第5組正戊烷冷凝器的設(shè)計(jì)

1、 2009級(jí)化學(xué)工程與工藝專業(yè)化工原理課程設(shè)計(jì)說明書 題 目：2.0×104噸/年正戊烷冷凝器的設(shè)計(jì)姓 名：班級(jí)學(xué)號(hào)：指導(dǎo)老師：同組學(xué)生姓名：完成時(shí)間：2012年5月18日化工原理課程設(shè)計(jì)評(píng)分細(xì)則評(píng)審單元評(píng)審要素評(píng)審內(nèi)涵評(píng)審等級(jí)檢查方法指導(dǎo)老師評(píng)分檢閱老師評(píng)分設(shè)計(jì)說明書35%格式規(guī)范是否符合規(guī)定的格式要求5-44-33-22-1格式標(biāo)準(zhǔn)內(nèi)容完整設(shè)計(jì)任務(wù)書、評(píng)分標(biāo)準(zhǔn)、主要設(shè)備計(jì)算、作圖、后記、參考文獻(xiàn)、小組成員及承擔(dān)任務(wù)10-88-66-44-1設(shè)計(jì)任務(wù)書設(shè)計(jì)方案方案是否合理及是否有創(chuàng)新10-88-66-44-1計(jì)算記錄工藝計(jì)算過 程計(jì)算過程是否正確、完整和規(guī)范10-88-66-44-

2、1計(jì)算記錄設(shè)計(jì)圖紙30%圖面布置 圖紙幅面、比例、標(biāo)題欄、明細(xì)欄是否規(guī)范10-88-66-44-1圖面布置標(biāo)準(zhǔn)標(biāo)注文字、符號(hào)、代號(hào)標(biāo)注是否清晰、正確10-88-66-44-1標(biāo)注標(biāo)準(zhǔn)與設(shè)計(jì)吻合圖紙?jiān)O(shè)備規(guī)格與計(jì)算結(jié)果是否吻合10-88-66-44-1比較圖紙與說明書平時(shí)成績(jī)20%出勤計(jì)算、上機(jī)、手工制圖10-88-66-44-1現(xiàn)場(chǎng)考察衛(wèi)生與紀(jì)律設(shè)計(jì)室是否整潔、衛(wèi)生、文明10-88-66-44-1答辯成績(jī)15%內(nèi)容表述答辯表述是否清楚5-44-33-22-1現(xiàn)場(chǎng)考察內(nèi)容是否全面5-44-33-22-1回答問題回答問題是否正確5-44-33-22-1總 分綜合成績(jī) 成績(jī)等級(jí) 指導(dǎo)老師 評(píng)閱老師 （

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39、;··················13一、設(shè)計(jì)任務(wù)書1.設(shè)計(jì)題目：正戊烷冷凝器的設(shè)計(jì)。設(shè)計(jì)課題工程背景：煉油廠精餾塔塔頂冷凝器蒸汽主要是正戊烷，以此為原料設(shè)計(jì)一正戊烷冷凝器。 2.設(shè)計(jì)任務(wù)及操作條件 （1）處理量： 2.0×104噸/年 （2）正戊烷冷凝溫度為51.7，冷凝液于飽和液體下離開冷凝器； （3）冷卻介質(zhì)，地下水，入口溫度：20； （4）允許壓強(qiáng)降：不大于105Pa（5）每年按330天計(jì)，每天

40、24小時(shí)連續(xù)運(yùn)行 （6）設(shè)備型式 立式列管冷凝器 （7）設(shè)計(jì)項(xiàng)目 設(shè)計(jì)方案簡(jiǎn)介：對(duì)確定的工藝流程及換熱器型式進(jìn)行簡(jiǎn)要論述； 換熱器的工藝計(jì)算：確定換熱器的傳熱面積； 選擇合適的立式列管冷凝器并進(jìn)行較核計(jì)算； 繪制換熱器總裝配圖。 3.設(shè)計(jì)說明書的內(nèi)容 （1）課程名稱、首頁、目錄及頁碼； （2）簡(jiǎn)述設(shè)計(jì)內(nèi)容，自己設(shè)計(jì)的特點(diǎn)，引用的標(biāo)準(zhǔn)等； （3）熱量衡算及初步估算換熱面積； （4）冷凝器的選型及流動(dòng)空間的選擇； （5）工藝流程圖； （6）冷凝器的校核計(jì)算； （7）結(jié)構(gòu)及附件設(shè)計(jì)計(jì)算； （8）冷凝器的主要數(shù)據(jù)一覽表； （9）設(shè)計(jì)結(jié)果評(píng)價(jià)； （10）附立式列管冷凝器總裝圖。 4.設(shè)計(jì)圖要求 A2圖紙

41、繪制冷凝器裝配圖一張、兩個(gè)局部放大圖。CAD圖自由選做1-2個(gè)部件。二、主要設(shè)備設(shè)計(jì)計(jì)算和說明1. 確定流體流動(dòng)空間冷水走管程，正戊烷走殼程，有利于正戊烷的散熱和冷凝。2. 計(jì)算流體的定性溫度，確定流體的物理性質(zhì)。正戊烷液體在定性溫度（51.7）下的物性數(shù)據(jù)：=596kg/，。井水的定性溫度：入口溫度=20，出口溫度為23。 井水的定性溫度為 兩流體的溫差，故選固定管式換熱器。 兩流體在定性溫度下的物性數(shù)據(jù)見下表流體溫度/密度/(kg/)黏度比熱容熱導(dǎo)正戊烷51.75960.182.340.13井水21.59980.98384.1820.6013. 計(jì)算熱負(fù)荷 kW4. 計(jì)算有效平均溫度差逆流

42、溫差 5. 選取經(jīng)驗(yàn)傳熱系數(shù)K值 根據(jù)管程走井水，殼程走正戊烷，總傳熱系數(shù)，現(xiàn)暫取K=500。6. 估算換熱面積 7.工藝結(jié)構(gòu)尺寸管徑和管內(nèi)流速管徑為25mm 2.5mm，管內(nèi)流速為ui=1.0m/s。管程數(shù)和傳熱管數(shù)根據(jù)傳熱管內(nèi)徑和流速確定單程傳熱管數(shù)ns=64（根）按單程管計(jì)算所需換熱管的長(zhǎng)度LL= m取傳熱管長(zhǎng)l=2m，則該換熱器的管程數(shù)為 =4/2=2 (管程)傳熱管的總根數(shù)=642=128 （根）殼體內(nèi)徑采用兩管程結(jié)構(gòu)，取管板利用率=0.7，則殼體內(nèi)徑D=1.05t450mm折流板采用弓形折流板，取弓形折流板圓缺高度為殼體內(nèi)徑的25%，則切去的圓缺高度為h=0.25450=112.5

43、，取h=113mm。取折流板間距為B=0.34D=0.34450=153mm。則折流板數(shù)NB=1=112 （塊） 折流板圓缺水平面安裝 拉桿直徑為12mm，殼程入口應(yīng)設(shè)置防沖擋板。 殼程流通截面積和殼程流體流速殼程流通截面積 接管 a 殼程接管 進(jìn)口接管 取接管內(nèi)蒸汽流速為10m/s,則接管內(nèi)徑mm出口接管 取結(jié)管內(nèi)的液體流速為1.5m/s，則接管內(nèi)徑 b 管程水進(jìn)出口接管 取接管內(nèi)水流速為1m/s,則接管內(nèi)徑 d=160mm 8. 初選換熱器規(guī) 立式固定板式換熱器的規(guī)格如下： 公稱直徑D：450mm 管長(zhǎng)L：2.0m 公稱換熱面積A：20 管子直徑：25mm 2.5mm 管程數(shù)： 2 管子排

44、列方式：正三角形 管數(shù)：128換熱器的實(shí)際換熱面積 9. 計(jì)算管程對(duì)流傳熱系數(shù)計(jì)算管程對(duì)流傳熱系數(shù)m3/s計(jì)算殼程對(duì)流傳熱系數(shù) 現(xiàn)假設(shè)管外壁溫=30，則冷凝液膜的平均溫度為，在此溫度下的物性沿用飽和溫度51.7下的數(shù)據(jù)，在層流下：確定污垢熱阻 總傳熱系數(shù) 碳素鋼：=45所選用換熱器的安全系數(shù)為：表明該換熱器的傳熱面積裕度符合要求。核算壁溫與冷凝液流型 核算壁溫時(shí)，一般忽略管壁熱阻，按以下近似計(jì)算公式計(jì)算這與假設(shè)基本一致，可以接受。核算流型，冷凝負(fù)荷10. 計(jì)算壓降 計(jì)算管程壓降計(jì)算殼程壓力降 殼程為恒溫恒壓蒸汽冷凝，其壓降可忽略。由此可知，所選換熱器合適。 三、工藝設(shè)計(jì)計(jì)算結(jié)果匯總表 換熱器主要工藝結(jié)構(gòu)參數(shù)和計(jì)算結(jié)果一覽表參數(shù)管程殼程流率kg/h718922525.25溫度（進(jìn)/出)/20/2351.7/51.7物性參數(shù)定