Method and manufacturing apparatus for manufacturing aviation fuel from waste plastic pyrolysis oil

Abstract

The present disclosure provides a method for producing aviation fuel, the method including: a first step of subjecting waste plastic pyrolysis oil to an olefin migration reaction; a second step of subjecting a product obtained in the first step to an olefin branching reaction; a third step of hydrotreating a product obtained in the second step in the presence of a hydrotreating catalyst; and a fourth step of hydrocracking a product obtained in the third step in the presence of a hydrocracking catalyst.

1 . A method for producing aviation fuel, the method comprising:
 a first operation of subjecting waste plastic pyrolysis oil to an olefin migration reaction;   a second operation of subjecting a product obtained in the first operation to an olefin branching reaction;   a third operation of hydrotreating a product obtained in the second operation in the presence of a hydrotreating catalyst; and   a fourth opertion of hydrocracking a product obtained in the third operation in the presence of a hydrocracking catalyst.   
     
     
         2 . The method of  claim 1 , wherein the first operation is performed in the presence of a weak acid site catalyst, and the second operation is performed in the presence of a catalyst of zeolite having a one-dimensional pore structure. 
     
     
         3 . The method of  claim 2 , wherein the weak acid site catalyst includes a titanium oxide catalyst. 
     
     
         4 . The method of  claim 2 , wherein a weight ratio of the weak acid site catalyst to the catalyst of zeolite having a one-dimensional pore structure is 60:40 to 90:10. 
     
     
         5 . The method of  claim 1 , wherein the hydrotreating catalyst in the third operation is a catalyst in which an active metal including one or two or more selected from molybdenum, nickel, cobalt, and tungsten is supported on a support. 
     
     
         6 . The method of  claim 1 , wherein the hydrocracking catalyst in the fourth operation is a catalyst in which an active metal including one or two or more selected from molybdenum, nickel, cobalt, and tungsten is supported on zeolite. 
     
     
         7 . The method of  claim 1 , wherein the produced aviation fuel has a freezing point of −45° C. or lower and a yield of 75% or more. 
     
     
         8 . The method of  claim 1 , wherein the produced aviation fuel has a chlorine content of 10 ppm or less and a nitrogen content of 10 ppm or less. 
     
     
         9 . The method of  claim 1 , wherein the first operation and the second operation are performed at a reaction temperature of higher than 300° C. 
     
     
         10 . The method of  claim 1 , wherein the first operation and the second operation are performed under conditions of a reaction pressure of 5 to 70 bar and a gas/oil ratio (GOR) of 100 to 3,000 in an inert atmosphere. 
     
     
         11 . The method of  claim 1 , wherein the third operation is performed under conditions of a reaction temperature of lower than 300° C., a reaction pressure of 100 bar or less, and a gas/oil ratio (GOR) of 100 to 3,000 in hydrogen gas. 
     
     
         12 . The method of  claim 1 , wherein the fourth operation is performed under conditions of a reaction temperature of higher than 300° C., a reaction pressure of 100 bar or less, and a gas/oil ratio (GOR) of 100 to 3,000 in hydrogen gas. 
     
     
         13 . The method of  claim 1 , further comprising a fifth operation of hydrofinishing a product obtained in the fourth operation under conditions of a reaction temperature of higher than 300° C., a reaction pressure of 100 bar or less, and a gas/oil ratio (GOR) of 100 to 3,000 in the presence of a hydrofinishing catalyst. 
     
     
         14 . An apparatus for producing aviation fuel, the apparatus comprising:
 a first reactor into which waste plastic pyrolysis oil is introduced and in which an olefin migration reaction and an olefin branching reaction are sequentially performed;   a second reactor into which a reaction product and hydrogen gas are introduced from the first reactor and in which hydrotreating is performed in the presence of a hydrotreating catalyst; and   a third reactor into which a reaction product and hydrogen gas are introduced from the second reactor and in which hydrocracking is performed in the presence of a hydrocracking catalyst.   
     
     
         15 . The apparatus of  claim 14 , wherein the first reactor includes a first zone filled with a weak acid site catalyst, and a second zone filled with a catalyst of zeolite having a one-dimensional pore structure, and the waste plastic pyrolysis oil is refined by sequentially passing through the first zone and the second zone. 
     
     
         16 . The apparatus of  claim 14 , wherein the first reactor to the third reactor are fixed bed reactors. 
     
     
         17 . The apparatus of  claim 14 , further comprising a fourth reactor into which a reaction product and hydrogen gas are introduced from the third reactor and in which hydrofinishing is performed in the presence of a hydrofinishing catalyst.