經(jīng)典word整理文檔，僅參考，雙擊此處可刪除頁眉頁腳。本資料屬于網(wǎng)絡(luò)整理，如有侵權(quán)，請聯(lián)系刪除，謝謝！操作條件溫度/℃管程流體物性（137.8℃）殼程凝液物性（151.7℃）bμ=0.0085/mPa·sbb=1.6748kJ/(kg·K)表面張力蒸汽壓曲線斜率b(p)=2.159×10K·m/kg-32s再沸器的設(shè)計一、設(shè)計條件0.5Mpa）的飽和水蒸汽作為熱源。設(shè)計條件如下：（1管程壓力以塔底壓力計算：P105.30.70.12w（2）將釜液視為純氯苯，在釜底壓力下，其沸點：C根據(jù)安托因公式：logpABt查資料得：9.25225.69C=1516.04則有：)6tbt=137.8℃b（3）再沸器的蒸發(fā)量由于該塔滿足恒摩爾流假設(shè)，則再沸器的蒸發(fā)量：D282.42112.6110864.61/hb1（4）氯苯的汽化潛熱35.310KJ/Kmol（即為313.5KJ/kg）.純組分常壓沸點下的汽化潛熱為的汽化潛熱與溫度的關(guān)系可用下式表示：rtt0.38t(c=359.2℃)20.38tct2rc11其中tt137.8℃,t℃,r,則：2b11359.2137.80.38r313.50.38359.2131.82二、工藝結(jié)構(gòu)尺寸的估算（1QQDr10864.61310.3/9.3647W5bb、計算傳熱溫差△tmt=T-t=151.7-137.8=13.9℃△mb(3)、假定傳熱系數(shù)K依據(jù)殼程及管程中介質(zhì)的種類，按豎直管式查表，從中選取K=800W/（m.k）2(4)、計算傳熱面積pQ9.364710513.9A=m2Kp（Φ25mm×2mm,=4000mm,按正三角形排列，L則傳熱管的根數(shù)為AN8dL3.140.0254To（2按3.4.3.2N3a(a1268T解得a9(另外一負值舍去)則b2a1。于是：Dt(bd3648o取進口管直徑，出口管直徑D250D600io三、傳熱系數(shù)校核1.顯熱段傳熱系數(shù)KL①假設(shè)傳熱管出口氣化率為,釜液蒸發(fā)量為D,則循環(huán)量xebW為tDW30(/s)bxte②顯然段傳熱管內(nèi)傳熱膜系數(shù)則傳熱管內(nèi)釜液的質(zhì)量流率G為設(shè)傳熱管內(nèi)流通截面積為,SIS4)diN0.7850.0210.928m222iTWG/(ms)2tSI0.021325.05R0.223ebC0.2233Prbb顯熱段傳熱管內(nèi)傳熱膜系數(shù)為ibd0.023740.75RP0.80.42ieri③殼程冷凝傳熱膜系數(shù)o2g31.87(1/3c.5R1/32co2eoc3④污垢熱阻沸騰側(cè)：冷凝側(cè)：RmR1.72m5252iO管壁：R4.29910mK/W62w⑤顯熱段的傳熱系數(shù)1RdKdRd1LR0i0wd0dd0iiimo1W/(mK4.2994.2291561.72511369.722.蒸發(fā)段傳熱系數(shù)E(1)管內(nèi)沸騰-對流傳熱膜系數(shù)①泡核沸騰的平均修正系數(shù)avvbaaaE2G3600G325.051.1762h977.5()()()(0.5)0.1V0.5b0.1bvx0.13()0.9()0.911x10.13當時xx0.10Xex0.021tt查圖得a=0。Ex()0.9()0.911x1當時x0.4x0.04Xex0.0084tt查圖得a=0.43。＇4aa'00.43a0.215E22②泡核沸騰傳熱膜系數(shù)bbd0.1040.0210.225()（0.69()0.31i0.2253.543Pr0.690.330.69ibbibbV9.3650.0215（（）0.69310.30.223-3977.53.9551.20.0215—）（）163W/(m0.310.3321.9610-2③質(zhì)量分數(shù)0.4x處的對流傳熱膜系數(shù)etp13.5()3.50.652.820.50.5Xtt0.1040.021Rx)P0.0232.8210.04）3.5430.80.40.80.4btpderi2023.3W/(m2④管內(nèi)沸騰對流傳熱膜系數(shù)v0.2312023.32058.4W/(mab2vbtp（2）蒸發(fā)段傳熱系數(shù)KE3.顯熱段和蒸發(fā)段長度LL顯熱段長度和傳熱管總長之比為BCLBCL(tp)2.1591030.4398stdNKt3.140.0211047376.4413.92.159103iTLWmpC1674.8977.530pbbtL0.439841.7592(m)L41.75922.2408(m)4.平均傳熱系數(shù)KcKLKL376.441.75922.2408KCD960W/(m2LBCEL4c55.面積裕度核算KKKK比比較和，若高出20%，則說明假定值尚可，K否則要重新假定值。KK20.11%cK四、循環(huán)流量的校核1.循環(huán)推動力pDxxX(1x)0.90.08807(110.033)0.90.6363當3x0.033ettX0.6363(0.6363210.6363R0.279tt(X21XL20.520.5tttt)RRm33.9550.279)977.50.279275.9/tpvLbL當，按上述同樣的方法求得xx時165/m3etp查表并根據(jù)焊接需要選取再沸器上部管板至接管入塔口間的高度l0.9m計算循環(huán)推動力pDpgL(p)l9.812.2408(977.5245.8)0.9Dbtptp2.循環(huán)阻力pfppppppf12345（1）管程進口管阻力p1W0.252G2t0.785D2iDG0.25615.16.99105Riei0.22103b0.012270.7543R0.01680.38eii6(0.250.0254)2Lii0.3426(D0.1914)0.3426(0.250.1914)iLGi2ipD21ib(2)加速損失p2x)x22M()16.85ebe1RRLvLGWdN325.05kg/(m224tiTPGM/187.539.14/977.5740Pa222b(3)傳熱管顯熱段阻力損失p3按直管阻力損失計算0.012270.7543R0.012270.7543/0.02710.380.38eG2LBCd122PaP23ib(4)傳熱管蒸發(fā)段阻力損失p4求得阻力損失。①氣相流動阻力損失取該段內(nèi)的平均氣化率pv42，則氣相質(zhì)量流速為xx0.067Gv3eG0.067325.05kg/(m2VdGi氣相流動的:ReVVRV0.75430.012270.0243R0.38VV7LG2V153PaVPd2V4iV②液相流動損失pL4GGG303.38kg/(m2LVdG0.021303.38ReLiL0.2210-3b0.75430.012270.0275R0.38LeLLG2PLd2L4Lib③兩相壓降p4p(pp)2333Pa144144V4L4（5）管程出口阻力p5①氣相流動阻力損失p出口管中氣相質(zhì)量流率為：v5GxG0.1021.67kg/(m20.7850.62Ve出口管中氣相流動的為：RDGo0.621.67ReVV1.5260.0085103VVR0.38(/0.0254)2(0.6/0.0254)2lm0.3426(/0.1914)0.3426(0.6/0.1914)l'G2VVPD2V5oV②液相流動阻力pL568液相流率為：GGGG31.26209.2kg/(ms)20.7850.62LLV80.6209.2DGo液相c動為：RRL5.750.223b0.75430.012270.02748LR0.38l'G2PLD2L5L