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在1.2 Mt/a催化裂解装置上以陆丰与涠洲原油的常底渣油为原料,采用OMT-2催化剂,通过运行分析考察了装置的物料平衡、产品分布和装置能耗,并对反应-再生系统和分馏系统技术参数进行了核算。运行结果表明,装置的总液体收率为82.4%(w),实际产品分布低于设计工况。干气收率较设计值低1.3百分点;汽油收率较设计值高11.8百分点;液化气收率较设计值低6.5百分点;油浆产量及焦炭产率稍高于设计值;柴油收率较设计值低3.1百分点。90%负荷下的综合能耗为84.0 kg-oil/h。干气中的H2含量为28.81%(φ),C3以上重组分含量达到0.86%(φ)左右,含微量丁烷和丁烯,N2含量偏底,乙烯含量较设计值偏低7.76百分点。焦炭中氢含量7.99%(w),需进一步观察喷嘴的雾化效果。装置再投产时需解决催化剂跑损、粗汽油泵流量小以及余热锅炉过热段负荷不足的问题。
On the 1.2 Mt / a catalytic cracking unit, the natural residue of Lufeng and Weizhou crude oil was used as raw material. The OMT-2 catalyst was used to analyze the material balance, product distribution and energy consumption of the unit through the operation analysis. Regeneration system and fractionation system technical parameters were accounted for. Operating results show that the total liquid yield of the device is 82.4% (w), the actual product distribution is lower than the design conditions. The dry gas yield was 1.3 percentage points lower than the designed value; the gasoline yield was 11.8 percentage points higher than the designed value; the liquefied gas yield was 6.5 percentage points lower than the designed value; the yield of oil slurry and the coke yield slightly higher than the designed value; 3.1 percentage points lower value. The combined energy consumption at 90% load is 84.0 kg-oil / h. The content of H2 in dry gas was 28.81% (φ), and the content of heavy components above C3 reached 0.86% (φ), with traces of butane and butene. The content of N2 was partial and the ethylene content was 7.76% lower than the designed value. The coke hydrogen content of 7.99% (w), need to further observe the nozzle atomization effect. When the device is put into operation, it is required to solve the problem of catalyst running loss, small flow rate of the crude gasoline pump and insufficient load of the superheating section of the waste heat boiler.