TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The soluble organometallic compound and the solid alcoholysis catalyst each comprise the same Group II to Group VI element. The solid alcoholysis catalyst comprises at least one of an immobilized organotitanium compound and a supported titanium compound, immobilized organocalcium compound and supported calcium compound, immobilized organomagnesium compound and a supported magnesium compound, immobilized organozinc compound and a supported zinc compound, immobilized organotin compound and a supported tin compound or immobilized organoantimony compound and a supported antimony compound. The soluble organometallic compound comprises a titanium compound soluble in the feed reactants; calcium compound soluble in the feed reactants; magnesium compound soluble in the feed reactants; zinc compound soluble in the feed reactants; tin compound soluble in the feed reactants or antimony compound soluble in the feed reactants.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Method: The alcoholysis is a transesterification; disproportionation reaction. The method (M1) involves: contacting the reactants in the presence of the solid alcoholysis catalyst to alcoholyze at least a portion of the reactants; and recovering a reactor effluent comprising the soluble organometallic compound, alcoholysis product, and unreacted reactants; at least one of an alcoholysis, transesterification, and disproportionation reaction producing at least one of a dialkyl carbonate, diaryl carbonate, alkyl-aryl carbonate, biodiesel, organic ester and organic carbamate; and further involves: recovering at least a portion of the soluble organometallic compound from the reactor effluent or recycling at least a portion of the recovered soluble organometallic compound to the alcoholysis reactor. The soluble organometallic compound is fed at a rate of 1-2000 ppm by weight. The method (M2) further involves: reacting the alcohol and the alcoholysis reactant in the presence of the solid alcoholysis catalyst under condition to form at least one of an alkyl aryl carbonate and dialkyl carbonate; recovering an effluent from the first reaction zone comprising the soluble organometallic compound; feeding at least a portion of the effluent from the first reaction zone to a second reaction zone; disproportionating at least a portion of the alkyl aryl carbonate to form dialkyl carbonate. The method (M3) further involves: reacting the aromatic hydroxyl compound and the dialkyl carbonate in the presence of the solid transesterification catalyst under condition to form at least one of an alkyl aryl carbonate and diaryl carbonate and recovering an effluent from the first reaction zone comprising the homogeneous catalyst; feeding at least a portion of the effluent from the first reaction zone to a second reaction zone, disproportionating at least a portion of the alkyl aryl carbonate to form diaryl carbonate. The method (M4) further involves: reacting the aromatic hydroxyl compound and the dialkyl carbonate in the presence of the solid transesterification catalyst under condition to form an alkyl aryl carbonate and recovering an effluent from the first reaction zone comprising the homogeneous catalyst. The method (M5) further involves: reacting the alcohol and the glyceride in the presence of the solid transesterification catalyst under condition to form at least one of a glycerol and a fatty acid ester and recovering an effluent from the first reaction zone comprising the soluble organometallic compound. The removing and re-depositing are performed in situ in a transesterification reactor. The removing involves: contacting the solid catalyst with a solution comprising at least one of an alcohol and water. The method (M6) further involves: conditioning the solid catalyst prior to the re-depositing. The conditioning involves: drying the solid catalyst at 49-427 degrees C (120-800 degrees F) in an inert gas flow. Preferred Components: The alcohol is an alkyl alcohol. The reactor effluent further comprises alkyl aryl carbonate. The aromatic hydroxyl compound comprises phenol. The solution further comprises a solvent. The solvent comprises at least one of benzene, toluene, xylene, hexane, octane, decane, tetrahydrofuran and ether. EXAMPLE - A silicon oxide pellet support (0.3 cm) was used to prepare an immobilized titanium n-butoxide catalyst. Silicon oxide pellets (100 g) were treated at 52 degrees C for 5 minutes with stirring with a sodium hydroxide solution (10 g). The silica was treated and dried. The dried silicon oxide pellets (9.72 g) were loaded in the reactor. A reservoir for the catalyst solution was filled with a titanium n-butoxide solution prepared by dissolving titanium n-butoxide (135 g) in toluene (1600 ml). This catalyst solution was circulated up-flow through the reactor at a flow rate of 15 ml/minutes at ambient temperature for 20 minutes, and then at 135 degrees C (275 degrees F) and 3.4 bar (35 psig) for 6 hours. After cooling, the excess catalyst solution was drained from the reactor and then the in situ-prepared catalyst was washed up-flow with toluene at ambient temperature at a flow rate of 4 ml/minutes for 1.5 hours. After draining excess toluene from the reactor, the catalyst was dried at 138 degrees C (280 degrees F) for 2 hours in 350 cc/minutes nitrogen gas up-flow. The resulting catalyst was used in a 1st, 2nd and third cycle transesterification and 1st, 2nd and third catalyst reactivation. The results showed that the catalyst maintained a steady catalyst activity for an extended period of time. Trace analysis of a sample taken 270 hours on stream indicated 47 ppm Ti by weight. The water content in the feed stream was kept at less than 650 ppm by weight. Thus it was possible to reactivate deactivated catalyst and prolong the catalyst cycle time to more than 250 hours. This experiment also indicated that it was necessary to control water content in the feed to less than 650 ppm by weight to maintain a steady catalyst activity.