TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The base treatment is performed with sodium hydroxide, sodium borohydride, calcium hydroxide, and/or potassium hydroxide. The acidification is performed with hydrochloric acid, sulfuric acid, or phosphoric acid. The adsorbent agent is selected from activated charcoal, and clays.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Method: The acidification is performed until obtaining pH of 4-5. The treatment with base is performed until obtaining pH of 6. The current density applied in the electrodialysis unit is 100-500 A/m2. The process is performed in a continuous manner. The process additionally involves diluting the neutralized glycerin before feeding into the electrodialysis unit (preferably the glycerin is diluted with water up to 50%); clarifying the glycerin extracted with an adsorbent agent; and removing the water present in the glycerin (preferably by evaporation) that has been treated.    TECHNOLOGY FOCUS - POLYMERS - Preferred Components: The adsorbent agent is selected from ion exchange resins. EXAMPLE - Purification of glycerin produced in biodiesel manufacturing process, by electrodialysis was carried out as follows. The feed current of glycerin to be purified had concentration of 50%, included unconverted triglycerides, methanol, and soaps as impurities, and had dark brown color. Before electrodialysis, glycerin was treated with HCl for producing soap and fat-free glycerin, and then was treated with sodium hydroxide to remove excess acid, to result in brown colored glycerin solution contaminated with salts, water and methanol; and had pH of 5.7, % glycerin of 85.8, conductivity of 294 mu second/cm, density of 1.2949 g/ml, and Cl- concentration of 60.41 g/L. Subsequently, conditioned glycerin was subjected to electrodialysis in two-compartment press filter-type laboratory cell provided with 2 electrodes, anion exchange membrane and cation exchange membrane. The anode used was an IrO2/Ti (DSA-O2) anode and the cathode was a 316 stainless steel cathode. Neosepta AFN (RTM: anionic membrane) and Neosepta CMX (RTM: cationic membrane) were used. The distance between membranes was 3.3 cm and effective membrane area was 20 cm2. The current density applied was low i.e. 150 A/m2. The anodic reaction was oxidation of water to oxygen with simultaneous production of H+ ions, and cathodic reaction was reduction of water to hydrogen, producing OH- ions. Under action of electric field, salts were extracted from feed solution. The crude glycerin solution used was a very dense solution with barely any conductivity, and was diluted with water to apply treatment for removing chlorides by electrodialysis. For % glycerin in diluted compartment of 53.77, and Cl- concentration of 32.52 g/L at 7 volts before electrodialysis; the results after electrodialysis at 150 A/m2 performed for 8.78 hours at circulated charge of 0.098 Faradays, and voltage of 16.26 volts; showed that Cl- concentration was 0.06 g/L, % current efficiency for Cl- ions (%Ec-Cl-) was 94.01%, % reaction yield for Cl- ions (%R-Cl-) was 99.81, and specific energy consumption (SEC) was 0.362 kWh/kg. The results showed that as current density decreased, energy consumption was also reduced, and process current efficacy increased. The elimination of chlorides was close to 100%. In this case, glycerin diffusion from diluted solution to concentrated solution was observed, greater at lower current densities. Although, removal of chloride concentration from glycerin solution was virtually 100%; it had dark brown color, so glycerin solution from electrodialysis unit was treated with mineral coal powder, to obtain colorless transparent solution. For use of this glycerin for pharmaceutical purposes, chloride concentration should be less than or equal to 10 ppm. To meet this, solution was treated with anion exchange resins in OH- form. Finally, once colorless and chloride-free glycerin solution was produced, it was evaporated to remove water to obtain 98% pure glycerin.