【正文】 — — — 視鏡 見圖g 150 HG20592 S0 RF 汽相口 120h 80 HG20592 S0 RF 進料口 120i 150 HG20592 S0 RF 出料口 120j 50 HG20592 S0 RF 備用口 120k 100 HG20592 S0 RF 出料口 120m1,2,3 65 HG20592 S0 RF 進汽口 120n1,2 65 HG20592 PL RF 出汽口 120p — — M10 — 內螺紋 排氣口 28畢業(yè)設計27設計數(shù)據(jù)表如下：表 62 反應釜設計數(shù)據(jù)規(guī)范《鋼制容器》 《壓力容器用不銹鋼鍛件》《機械攪拌設備》 《鋼制化工容器制造技術要求》《壓力容器安全技術監(jiān)察規(guī)程》介質 容器 夾套 壓力容器類別 二類焊條：0Cr18Ni10Ti 之間為A132，Q235B 之間為 J422不銹鋼與碳鋼之間為A302，0Cr18Ni10Ti焊劑為 HJ260；碳鋼自動焊絲為H08A介質特性 易燃，中度 危害 蒸汽，水 焊條及焊 絲牌號焊劑為 HJ431工作溫度(℃) 85 25~95 焊接規(guī)程 JB/T4709 規(guī)定工作壓力(MPa) 0~ 焊縫結構 除注明外采用全焊透結 構設計溫度(℃) 100 110 除注明外角焊縫腰高 按 HG205831998 規(guī)定設計壓力(MPa) 管法蘭與接管焊接標 準 —腐蝕裕量(mm) 0 焊接接頭類別 標準 級別焊接接頭系數(shù) 1 容器 JB4730Ⅱ主要受壓元件材質0Cr18Ni10Ti Q235BA, B JB4730Ⅲ全容積(m 3) 25 容器 —加熱面積(m 2) 42 C, D 夾套 —保溫層厚度(mm) 50 50 攪拌器型式 槳式+渦輪式表面防腐要求 按 JB/T47112022 攪拌器轉速 (轉/min) 250管口及支座方位 按本圖 所用到的焊接方法畢業(yè)設計28畢業(yè)設計29畢業(yè)設計30畢業(yè)設計31畢業(yè)設計32畢業(yè)設計33畢業(yè)設計34第 7 章 其他設計 工廠布置設計參見《化工安全手冊》 ，設計時考慮到現(xiàn)代工廠發(fā)展的趨勢以及綠化環(huán)保的原則設計如下：設計時將主要分為四塊：西北為主反應車間、倉庫、質檢室及成品包裝等；東北為小會議室、水電設施、污水處理及消防設施等；西南為乙烯精制系統(tǒng)、原料儲存、主控室、配料室、裝配車間；東南為辦公樓與食堂。不同的氣體在有機蒸氣膜中透過速率會有所不同，利用有機蒸氣膜的這一性能，就可以實現(xiàn)對混合氣體中不同組分的分離。之后，完成了主要設備的的設計、物料及能量衡算，在此基礎上完成了包括：工廠布置、設備布置、主要設備圖、工藝過程圖、及乙烯精制系統(tǒng)圖五張圖紙。在此我要向一直以來辛苦工作的三位老師表示我最衷心的感謝和最崇高的敬意! 衷心祝愿三位老師，身體健康，工作順利，生活幸福，一生平安！畢業(yè)設計40附 錄附錄一：外文翻譯附錄二：各張圖紙附圖 1：附圖 2：工藝流程圖附圖 3：乙烯精制系統(tǒng)圖附圖 4：設備布置圖附圖 5：工廠布置圖畢業(yè)設計41附錄一：畢業(yè)設計42The cocatalyst modifiers that may be optionally employed by the present invention are hydrocarbyl alkoxysilanes. It is again emphasized that when an alcohol is employed in preparing the polymerization catalyst the cocatalyst modifier is not optional. Rather it is required in that embodiment of the present invention. Preferred hydrocarbyl alkoxysilanes include: hydrocarbyl trialkoxysilanes, dihydrocarbyl dialkoxysilanes and trihydrocarbyl alkoxysilanes. Of the hydrocarbyl trialkoxysilanes,diisopropyldimethoxysilane (DIPS) is highly preferred.When a cocatalyst modifier is employed, the molar ratio of said cocatalyst modifier to transition metal in said solid catalyst is from about to about 100. More preferably, the molar ratio of cocatalyst modifier to transition metal in said solid catalyst employed is from about to about 10.The polymerization process can be conducted in either the gas phase (stirred or fluidized bed) or solution phase. When gas phase polymerization is employed, a single or multiple reactor connected in parallel or series may be employed. The conditions of gas phase polymerization employed in the present invention include any that have heretofore been utilized. Examples of suitable conditions for operating in the gas phase that can be employed herein are disclosed, for example, in . Pat. No. 5,258,345 to Kissin, et al., the contents of which are being incorporated herein by reference.When solution polymerization is employed, the polymerization is carried out in a liquid anic medium in which the solid ethylene polymerization catalyst is suspended using any slurry polymerization conditions heretofore utilized. A pressure sufficient to maintain the anic diluent and at least a portion of the onomer in the liquid phase is maintained. Examples of typical operating conditions for slurry polymerization that can be employed herein are described in EPO 848 021 A2, the contents of which are being incorporated herein by reference.The above ethylene polymerization catalyst and polymerization process provide the ethylene copolymer resin having the abovedescribed unique melt elastic properties. Hence, the ethylene copolymer resin has all of the properties mentioned hereinabove which include having a density of cc/g or lower and having a work structure. Moreover, the ethylene copolymer resin exhibits the unique melt elastic properties mentioned hereinabove. Such melt elastic properties distinguish the inventive copolymer resin from any mercially known copolymer 畢業(yè)設計43since the same do not exhibit the abovementioned melt elastic properties.Another aspect of the present invention relates to a highimpact strength film that can be produced from the ethylene copolymer resin of the present invention. Specifically, the highimpact strength film is formed from the pellet of the ethylene copolymer resin of the present invention, and it exhibits improvement in film properties and/or processability. Specifically, the film of the present invention exhibits a dart impact strength of greater than about 300 g/mil and a MD tear of greater than about 300 g/mil. In one embodiment of the present invention, the film has a dart impact strength greater than about 350 g/mil and a modulus of elasticity of from about 20 to about 35 Ksi.The film is formed in the present invention using a single layer blown film extrusion line which operates under the following conditions:1 mil, Blowupratio, 150 lb/hr, 8 inch die, 100 mil die gap, dual lip air ring, 16 inch frostline height, 4。 聚乙烯尾氣組成畢業(yè)設計36表 81 尾氣成分尾氣的組成 kg/h wt/%氮氣 550 己烷 420 乙烷 乙烯 丁烷 HCl 水 51 總流量 kg/h 1022 —壓力 Pa 正常 最大 溫度 ℃ 正常 102 最大 120聚乙烯的回收效果正己烷為 %。 工作原理 [14]膜分離的基本原理就是利用各氣體組分在高分子聚合物中的溶解、擴散速度不同，在膜兩側分壓差的作用下，導致其滲透通過纖維膜壁的速度不同而分離。 反應器生產(chǎn)能力、數(shù)量和容積的確定 反應器容積的確定反應器容積選用 25m3 罐 生產(chǎn)能力的計算由物料衡算得：畢業(yè)設計25毎釜填料為： 333)H(C)( )/( ??????物填料系數(shù)為 70%，則所用反應釜體積為： 339.%選用數(shù)量由物料衡算設計為 4 個。(7)攪拌釜中攪拌槳的特性。在此忽略副反應，一般來說，0℃時與 25℃時的反應熱相差不大，熱量衡算時就拿25℃時的反應熱當作 0℃時的反應熱。℃1己烷 Cp kJ反應溫度為 85℃，輸出物質的溫度為 55℃。釜/???由于加料時需先進性氣體置換，放空后裝置內壓力為 ，加入 氫氣使總壓為 ，置換完畢后聚合釜通過己烷進料管加入己烷。表 42 三井油化參數(shù)表項目 三井油化聚合釜容積 /m3 87乙烯進料量/ t在正常生產(chǎn)裝置中，控制 MFR 的方法是控制聚合釜氣相中氫氣與乙烯的摩爾比，其規(guī)律是 MFR 隨聚合釜內氣相中氫氣與乙烯的摩爾比增高而上升 [7]。圖 31 聚合時間對 BCEI和參考催化劑活性的影響■ BCEI catalyst；● Reference catalyst BCEI 和參考催化劑氫調敏感性的比較BCEI