480萬噸常壓蒸餾工藝計算

摘  要

　　　本設(shè)計綜述部分論述了清潔燃料生產(chǎn)的現(xiàn)狀，并且對未來煉油企業(yè)生產(chǎn)清潔燃料的趨勢進(jìn)行討論，設(shè)計部分主要完成了年處理能力為480萬噸的大慶原油常壓塔的設(shè)計計算，其次為塔板的設(shè)計。
　　　常壓塔的設(shè)計主要是依據(jù)所給的原油實沸點蒸餾數(shù)據(jù)及產(chǎn)品的恩氏蒸餾數(shù)據(jù)，計算產(chǎn)品的各物性數(shù)據(jù)，確定原油切割方案，計算產(chǎn)品收率。參考同類裝置確定塔板數(shù)，進(jìn)料及側(cè)線抽出位置，假設(shè)各主要部分的操作溫度及操作壓力，對全塔進(jìn)行熱平衡計算，確定全塔回流熱。本次設(shè)計塔頂采用二級冷凝冷卻回流，塔中采用兩個中段循環(huán)回流，塔頂取熱：第一中段回流取熱：第二中段回流取熱為 3：3.5：3.5，最后校核各主要部位操作溫度都在允許的誤差范圍內(nèi)。
　　　塔板型式選用F1型33克重閥浮閥塔板，依常壓塔內(nèi)最大汽相負(fù)荷處為2099.64Kmol/h，算得塔徑為6.0m，塔板間距為0.6m，最后算得塔高為29.8m。對塔板流體力學(xué)性能進(jìn)行核算，操作彈性為4.43，塔的操作性能良好。
　　　本次設(shè)計主要采用經(jīng)驗圖表和經(jīng)驗公式進(jìn)行計算，計算結(jié)果表明，參數(shù)的核算結(jié)果均在誤差允許范圍內(nèi)和經(jīng)驗值范圍內(nèi)。
關(guān)鍵詞：清潔燃料；發(fā)展趨勢；大慶原油；常壓塔；塔板；設(shè)計

Abstract
　　　Current state of producting clearer fuel and the trend of producting clearer fuel in refinery in the future are discussed in summary department. An atmospheric distillation column, which is able to treat crud oil 4.8MT a year, is designed mainly, and a type of tray is included.
　　　The design of the atmospheric distillation column is based on the datum of true point distillation of the crude oil and of Engler distillation of the products. The calculation of products′ phsical property parameters and the cut comceptual and products′ yields are also based on the datum. The tray number, the feed tray and the side stream withdrawal tray are determined by referring to the same kind unit. The following work is to assume the operating temperature and pressure of all the important points of the column and to make the energy balance calculation for the whole column, and make sure heat of reflue. A two-grade condenser is be used on the overhead of the column, and two mid-pump around on the body.  The ratio of the energy taken by the condensers from top to bottom is 3:3.5:3.5. Finally, the temperature assumed should be checked up. It is very important.
　　　A type of F1 valve tray, which weighs 33g a valve, is being chosen. It′s maximum vapor load of the column is 299.64Kmol/h, and outside diamete is 6.0m.The tray spacing 0.6m. So the height of the column body is 29.8m.In this section, the most important work is to calculate the hydromechanics performance and the operating flexibility of tray is 4.43. The tray should be operated in a proper area.
　　　The design is mainly adopted empirical figures and empirical equations. The results show that the results are in the range permitted and in the range of empirical values.
Keywords: Clearer fuel; development trend;daqing crude oil; atmospheric distillation column; tray; design
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目  錄
1 前 言 1
1.1文獻(xiàn)綜述 1
1.1.1清潔燃料生產(chǎn)技術(shù) 1
1.1.2常減壓蒸餾裝置的重要地位 10
1.2 本設(shè)計的主要內(nèi)容 16
2 設(shè)計說明書 18
2.1 原油性質(zhì)及評價 18
2.2 產(chǎn)品性質(zhì) 18
2.3 常壓塔設(shè)計的參數(shù)確定 19
2.3.1 操作壓力的確定 19
2.3.2 操作溫度的確定 20
2.4常壓塔設(shè)計中的一些經(jīng)驗數(shù)據(jù) 21
2.5塔板設(shè)計中的一些經(jīng)驗數(shù)據(jù) 22
3 常壓塔的工藝計算 24
3.1 設(shè)計任務(wù) 24
3.2 基礎(chǔ)數(shù)據(jù) 24
3.3 油品性質(zhì)參數(shù) 25
3.4 實沸點切割點和產(chǎn)品收率 29
3.5 汽提蒸汽用量 30
3.6 塔板型式和塔板數(shù) 31
3.7 精餾塔計算草圖 31
3.8 操作壓力 32
3.9 汽化段溫度 32
3.10 塔底溫度 39
3.11 塔頂及側(cè)線溫度的假設(shè)與回流熱分配 39
3.12 側(cè)線及塔頂溫度的校核 42
3.13 全塔汽、液相負(fù)荷分布圖 46
3.13.1 對所選塔板進(jìn)行汽、液相負(fù)荷的計算 46
3.13.2 繪制汽、液相負(fù)荷分布圖 60
4 塔板的工藝計算 65
4.1 塔板工藝尺寸計算 65
4.1.1塔徑 65
4.1.2 溢流裝置 66
4.2 塔板流體力學(xué)核算 68
4.3 塔板負(fù)荷性能圖 70
4.4 浮閥塔板工藝計算結(jié)果匯總 74
致 謝 76
參考文獻(xiàn) 77