第一章塔的工藝計(jì)1-1原料組成（重量丁烯-丁烯-11、2、3、4、5、6、7、8分別代表組分乙原料中的質(zhì)量分率ω1、ω2、ω3、ω4、ω5、ω6、ω7、ω8丙烷98%97%，則有：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塔底各組分的摩爾流率：WχWWχMW2Ww2M226.1944.0970.594kmol/88WWχW1W2W3W4W5W6W780.59432.57714.56322.66530.50912.779113.687kmol/8xwχWχxW2W1W0.594113.687表1- 質(zhì)量衡算表率率率丁烯-表1- 摩爾衡算表率率率丁烯-由任務(wù)已知回流液的溫度為根據(jù)烴類相平衡常數(shù)圖和iKi進(jìn)行試差得到冷凝器的壓強(qiáng)，試差1-i由上表可知當(dāng)壓強(qiáng)為21.9atm時(shí)，iKi1則回流罐的壓強(qiáng)為21.9atm

再次利用

yi1由上表可知當(dāng)溫度為53.5℃時(shí)

11-1則塔頂?shù)臏囟葹?3.5℃,誤差為215mmHg,則塔底的壓又由烴類相平衡常數(shù)圖和Kixi11-℃Kixi烷烷烯-1214)進(jìn)料壓強(qiáng)約為： 進(jìn) (Kixi1和烴類相平衡常數(shù)圖試1-℃Kixi烷烷烯-5）1-溫度溫度℃℃ijDi ijFi1ij

ijt111553.52P1(2222.1382利用烴類相平衡常數(shù)圖查得22.069atm84.25℃

K K14.39K1

18

1-烷烷烯-1Θ由 ijFi1q,而泡點(diǎn)進(jìn)料時(shí)qijijFiij

1q0對(duì)Θ在3.130＜Θ＜6進(jìn)行試差,直 ijFi0為止,試差結(jié)果ij

1-Θ4ijij----Θ=3.763時(shí)，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分別為輕重關(guān)鍵組分的摩爾分率，m1-51-6K2DK4W

K4D

K2W則

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，再通過YN，對(duì)R1NR/Rmin作圖。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（不包括再沸器實(shí) 實(shí)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即精餾段理論板數(shù)為8.346層，提餾段為9.516NSNNR

NR110.2431-kg/ 00000丁烯-yiiD

yi/i i

/K其中 Kj

Kj為組分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

根據(jù)經(jīng)驗(yàn)，取板間距HT0.45m0.5mhl0.08mHT0.45SmithC20

板上液層高度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為組分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

根據(jù)經(jīng)驗(yàn)，取板間距HT0.45m0.5mhl0.08mHT0.45SmithC20

板上液層高度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，所以選擇第一組，此時(shí)塔板的半徑為D 則空塔氣速為：u d

43.141.62

1-烷烷烯烯碳五轉(zhuǎn)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卻水升溫10℃，則冷卻水用量為：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令水蒸氣壓力為10atm,查得該壓力下飽和水蒸汽的溫度為180℃，汽化潛熱為2020kJ/kg，則水蒸汽用量為：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-溫度壓強(qiáng)溫度壓強(qiáng)溫度壓強(qiáng)溫度壓強(qiáng)最小回流實(shí)際回流最小理論板理論板全塔效實(shí)際板實(shí)際精餾板9實(shí)際提餾板加料位10

1-進(jìn)入熱量帶出熱量熱量損失5.3743.83912.672第二章塔板的工藝尺寸設(shè)

lwD

Wd/D Ad/AT則降液管寬度為：Wd0.2D0.21.2AD21.22 hw60hbhb

F-1型浮閥閥孔直徑d039mmd02.5mm，最大開度為

最小開度為F根據(jù)閥孔動(dòng)能因數(shù)F09~12F010FF0

得到閥孔氣速：u0

1.419m/uT

N0

d

0.03921.419

71.61040 在方格紙上畫出草圖（如附件），可以得到：閥孔數(shù)為t

分布區(qū)和破沫區(qū)為：WF邊緣區(qū)為：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

塔板壓力降為（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

克服表面張力的壓降h一般很小，可忽略不計(jì)'

液柱

00360.0580.①用阿列克羅山德羅夫經(jīng)驗(yàn)公式計(jì)算霧沫夾帶量eeA(0.052hl1.72)THnT

)3其中：A n

0.549

系數(shù)HT

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

26

37

48混合氣相的氣相粘度（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霧沫/kg氣浮閥塔的泛點(diǎn)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

相對(duì)密度?。篐d0.175

HT

0.450.04

在浮閥塔結(jié)構(gòu)參數(shù)的確定中已得到塔板的實(shí)際動(dòng)能因數(shù)為：F0

HT

0.450.161

滿足3~L液體在降液管中的流速：ud L

0.059m/（umax1（u）

)-d

u

6)在泛點(diǎn)率的計(jì)算中取的是F1，則過量霧沫夾帶線的方程式為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過量過量線方程為

21.5

225.798m3/L3600AdHT其中 留時(shí)間，取4sL3600Ad

36000.1610.454

3.070.962.947m3/Vh436.843 則操作線方程：Vh2-1由圖可知?dú)庀嘭?fù)荷的上下限分別為操作線與過量霧沫夾帶線和過量Vh

606.408m3/由過 線和操作線的交點(diǎn)，得到氣相負(fù)荷的上限hV257.384m3/hK

606.4083~4，可設(shè)堰長(zhǎng)lw80%D801.61.28lwD

Wd/D Ad/AT則降液管寬度為：Wd0.2D0.21.6AD21.62 Ad0.1424At0.14242.010hw6050mmF-1型浮閥閥孔直徑d039mmd0mm，最大開度為

最小開度為根據(jù)閥孔動(dòng)能因數(shù)F09~12F010根據(jù)公式：F0

得到閥孔氣速：u0 FVF

1.274m/uT0.067m則開孔率為：uT1000.067100%

N0

d

0.03921.274

88.77240 在方格紙上畫出草圖（如附件），可以得到：閥孔數(shù)為t

分布區(qū)和破沫區(qū)為：WF邊緣區(qū)為：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塔板壓力降為（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

克服表面張力的壓降h一般很小，可忽略不計(jì)'

液柱

00450.0630.①用阿列克羅山德羅夫經(jīng)驗(yàn)公式計(jì)算霧沫夾帶量eeA(0.052hl1.72)THnT

)3其中：A n

1.391

系數(shù)HT

hlhwhow4049m

0

15

26

37

48混合氣相的氣相粘度（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霧沫kg氣浮閥塔的泛點(diǎn)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液相對(duì)密度?。篐d0.233

HT

0.450.04

在浮閥塔結(jié)構(gòu)參數(shù)的確定中已得到塔板的實(shí)際動(dòng)能因數(shù)為：F0

HT

0.45

滿足3~L液體在降液管中的流速：ud L

0.286

0.084m/（umax1HT(l-v（HT(l-vd （udmax6)在泛點(diǎn)率的計(jì)算中取的是F1，則過量霧沫夾帶線的方程式為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過量過量線方程為

21.5

243.694m3/L3600AdHT其中 留時(shí)間，取3.56sL3600Ad

36000.2860.45130.146m3/h

3.071.283.930m3/Vh485.950 則操作線方程：Vh2-2由圖可知?dú)庀嘭?fù)荷的上下限分別為操作線與淹塔線和過量線的交點(diǎn)LVh

731.160m3/由過 線和操作線的交點(diǎn)，得到氣相負(fù)荷的上限hV257.384m3/hK

731.160塔徑堰長(zhǎng)堰高降液管底隙降液管面積(m2分布區(qū)/破沫區(qū)霧沫夾帶量(kg霧沫kg氣體泛點(diǎn)核算塔板壓降降液管內(nèi)液面高度停留時(shí)間液體在降液管中流速第三章根據(jù)平均溫度84.25℃，平均壓力22.069atm，選擇筒體材料Q235-C鋼，壁厚30mmDgs

h2DgsDg

h22062個(gè)人孔，除s2個(gè)TH'T4)HD1.2mHB3mHF1.1m

HHBHDHF(n2s)HT'TT

1.231.1(2022)0.4520.7D

30D

D

H厚度取6mmDg450內(nèi)徑DibDis0.2

四個(gè)排氣管：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混合液體平均密度： i

GF

29.310443.142

P1093-6dFuF

43.140.0742

1.796m/

1.04L44L43.141

3-6dw

uw

3.1402192

0.638