Aromatization processes using both fresh and regenerated catalysts, and related multi-reactor systems
Multi-reactor systems with aromatization reactor vessels containing a catalyst with low surface area and pore volume, followed in series by aromatization reactor vessels containing a catalyst with high surface area and pore volume, are disclosed. Related reforming methods using the different aromatization catalysts also are described.
1. An aromatization reactor vessel system comprising:
(A) at least one first reactor vessel comprising:
(a1) a first reactor inlet for introducing a first hydrocarbon feed into the at least one first reactor vessel;
(a2) a first aromatization catalyst for catalytically converting at least a portion of the first hydrocarbon feed under first reforming conditions to produce a first aromatic product; wherein the first aromatization catalyst comprises a first transition metal and a first catalyst support, the first aromatization catalyst characterized by:
a first surface area in a range from about 80 m 2 /g to about 150 m 2 /g; and/or
a first micropore volume in a range from about 0.01 cc/g to about 0.048 cc/g; and
(a3) a first reactor outlet for discharging a first effluent comprising the first aromatic product from the at least one first reactor vessel;
(B) at least one second reactor vessel comprising:
(b1) a second reactor inlet for introducing a second hydrocarbon feed into the at least one second reactor vessel;
(b2) a second aromatization catalyst for catalytically converting at least a portion of the second hydrocarbon feed under second reforming conditions to produce a second aromatic product; wherein the second aromatization catalyst comprises a second transition metal and a second catalyst support, the second aromatization catalyst characterized by:
a second surface area in a range from about 160 m 2 /g to about 260 m 2 /g; and/or
a second micropore volume in a range from about 0.05 cc/g to about 0.09 cc/g; and
(b3) a second reactor outlet for discharging a second effluent comprising the second aromatic product from the at least one second reactor vessel; and
(C) a furnace positioned between the first reactor outlet and the second reactor inlet, the furnace capable of heating the first effluent to form the second hydrocarbon feed.
2. The system of claim 1 , wherein the at least one first reactor vessel and the at least one second reactor vessel are radial flow reactors.
3. The system of claim 1 , wherein the system comprises:
from 1 to 3 first reactor vessels in series; and
from 2 to 6 second reactor vessels in series.
4. The system of claim 1 , wherein a weight ratio of the first aromatization catalyst to the second aromatization catalyst in the reactor vessel system is in a range from about 1:5 to about 1:15.
5. The system of claim 1 , wherein the furnace is configured to heat the first effluent to a temperature in a range from about 350° C. to about 600° C.
6. The system of claim 1 , wherein:
the first aromatization catalyst has a lower catalyst activity than that of the second aromatization catalyst;
the first aromatization catalyst has a catalyst selectivity that is substantially the same as or better than that of the second aromatization catalyst;
the first transition metal and the second transition metal comprise platinum;
the first catalyst support and the second catalyst support comprise a KL-zeolite and a binder comprising alumina, silica, a mixed oxide thereof, or a mixture thereof; and
the first aromatization catalyst and the second aromatization catalyst further comprise chlorine and fluorine.
7. The system of claim 1 , wherein the first aromatization catalyst contains more carbon, more sulfur, and more iron than that of the second aromatization catalyst.
8. The system of claim 1 , wherein the first aromatization catalyst has a lower platinum dispersion than that of the second aromatization catalyst.
9. The system of claim 1 , wherein:
the first surface area is in a range from about 85 m 2 /g to about 140 m 2 /g;
the first micropore volume is in a range from about 0.02 cc/g to about 0.04 cc/g;
the second surface area is in a range from about 160 m 2 /g to about 220 m 2 /g; and
the second micropore volume is in a range from about 0.055 cc/g to about 0.09 cc/g.
10. The system of claim 1 , wherein:
the first aromatization catalyst comprises platinum and is a regenerated catalyst;
the second aromatization catalyst comprises platinum;
the first aromatization catalyst has a lower platinum dispersion than that of the second aromatization catalyst;
the first aromatization catalyst and the second aromatization catalyst further comprise chlorine and fluorine;
the first catalyst support and the second catalyst support comprise a KL-zeolite and a binder comprising alumina, silica, a mixed oxide thereof, or a mixture thereof; and
the first aromatization catalyst has an aromatics selectivity that is substantially the same as or better than that of the second aromatization catalyst.
11. The system of claim 10 , wherein:
the first surface area is in a range from about 85 m 2 /g to about 140 m 2 /g;
the first micropore volume is in a range from about 0.015 cc/g to about 0.045 cc/g;
the second surface area is in a range from about 165 m 2 /g to about 240 m 2 /g; and
the second micropore volume is in a range from about 0.05 cc/g to about 0.085 cc/g.
12. The system of claim 10 , wherein a weight ratio of the first aromatization catalyst to the second aromatization catalyst is in a range from about 1:2 to about 1:20.
13. The system of claim 10 , wherein the first aromatization catalyst contains more carbon, more sulfur, and/or more iron than that of the second aromatization catalyst.
14. The system of claim 10 , wherein the first aromatization catalyst has from 10% to 30% lower platinum dispersion than that of the second aromatization catalyst.
15. The system of claim 10 , wherein:
the first aromatization catalyst is characterized by a platinum dispersion in a range from about 30% to about 50%; and
the second aromatization catalyst is characterized by a platinum dispersion in a range from about 60% to about 75%.
16. The system of claim 10 , wherein:
the first aromatization catalyst has a lower catalyst activity than that of the second aromatization catalyst; and/or
the first aromatization catalyst has a benzene+toluene selectivity that is substantially the same as or better than that of the second aromatization catalyst.
17. The system of claim 10 , wherein the first aromatization catalyst and the second aromatization catalyst, independently, comprise from about 0.3 wt. % to about 5 wt. % of platinum.
18. The system of claim 17 , wherein:
the first aromatic product and the second aromatic product, independently, comprise benzene, toluene, or a combination thereof; and
the first reforming conditions and the second reforming conditions, independently, comprise a reforming temperature in a range from about 350° C. to about 600° C.
19. The system of claim 17 , wherein:
the first surface area is in a range from about 85 m 2 /g to about 140 m 2 /g;
the first micropore volume is in a range from about 0.02 cc/g to about 0.04 cc/g;
the second surface area is in a range from about 160 m 2 /g to about 220 m 2 /g; and
the second micropore volume is in a range from about 0.055 cc/g to about 0.09 cc/g.
20. The system of claim 19 , wherein the system comprises:
from 1 to 3 first reactor vessels in series; and
from 2 to 6 second reactor vessels in series.
21. The system of claim 19 , wherein:
the at least one first reactor vessel and the at least one second reactor vessel are radial flow reactors;
a weight ratio of the first aromatization catalyst to the second aromatization catalyst in the reactor vessel system is in a range from about 1:5 to about 1:15; and
the furnace is configured to heat the first effluent to a temperature in a range from about 350° C. to about 600° C.