Study On The Optimization Of Process To Produce Heat Transfer Oil For A Lubricating Plant

Group ? base oils of lubricating oils are prepared by a combination process(“old process of lubricant”and hydrogenation process).The main production processes are atmospheric and vacuum distillation(or solvent deasphalting),solvent refining,solvent dewaxing,hydrogenation and white clay refining.Therefore,the group II base oil has less impurities(aromatic content less than 10%),high saturated hydrocarbon content,good thermal stability and oxidation resistance.As a medium for conducting heat,heat transfer oil has a very good heat transfer effect.The mineral-type heat transfer oil produced by the existing"hydrogenation process"in China has low working temperature,poor thermal oxidation stability and short service life.This study used the existing lubricant base oil production units to carry out the trial production process of the heat transfer oil.Due to the difference in performance requirements between the heat transfer oil and the lube base oil,each production unit needs to undergo certain process adjustments when converting from the production of the lubricating oil to the production of the heat transfer oil.The original lubricating oil production process is VGO 3#through furfural refining,hydrofining,ketone-benzene dewaxing and white clay refining.Compared with the base oil,the heat transfer oil requires a low viscosity,a high viscosity index,high opening flash point and good the oxidation stability.The operation parameters of produced heat transfer oil process were adjusted.The top temperature of the extraction tower is 109?,the bottom temperature is 74?,and the ratio of solvent to oil is 1.7:1 for the furfural device sets.The hydrogenation unit the hydrotreating reaction temperature is 369?,hydrofining reaction temperature is 283?,the bottom temperature of the vacuum tower is 235?,the side line distillation temperature of the vacuum diesel side line and the light lubricant side line is 165? and 202? respectively,the steam stripping amount of the vacuum tower is 580 kg/h.The ketone benzene dewaxing unit is set to the ammonia amount of 47%valve position,the ratio of ketone to 70/30,the proportion of ammonia entering the three sets of casing crystallizers is 2.5:3.5:4.The amount of white clay added to the clay plant is 0.8 m%,the contact temperature is 202°C,and the contact time is 28 min.The heat transfer oil of obtained final product has a viscosity(40?)of 27.99 mm~2/s,a pour point of-22?,a residual carbon of 0.03%,an acid value of 0.003 mg KOH/g,an opening flash point of 222?,and oxidation stability(rotary oxygen bomb experiment 150?)389 min.It conforms to GB 23971-2009"Organic Heat Carrier"standard and is at the leading level in China.The original production device is utilized,the investment,the energy consumption,and the operation cost is low,no waste liquid discharge,operation stable and so on.