TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Components: The primary carbon source for the method is crude glycerol. The high cell density is 200000 to 1000000 cells per milliliter of medium (preferably at least 800000). Preferred Method: The conditions that promote high cell density include at least one of: maintaining a culture temperature of 25-35 (preferably 30) degrees C; maintaining dissolved oxygen level of at least 10 to 50 (preferably 20)%; and maintaining a level of nitrogen at 1.0 to 1.5 g/l. The conditions that promote an increase in cell size and accumulation of fatty acids include at least one of: maintaining a culture temperature of 25-35 (preferably 30) degrees C; maintaining dissolved oxygen at a level of 2 to 10 (preferably 3-5)%; and maintaining a level of nitrogen at 0.5 to 1.0 g/l. The conditions that promote an accumulation of fatty acids include at least one of: maintaining a culture temperature at 20 to 25 degrees C; maintaining dissolved oxygen at a level of 0 to 0.5%; and cessation of nitrogen feeding. The step of culturing microalgae under conditions that promote high cell density is carried out for 12-36 (preferably 24) hours. The step of culturing microalgae under conditions that promotes an increase in cell size and accumulation of fatty acids is carried out for 60 to 80 hours. The steps (A)-(C) are carried out in a single fermentor or are each carried out in a separate fermentor. The step (A) is carried out in a first fermentor and steps (B) and (C), are carried out in a second fermentor. In the integrated biofuel and omega-3 fatty acid production method, the pre-treating step includes the steps of culturing microalgae under conditions that promote high cell density; then culturing the microalgae under conditions that promote an increase in cell size and accumulation of fatty acids; and then culturing the microalgae under conditions that promote accumulation of fatty acids, where the conditions of each of the three culturing steps are different from one another.    TECHNOLOGY FOCUS - PHARMACEUTICALS - Preferred Components: The microalgae is from a genus selected from Thraustochytrium and Schizochytrium (preferably Schizochytrium limacinum SR21). ACTIVITY - Nootropic; Neuroprotective; Ophthalmological. No biological data given.    MECHANISM OF ACTION - None given.    EXAMPLE - An initial culture medium consisting of 40 g/l glycerol, 5 g/l yeast extract and 5 g/l ammonium acetate as the nitrogen source, and other factors in the salt-water broth was used. The seed cells from a smaller culture vessel were inoculated to the fermentor. The temperature was controlled at 30 degrees C and the dissolved oxygen (DO) was controlled at 20-50%. A first stage or cell number increasing stage was carried out which lasted for about 24 hours, in which the cell number increased very quickly with the final cell density of 400-800 million cells/ml. When the cell number had stopped increasing, the second stage began, in which fatty acids were accumulated. The DO was controlled at 3-5% during this stage with the glycerol and nitrogen concentration was controlled at 30-50 g/l and 0.5-1.0 g/l by feeding, respectively. The temperature in this stage was maintained at 30 degrees C and this stage lasted until the 60-80 hours of the whole process and until the dry cell weight had stopped increasing. Then, nitrogen feeding was stopped while glycerol was still fed and controlled at 30 g/l. In the final time period the temperature was decreased to 20-25 degrees C and DO was controlled at about 0.5%, to further accumulate fatty acids. After about 24-40 hours, the dry cell weight started to decrease and the whole process was finished and the cells were harvested. The docosahexaenoic acid (DHA) content in the biomass was about 13-17%, which was further increased by decreasing the temperature and DO. At the end of the whole process, the nitrogen was depleted and low temperature and even low DO further enhanced the DHA content to about 20% of the dry biomass. The final biomass concentration was 137 g/l, and on average the overall conversion rate was 46.2% with average biomass productivity of 1.14 g/l/hour.