The TiO ₂-SiO ₂-Al ₂O ₃ composite support was prepared by sol-gel method, and then the MoP/TiO ₂-SiO ₂-Al ₂O ₃ catalyst was prepared in the way of co-impregnation. XRD results show that the diffraction peaks of TiO ₂ crystalline phase is due to anatase and SiO ₂ is mostly amorphous dispersed in γ-Al ₂O ₃ cystal surface. After in-situ reduction, the hydrodearomatization (HDA) activity of the catalyst was investigated in the fixed bed reactor. The results suggest that the mole ratio of Ti, Si and Al have a great influence on the activity of composite support catalyst. HDA activity of the MoP/TiO ₂-SiO ₂-Al ₂O ₃ catalyst shows the highest activity (65.6%) when the ratio of n(Ti)∶n(Si)∶n(Al) was 1∶1∶4, the Mo loading amount is 20%. In addition, the results also show that the HDA rate of the catalyst with the composite TiO ₂-SiO ₂-Al ₂O ₃ support was 19.6% and 13.6% higher than the traditional cataslysts of γ-Al ₂O ₃ and SiO ₂-Al ₂O ₃, respectively.

        The carbonized resin w as prepared using strong acid cation exchange resin as the precursor .Using the carbonized resin as carrier , the carbonized resin supported PW ₁₂ catalyst was prepared by loading PW ₁₂ on the carbonized resin .Effect of activation condition of the carbonized resin on the surface performance, loadings of PW ₁₂and stability of PW ₁₂ were investigated.The adsorption process of solid acid catalyst PW ₁₂ on carbonized resin w as influenced.Research results show that activation of HNO ₃ is better than that of HCl, H ₂SO ₄ and H ₃PO ₄ , and the optimal concentration of HNO ₃ of the pretreatment solution is 4.5mol/L .The etherification of light catalytic cracking gasoline and methanol w as carried out under the conditions of reaction temperature is 70 ℃,methanol and olefin mole ratio is 1.1, pressure is 1 .0 MPa , LHSV is 1.0 h-1 .The conversion of tertiary carbonic olefin is up to 56.68 %, which is higher than that of D005 strong acid cation exchange resin catalyst.