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 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; a zinc compound soluble in the feed reactants; tin compound soluble in the feed reactants; an antimony compound soluble in the feed reactants; lanthanide compound soluble in the feed reactants; actinide compound soluble in the feed reactants (preferably La or Ac). The solid alcoholysis catalyst comprises at least one of an immobilized organocalcium compound and supported calcium compound; at least one of an immobilized organotitanium compound and a supported titanium compound; at least one of an immobilized organomagnesium compound and a supported magnesium compound; at least one of an immobilized organozinc compound and a supported zinc compound; at least one of an immobilized organotin compound and a supported tin compound; at least one of an immobilized organoantimony compound and a supported antimony compound; at least one of an immobilized organolanthanide compound and a supported lanthanide compound; immobilized organoactinide compound and a supported actinide compound (preferably La or Ac).    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Method: The alcoholysis is a transesterification or disproportionations. The process (A) 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. The soluble organometallic compound is fed at a rate of 1-2000 ppm by weight. The process (A) further involves: recovering at least a portion of the soluble organometallic compound from the reactor effluent; recycling at least a portion of the recovered soluble organometallic compound to the alcoholysis reactor. The process (B) further involves: contacting the alcohol and the alcoholysis reactant in the presence of the solid alcoholysis catalyst under condition to react at least a portion of the alcoholysis reactant with the alcohol to form at least one of an alkyl aryl carbonate and a 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; and disproportionating at least a portion of the alkyl aryl carbonate to form dialkyl carbonate. Preferred Components: In the process (B), the alcohol is an alkyl alcohol; the reactor effluent further comprises alkyl aryl carbonate. SPECIFIC COMPOUNDS - Preparation of 2 compounds are specified as the dialkyl carbonates i.e. diethyl carbonate (IA) and dimethyl carbonate.    EXAMPLE - A magnesium nitrate solution was prepared by dissolving Mg(NO3)2.6H2O (10.96 g) in deionized water (24 g). Silica gel sphere support (1.7-4 mm diameter; 6 hydroxyl groups per nm2, 314 m2/g Brunauer emmitt and teller (BET), 1.055 cm3/g pore volume and 13.46 nm average pore diameter) (30 ml; 11.91 g) was impregnated with the above magnesium nitrate solution by an incipient wetness technique. The silica gel sphere support was prepared by an oil dropping technique. After drying the impregnation product at 100 degrees C for 1 hour, it was then calcined at 510 degrees C for 2 hours. MgO/SiO2 catalyst (15 ml; 6.30 g) was loaded in the reactor. Canola oil feed was prepared by mixing methanol (5.39 wt.%) with the canola oil (94.61 wt.%). The acid value of free fatty acid of this feed was 0.48 mg KOH/g. The transesterification of canola oil with methanol was performed at 165 degrees C (330 degrees F) and 19.4 bar (267 psig) by feeding the canola oil feed and methanol at 0.2 ml/minutes each. Magnesium ethoxide was dissolved in the methanol feed to have 28 ppm Mg by weight in the catalytic reaction zone. The effluent streams were composed of two clear layers. Top layers contained the product methyl esters and small amounts of unconverted triglycerides. The average content of unconverted triglycerides in the reaction products, excluding methanol from the top layers, was 1.2 wt.%. The bottom layer contained most of the unconverted triglycerides. The result indicated a stable catalyst performance.