本文選題：蠟油加氫 + LOPA分析　； 參考：《中國(guó)石油大學(xué)(華東)》2015年碩士論文

【摘要】：隨著重質(zhì)、高硫原油煉制數(shù)量的增加以及汽柴油標(biāo)準(zhǔn)升級(jí),加氫技術(shù)在石油煉制中得到廣泛應(yīng)用。對(duì)減二、減三線蠟油進(jìn)行加氫處理,可以獲得高質(zhì)量的石油加工產(chǎn)品,并能增產(chǎn)石油化工原料和中間餾分油。但蠟油加氫裝置處于高溫、高壓、臨氫等操作環(huán)境下,且裝置內(nèi)介質(zhì)具有易燃、易爆、有毒性,根據(jù)GB50160-2008,加氫裝置屬甲類火災(zāi)危險(xiǎn)裝置。因此,應(yīng)重點(diǎn)加強(qiáng)蠟油加氫裝置的風(fēng)險(xiǎn)控制與預(yù)防。因此本文從以下幾方面對(duì)蠟油加氫裝置進(jìn)行研究:(1)本文通過(guò)對(duì)某企業(yè)蠟油加氫裝置進(jìn)行危險(xiǎn)與可操作性分析(HAZOP),系統(tǒng)辨識(shí)出裝置存在的風(fēng)險(xiǎn)有害因素,并根據(jù)企業(yè)風(fēng)險(xiǎn)矩陣,判斷風(fēng)險(xiǎn)等級(jí),并結(jié)合企業(yè)常見(jiàn)事故統(tǒng)計(jì)及現(xiàn)場(chǎng)工藝專家的意見(jiàn),選取“循環(huán)氫中斷,反應(yīng)器超溫,設(shè)備破裂泄漏,引發(fā)火災(zāi)爆炸”、“回流塔頂超溫超壓,設(shè)備破裂泄漏,引發(fā)火災(zāi)爆炸”等事故場(chǎng)景進(jìn)行LOPA分析。(2)結(jié)合某企業(yè)蠟油加氫工藝,運(yùn)用流程模擬軟件HYSYS對(duì)蠟油加氫裝置的反應(yīng)部分和分餾部分進(jìn)行穩(wěn)態(tài)和動(dòng)態(tài)建模。加氫反應(yīng)器是根據(jù)蠟油加氫工藝的原料和產(chǎn)品,將物料分為原料油、柴油、航空煤油、重石腦油、輕石腦油、氣體,構(gòu)造了6集總反應(yīng)模型。模擬結(jié)果與實(shí)際運(yùn)行結(jié)果基本一致,符合工程設(shè)計(jì)要求,建立的模型合理有效。(3)HAZOP分析出導(dǎo)致分餾塔超溫的故障原因,運(yùn)用HYSYS模擬各故障導(dǎo)致分餾塔頂溫度變化趨勢(shì),通過(guò)對(duì)溫度變化趨勢(shì)分析,從而實(shí)現(xiàn)對(duì)分餾塔頂超溫的故障診斷。(4)結(jié)合LOPA分析結(jié)果,并應(yīng)用HYSYS模擬得出當(dāng)主分餾塔塔頂中斷回流時(shí),降低進(jìn)料溫度由328℃降至298℃,可控制塔頂溫度穩(wěn)定在159℃;當(dāng)一中回流中斷,將進(jìn)料溫度降低23℃,或者進(jìn)料量降低25%時(shí),可將主分餾塔頂溫度控制在設(shè)計(jì)范圍之內(nèi)。
[Abstract]:With the increase of heavy quality, high sulfur crude oil refining quantity and the upgrading of gasoline and diesel standard, hydrogenation technology has been widely used in petroleum refining. High quality petroleum processing products can be obtained by hydrogenation of the second and third line wax oil, and the production of petrochemical feedstock and intermediate distillate oil can be increased. However, the hydrogenation unit of waxy oil is in the operating environment of high temperature, high pressure and hydrogen, and the medium in the unit is flammable, explosive and toxic. According to GB50160-2008, the hydrogenation unit is a kind of fire hazard unit. Therefore, the risk control and prevention of waxy oil hydrogenation unit should be strengthened. Therefore, this paper studies the waxy oil hydrogenation unit from the following aspects: (1) based on the hazard and maneuverability analysis (HAZOP) of a waxy oil hydrogenation unit in a certain enterprise, the risk and harmful factors of the unit are identified systematically, and the risk matrix of the unit is analyzed according to the enterprise risk matrix. Judging the risk level, combining with the statistics of common accidents in enterprises and the opinions of the experts in the field, selecting "cyclic hydrogen interruption, reactor overtemperature, equipment rupture and leakage, causing fire and explosion", "reflux tower top temperature overpressure, equipment rupture leakage," The scene of fire and explosion was analyzed by LOPA. (2) combined with the process of wax oil hydrogenation in a certain enterprise, the steady and dynamic models of the reaction and fractionation parts of the hydrogenation unit were established by using the process simulation software HYSYS. According to the raw materials and products of the wax oil hydrogenation process, the hydrogenation reactor divides the materials into feedstock oil, diesel oil, aviation kerosene, heavy naphtha, light naphtha and gas. The simulation results are basically consistent with the actual operation results, which accord with the engineering design requirements, and the established model is reasonable and effective. (3) HAZOP analyzes the causes of the faults leading to the overtemperature of the fractionator, and simulates the variation trend of the top temperature of the fractionating tower by using HYSYS. By analyzing the trend of temperature change, the fault diagnosis of the overtemperature of the top of the fractionator is realized. (4) combined with the result of LOPA analysis and the application of HYSYS simulation, it is concluded that when the top of the main fractionator breaks the backflow, the feed temperature will be reduced from 328 鈩，

本文編號(hào)：2116029