The denitrification effect of processing reduced third-line oil reduces the nitrogen removal effect of the three-line oil. Under the condition of the agent to oil ratio of 1B390, the denitrification rate averages about 44%, and the total denitrification rate after refined by the white clay reaches about 71%; due to the base oil finished product tank The maximum value of the rotary oxygen bomb is only 10 minutes higher than the control index, so it can be considered that under the conditions of raw alkali nitrogen, the ratio of 1B390 to oil and gas is close to the minimum of the nitrogen removal agent. Effects of different feedstock oils on the effect of denitrification The effect of feedstock oils with different viscosity on the effect of denitrification at the same oil ratio. With the increase of raw materials and the increase of viscosity, the effect of denitrification decreases, while the increase of the value of denitrified oleic acid indicates that the denitrogenation tailings of refinery tanks have a poor settling effect. The effect of denitrification refining temperature on the denitrification effect, with the increase of refining temperature, the denitrification effect has a tendency to decrease. The recommended temperature for the denitrification agent is 7080e. According to the frontal furfural device, the processing load is as high as 160%, and the cooling temperature before entering the denitrification system can be controlled at 8085e. Too lower the temperature to increase the cooling load of furfural refined oil and increase the consumption of cooling water, while the denitrification effect does not increase significantly. There is no obvious difference in the quality of the base oil produced by the two processes, and both meet the requirements of the professional oil standards for base oils. At present, there is a problem that the denitrification system has a large acid value after denitrification, that is, the denitrification agent does not have a satisfactory degree of sedimentation after the reaction, resulting in denitrification of the refined oil with slag, and the acid value increases with the denitrification of the feedstock oil. One of the reasons for the analysis may be that the mixing and dispersing degree of the static mixer is too large, the droplet size after the denitrogenation agent is dispersed is too small, and the coalescence is difficult to grow. The second possibility is that the design of the electrorefinery sedimentation tank has defects, resulting in Some of the denitrification agent after the reaction could not settle down and be brought into the refined oil.