课程设计-课设模板

第一章塔的工艺计1-1原料组成（重量丁烯-丁烯-11、2、3、4、5、6、7、8分别代表组分乙原料中的质量分率ω1、ω2、ω3、ω4、ω5、ω6、ω7、ω8丙烷98%97%，则有：1)GχG

FGM

88FχFχWD1G1260.55kg/WD2G298%1309.598%1283.31kg/WD3G35225.85kg/WD4G43%1952.13%58.563kg/WD5WD6WD7WD888WχWD1WD2WD3WD4WD5WD6WD7WD8260.551283.315225.8558.5636828.273kg/8DχWDχWDD1260.556828.273DχWχMD1WD1M1260.5528.0549.287kmol/88DDχD1D2D3D4D5D6D79.28729.102124.1851.008163.582kmol/D.χDχxD1D1D9.287163.582Ww1Ww2G22%1309.52%26.19kg/Ww3Ww4G497%1952.13%1893.537kg/Ww5G5846.45kg/hWw6G61271.7kg/hWw7G71711.8kg/hWw8G8922.05kg/88WWχWw1Ww2Ww3Ww4Ww5Ww6Ww7Ww826.191893.537846.451271.71711.8922.056671.727kg/8wχWwχWwD226.196671.727塔底各组分的摩尔流率：WχWWχMW2Ww2M226.1944.0970.594kmol/88WWχW1W2W3W4W5W6W780.59432.57714.56322.66530.50912.779113.687kmol/8xwχWχxW2W1W0.594113.687表1- 质量衡算表率率率丁烯-表1- 摩尔衡算表率率率丁烯-由任务已知回流液的温度为根据烃类相平衡常数图和iKi进行试差得到冷凝器的压强，试差1-i由上表可知当压强为21.9atm时，iKi1则回流罐的压强为21.9atm

再次利用

yi1由上表可知当温度为53.5℃时

11-1则塔顶的温度为53.5℃,误差为215mmHg,则塔底的压又由烃类相平衡常数图和Kixi11-℃Kixi烷烷烯-1214)进料压强约为： 进 (Kixi1和烃类相平衡常数图试1-℃Kixi烷烷烯-5）1-温度温度℃℃ijDi ijFi1ij

ijt111553.52P1(2222.1382利用烃类相平衡常数图查得22.069atm84.25℃

K K14.39K1

18

1-烷烷烯-1Θ由 ijFi1q,而泡点进料时qijijFiij

1q0对Θ在3.130＜Θ＜6进行试差,直 ijFi0为止,试差结果ij

1-Θ4ijij----Θ=3.763时，ijij

＜0.005ijDi19.095.68%617.79%6.60975.92%3.130.62%ij 6 2.280RminRmin2.2801

lhlg

1 hD lW 其中

h分别为轻重关键组分的摩尔分率，m1-51-6K2DK4W

K4D

K2W则

0.862

2.03 m

lg

1 hD lW 0.52%

Nmin11.0301

（不包括再沸器Y1

1

X111117.2X

X05YNN

XRRRRmin1.0～3.0RX、Y，再通过YN，对R1NR/Rmin作图。1-RXYN1-1R1N

R1.70Rmin1.701.280N

56.730R

（不包括再沸器

)0LiF21-00丁烯-LiF00.00500.0090.0050.0070.0100.007其中m1-9

(l

)t84

1.38 E0.49()02450.49(1.9170.043)02450.903

N理17.86219.781（不包括再沸器实 实N'NN' (hkN'

(lkW)2Fhk F

0

RNRhk

N'SlkS1-3lkF

lkW

hkFhkD

D163.582kmol/N'NN' (hkN'

(lkW)2Fhk F

0

)

)2((

0

RNR

N

NSRNSR

'NS即精馏段理论板数为8.346层，提馏段为9.516NSNNR

NR110.2431-kg/ 00000丁烯-yiiD

yi/i i

/K其中 Kj

Kj为组分ij1-5MGyiMLiMiiMi L1-烷烯0000000MLiMi0.4659.05532.1100.896042.527g/iMi

32.110

4

5

8L

0.011

PcmPciyi5.68%5.0317.79%4.2575.92%4.620.62%4.572

TcmTciyi5.68%282.3517.79%369.875.92%364.950.62%361.466

T

Pr和TrZ

41.7462210130049.648kg/mllSmith

max其中C

()0mii3.5690.7630.0158.246SLS

2.176163.58241.74633.998m3/hsVVs

(R

(2.1761)163.58241.746436.843m3

根据经验，取板间距HT0.45m0.5mhl0.08mHT0.45SmithC20

板上液层高度CC()020

)0

ll445.250umax

u0.7，u0.7umax0.80.1360.109m/43.1443.140.109

DTD2H1.22450T1-CudDD2HT0.45D2HTDud

43.141.22

0.107m/

K其中 Kj

Kj为组分ij1-5M

y'Miiiiiiii

1-0000MGyiMi0.46418.2707.35111.93815.1683.74857.669MLiMi0.22916.6587.44611.18815.0598.111-2

28.38%12.69%19.06%25.66%

i P'0.52%4.24628.66%3.64812.81%3.819.94%i26.84%4.02311.24%3.3743.836

2.2138TcmTcii0.52%369.828.66%408.112.81%425.219.94%26.84%419.611.24%469.6417.944

T

Pr和TrZ

57.66922.13810130061.655kg/mllSmith

max其中C

()0mii '28.66%1.33512.81%2.7419.94%mii26.84%2.43211.24%6.3382.556L (LqFL l

(RDF'l

(2.176163.582277.27)58.69086.493sV'sL'LVsVs

V''v''v

(R'v

(2.1761)163.582

根据经验，取板间距HT0.45m0.5mhl0.08mHT0.45SmithC20

板上液层高度CC()020

0.057

)0

'vmax

0.036

0.092u0.7，u0.7umax0.70.0920.074s4s43.140.071

1.526DD2HT1.624501-CudDD2 H0.45D2H最小，所以选择第一组，此时塔板的半径为D 则空塔气速为：u d

43.141.62

1-烷烷烯烯碳五转化成kcal/kmol1-烷烷烯烯1）Hv1HivyiD5.68%507817.79%747475.92%71540.62%7108.724HLDHiLiD5.68%359117.79%434475.92%42500.62%QC(R1)D(HV1HLD)(2.1671)163.582(7108.7241.488106kcal/h5.374106却水升温10℃，则冷却水用量为：mQCP CP

5.3744.176

H HH

y'1.1%586333.2%1057912.6%1121821.3%i27.0%108114.80%1439411005.098iH H'H

0.52%443328.66%802112.81%796319.94%26.84%776211.24%94888066.436QV'(H H )(R1)D(H H 1.522106kcal/h6.374106令水蒸气压力为10atm,查得该压力下饱和水蒸汽的温度为180℃，汽化潜热为2020kJ/kg，则水蒸汽用量为：mQB

6.374

3155.4463）HFHiFiF38433.40%509311.40%496643.41%621961035.33%59238.30%567411.17%FHF277.275425.1891.504106kcal/h6.298106kJ/DHLD163.5824236.5736.930105kcal/h2.901106kJ/Q

QDHLDWHLW2.9011063.8391065.37410612.114106 -

-.

106

kJ/h1.9

1-20率率率丁烯-1-21率率率丁烯-

1-温度压强温度压强温度压强温度压强最小回流实际回流最小理论板理论板全塔效实际板实际精馏板9实际提馏板加料位10

1-进入热量带出热量热量损失5.3743.83912.672第二章塔板的工艺尺寸设

lwD

Wd/D Ad/AT则降液管宽度为：Wd0.2D0.21.2AD21.22 hw60hbhb

F-1型浮阀阀孔直径d039mmd02.5mm，最大开度为

最小开度为F根据阀孔动能因数F09~12F010FF0

得到阀孔气速：u0

1.419m/uT

N0

d

0.03921.419

71.61040 在方格纸上画出草图（如附件），可以得到：阀孔数为t

分布区和破沫区为：WF边缘区为：WCu0

d2

0.039274

4 r2Ar2

r2

1

(rD(WW)1.2(0.240.06) rD

1.20.112r2Ar2

r2

1

(r0.49020.4902

0.4902sin1(

)F0

塔板压力降为（m液柱）：hhh'

uhc5.37

5.37

1.373229.8

0.058(m液柱h'(hh 0.5，how0.00284E(hEhow0.00284

30.032(m液柱lh'0.5(0.040.032).6l

克服表面张力的压降h一般很小，可忽略不计'

液柱

00360.0580.①用阿列克罗山德罗夫经验公式计算雾沫夹带量eeA(0.052hl1.72)THnT

)3其中：A n

0.549

系数HT

hlhwhow4032m5.63105(l)0295(lv)0 15

26

37

48混合气相的气相粘度（μPasviDi5.68%11.13717.79%8.88775.92%9.3880.62%9.394μPas9.58107kgf53.5℃lm5.63105(2.851)0295(445.25049.648)0

e0.159(0.052721.72)(4500950.62

)370.034kg雾沫/kg气浮阀塔的泛点率由以下公式得到（取其中最大值12F100Cv136Ls F 12Ab

0.78

其中

Vs

436.843VV445.250

CFKs

1000.04313633.99836000.7259.037%0.8080.9600.114F2

1000.781.1300.96

Hdhwhowhhd其中hhdhd1

lwhb

2

0.960.05

20.006m液

200..11

2

20.004m液Al Al

相对密度取：Hd0.175

HT

0.450.04

在浮阀塔结构参数的确定中已得到塔板的实际动能因数为：F0

HT

0.450.161

满足3~L液体在降液管中的流速：ud L

0.059m/（umax1（u）

)-d

u

6)在泛点率的计算中取的是F1，则过量雾沫夹带线的方程式为V lv-（2.952103 1.36ZL v

a abcL2-0la0.01480l

0.0148

3.01410-N2 742bHT(1)hw0.70.45(0.710.5)0.041.952wc (lhw

1.952108

8.472d

l)l)

Vh 969.0435.302L2hh③过量过量线方程为

21.5

225.798m3/L3600AdHT其中 留时间，取4sL3600Ad

36000.1610.454

3.070.962.947m3/Vh436.843 则操作线方程：Vh2-1由图可知气相负荷的上下限分别为操作线与过量雾沫夹带线和过量Vh

606.408m3/由过 线和操作线的交点，得到气相负荷的上限hV257.384m3/hK

606.4083~4，可设堰长lw80%D801.61.28lwD

Wd/D Ad/AT则降液管宽度为：Wd0.2D0.21.6AD21.62 Ad0.1424At0.14242.010hw6050mmF-1型浮阀阀孔直径d039mmd0mm，最大开度为

最小开度为根据阀孔动能因数F09~12F010根据公式：F0

得到阀孔气速：u0 FVF

1.274m/uT0.067m则开孔率为：uT1000.067100%

N0

d

0.03921.274

88.77240 在方格纸上画出草图（如附件），可以得到：阀孔数为t

分布区和破沫区为：WF边缘区为：WCu0

d2

0.039289

1.270m/4 r2Ar2

r2

1

(rD(WW)1.6(0.320.105) rD

1.60.12r2Ar2

r2

1

(r0.790220.470 0.7902sin1(0.470)0.7902F0

0.790塔板压力降为（m液柱）：hhh'

uhc5.37

5.37

1.270229.8

0.063(m液柱h'(hh 0.5，how0.00284E(hEhow0.002841.048

30.049(m液柱lh'0.5(0.040.049)0.05l

克服表面张力的压降h一般很小，可忽略不计'

液柱

00450.0630.①用阿列克罗山德罗夫经验公式计算雾沫夹带量eeA(0.052hl1.72)THnT

)3其中：A n

1.391

系数HT

hlhwhow4049m

0

15

26

37

48混合气相的气相粘度（μPasviDi0.52%11.39928.66%10.93412.81%10.46519.94%10.626.84%10.16311.24%10.503μPas1.07106kgf53.5℃l2.556m5.63105(2.556)0295429.68061.655)0425 e0.195(0.05289450095

1.07106(0.6920.093

)3

0.004kg雾沫kg气浮阀塔的泛点率由以下公式得到（取其中最大值12F100Cv136Ls F 12Ab

0.78

其中

Vs

485.950VV429.680

CFKs

1000.05513686.49336000.961.4370.960F2

1000.782.0100.96

Hdhwhowhhd其中hhdhd1h

2

20.022m液w

1.2800.05ld 01Ls2 2ld

20.014m液Al wAl

1.2800.05hdhd1hd20.0220.0140.036m液相对密度取：Hd0.233

HT

0.450.04

在浮阀塔结构参数的确定中已得到塔板的实际动能因数为：F0

HT

0.45

满足3~L液体在降液管中的流速：ud L

0.286

0.084m/（umax1HT(l-v（HT(l-vd （udmax6)在泛点率的计算中取的是F1，则过量雾沫夹带线的方程式为V l-

2.952103KA

1.36ZL sb v a abcL2-0la0.01480l

2.68110-N2 892bHT(1)hw0.70.45(0.710.5)0.041.952c

1.952

4.7662b(lwhb

(1.28d0.00284(1

ll

0.00284(1

Vh 1027.4124.216L2hh③过量过量线方程为

21.5

243.694m3/L3600AdHT其中 留时间，取3.56sL3600Ad

36000.2860.45130.146m3/h

3.071.283.930m3/Vh485.950 则操作线方程：Vh2-2由图可知气相负荷的上下限分别为操作线与淹塔线和过量线的交点LVh

731.160m3/由过 线和操作线的交点，得到气相负荷的上限hV257.384m3/hK

731.160塔径堰长堰高降液管底隙降液管面积(m2分布区/破沫区雾沫夹带量(kg雾沫kg气体泛点核算塔板压降降液管内液面高度停留时间液体在降液管中流速第三章根据平均温度84.25℃，平均压力22.069atm，选择筒体材料Q235-C钢，壁厚30mmDgs

h2DgsDg

h22062个人孔，除s2个TH'T4)HD1.2mHB3mHF1.1m

HHBHDHF(n2s)HT'TT

1.231.1(2022)0.4520.7D

30D

D

H厚度取6mmDg450内径DibDis0.2

四个排气管：57

DobDis0.4

uv1043.1443.1410

3-8dv

uv

43.140.1252

9.893m/

2.0 4 43.142

P1093-6dR

uR

43.140.0892

1.59m/

i68.8℃（i15

26

37

48i混合液体平均密度： i

GF

29.310443.142

P1093-6dFuF

43.140.0742

1.796m/

1.04L44L43.141

3-6dw

uw

3.1402192

0.638