ZEOLITE WITH IMPROVED HYDRO-ISOMERIZATION ACTIVITY
According to an aspect of the present invention, provided is a zeolite catalyst having an MRE structure for hydro-isomerization. The zeolite catalyst has an adsorption volume ratio of lutidine to collidine measured by Fourier-transform infrared spectroscopy (FTIR) using lutidine and collidine as adsorbents of greater than 3 and less than or equal to 10. According to an aspect of the present invention, provided is a method of hydro-isomerization for a hydrocarbon feedstock, including subjecting the hydrocarbon feedstock to a hydro-isomerization reaction under conditions of a temperature of 200° C. to 500° C., a hydrogen pressure of 1 to 200 atmospheres, a liquid space velocity (LHSV) of 1.0 to 10.0 hr −1 , and the hydrogen/feedstock ratio of 45 to 1780 Nm 3 /m 3 in the presence of the zeolite catalyst.
1 . A zeolite catalyst having an MRE structure for a hydro-isomerization reaction, wherein an adsorption volume ratio of lutidine to collidine greater than 3 and less than or equal to 10, as measured by Fourier-transform infrared spectroscopy (FTIR) using lutidine and collidine as adsorbents, and wherein the zeolite catalyst has a total volume of pores having a diameter in a range of 2 to 50 nm of less than 0.2 cc/g.
2 . The zeolite catalyst of claim 1 , wherein the zeolite catalyst having an MRE structure is any one of EU2, ZSM-48, or ZBM-30 zeolite.
3 . The zeolite catalyst of claim 1 , wherein an adsorption volume ratio of lutidine to collidine is greater than or equal to 8 measured by FTIR using lutidine and collidine as adsorbents.
4 . The zeolite catalyst of claim 1 , wherein the zeolite catalyst has silica-alumina ratio (SAR) of 100 to 250.
5 . The zeolite catalyst of claim 4 , wherein the zeolite catalyst has silica-alumina ratio (SAR) of 120 to 200.
6 . The zeolite catalyst of claim 4 , wherein the zeolite catalyst has silica-alumina ratio (SAR) of 150 to 170.
7 . The zeolite catalyst of claim 1 , wherein the zeolite catalyst has a total volume of pores having a diameter in a range of greater than 50 nm of less than 0.1 cc/g.
8 . The zeolite catalyst of claim 1 , wherein the zeolite catalyst has a morphology selected from the group consisting of a granular shape, a needle shape, and a rod shape.
9 . The zeolite catalyst of claim 8 , wherein the zeolite catalyst has a granular shape.
10 . The zeolite catalyst of claim 1 , wherein the zeolite catalyst has a BET surface area greater than or equal to 250 m 2 /g and not greater than 300 m 2 /g.
11 . A method of hydro-isomerization for a hydrocarbon feedstock, the method comprising:
subjecting the hydrocarbon feedstock to a hydro-isomerization reaction under conditions of a temperature of 200° C. to 500° C., a hydrogen pressure of 1 to 200 atmospheres, a liquid space velocity (LHSV) of 1.0 to 10.0 hr −1 , and a hydrogen/feedstock ratio of 45 to 1780 Nm 3 /m 3 in the presence of the zeolite catalyst of claim 1 .
12 . The method of claim 11 , wherein at least some of the hydrocarbons in the feedstock have a number of carbon atoms of at least 22.
13 . A method of hydro-isomerization of a hydrocarbon feedstock, the method comprising:
providing a zeolite catalyst having an adsorption volume ratio of lutidine to collidine greater than 3 and less than or equal to 10,
and
subjecting the hydrocarbon feedstock to a hydro-isomerization reaction in the presence of the selected zeolite catalyst.