选用150 m长的DB-1色谱柱，在程序升温的条件下，用气相色谱法分离并测定了催化裂化（FCC）轻汽油及其醚化产物中甲醇、异戊烷、3-甲基-1-丁烯、2-甲基-1-丁烯、2-甲基-2-丁烯及叔戊基甲醚等6种组分。根据相应组分的峰面积A_i及其相对响应因子R_i，用校正归一法计算上述6种组分的含量；在计算相对响应因子时，取碳及氢的相对原子质量（分别为12.011，1.008 0）为基础。甲醇的检出限为0.002%，其余5种组分的检出限均为0.001%。应用该方法分析了醚化FCC轻汽油样品，测得上述6种组分测定值的相对标准偏差（n=6）依次为0.82%，0.64%，1.1%，0.54%，0.33%，1.3%。用标准加入法测定了6种组分的回收率，所得回收率在88.9%~99.0%之间。为对催化裂化装置的催化剂反应性能作出评价，可从预反应器出口物料、醚化蒸馏塔顶物料和后反应器出口物料中分别取得样品，应用该方法对其中相应组分进行测定。异戊烷在此反应工艺中不参与反应，根据每个反应器入口和出口的异戊烯与异戊烷的比值可以计算出异戊烯在整个工艺过程中的转化率。经计算得异戊烯在预反应器中的转化率为66.5%，在醚化蒸馏塔中的转化率为76.1%，在后反应器中的转化率为37.5%，醚化反应的总转化率为95.0%。

GC separation and determination of 6 components, i.e., methanol, isopentane, 3-methyl-1-butene, 2-methyl-1-butene, 2-methyl-2-butene and tert-amyl-methyl ether in fluid catalytic cracking (FCC) light gasoline and its etherified products were applied using a chromatographic column of DB-1 (150 m length) under the mode of programmed temperature elevation. Contents of the 6 components were calculated by the method of correction-normalization based on the values of peak area A_i and relative pesponse factors R_i of the related component, taking the relative atomic masses of 12.011 for carbon and 1.008 0 for hydrogen in the calculation of the relative response factors. The detection limit of methanol was 0.002%, and the detection limits of the remainder 5 components were same as 0.001%. A sample of etherified light gasoline of FCC was analyzed by the proposed method, giving RSDs (n=6) of 0.82%, 0.64%, 1.1%, 0.54%, 0.33% and 1.3% for the 6 components respectively. Recovery of the 6 components was tested by standard addition method, giving results in the range of 88.9%-99.0%. The proposed method was used to evaluate the capacity of the catalyst of the catalytic cracking installation. In this case, samples were taken from the substances separately at the outlet of pre-reactor, at the top of the etherification distillation tower and at the outlet of post-reactor, and analyzed by the method for their components. As isopentane did not take part in the FCC process, the conversion rates of isoamylene of the technology process could be calculated on the base of the ratio of isoamylene to isopentane at the inlet and outlet of each reactor. It was found that the conversion rates of isoamylene in the pre-reactor, in the etherification distillation tower and in the post-reactor were found to be 66.5%, 76.1% and 37.5% respectively. The total conversion rate of etherification was 95.0%.