg12ep p1H u u )Z2122212gge(21540)31(4.246 )0.422 9.8129.813N g 303600109.8127.07kW3eN2.2133.45100%100%64.1%eN第二章 非均相物系分离m m 33s s3-3）d ( )g ) (265026 2u t s4181.013 8.02 64 2.38 0 2)t241.01t3 u -4t s3-5d ( )g ) (265026 2u t7.18 s2181.815 7.18 62 0 2)t41.81t5

6、u -2t m 33s查 3-5 2当ttd ( )g du 3 2st182363610 )2d 7.7310 m m533( )g(21509.811.21s m 、 、 uigu/R 即id ( ) u (2650 222u i0.0262m/s s18R1.013r 5 2)r41.01t3u ru22iK c 2 m -3-33m 3 t V m t V m t 2-33-3311223V 2.273q 24.4131A1V 3.353q 236.0232A）q 2q q Kt(24.4110 ) 224.4110 q 50K213 23e 11eq 2q q Kt(36.0210

7、) 236.0210 q 100K223 23e22eq -5-3eq 24.1410 q 2001.5961023353q 3 V =q m-3333第三章 传热. ,t 13t t t tq2123bb21t 75 753010.250.160.050.16t 455753001 和W/(mW/(m和W/(m过t tt0.5）q 1t t4 12 20.50.251 b2 b31b2 1.02 0.14 0.921.021231将t b 22t t4t tt (b)q 1 34 30.50.250.250.921 b2 b3b3b2 1.02 0.14 0.921233将t b 32将b

8、t 22 5=16W/mK管内半径r 20mm0.02m,管外半径r 25mm0.025m12管外半径保温层厚度 r 0.0250.030.055m3Ql2t t )23.14100)131 r 1 r r 1 123r1122Qlt t )131 r 1 r 23 r r1122t tt tt1 t 2122321 r1 r12211rr11t 2 205035t2 62.5710 W/m Kc 4.174kJ/kgK2 7.2810 Pas5，p 994kg/m3u 1du0.02172.8105 c p4.8762.57102 0.023 Re Pr 0.02327307 4.870.8

9、0.40.80.4d0.020.719535401.884788W /(m )2 的q m/s, r /Qq r m(2) T 333K c 2.19 /(K)2mpQq c T T )2.19mp12(2) c 3.77 /(K)pQq c T T )126mp12(4) t c 1.009 /()p2mQq c t t )54.7mp12p t , r 2230 /st 502t m80.52c 4.2 /()pQq rc t t (22304.2 1035.9.mp12和 T 325K c /(K)2m1Qq c T T )300)m1 112t mc 4.174 /()p2Qq mc

10、t t ) p212 15加热至 120降至 60.试计算换t ,t 12t t t m60.812t1t2t ,t 12t t t m51.312t1t2 Qq c T T )q c t t )m1 112m2 p212c 4.19 /,c 4.174 /1p24.19q m2q m2t ,t 12t 40mQ 3Q KSt S 1.309m2Ktmmss l md 3t ,t 12t t t 21tm1t2Q 3S m2Ktmsl md 3 平22 。233H。 4.2kPa psp p p 101.34.2 97.1kPa*Asc3MS2.875cAc2x 5.17455.5697.1p

11、*E 1.876 5Ax5.1742.875102cH 2.9610kmol/(kPam )43A*97.1pAE 5m p101.3 0.4 0.012Y* 2.52X 0.06yY 1 2.52X 2.520.012 *Y111 y 10.0611yY 2Y X 2.52 2.520 0*21 y1222Y Y Y *222Y Y Y *111 2 2中 222 222解 : 通 过 静 止 空 气 层 扩 散 到 某 碱 溶 液 液 面 属 单 向 扩 散 ， 可 用 式2N (p p )。A m 2-522 p = 2 p 2p =p p =p p p101.381.06p Bm90.

12、8kPa=B2B1101.3plnlnB2B181.06p(p p )NAN (p p )A1.85101.3(20.27= 90.8 -42 用 kPa 30.757XY* 2 pY1）Ap 101.3BY Y ) 0.99) 14 31.8kmol/h31.8(0.0121773273V 29322.4Y Y1L V 23.8kmol/h20.01X Xmin*0120.757L =231.8(0.010.0066）X =X +Y Y 121247.6分A A 2.5XAY*yY 1 11 y 11yY 221 y12x1X 1x 111Y YY YY2Y0.005L m ) ) V 12

13、12X X0.0417Y*1mmin121 2.2Y Y0L12V X X12LL3 .03/ 1 .38V V 2 .2min 为-322的 2217.8X为Y*37800 2100kmol/hL180.09yY 1 11 y 10.091Y Y ) 21 y ) 0.09) V1V91X X Y Y ) 1.110 (0.099 4.531033L21001212Y Y Y 17.8 *3111Y Y Y 17.81.1 2.24*3222Y Y 0.01842.2104Y 2 4.11031Y0.0184mlnln1Y2.21042Y YN 219.31Y4.13m 2 2 kPa,K

14、a 3Yy Y11 y 111Y Y ) 0.02 21E 177m 1.77p 100mV 1.770.024S 0.653L0.06511N OGln S)S1S111N 11VH 1.039mK a YZ N H 9.761.03910.14m 96 P P 。*ABP x + P x*AABBx x )AAx A=P xy *AAAA M /M /AM 1140.31280.7123.8kg/kmolF 5000/123.840.39kmol/hDxB100%0.88DDFxFDx 0.88Fx 0.8840.390.310.66kmol/hDFFx Dx WxFDWWx Fx Dx

15、0.12FxWFDFW 0.12Fx /x 0.1240.390.3/0.0529.08kmol/hFWD F W 40.3929.08kmol/h/0.88 40.39 0.3/11.31 0.943x Fx D DDF6-7在Rx30.964Ry x n xR1 4Dn1 R1精馏段操作线方程y 0.75x0.24L RD330.5291.59kmol/h,V (RD4Dkmol/h泡点进料q VV kmol/hL LF 91.5975166.59kmol/h166.59122.144.180.1LWy x x xV122.1VW提馏段操作线方程y 1.364x0.03646-8某连续精馏塔，泡点进料