推薦-苯乙烯裝置精餾工段的工藝設(shè)計(jì)

書:3：3330/年55%()苯Wt%0.150.4298.111.310.01()Wt%0.2599.60.15:→＋氫氣-CH2-

CH3

-CH=CH2 H+2+

117.8KJ/mol烷-C2H5

+C2H4 105KJ/mol2-C2:

2H5+H

CH3+

CH -54.5KJ/mol_4_:2.6:1一次氣1:0.38二次氣1:1.48三次氣7.說明:為了簡(jiǎn)化計(jì)算,假設(shè)混合中二不參加化學(xué)反應(yīng),并且無結(jié)焦,過程的物系按理想397.4%.粗95.39%.三設(shè)計(jì)要求:編制設(shè)計(jì)說明書(1)(2).設(shè)備的物衡算(3).設(shè)備的熱量衡算塔的工藝計(jì)算及主體設(shè)備計(jì)算(6).五時(shí)間20XX4錄5一.物料衡算 11乙苯蒸發(fā)器物料衡算 11乙苯過熱器物料衡算 11反應(yīng)器物料衡算 11循環(huán)水冷卻器物料衡算 12油水分離器物料衡算 13粗苯乙烯塔物料衡算 14精苯乙烯塔物料衡算 15循環(huán)乙苯塔物料衡算 15苯,甲苯塔分離塔物料衡算 16二.熱量衡算 17脫氫反應(yīng)器的熱量衡17乙苯過熱器的熱量衡算及選型 19廢熱鍋爐的熱量衡算及選型 21乙苯蒸發(fā)器的熱量衡算及選型 22水冷卻器的熱量衡算及選型 25冷凝器的熱量衡算及選型 26粗笨乙烯塔熱量衡算及選型 28循環(huán)乙苯塔熱量衡算及選型 30精苯乙烯塔熱量衡算及選型 32三.粗苯乙烯塔的設(shè)計(jì)計(jì)算 33塔的工藝計(jì)算部分 34塔的設(shè)備計(jì)算部分 37四 51前 言苯乙烯英文名稱：StyreneMonomer，分子式CH8 8

，是苯環(huán)側(cè)鏈上帶有雙鍵的一種芳烴，它是不飽和芳烴中十分普通但有十分重要的一員。被廣泛地用作生產(chǎn)塑料和合成橡膠的原料，在國民經(jīng)濟(jì)中占有舉足輕重的地位。苯乙烯的化學(xué)結(jié)構(gòu)式如下：或者HH2 HH2或者苯乙烯又名乙烯基苯，系無色至黃色的油狀液體。具有高折射性和特殊芳香氣味。沸點(diǎn)為 5℃，凝固點(diǎn) －4℃，難溶于水，能溶于甲醇、乙酸及乙醚等溶劑。在高溫下容易裂解和燃燒，生成苯、甲苯、甲烷、乙烷、碳、一氧化碳、二氧化碳和氫氣等。苯乙烯蒸氣與空氣能成合，為 0。它具有乙烯基烯烴的性，性能，如氧化、原、化等，能與化氫生成。苯乙烯于空氣中，易被氧化成、。苯乙烯易生成苯乙烯P。易與雙鍵的不飽和化合。苯乙烯用是生產(chǎn)苯乙烯，苯乙烯與二烯、烯，用生產(chǎn) ABS塑料與烯ABS與二烯生工耐水性，又具有的性和成性能。用于高料，，日用品等，二戰(zhàn)期間對(duì)合成橡膠的迫切需要促進(jìn)了苯乙烯生產(chǎn)工藝和方法的不斷改進(jìn)及飛速發(fā)展，戰(zhàn)后塑料工業(yè)和汽車工業(yè)的興起又加速了苯乙烯的生產(chǎn)技術(shù)革新步伐。如今苯乙烯已經(jīng)發(fā)展成石油化工領(lǐng)域的大噸位基本有機(jī)原料，它被用來合成各種合成樹脂，不飽和聚脂樹脂等，廣泛應(yīng)用于汽車制造，家用電器和玩具制造等工業(yè)部門。苯乙烯和丁二烯制成的橡膠大量用于輪胎制造和紡織造紙等，丁苯嵌段其聚物SBS熱塑性彈性體，用于制造鞋等輕工，手工部門。上述這些產(chǎn)品都是與人類日常生活息息相關(guān)的，需要量大的。這是發(fā)展苯乙烯生產(chǎn)的本原上苯乙烯的生產(chǎn)1177萬噸/，的生產(chǎn)有 40噸/。，有要發(fā)展苯乙烯生產(chǎn)工藝及技術(shù)。㈠Th產(chǎn)方法的選擇工業(yè)生產(chǎn)苯乙烯的方法乙苯的方法，了乙苯和烯化產(chǎn)苯乙烯和工藝、乙苯氣相工藝等新的工業(yè)生產(chǎn)路線，同時(shí)積極探索以甲苯和裂解汽油等新的原料路線。迄今工業(yè)上乙苯直接法生產(chǎn)的苯乙烯占總生產(chǎn)的 90％，仍然是生產(chǎn)苯乙烯的主要方法，其次為乙苯和烯的化法和催化法由受平衡限高溫并采水蒸氣使增高，采用方法為放熱反應(yīng)，可不受平衡限制，同時(shí)降低了耗。鑒于方法技術(shù)熟權(quán)衡利弊次設(shè)計(jì)采在負(fù)壓操作條件下乙烯法。㈡工藝流程的確定L-301B-207R-301B-301L-301C2L-301B-301abH-40283℃FRC-404H-403塔頂凝器循環(huán)凝R-401未凝部H-404塔鹽器步凝至R-4011乙塔回部打F401成T-403三廢理學(xué)污理學(xué)污粗塔真空系統(tǒng)凝系統(tǒng)利閃方式回收芳芳含2100PPM下理學(xué)污排放掉。尾理尾主要含氮環(huán)縮機(jī)直接并網(wǎng)電應(yīng)用應(yīng)用。11㈢主要操作條件確定及產(chǎn)品的技術(shù)規(guī)格乙苯脫氫需控制的主要操作參數(shù)及溫度壓力蒸氣量和原料的烴空速。溫度溫度高雖有利脫氫和加快速度600—630℃。操作壓力受到熱力學(xué)素影響低操作壓力和減少系統(tǒng)壓力對(duì)有利最好減壓操作但減壓操作對(duì)設(shè)備要求設(shè)備費(fèi)增故工業(yè)均在略常壓操作為了盡可采用低壓操作系統(tǒng)壓力盡可小。水蒸氣和烴用量比低了烴分壓改善平積炭發(fā)水煤氣達(dá)到清了CAT提了熱量但用量對(duì)面有利但氣HO(g)/烴=2.62影響小轉(zhuǎn)率但表面量小力受到但轉(zhuǎn)率小轉(zhuǎn)量增故慮。四）工藝流程圖下圖所示烯離與精制下圖所示一.物料衡算乙苯蒸發(fā)器物料衡算F=(3×107／330×24)×(106／104)／0.92／0.9／0.55=8477.652kg/h=79.978kmol/h鑒于原料中含二乙苯很少,所以能夠忽略水蒸氣S=F×0.38=3221.5078kg/h=178.973kmol/h1原料一次配氣原料一次配氣出料組成Kmol/hXKmol/hXKmol/hXi i i苯01630.0021000.1630.006甲苯0.3870.0048000.3870.0015乙苯78.4660.97970078.4660.3029苯乙烯1.0680.0133001.0680.0041二乙苯0.006微量000.006微量水蒸汽00178.9731178.9730.6908合計(jì)80.091.0000178.9731259.0631.0000乙苯過熱器物料衡算因?yàn)槲锪线M(jìn)入過熱器沒有變化,因此表同上反應(yīng)器物料衡算主反應(yīng)：乙苯→苯乙烯＋氫氣生成苯乙烯量：78.466×55%×92%=39.704kmol/h副反應(yīng)：乙苯→苯＋乙烯78.466×55%×4.5%=1.942kmol/h→甲＋甲烷甲烷，甲及消耗氫氣水蒸氣配入二次配入水蒸氣S=8477.652×1.48/18=697.051kmol/h2三次配入水蒸氣S=8477.652×0.74/18=348.526kmol/h3二次配氣進(jìn)料二次配氣進(jìn)料三次配氣出料組成XKmol/h iKmol/hXXKmol/hiXiKmol/hi苯 000.1630.0002 002.1050.0016甲000.3870.0004 001.8980.00140078.4660.0821 0035.310.0262001.0680.0011 0040.7720.0303二000.006微量000.006微量水 697.0511876.0240.9162 348.52611224.550.9085氫氣 0000 0039.7040.0294甲烷 0000 001.5110.00110000 001.9420.0014合計(jì) 1956.1141.0000 348.52611347.7981.0000苯 2.1050.0016002.1050.0016甲苯 1.8980.0014001.8980.0015乙苯 35.310.02620035.310.0271苯乙烯 40.7220.03030040.7220.0312二乙苯 0.006微量000.006微量水1224.550.9085001224.550.9386氫氣 39.7040.029439.7040.920000甲烷 1.5110.00111.5110.035000乙烯 1.9420.00141.9420.045000合計(jì) 13747.7981.000043.1571.00001304.5911.0000不凝氣凝氣Kmol/h不凝氣凝氣Kmol/hXKmol/hXKmol/hXi i i乙苯損失3% 苯乙烯損失3% (假設(shè)爐油中不再含)污水爐油污水爐油Kmol/hXKmol/hXKmol/hX1224.550.93861224.550.998100iii苯2.1050.0016002.1050.0271甲苯1.8980.0015001.8980.0244乙苯35.310.02711.05930.000934.25070.4405苯乙烯40.7220.03121.22170.001039.50030.5080二乙苯0.006微量000.006微量1304.5911.00001226.8311.00001304.5911.00001226.8311.000077.761.0000,,.,,TBC99.934.250×99.9%=34.2164kmol/h底34.250×0.1%=0.0343kmol/h重95.39底39.500×95.39%=37.6793kmol/h39.500×4.61%=1.821kmol/h釜成釜成Kmol/hXKmol/hXKmol/hX77.761.000040.04041.000037.71961.0000iii2.1050.0271 2.1050.052600甲苯1.8980.0244 1.8980.04740034.25070.4405 34.21640.85450.03430.000939.50030.5080 1.8210.045537.67930.9989二0.006微量 000.0060.0002精乙烯塔物料衡算97.4%底37.6793×2.6%=0.9797kmol/h重二二100%也即二全在底沒有二進(jìn)料釜進(jìn)料釜成Kmol/hXKmol/hXKmol/hXi i i0.03430.00090.03430.00090037.67930.998936.69960.99910.97970.9939二0.0060.0002000.0060.0061合計(jì)37.71961.000036.73391.00000.98571.0000乙苯塔物料衡算%8×8×4×4×Kmol/hXKmol/hXKmol/hXi i i2.1050.05262.1050.5406001.8980.04741.72740.44360.17060.004734.21640.85450.06160.015834.15480.94491.8210.0455001.8210.050440.04041.00003.8941.000036.14641.0000,分離物料衡算95.43%5×5×重95.21%4×4×Kmol/hXKmol/hXKmol/hXi i i苯2.1050.54062.00880.96050.09620.05341.72740.44360.08270.03951.64470.91250.06160.0158000.06160.03413.8941.00002.09151.00001.80251.0000二.熱量衡算℃狀態(tài)氣態(tài)各組分熱量公式Cp=a+bT+c2+d3 ca／mo℃脫氫反應(yīng)器的熱量衡算H1,500H2,770℃,進(jìn)入脫反映器的630H3770℃，H4H4580℃。H+H +H=H +Q1 2 3 4 V定性=(630+580)/2=605℃）H1H20）三H30）H4）25H298A=117.8KJ/molH298B=105KJ/molH298C=54.5KJ/mol分 a92%4.5%4.5%bcd6.4832.215E-3-3.298E-61.826E-94.5981.245E-2-2.860E-6-2.703E-90.9093.740E-2-1.994E-54.192E-9苯 -8.1011.133E-1-7.206E-51.703E-8苯 -5.8171.224E-1-6.605E-51.173E-8苯 -10.2941.689E-1-1.149E-43.107E-8烯 -6.7471.471E-1-9.609E-52.373E-8水 7.7014.595E-42.521E-6-0.859E-9苯 -8.9372.071E-1-1.328E-43.370E-8Cp8787.12215.88521.21247.35358.67270.45464.394H898A=H298A+(Cp-Cp)584.1-]92n=4.7106

KJ/hH898A=H298B+(Cp-Cp)584.10-]4.5n=0.19106

KJ/hH898A=H298C+(Cp-Cp)584.1-]3.5n=-0.093106

KJ/hQ =H +H +H =4.78+0.195-0.093×106/4.×103=1.1×103Kcal/hV A B CH=∑FiCpi△t說明：以下各表計(jì)算中HKcal/）配料氣H配料氣H組成1H2H3H4H3.97×1065.34×1062.67×1062.01×104tCp0-500CpiFiCp0-770CpiFiCp0-770CpiFiCp0-580CpiFi氫氣7.067507.277107.277107.1058282.1366甲烷14.6832017.6272017.6272015.621223.6063乙烯19.8401022.9814022.9814020.904540.5965苯44.28807.218951.0045051.0045046.682198.2658甲苯54.749021.187969.3037069.3037057.811222.3729乙苯65.96655176.127476.1282076.1282069.45985450.1699苯乙烯60.505364.619769.0725069.0725063.54142590.7112水9.16581640.43079.94826934.40289.94823467.20649.394111503.545二乙苯87.36510.5242100.8390100.839092.00870.5221根據(jù)脫氫反映器的熱量平衡關(guān)系式HH +HH Q t=596℃1 2 3 4 V校核:(t計(jì)-t設(shè))/t設(shè)×100%=(596—580)/580×100%=2.76%因?yàn)?.76%＜10%，假設(shè)與實(shí)際誤差在允許范圍內(nèi)，所以假設(shè)正確。乙苯過熱器的熱量衡算及選型(1).熱量衡算進(jìn)口原料氣為H,t =150℃ 出口配料氣為H,t =500℃1 1 3 3H ,t =596℃ 出H ,設(shè)t=45℃2 2 4 4氣H1H1(150℃)H4設(shè)450℃H2(596℃)H3(500℃)氣配料配料H組成1出配料H3H2出H4H648290.4752800975.258955059.54914349.6175tCp0-150CpiFiCp0-500CpiFiCp0-596CpiFiCp0-450CpiFi氫6.968207.067207.0129278.44026.9841272.2967甲烷 014.6832012.138018.337511.153716.8532乙烯 019.8404016.543132.127614.875928.8889苯 23.31833.800933.880665.522536.268873.081631.767866.8712甲苯 11.328941.809616.180344.722284.882739.387474.7573乙苯 2815.179651.05694006.230754.46981923.328648.00421695.0283苯乙烯 36.105947.297550.513750.33562052.28344.58561817.8441二乙苯 0.290867.87260.407292.29280.553864.03050.3842水 8.13151455.22958.51021523.0968.625410562.2338.469810371.693H+H =H+H1 2 3 4→t=474℃tt)/t×100%=(474—450)/450×100%=5.33%5.33%＜10%，假與實(shí)際誤差在允許范圍內(nèi)，所以假正確(2).換熱器的選型Q=KA△tmQ=H-H =2800975.25-648290.475=2152684.775kcal/h3 1K=21.24Kcal/m2h℃△tm=(△t1-△t2)/ln△t1/△t2=187.44℃→A=Q/K△tm=540.71m2查化工工藝手冊(cè)選型：應(yīng)采用三個(gè) G800IV—6—200型換熱器串聯(lián)及選型熱量衡算進(jìn)口接觸氣H1

4H1

t0℃2水164℃(l)→164℃(g)接觸接觸氣水（）164℃水（）164℃接觸氣HHH12H6878618.6542792084.568Cp0-474CpiFiCp0-210CpiFi6.9971277.81296.9472275.83169.845014.87589.566114.454429.814912.367124.016969.882225.156152.953677.786531.452459.69671767.653938.51821360.07761892.995736.15451474.09130.399751.84440.31118.477110380.632868.194210034.2076Am =H-H1 2

=6878618.654-2792084.568=4086534.086kcal/hm2h℃(-n/7℃Km2G800IV—6—200串聯(lián)乙苯蒸發(fā)器的熱量衡算及選型(1).乙苯（G）150℃接觸氣0164℃原料乙苯0L）接觸氣1376rl℃0l℃06l℃0)6)6)0H H H1 2 3H1

H 2

Hit340

H it4H5×601H =78.466×8518=668373.388kcal/h2H5×663H 8×304原料吸H(L)

H =H(1

+H +H -H2 3

=997421.1622kcal/h137℃HHH12H2790706.54812946.6183tCp0-210CpiFiCp0-137CpiFi6.9477275.85156.9253274.96219.566814.45549.075713.713424.017511.498122.329353.362022.779847.951559.692928.662454.40121360.077635.09291239.13031474.083133.11421350.13320.311147.48870.28498.188510027.22778.12039943.7134H=H-H3 1

H=H3 (L)9℃ 97×與實(shí)際誤差在允許范圍內(nèi)，所以假(2).換選型Am =H-H 1 2m2h℃ t(-tn/t7℃m 1 2 1 2→Ktm2m查化工工藝手冊(cè)選型G800IV—6—200冷卻器的熱量衡算及選型接觸氣139接觸氣139℃設(shè)52℃32℃

（設(shè)108℃）XS' XSH418103.975水冷卻器的H418103.975組成Cp139-108CpiFi氫氣6.9566276.2049甲烷9.815514.8312乙烯12.864624.9831苯26.555455.8991甲苯33.061962.7515乙苯40.54791431.7464苯乙烯37.95091547.3341二乙苯54.40110.3264水8.226110073.1483換器的選型Q=KA△tm Q=418103.975kcal/h K=90.54Kcal/m2h℃△t(△-△tn△/△t8℃m 1 2 1 2A=Q/Ktm=56.75m2G600I1060冷凝器的熱量衡算及選型接觸接觸氣108℃XS'52℃XS32℃冷40℃P =A-B/(T+C) PP av i avii 總P=P =1.4kgf/c2 =1029.34mmHg P=ii 總ABCPavPi13.6333164.903.194.95×10530.2626甲烷15.2243897.84-7.162.17×1051.1323乙烯15.53681347.01-18.155.8×1041.4823苯15.90082788.51-52.36183.111.647甲苯16.01373096.52-53.6758.751.4514乙苯16.01953279.47-59.9521.3226.9687苯乙烯16.01933328.57-63.7214.3931.189二乙苯16.11403657.22-71.182.690.0046水18.30363816.44-46.1354.76935.1554PP i av,PP ,,i av,PP ,i av,PP ,i avQA(g)10℃→ A(g)10℃↓Q ↑Q → Q=Q+Q +Q1 A(g)Tb → A(l)Tb

1 2 3Q2QQ1=3747.5842Q2=735358.862Q3=452358.0342器熱量衡算（含量較少,計(jì)算QQ1=3747.5842Q2=735358.862Q3=452358.0342組成 沸點(diǎn)Cp108-TbCpiFi△tQvFiQvCpTb-40CpiFi△t6.930818712.2739.1496940.103111.66101539.905080.1524.62611443.6866735315478.06534.022875.225831.9785-159.3249793915068.22241.5835574.045240.4213-40229.218596303524.7649.96169680.5338.4807-58198.798954364624.7946.72200032.19水 100.058.186779698.93729.9436663.0271.00974196.036Q=Q+Q +Q=1191464.48Kcal/h1 2 3換熱器選型Q=KAt Q=1191464.48Kcal/h K=264Kcal/m2h℃mt=(-t)/ln/t=24.667℃m 1 2 1 2A=Q/Ktm=182.962m2G800VI—10—200換熱器乙烯塔熱量衡算及選型(1).塔頂冷凝器R=6.7 F=(R+1)FiXS'40℃XS合計(jì)H1=381533.9712合計(jì)H1=381533.9712H2=15040.2043組成Hv56.3FiHvCp56.3-48CpiFi苯7649.2916101.755533.60587.04724甲苯8650.8816419.370239.78626.6703乙苯9671.09330909.883946.3813171.7401苯乙烯9941.2218102.961643.32654.7515H=H+H =396574.1755Kcal/h1 2Q=KAtm K=115Kcal/m2h℃t=(-t)/ln/t=16.129℃m 1 2 1 2A=Q/Kt=213.8056m2mG800—16—225換熱器(2).塔底再沸器H=∑(＋1)DHvXwi （二乙苯忽略不計(jì)）106106℃水（）132.8℃水（）132.8℃106℃塔底再沸器熱量衡算表組成乙苯苯乙烯∑(R＋1)DHvXwiHv1069024.89354(R＋1)DHvXwi2139.9576131017.7069H=133154.665At m2h℃mt(-tn/t8℃m 1 2 1 2Ktm2mG400IV—25—10換熱器乙苯塔熱量衡算及選型109.6℃109.6℃XS'40℃XS塔頂冷凝器熱量衡算表組成苯甲苯乙苯∑(R＋1)FHvHv6935.887949.648937.68FiHv14600.027413732.2081550.5611△H1=508337.221Cp109.6-10136.89243.96451.42∑(R＋1)CpiFi△tCpiFi77.657775.94343.1675△H2=23728.4953△H=△H1+△H2=532065.7155Kcal/h設(shè)備Q=KA△t K=396Kcal/m2h℃m△t(△-△tn△/△t5℃m 1 2 1 2→A=Q/K△t=19.49m2mG400IV—25—20換熱器147℃）157.9℃）157.9℃147℃RH78775.3R1054.24498612.332814174.740723841.3136At m2h℃mt(-tn/t9℃m 1 2 1 2Ktm2m3—5—4乙烯塔熱量衡算及選型頂冷凝器R=0.5XS'40℃XS32℃(RHv64.99580.799848.11FiHv328.6211361421.6978H1=542625.4784Cp64.9-5046.92844.762RtCpiFi1.60961642.7475H2=1644.3571At m2hH=H+H m 1 2t(-tn/t5℃m 1 2 1 2Ktm2m0—6—02).底再沸器85℃）132.8℃）132.8℃85℃Hv859737R532746.3102At m2h℃mt(-tn/t8℃m 1 2 1 2Ktm2m0—6—5三.粗笨乙烯塔的設(shè)計(jì)計(jì)算粗笨5,1080.℃50mmHg,230mmHg140mmHg,,,ρ=PM/RTM組分=104.456σρ(g/cm3)ρ(kg/m3)粘度Lv苯21.270.81500.49520.3080甲苯21.090.81000.58410.3110乙苯22.920.81360.67300.3540苯乙烯24.820.85560.66030.3860值22.93130.8210.66290.365塔的操作及根據(jù)氣液相泡點(diǎn)方程 ∑y=∑kx=1i ii露點(diǎn)方程 ∑x=∑y/k=1i i i(1).操作的確定根據(jù)回流缸內(nèi)物料,塔頂物料冷卻冷凝為液相,則回流時(shí)回流缸內(nèi)為塔頂物料的泡點(diǎn),用泡點(diǎn)方程∑y=∑kx=1本設(shè)計(jì)中取參考現(xiàn)場(chǎng)情況的i ii50mmHg0.006666mpa,回歸符合(2).塔頂即定的操作塔頂露點(diǎn)方程∑x=∑y/k=156i i i(3).塔釜,,ykx=1,105,i ii.(4).,,8,.Rminα

/(α-θ)=1－q

=α

/(α-θ)-1iFi i

min

iDi i因?yàn)閝=1 所以αx/(α-θ)=0iFi iρ(mmHg)α(以乙苯組分x％ vi i αF α-θFi 83料為準(zhǔn)) ii i苯2.705836.6045.8670.15875.012甲苯2.44325.8662.2850.05581.43乙苯44.05142.59310.44050.145苯乙烯50.8104.6190.7340.3729-0.121設(shè)=0.855(θ值輕重關(guān)鍵組分相對(duì)揮發(fā)之間）θ值應(yīng)使αx/(α-θ)=0組分苯組分苯甲苯乙苯苯乙烯X％Di5.264.7485.454.55αxiDi0.16260.00540.85450.0635α-θi5.0121.430.145-0.121R =αx/α-θ)-1=4.4043min iDi i1.6.7/R2.0

minN +1=l(x/x)(x/x)/lg(αα)1/2min l hD h lw D w在塔頂溫度為50℃，P=50mmHg條件下，P =47.332mmHg P =33.143mmHg α=1.428r乙苯 r苯乙烯 D在塔釜溫度為105℃，P=230mmHg條件下，P =306.035mmHg P =231.525mmHg α=1.322r乙苯

r苯乙烯 wα=(αα)1/2=1.374D w塔頂 X=0.0455 X=0.8545h l塔釜 X=0.0009 X=0.9991l h→N=31.3 (因?yàn)椴捎脽岷缥俜衅?minN定(R－R)/(R＋1)=(6.7－4.4043)/(6.7＋1)=0.2981min查吉利蘭圖得 (N－N )/(R＋2)=0.85minR=1.5N=51.21

min

=6.6065全塔平均效率及實(shí)際塔NpE=N/Nt p

E=0.49(αμ)-0.245t cp Lα=1.377cpx％μx苯Fi2.705Li0.319Li Fi0.00862.440.3210.007844.050.3650.160850.80.4000.2032E=0.49(α)-0.245=0.5744t cp LN =N/E=89.1538=90p t確定加料板的位置n＋m=Npn/m=［(W/D)(x

/x)(x

/x)2］0.25Fh Fl Wl DhW=37.7196Kmol/h xFh

=0.50798 xWl

=0.00091D=34.2164Kmol/h x=0.4405

=0.04548Fl Dh于是：n/m=0.4936 n+m=90解之：m=60.2571=61塊 n=90-61=29塊故：進(jìn)料板位置應(yīng)取在從塔底往上數(shù)61塊，從塔頂向下數(shù)29塊之間。精餾段(1).操作氣速F -4.51=0.00848(d+1.27)(h+27.9)

=V ρh,w o l

h,w

vd=10mm,板間距HT=450mm,假設(shè)液層高度h=40mmo lF -4.51=0.00848(10+1.27)(40+27.9)=10.9992h,wV =14.1622m/sh,w1.331.51.752.0Vhh,wh1.331.51.752.0V19.11921.243324.783928.3244A=Q/V3600h v hQ=(R+1)D=48229.23/h=13.3973/sv vQ=RD=33.123/h=0.00923/sVV×3600h68828.4 76475.88 89222.04 101967.84A(m)h0.70070.63060.54060.4730排列方式為正三角形排列如果和距定后，則開率φht/d=2.5～3t=25mmoh on=Q/（π/4）d2Vv o hAh on=Q/（π/4）d2Vv o hA=A/φp h hA 4.8291p4.34603.72573.2598n 8926.32578033.70576886.01966025.2793。TAHT/Q=16.0973d lT=AHT/Q=26.5158sd lTA徑p面積m2m2W/DA/Ad tA m2WdmLmL/DDm）ddAtm2WmWd4.8422003.7257 3.7488 12.06.80.3291 0.264 1.43 0.65 0.06 0.075

U=Q/A=0.058m/s 0.03-012d l dT=AHT/Q=16.0973sd l(1).P P=51(V/C)2(/)d d h o v Lδ=2.0mm 查表并校正后得C=0.788o所以 P=36.9489mm柱d層高h(yuǎn) h=2.84E(Q/L)2/3ow ow l查圖6—6E=1.04 所以h=23.9987mm層高

owh=h+hl l w owh=17mm則 h=17+23.9987=40.9987mmw l檢驗(yàn)誤差 為h-40絕對(duì)值小1m所以假設(shè)符合lheh=40.9987mm h=0.0385ml ePtPP+h=36.9489+38.5=75.4489mmt d e

h

/-1f f l2A=0.65822,A=/4D2=4.842,A-2A=4.18182d t t dV=Q/4.1818=3.1993m/sn vV1/=2.4848 67=0.5715n vh=286.7042mm h+10HT )f fh h=1.165×10-5(Q/LS)2c c l取S=0.037m h=2.0815mmc面梯△平均流寬b=D+L/2=1.8m 弓形寬W=0.4md內(nèi)外堰距離Z=1.7m 相流量Q=17.39m3/sl相黏μ=0.0365厘泊 h=286.7042f相密=821kg/3L=［215(25×b+1000h)2×μQ×Z］(100×b×h)3ρf l f L=3.514×10-7mm面HdH=P+2h+h+=120.3795mmd t c l因?yàn)镠1/2HT d(1).h=2.84E(Q/L)2/3=6ow lL=Q/LL=2.8953m2/slh=2.84E(Q/L)2/3=40ow lL=Q/L=49.83822/slF -4.51=0.00848(d+1.27)(h+27.9)h,w o lh=20+2.84E(L2/; F=V1/;VA=VAlV1/=FA

h,w

h,w

kt hhk v h,wh tLV1/2LV1/2LV1/2LV1/2LV1/210k v1.356830k v1.535250k v1.649970k v1.747290k v1.7537201.4227401.5877601.6782801.78961001.7968H=P+2h+hd t c la.h=h+h=20+2.84E(L)2/3E=1l w owb.P=P+h P=51(V/C)2(/)=0.0752V2t d e d h o v L hc.h=1.165×10-5(Q/LS)2 S=0.035m h=0.0095L2c l cd.H=1/2H=225mmd T導(dǎo)出：225=0.0752V2+h+h+0.019L2h e lLhLh(m)h(mm)VVV1/2lehkk v100.0328635.3745.00735.83594.9836200.0507338.2141.03655.23544.5425300.0455342.3739.32714.86763.8793400.0532744.6935.55364.25323.5325500.0583445.5330.73253.71433.2142600.0637247.2124.30113.22742.1916700.0682548.0913.82692.10541.9936800.0723149.32900.0757150.531000.0816651.22e=0.0057V/(H-h)3.2 V=Q/(A-A)a T f a v t dH=0.45m,h=0.018m,=22.9313,h=2.5hT w f le=0.1kg/kg0.1=0.0057/22.931V/(0.45-2.5h3.2a fV=8.830.45-8.832.(0.02+0.002842/)aLVV=0.947VV1/210a2.4537k a2.2765k v1.9636302.13552.30571.6525501.95561.88421.5166701.87311.73651.4011Q=(R+1)D/ρ=48229.2m3/h=13.397m3/sv vQ=RD/ρ=33.12m3/h=0.0092m3/sl LV=Q/3600A=2.768k v tVρ1/2=2.1498 L=Q/L=18.9986v l適宜區(qū)分析將上述液體負(fù)荷下限,液體負(fù)荷上限,漏液,液泛,霧沫夾帶繪成精餾段負(fù)荷性能圖中所圍面積即為適宜區(qū),由霧沫夾帶相交為氣液負(fù)荷上限V

ρ1/2=2.058,L=16.5,由漏液交為氣液負(fù)荷下限V

ρ1/2k v k v=0.97,L=7.82.058/0.972.1217,由上限下限比16.5/7.8=2.115423氣相為設(shè)計(jì)負(fù)荷的情況.即塔板可以在減半量情況下正常又可在裝置需超負(fù)荷運(yùn)轉(zhuǎn)情況下留有適當(dāng)潛力.由圖中可以看出液相負(fù)荷上限在降液管右側(cè),表明沒達(dá)到上限時(shí)即發(fā)生現(xiàn)象,故降液管超負(fù)荷在液泛右側(cè),霧沫夾帶較低于液泛時(shí)霧沫夾帶.提餾段塔板的設(shè)計(jì)(1).氣速F -4.51=0.00848(d+1.27)(h+27.9)h,wF =V

o lρ1/2h,w h,w v孔徑d=10mmHT=450mmh=42mmo lF -4.51=0.00848(6.7+1.27)(36+27.9)=1.8081h,wV =13.9154h,w1.331.51.752.0Vhh,wh1.331.51.752.0V18.507520.873124.352027.8308A=Q/V3600h v hQ=(R+1)D=48229.23/h=13.3973/sv vQ=RD=37.563/h=0.01043/sVV×3600h6662774631.687667.2100190.88A(m)h0.72390.64620.55140.4814排列方式為正三角形排列如果和距定后，則開率φht/d=2.5～3t=25mmo開φ=0.9069（d/t）2=0.1451h on=Q/（π/4）d2V A=A/φApAp4.9994.45353.79153.3177n63681.5287 56477.707 48299.3631 42263.6943。TAHT/Q=14.1989sd lT=AHT/Q=23.3888sd lTA徑p面積m2m2W/DA/Ad tA m2WdmLmL/DDm）ddAtm2WmWdm4.8422003.7915 3.7488 12.06.80.3291 0.264 1.43 0.65 0.06 0.075

U=Q/A=40.708m/sd l dT=AHT/Q=14.1989sd l(1).P P=51(V/C)2(/)d d h o v Lδ=2.0mm 查表得C=0.788o所以 P=35.6724mm柱d層高h(yuǎn) h=2.84E(Q/L)2/3ow ow l查圖6—6E=1.045所以h=26.0982mm層高

owh=h+hl l w owh=16mm h=16+26.0982=42.0982mmw l檢驗(yàn)誤差 為h-42絕對(duì)值小1m假符合lhe

h=42.0982mm h=0.0356ml e(5).P P=P+h=71.2724mmt

t h=h

e/-1f f l2A=0.65822,A=/4D2=4.842,A-2A=4.18182d t t dV=Q/2.8134=3.2036m/sn vV1/=2.4881 67=0.5735n vh=286.382 h +100HTf fh h=1.165×10-5(Q/LS)2c c l取S=0.045m h=2.1827mmc面梯△平均流寬b=D+L/2=1.8m弓形寬W=0.264md內(nèi)外堰距離Z=1.672