Hydroprocessing of heavy hydrocarbon feeds in liquid-full reactors
A process to treat a heavy hydrocarbon feed in a liquid-full hydroprocessing reactor is disclosed. The heavy feed has a high asphaltenes content, high viscosity, high density and high end boiling point. Hydrogen is fed in an equivalent amount of at least 160 liters of hydrogen, per liter of feed, l/l (900 scf/bbl). The feed is contacted with hydrogen and a diluent, which comprises, consists essentially of, or consists of recycle product stream. The hydroprocessed product has increased value for refineries, such as a feed for an fluid catalytic cracking (FCC) unit.
1. A process to treat a heavy hydrocarbon feed comprising:
(a) contacting the 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;
(b) contacting the feed/diluent/hydrogen mixture with a catalyst, in a liquid-full fixed bed reactor of plug flow or tubular design, to produce a product mixture; and
(c) recycling a portion of the product mixture as a recycle product stream by combining the recycle product stream with the feed to provide at least a portion of the diluent in step (a) at a recycle ratio in a range of from about 1 to about 10;
wherein the feed has an asphaltene content of at least 3%, based on the total weight of the feed; wherein hydrogen is fed in an equivalent amount of at least 160 l/l (900 scf/bbl); wherein the diluent comprises, consists essentially of, or consists of recycled product stream; and wherein the asphaltene content of the product mixture is reduced by more than an order of magnitude as compared to the feed.
2. The process of claim 1 wherein hydrogen is fed in an equivalent amount of 180-530l/l (1000-3000 scf/bbl).
3. The process of claim 2 wherein hydrogen is fed in an equivalent amount of 360-530l/l (2000-3000 scf/bbl).
4. The process of claim 1 wherein the feed is first contacted with the diluent to produce a feed/diluent mixture and then the feed/diluent mixture is contacted with hydrogen to provide the feed/diluent/hydrogen mixture.
5. The process of claim 1 wherein the heavy hydrocarbon feed has a viscosity of at least 5 cP, a density of at least 900 kg/m 3 at a temperature of 50° C. (120° F.), an end boiling point in the range of from about 450° C. (840° F.) to about 700° C. (1300° F.), and a Conradson carbon content in the range of from about 0.25% to about 8.0% by weight.
6. The process of claim 1 wherein the heavy hydrocarbon feed is selected from the group consisting of clarified slurry oil, bitumen, coker product, coal liquefied oil, product from heavy oil thermal cracking process, product from heavy oil hydrotreating and/or hydrocracking, straight run cut from a crude oil unit, and mixtures of two or more thereof.
7. The process of claim 5 wherein the heavy hydrocarbon feed is bitumen extracted from oil sands.
8. The process of claim 1 wherein the catalyst is a hydroprocessing catalyst comprising a metal selected from the group consisting of nickel and cobalt, and combinations thereof, and the catalyst is supported on a mono- or mixed-metal oxide, a zeolite, or a combination of two or more thereof.
9. The process of claim 8 wherein the metal is a combination of metals selected from the group consisting of nickel-molybdenum (NiMo), cobalt-molybdenum (CoMo), nickel-tungsten (NiW) and cobalt-tungsten (CoW).
10. The process of claim 9 wherein the mono- or mixed-metal oxide is alumina, silica, titania, zirconia, kieselguhr, silica-alumina or a combination of two or more thereof.
11. The process of claim 1 further comprising, prior to step (a), sulfiding the catalyst by contacting the catalyst with a sulfur-containing compound at an elevated temperature.
12. The process of claim 1 wherein the recycle ratio is 1 to 5.
13. The process of claim 1 wherein the diluent consists or consists essentially of the recycle product stream.
14. The process of claim 1 wherein the diluent comprises an organic liquid selected from the group consisting of light hydrocarbons, light distillates, naphtha, diesel and combinations of two or more thereof.
15. The process of claim 1 wherein the fixed bed reactor is a single packed bed reactor.
16. The process of claim 1 wherein the fixed bed reactor is two or more (multiple) packed beds in series or in parallel or in a combination thereof.
17. The process of claim 16 wherein fresh hydrogen is added at the inlet of each reactor bed.
18. The process of claim 1 wherein temperature ranges from about 250° C. to about 450° C.; pressure ranges from 3.45 to 17.25 MPa (500 to 2500 psig), and hydrocarbon feed (LHSV) ranges from 0.1 to 10 hr −1 .
19. The process of claim 18 wherein temperature ranges from about 300° C. to 400° C.; pressure ranges from 6.9 to 13.9 MPa (1000 to 2000 psig).
20. The process of claim 1 wherein the asphaltene content of the product mixture is about 0.1-1%.
21. The process of claim 1 wherein the product mixture has a viscosity of about 1-5 cP, a density of from about 900 to about 1075 kg/m 3 , a API gravity of from about 25 to about 0, a boiling point range from about 150° C. to about 600° C., and a Conradson carbon (MCR) of from about 0.1% to about 3%.
22. The process of claim 1 wherein the catalyst is a hydroprocessing catalyst comprising one or more non-precious metals.