化工原理课本复习题答案.docx
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化工原理课本复习题答案
《化工原理》课本习题答案
第一章 流体流动
1 PA(绝)= 1.28×105 N/m2
PA(表)= 2.66×104N/m2
2 W = 6.15吨
3 F = 1.42×104N
P = 7.77×104Pa
4 H = 0.39m
5 △P = 2041×105N/m2
6 P = 1.028×105Pa △h = 0.157m
7 P(绝)= 18kPa H = 8.36m
8 H = R PA> PB
9 略
10 P = Paexp[-Mgh/RT]
11 u = 11.0m/s ; G = 266.7kg/m2s
qm = 2.28kg/s
12 R = 340mm
13 qv = 2284m3/h
14 τ= 1463s
15 Hf = 0.26J/N
16 会汽化
17
18 F = 4.02×103N
19 略
20 u2 = 3.62m/s ; R = 0.41m
21 F = 151N
22 v = 5.5×10-6m2/s
23 =0.817 a = 1.06
24 略
25 P(真)= 95kPa ; P(真)变大
26 Z = 12.4m
27 P(表)= 3.00×105N/m2
28 qv = 3.39m3/h P1变小 P2变大
29 qv = 1.81m3/h
30 H = 43.8m
31 τ= 2104s
32 He = 38.1J/N
33 qv =0.052m3/s=186m3/h
34 qv1 = 9.7m3/h ; qv2 = 4.31m3/h
qv3 = 5.39m3/h ; q,v3 = 5.39m3/h
35 qvB/qvC = 1.31 ; qvB/qvC =1.05 ;能量损失
36 P1(绝)=5.35×105Pa
37 = 13.0m/s
38 qv = 7.9m3/h
39 qVCO2(上限)=3248l/h
40 = 500 l/s ; τ=3×104Pa
F = 3×102N P = 150w
41 he = 60.3J/kg
42 τy = 18.84Pa μ∞ = 4.55Pa·s
43 τy = 39.7Pa
44 略
第二章 流体输送机械
1 He = 15+4.5×105qV2
He = 45.6J/N Pe = 4.5KW
2 P = ρω2r2/2 ; Φ/ρg = u2/2g = 22.4J/N
3 He = 34.6J/N ; η = 64%
4 略
5 qV = 0.035m3/s ; Pe = 11.5KW
6 串联
7 qV = 0.178m3/min ; qV, = 0.222m3/min
8 会汽蚀
9 安装不适宜,泵下移或设备上移
10 IS80-65-160 或 IS100-65-315
11 ηV = 96.6%
12 不适用
13 P = 33.6KW ; T2 = 101.0℃
14 qV = 87.5m3/h ; 选W2
第三章 流体的搅拌
1 略
2 P = 38.7w ; P’ = 36.8w
3 d/d1 = 4.64 ; n/n1 = 0.359 ; N/N1 = 100
第四章 流体通过颗粒层的流动
1 △φ = 222.7N/m2
2 △φ/L = 1084Pa/m
3 V = 2.42m3
4 K = 5.26×10-4m2/s ; qe = 0.05m3/m2
5 A = 15.3m2 ; n = 2台
6 略
7 △V0 = 1.5L
8 △V = 13L
9 q = 58.4l/m2 ; τw = 6.4min
10 τ = 166s ; τw = 124s
11 K = 3.05×10-5m2/s
Ve = 5.06×10-2m3 ; V = 0.25m3
12 n’ = 4.5rpm ; L’/L = 2/3
第五章 颗粒的沉降和流态化
1 ut = 7.86×10-4m/s ; ut’ = 0.07m/s
2 dP = 88.8μm
3 τ = 8.43×10-3s ; s = 6.75×10-5m
4 dpmax = 3.6μm
5 dpmin = 64.7μm ; ηP = 60%
6 可完全分开
7 ζRe2<48
8 η0 = 0.925 ; x出1 = 0.53
x出2 = 0.27 ; x出3 = 0.20
x出4 = 0 ; W出 = 59.9kg/day
9 ε固 = 0.42 ; ε流 = 0.71 ; ΔФ = 3.14×104N/m2
10 略
11 D扩 = 2.77m
12 略
第六章 传热
1 δ1 = 0.22m ; δ2 = 0.1m
2 t1 = 800℃
3 t1 = 405℃
4 δ = 50mm
5 (λ’-λ)/ λ = -19.7%
6 略
7 Q,/Q = 1.64 λ小的放层
8 a = 330W/m2*℃
9 a = 252.5W/ m2*℃
10 q = 3.69kw/m2
11 q1/q2 =1
12 w = 3.72×10-3kg/s ; w’= 7.51×10-3kg/s
13 Tg = 312℃
14 Tw = 746K
15 τ = 3.3hr
16 εA = 0.48 ; εB = 0.40
17 略
18 热阻分率0.3% K’= 49.0W/m2·℃ ; K,, = 82.1W/m2·℃
19 w = 3.47×10-5kg/m·s ; tw = 38.7℃
20 δ= 82mm
21 a1 =1.29×104W/m2·℃ ; a,2 = 3.05×103W/m2·℃ ; R = 7.58*10-5m2·℃/W
22 δ= 10mm ; Qmax = 11.3KW
23 R = 6.3×10-3m2·℃/W
24 n = 31 ; L = 1.65m
25 L = 9.53m
26 qm = 4.0kg/s ; A = 7.14m2
27 qm2 = 10.9kg/s ; n = 36 ; L = 2.06m ; q,m1 = 2.24kg/s
28 qm = 0.048kg/s
29 t2 = 76.5℃ ; t2 = 17.9℃
30 t,2 = 98.2℃ ; 提高水蒸气压强 T’= 112.1℃
31 qm1 = 1.24kg/s
32 T,2 = 78.7℃ ; t,2 = 61.3℃
33 T = 64.6℃ ; t2a = 123.1℃ ; t2b = 56.9℃
34 t2 = 119℃
35 τ = 5.58hr
36 单壳层 Δtm = 40.3℃ ; 双壳层Δtm’= 43.9℃
37 a = 781W/m2·℃
38 L = 1.08m ; t2’= 73.2℃
39 NP = 2 ; NT = 114 ; L实 = 1.2L计 = 3.0m ; D = 460mm
第七章 蒸发
1 W = 1500kg/h ; w1 = 12.8% ; w2 = 18.8%
2 Δt = 12.0℃
3 A = 64.7m2 ; W/D = 0.839
4 W = 0.417kg/s ; K = 1.88×103W/m2·℃ ; w’= 2.4%
5 t1 = 108.6℃ ; t2 = 90.9℃ ; t3 = 66℃
6 A1 = A2 = 9.55m2
第八章 吸收
1 E=188.1Mpa;偏差0.21%
2 G=3.1×10-3kgCO2/kgH2O
3 Cmin=44.16mg/m3水;Cmin=17.51mg/m3水
4 (xe-x)=1.19×10-5;(y-ye)=5.76×10-3 ;(xe-x)=4.7×10-6 ;(y-ye)=3.68×10-3
5 (y-ye)2/(y-ye)1=1.33 ; (xe-x)2/(xe-x)1=2.67
6 τ=0.58hr
7 τ=1.44×106s
8 Kya=54.9kmol/m3·h ; HOG=0.291m ;液相阻力分率15.1%
9 NA=6.66×10-6kmol/s·m2 ; NA’=1.05×10-5kmol/(s·m2)
10 略
11 略
12 NOG=
13 略
14 略
15 x1=0.0113; =2.35×10-3 ;H=62.2m
16
(1)H=4.61m;
(2)H=11.3m
17 Gmin=0.489kmol/m2·h ; x2=5.43×10-6
18 HA=2.8m ; HB=2.8m
19
(1)HOG=0.695m;Kya=168.6kmol/m3·h;
(2)w=4.36kmol/h
20 y2=0.002
21 η’=0.87;x1’=0.00325
22 y2’=0.000519
第九章 精馏
1
(1)α1=2.370 ;α2=2.596 ;
(2)αm=2.484
2 t=65.35℃ ; xA=0.512
3 t=81.36℃ ; yA=0.187
4 =1.35
5
(1) =31.3kmol; =0.619
(2) =38.0kmol;y=0.563
6
(1)D/F=0.228;
(2)L/V=0.667; =0.470 (3)L/V=0.8 ; =1.68
7 =14.32kmol/h
8
(1)V=10kmol/h ;
(2)R=16; L/V=0.941
9 =120kmol/h ; yn+1=1.17xn-0.025
10 略
11 略
12 NT=16 ; 加料板为第8块
13
(1) =12.8kmol/h ; η=92.5%;
(2)NT=7
14
(1)S=11.5kmol/h ; η=83.2%;
(2)NT=7
15 NT=15
16 NT=8; xDmax=0.644
17 NT=18
18 η=96.7%; Rmin=1.51
19 xD=0.889; xW=0.194
20 xD=0.873; xW=0.207
21 xD=0.00869; xW=3.27×10-4
22 xW=0.0935; EmV=66.4%
23
(1) xD=0.8; xW=0.05;
(2)略
24
(1)NT=7;
(2)V=20.3kmol/h; (3)D=47.4kmol; W=52.6kmol
25 t=60℃; xA=0.188; xB=0.361; xC=0.451
26 x(A-D) :
0.030;0.153;0.581;0.237 y(A-D) :
0.141;0.306;0.465;0.085
27 D/F=0.4975;W/F=0.5025; xD(A-D):
0.402;0.591;0.007;9.7×10-5 ;
xW(A-D):
1.4×10-5;0.012;0.690;0.298
28 N=14.1 ; N1=7.9
第十章 气液传质设备
1 EmV=0.758
2 ET=41%
3 N实=10
4 D=1.2m
5 HETP=0.356m
6 D=0.6m; △P/H=235.44Pa/m
第十一章 萃取
1
(1)E=64.1kg;R=25.9kg;x=0.06;y=0.046
(2)kA=0.767;β=14.6
2
(1)E=92.2kg;R=87.8kg;yA=0.13; xA=0.15
(2)E°=21.31kg;R°=78.69kg;yA°=0.77;xA°=0.16
3
(1)R=88.6kg;E=130.5kg;yA=0.0854;yS=0.862;yB=0.0526;xS=0.0746;xB=0.825
(2)S=119.1kg
4 xA2=0.22
5 E1=125kg;RN=75kg;yA1=0.148;yS1=0.763;yB1=0.089;xSN=0.0672;xBN=0.913
6
(1)S/B=24.9;
(2)S/B=5.13
7
(1)Smin=36.47kg/h
(2)N=5.1
第十二章 其它传质分离方法
1 m=47.7kg
2 t1=44.9℃
3 a=138.3m2/g
4 τB=6.83hr
5 W3=0.0825;qm2=5920.3kg/h; JV1=0.0406kg/m2·s; JV2=0.0141kg/m2·s
第十三章 热质同时传递的过程
1 略
2
(1)θ1=20℃;
(2)t2=40℃;H=0.0489kg水/kg干空气
3 H=0.0423kgH2O/kg干H2
4
(1)W=0.0156kgH2O/kg干空气
(2)tw3=18.1℃
5 t2=45.2℃;H2=0.026kg水/kg干气
6 W=2.25kg水/kg干气
7 P2=320.4kN/m2
8 Z=2.53m
第十四章 固体干燥
1 =74.2%; =5.6%
2 W水=0.0174kg水/kg干气; Q=87.6kJ/kg干气
3 略
4
(1)ΔI=1.25kJ/kg干气;
(2)t2=55.9℃;(3)t2=54.7℃
5
(1)t2=17.5℃;H2=0.0125kg水/kg干气
(2) =10.0%
6 自由含水量=0.243kg水/kg干料 结合水量=0.02kg水/kg干料
非结合水量=0.23kg水/kg干料
7 τ=7.06hr
8 τ=21.08hr
9
(1) =250.75kg干/h
(2)QP=25798.2kJ/h (3)QD=13984.3kJ/h
10 V=223kg/s; t1=163℃; η=81.1%
11
(1)V=10.9kg/s ; η=78%
(2)V=6.59kg/s; η=80.5%
12 V=2.49×104kg/h; Q预=3.01×106kJ/h