1.2 Mt/a催化裂解装置运行分析

Operation Analysis of a 1.2 Mt/a Catalytic Cracking Unit

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。

The material balance,product distribution and energy consumption of a 1.2 Mt/a catalytic cracking（DCC） unit were investigated with residue oil from Lufeng and Weizhou as feedstock using the OMT-2 catalyst. The technical parameters of the reaction-regeneration system and fractionation system were calculated. The results showed that the total liquid yield was 82.4%（w）,and actual product distribution was lower than the design values. The yields of dry gas,liquefi ed gas and light diesel oil were 1.3,6.5 and 3.1 percent points lower than the design values,respectively. The yield of gasoline was 11.8 percent points higher than its design value. The slurry oil yield and coke yield were slightly higher than their design values. The comprehensive energy consumption at 90% load was 84.0 kg-oil/t. In the dry gas containing trace butane and butane,the H2 content was 28.81%（φ）,the content of C3＋ components was 0.86%（φ）,and the ethylene content was 7.76 percent points lower than its design value. The hydrogen content in coke was 7.99%（w） which was too high for the DCC system. Further observation for the atomization nozzle was needed. When the unit is restarted,the measures,namely reducing the catalyst loss,increasing the cold refl uxing fl owrate and increasing the heat load of waste heat boiler,should be taken.