工业催化
工業催化
공업최화
INDUSTRIAL CATALYSIS
2015年
6期
480-485
,共6页
石油化学工程%催化干气%乙苯%高辛烷值汽油组分%烷基化%能耗
石油化學工程%催化榦氣%乙苯%高辛烷值汽油組分%烷基化%能耗
석유화학공정%최화간기%을분%고신완치기유조분%완기화%능모
petrochemical engineering%FCC dry gas%ethylbenzene%high-octane rating gasoline%alkylation%energy consumption
为充分利用炼油厂干气中的稀乙烯资源，设计开发了稀乙烯制乙苯成套技术（SGEB）。该技术采用预处理工艺脱除原料干气中的丙烯和丁烯，苯和乙烯气相烷基化反应部分使用高效 SEB系列稀乙烯制乙苯催化剂，在反应温度（320~380）℃、反应压力（0.7~1.0）MPa 和苯烯物质的量比为5.0~7.0条件下，乙烯转化率达99%以上。利用该技术进行生产的能耗和物耗较低，每吨乙苯的苯单耗为0.75 t、乙烯单耗0.275 t、综合能耗150 kg 标准油，产品乙苯纯度超过99.8%，主要杂质二甲苯含量低于0.08%，该技术已在国内9套装置上成功应用。同时，根据部分炼油厂汽油辛烷值不够的实际情况，对干气制乙苯技术进行工艺优化设计，停用脱丙烯预处理单元，分离单元仅到苯分离塔为止，烷基化反应苯烯物质的量比可降低至4.0~5.0，每吨产品的能耗降低至约80 kg标准油，得到的调和汽油组分辛烷值高达108.1，有效利用干气资源满足了企业汽油调和辛烷值的要求。采用开发的两种技术，企业可根据市场和自身情况灵活选择生产乙苯或高辛烷值汽油组分。
為充分利用煉油廠榦氣中的稀乙烯資源，設計開髮瞭稀乙烯製乙苯成套技術（SGEB）。該技術採用預處理工藝脫除原料榦氣中的丙烯和丁烯，苯和乙烯氣相烷基化反應部分使用高效 SEB繫列稀乙烯製乙苯催化劑，在反應溫度（320~380）℃、反應壓力（0.7~1.0）MPa 和苯烯物質的量比為5.0~7.0條件下，乙烯轉化率達99%以上。利用該技術進行生產的能耗和物耗較低，每噸乙苯的苯單耗為0.75 t、乙烯單耗0.275 t、綜閤能耗150 kg 標準油，產品乙苯純度超過99.8%，主要雜質二甲苯含量低于0.08%，該技術已在國內9套裝置上成功應用。同時，根據部分煉油廠汽油辛烷值不夠的實際情況，對榦氣製乙苯技術進行工藝優化設計，停用脫丙烯預處理單元，分離單元僅到苯分離塔為止，烷基化反應苯烯物質的量比可降低至4.0~5.0，每噸產品的能耗降低至約80 kg標準油，得到的調和汽油組分辛烷值高達108.1，有效利用榦氣資源滿足瞭企業汽油調和辛烷值的要求。採用開髮的兩種技術，企業可根據市場和自身情況靈活選擇生產乙苯或高辛烷值汽油組分。
위충분이용련유엄간기중적희을희자원，설계개발료희을희제을분성투기술（SGEB）。해기술채용예처리공예탈제원료간기중적병희화정희，분화을희기상완기화반응부분사용고효 SEB계렬희을희제을분최화제，재반응온도（320~380）℃、반응압력（0.7~1.0）MPa 화분희물질적량비위5.0~7.0조건하，을희전화솔체99%이상。이용해기술진행생산적능모화물모교저，매둔을분적분단모위0.75 t、을희단모0.275 t、종합능모150 kg 표준유，산품을분순도초과99.8%，주요잡질이갑분함량저우0.08%，해기술이재국내9투장치상성공응용。동시，근거부분련유엄기유신완치불구적실제정황，대간기제을분기술진행공예우화설계，정용탈병희예처리단원，분리단원부도분분리탑위지，완기화반응분희물질적량비가강저지4.0~5.0，매둔산품적능모강저지약80 kg표준유，득도적조화기유조분신완치고체108.1，유효이용간기자원만족료기업기유조화신완치적요구。채용개발적량충기술，기업가근거시장화자신정황령활선택생산을분혹고신완치기유조분。
Aiming to fully utilize the dilute ethylene of FCC off gas of the refinery,the process technology for ethylbenzene production from dilute ethylene was developed. The technique used the pre-treatment process to remove propylene and butylenes from raw dry gas,and SEB series catalysts for the vapor phase alkylation of benzene with dilute ethylene. Under the condition of reaction temperature(320 - 380)℃,reaction pressure(0. 7 - 1. 0)MPa,benzene / ethylene molar ratio 5. 0 - 7. 0,ethylene conversion was more than 99% . For production of 1 ton ethylbenzene,the consumption of benzene and ethylene in FCC off-gas,and the energy consumption were 0. 75 t,0. 275 t and 150 kilograms of standard oil,respectively. The purity of ethylbenzene was over 99. 8% and the content of main impurity xylene in the product was < 0. 08% . This process technology had been applied successfully in 9 plants. Because the octane rating in the blended gasoline was insufficient,the process for dilute ethylene to produce ethylbenzene was optimized,in which the pre-treatment unit of removing propylene was omitted and other distillation units following benzene column were cut,and therefore benzene / ethylene molar ratio could be reduced to 4. 0 - 5. 0. Energy consumption of per ton product was reduced to about 80 kilograms of standard oil,and the octane rating of the obtained blended gasoline was up to 108. 1,which met the requirement of octane rating of the blended gasoline. The resource of dilute ethylene was effectively utilized. The two techniques could help the comprise to flexibly produce ethylbenzene or high-octane rating gasoline component according to the market and plant’s operation situation.
