Liquid-full hydrotreating and selective ring opening processes
This disclosure relates to liquid-full processes for hydroprocessing a light cycle oil (LCO). The processes involve hydrotreatment followed by selective ring opening in the presence of hydrotreating catalyst and selective ring opening catalyst respectively. The selective ring opening catalyst can be either zeolite ring opening catalyst or amorphous ring opening catalyst. In aspects of zeolite ring opening catalyst, the volume ratio of the total amount of the zeolite ring opening catalyst to the total amount of the hydrotreating catalyst is from about 0.2 to about 1.5. In aspects of amorphous ring opening catalyst, the volume ratio of the total amount of the amorphous ring opening catalyst to the total amount of the hydrotreating catalyst is from about 0.2 to about 3.
1. A liquid-full process for hydroprocessing a hydrocarbon feed, comprising:
(a) contacting the hydrocarbon feed with (i) a diluent and (ii) hydrogen, to produce feed/diluent/hydrogen mixture, wherein the hydrogen is dissolved in the mixture to provide a liquid feed, and wherein the hydrocarbon feed is a light cycle oil (LCO) having a polyaromatic content greater than 25% by weight, a nitrogen content greater than 300 parts per million by weight (wppm), and a density greater than 890 kg/m 3 at 15.6° C.;
(b) contacting the feed/diluent/hydrogen mixture with a first catalyst in a first liquid-full reaction zone, to produce a first product effluent;
(c) contacting the first product effluent with a second catalyst in a second liquid-full reaction zone, to produce a second product effluent; and
(d) recycling a portion of the second product effluent as a recycle product stream for use in the diluent in step (a)(i) at a recycle ratio of from about 1 to about 10;
wherein the first catalyst is a hydrotreating catalyst and the second catalyst is a zeolite ring opening catalyst, the total amount of hydrogen fed to the process is greater than 100 normal liters of hydrogen per liter of the hydrocarbon feed, and the volume ratio of the total amount of the second catalyst to the total amount of the first catalyst is from about 0.2 to about 1.5; and
wherein the recycled portion of the second product effluent is recycled without separating ammonia, hydrogen sulfide, and remaining hydrogen from the second product effluent.
2. The liquid-full process of claim 1 , wherein the volume ratio of the total amount of the second catalyst to the total amount of the first catalyst is from about 0.2 to about 1.2.
3. The liquid-full process of claim 1 , wherein the volume ratio of the total amount of the second catalyst to the total amount of the first catalyst is from about 0.2 to 0.95.
4. The liquid-full process of claim 1 , wherein the volume ratio of the total amount of the second catalyst to the total amount of the first catalyst is from about 0.7 to 0.95.
5. The liquid-full process of claim 4 , wherein naphtha yield of the process is no more than about 6 wt %, and the density of diesel product is reduced by at least about 70 kg/m 3 at 15.6° C. compared with the density of the hydrocarbon feed.
6. The liquid-full process of claim 4 , wherein diesel product cetane increase is at least about 11.
7. The liquid-full process of claim 1 , wherein the first product effluent is contacted with the second catalyst without prior separation of ammonia, hydrogen sulfide, and remaining hydrogen from the first product effluent.
8. The liquid-full process of claim 1 , wherein the first product effluent produced in step (b) has a nitrogen content no more than about 10 wppm.
9. The liquid-full process of claim 1 , wherein the first product effluent produced in step (b) has a nitrogen content no more than about 2 wppm.
10. The liquid-full process of claim 1 , wherein the zeolite ring opening catalyst comprises nickel-tungsten (NiW) loaded on a zeolite support.
11. A liquid-full process for hydroprocessing a hydrocarbon feed, comprising:
(a) contacting the hydrocarbon feed with (i) a diluent and (ii) hydrogen, to produce a feed/diluent/hydrogen mixture, wherein the hydrogen is dissolved in the mixture to provide a liquid feed, and wherein the hydrocarbon feed is a light cycle oil (LCO) having a polyaromatic content greater than 25% by weight, a nitrogen content greater than 300 parts per million by weight (wppm), and a density greater than 890 kg/m 3 at 15.6° C.;
(b) contacting the feed/diluent/hydrogen mixture with a first catalyst in a first liquid-full reaction zone, to produce a first product effluent;
(c) contacting the first product effluent with a second catalyst in a second liquid-full reaction zone, to produce a second product effluent; and
(d) recycling a portion of the second product effluent as a recycle product stream for use in the diluent in step (a)(i) at a recycle ratio of from about 1 to about 10;
wherein the first catalyst is a hydrotreating catalyst and the second catalyst is an amorphous ring opening catalyst, the total amount of hydrogen fed to the process is greater than 100 normal liters of hydrogen per liter of the hydrocarbon feed, and the volume ratio of the total amount of the second catalyst to the total amount of the first catalyst is from about 0.2 to about 3.0; and
wherein the recycled portion of the second product effluent is recycled without separating ammonia, hydrogen sulfide, and remaining hydrogen from the second product effluent.
12. The liquid-full process of claim 11 , wherein the volume ratio of the total amount of the second catalyst to the total amount of the first catalyst is from about 0.6 to about 2.0.
13. The liquid-full process of claim 11 , wherein the volume ratio of the total amount of the second catalyst to the total amount of the first catalyst is from about 0.8 to about 1.4.
14. The liquid-full process of claim 13 , wherein naphtha yield of the process is no more than about 10 wt %, and the density of diesel product is reduced by at least about 70 kg/m 3 at 15.6° C. compared with the density of the hydrocarbon feed.
15. The liquid-full process of claim 13 , wherein diesel product cetane increase is at least about 10.
16. The liquid-full process of claim 11 , wherein the first product effluent produced in step (b) has a nitrogen content no more than about 100 wppm.
17. The liquid-full process of claim 11 , wherein the first product effluent is contacted with the second catalyst without prior separation of ammonia, hydrogen sulfide, and remaining hydrogen from the first product effluent.
18. The liquid-full process of claim 11 , wherein the amorphous ring opening catalyst comprises nickel-tungsten (NiW) loaded on an amorphous support.
19. A liquid-full process for hydroprocessing a hydrocarbon feed, comprising:
(a) contacting the hydrocarbon feed with (i) a diluent and (ii) hydrogen, to produce a feed/diluent/hydrogen mixture, wherein the hydrogen is dissolved in the mixture to provide a liquid feed, and wherein the hydrocarbon feed is a light cycle oil (LCO) having a polyaromatic content greater than 25% by weight, a nitrogen content greater than 300 parts per million by weight (wppm), and a density greater than 890 kg/m 3 at 15.6° C.;
(b) contacting the feed/diluent/hydrogen mixture with a first catalyst in a first liquid-full reaction zone, to produce a first product effluent;
(c) contacting the first product effluent with a second catalyst in a second liquid-full reaction zone, to produce a second product effluent; and
(d) recycling a portion of the second product effluent as a recycle product stream for use in the diluent in step (a)(i) at a recycle ratio of from about 1 to about 10;
wherein the first catalyst is a hydrotreating catalyst and the second catalyst is a zeolite ring opening catalyst, the total amount of hydrogen fed to the process is greater than 100 normal liters of hydrogen per liter of the hydrocarbon feed, and the volume ratio of the total amount of the second catalyst to the total amount of the first catalyst is from about 0.2 to 0.95.
20. The liquid-full process of claim 19 , wherein the volume ratio of the total amount of the second catalyst to the total amount of the first catalyst is from about 0.7 to 0.95.
21. The liquid-full process of claim 20 , wherein naphtha yield of the process is no more than about 6 wt %, and the density of diesel product is reduced by at least about 70 kg/m 3 at 15.6° C. compared with the density of the hydrocarbon feed.
22. The liquid-full process of claim 20 , wherein diesel product cetane increase is at least about 11.
23. The liquid-full process of claim 19 , wherein the first product effluent is contacted with the second catalyst without prior separation of ammonia, hydrogen sulfide, and remaining hydrogen from the first product effluent.
24. The liquid-full process of claim 19 , wherein the first product effluent produced in step (b) has a nitrogen content no more than about 10 wppm.
25. The liquid-full process of claim 19 , wherein the zeolite ring opening catalyst comprises nickel-tungsten (NiW) loaded on a zeolite support.