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摘要
本次設計主要是針對年處理量150萬噸俄羅斯混合原油的常壓設計。
原油常壓蒸餾作為原油的一次加工工藝,在原油加工總流程中占有重要作用,在煉廠具有舉足輕重的地位,其運行的好壞直接影響到后續(xù)的加工過程。其中重要的分離設備—常壓塔的設計,是能否獲得高收率、高質(zhì)量油的關鍵。近年來常減壓蒸餾技術和管理經(jīng)驗不斷創(chuàng)新,裝置節(jié)能消耗顯著,產(chǎn)品質(zhì)量提高。但與國外先進水平相比,仍存在較大的差距。
為了更好地提高原油的生產(chǎn)能力,本著投資少,能耗低,效益高的思想對俄羅斯混合原油進行常壓蒸餾設計。設計的基本方案是:初餾塔拔出石腦油,常壓塔采取三側(cè)線,常壓塔塔頂生產(chǎn)汽油,三個側(cè)線分別生產(chǎn)煤油,輕柴油,重柴油。設計了一個初餾塔一個常壓塔一段汽化蒸餾裝置,此裝置由一臺管式加熱爐、一個初餾塔,一個常壓塔以及若干臺換熱器(完善的換熱流程應達到要求:充分利用各種余熱;換熱器的換熱強度較大;原油流動壓力降較小。)冷凝冷卻器、機泵等組成,在常壓塔外側(cè)為側(cè)線產(chǎn)品設汽提塔。流程簡單,投資和操作費用較少。原油在這樣的蒸餾裝置下,可以得到350-360℃以前的幾個餾分,可以用作石腦油、汽油、煤油、輕柴油、重柴油產(chǎn)品,也可分別作為重整化工(如輕油裂解)等裝置的原料。蒸余的塔底重油可作鋼鐵或其它工業(yè)的燃料。在某些特定的情況下也可以作催化裂化或加氫裂化裝置的原料。本次設計共用34塊浮閥塔板,塔距0.8m,塔徑3.4m,塔高28.23m.換熱流程一共通過12次換熱達到工藝要求,換熱效率是73.1%。
關鍵詞:原油;常壓蒸餾;物料衡算;熱量衡算;塔;換熱
Abstract
This design mainly regards to which Russia commingled crude oil are distilled by a process capacity of 1.5×104t/a in normal pressures.
As a part of crude oil processing technic ,the normal pressures distilion of crude oil is very important in the whole processing schemes of crude oil and refineries and its operation status directly affects the continuing machine process.There are a kind of important separate equipment---- normal pressures columns ,which is the key to attain high efficient , high quality oil. In recent years,firstly the distillion technique of normal pressures and manage experience were innovated constantly ;secondly equipments’ effect of saving energy is remarkable ;thirdly product quality was improved.But compare to international advanced techniques,there are a long distance.
In order to improve the product ability of crude oil ,In the principle of shoestring , low—energy consumption , high-efficiency ,designing the normal pressures distillion of Russia commingled crude oil.Design’s basic scheme : Prefractionator extracts naphtha. atmospheric column has three lateral line .Its tower top extracts gasoline and three lateral line respectively extrct kerosene, light diesel fuel, heavy diesel fuel.Design a distillion device with a prefractionator,a atmospheric column with a piece of gasification.This device is consist of a tubular-furnace,a prefractionator,a atmospheric column ,several heat exchangers, cooling
condenser and pumps.This procedure is simple; Investment and operation fee is short .According to this design device ,we can attain 350—360℃ previous some fraction.They can be used to be naphtha ,gasoline, kerosene,light diesel fuel, heavy diesel fuel products and they can be used tobe reforming chemical engineering’s raw material.Other tower bottle’ heavy oil can be as raw material of steel industries or other industries. At all under certain condition, they can be as raw material of catalytic cracking and hydrogen cracking .This design adopts 34 block floating valve trays. Tower distance is 0.8m. Tower diameter is 3.4m.Tower level is 28.23m.Heat exchangers process reach to the technics requirement by 12 time heat exchangers processes.The heat exchangers efficiency is 73.1%.
Key words: Oil; Atmospheric distillation; Material balance;
Heat balance; Tower; Heat exchange
目錄
前 言 ................................................ 1
第一章 產(chǎn)品方案及工藝流程 .............................. 5
1.1產(chǎn)品方案 ......................................... 5
1.2 工藝流程 ......................................... 5
第二章 工藝計算及說明 .................................. 7
2.1設計數(shù)據(jù) ......................................... 7
2.1.1 已知數(shù)據(jù) ...................................... 7
2.1.2 原油的實沸點及窄餾分數(shù)據(jù) ....................... 7
2.2 原油實沸點蒸餾曲線的繪制 .......................... 9
2.3 常壓塔工藝計算................................... 10
2.3.1 各產(chǎn)品的恩氏蒸餾數(shù)據(jù)和實沸點數(shù)據(jù)的換算 ......... 10
2.3.2 產(chǎn)品的有關數(shù)據(jù)計算 ........................... 13
2.3.3 物料衡算 ..................................... 14
2.3.4 確定塔板數(shù)和汽提蒸汽用量 ...................... 16
2.3.5 操作壓力 ..................................... 18
2.3.6 汽化段溫度 ................................... 19
2.3.7 塔底溫度 ..................................... 21
2.3.8 塔頂及側(cè)線溫度的假設與回流熱的分配 ............ 21
2.3.9 側(cè)線及塔頂溫度的校核 ......................... 22
2.4 全塔氣、液相負荷分布 ............................. 23
第三章 塔的設計及水力學計算 ........................... 32
3.1塔板的操作條件 ................................... 32
3.2塔板間距初選 ..................................... 33
3.3塔徑初算 ........................................ 33
3.4浮閥數(shù)及開孔率的計算 ............................. 34
3.5溢流堰及降液管的決定 ............................. 34
3.6水力學計算....................................... 35
3.7塔板上的適宜操作區(qū)和負荷上下限 .................... 36
第四章 塔的內(nèi)部工藝結(jié)構(gòu) ............................... 39
4.1板式塔的內(nèi)部工藝結(jié)構(gòu) ............................. 39
4.2 塔高H .......................................... 41
第五章 換熱流程設計 ................................... 42
5.1換熱流程計算 ..................................... 42
5.1.1初餾塔之前的換熱流程 .......................... 43
5.1.2常壓塔前換熱流程 .............................. 47
5.2熱量利用率計算 ................................... 48
結(jié) 論 ................................................ 49
致謝 ................................................. 50
附錄 ................................................. 61
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