Method for purifying 1-octylene from Fischer-Tropsch synthetic oil products

[0076] Example 1

[0077] This example is based on figure 1 The flow shown is carried out.

[0078] The Fischer-Tropsch synthesis light distillate stream 1 enters the 1# cutting tower with a theoretical plate number of 35, the reflux ratio is 4, and the feeding position is 19 plates (from top to bottom, the same below), from the 1# cutting tower column At the end get logistic 3 as C 8 + (including C 8 ) fraction, the purity reaches 99.95%, and the recovery rate reaches 99.97%;

[0079] the C 8 + The fraction enters the 2# cutting tower with a theoretical plate number of 35, the reflux ratio is 4, and the feed position is 19 plates, and C can be obtained from the top of the tower. 8 component stream 4;

[0080] C 8 The fraction enters an azeotropic distillation column with a theoretical plate number of 20. In the present embodiment, a heterogeneous azeotropic distillation process is selected. Ratio (referring to the mass ratio of ethanol and raw materials in the entrainer) 1.5, normal pressure operation, C 8 The feed position of the fraction is the 14th plate, the feed position of the azeotrope is the 1st plate, and the acid and oxygen-containing compounds are discharged from the bottom of the column because they do not form azeotropes with ethanol and water; C 8 The azeotrope formed by the hydrocarbon and the azeotroping agent is discharged from the top of the tower and cooled to room temperature by the cooler, and then enters the stratifier. Recycle, the oil phase (stream 11) enters the stripping tower with the theoretical plate number of 30, the feed position is the first plate, the normal pressure operation, and the azeotrope phase (stream 12) obtained from the top of the tower is returned to the cooler for further recycle and re-use;

[0081] C from the bottom of the tower 8 The hydrocarbon stream 13 enters an extractive distillation column with a theoretical plate number of 60, and uses NMP with a water mass fraction of 10% and water as binary extractants to conduct C 8 Alkene separation of hydrocarbons, solvent ratio of 5, reflux ratio of 4, C 8 The hydrocarbon feed position is the 40th plate, and the extractant feed position is the 3rd plate, operating at atmospheric pressure, the alkane stream 14 is taken from the top of the column, and the mixed stream 15 of olefin and extractant is taken from the bottom of the column, entering the theoretical plate number Be the solvent recovery tower of 30, reflux ratio is 2, normal pressure operation, feed position is the 9th plate, the extraction agent (stream 17) that obtains from the solvent recovery tower tower bottom returns to the extraction and rectification tower recycle after replenishing, get C from the top of the tower 8 The olefin stream enters the dehydrator to remove residues in C 8 water in the alkene to give C without water 8 The olefin stream 18 enters the precision rectification column with a theoretical plate number of 100, the reflux ratio is 32, and the feeding position is the 55th plate. From the top of the precision rectification column, a 1- Octene product (stream 21).

[0082] The analytical data of main stream in the technique of this embodiment purifying 1-octene are shown in Table 1:

[0083] Table 11-Analysis data of main logistics in octene purification process

[0084]