Slurry bubble reactor operated in well-mixed gas flow regime
View Patent ↗A gas-agitated multiphase reactor system for the synthesis of hydrocarbons gives high catalyst productivity and reactor capacity. The system includes operating a multi-phase reactor in the well-mixed gas flow regime, with a Peclet number less than 0.175 and a single pass conversion ranging from 35% to 75%, wherein the inlet superficial gas velocity decreases with the decreasing of the reactor aspect ratio, and is preferably at least 20 cm/sec.
1. A method for producing hydrocarbons from syngas in a three-phase catalytic system in which the catalyst comprises solid particles, comprising:
(a) providing a reactor containing the catalyst;
(b) feeding the syngas into the reactor so as to generate a liquid product;
(c) operating the three-phase system in a well-mixed gas flow regime, with a gas Peclet number less than 0.175; and
(d) removing hydrocarbons from the reactor.
2. The method according to claim 1 wherein the inlet superficial gas velocity is at least 20 cm/sec.
3. The method according to claim 1 wherein the reactor includes a recycle line.
4. The method according to claim 1 wherein the process comprises multiple stages and in which each stage may have one or more reactors, and wherein the inlet gas superficial velocity is at least 20 cm/sec and syngas per pass conversion in each reactor is between 35% and 75%.
5. The method according to claim 4 wherein the overall syngas conversion is at least 90%.
6. The method according to claim 1 wherein the mole ratio of hydrogen to carbon monoxide in the syngas is between about 0.67:1 and about 2.5:1.
7. The method according to claim 1 wherein the hydrocarbons in step (d) comprise C 1 to C 80+ hydrocarbons.
8. The method according to claim 1 wherein the catalyst comprises a supported or precipitated cobalt catalyst.
9. A method for operating a Fischer-Tropsch reactor system containing solid catalyst, gaseous feed, and gas and liquid products, comprising maintaining the rates of gaseous feed and liquid withdrawal such that the reactor system is maintained in a well-mixed gas flow regime described by
U G ≦0.175 D G /L,
where U G is the inlet superficial gas velocity, L is the expanded slurry bed height, and D G is the dispersion coefficient.
10. The method according to claim 9 wherein the inlet superficial gas velocity is at least 20 cm/sec.
11. The method according to claim 9 wherein the expanded slurry bed height is at least 60% of the total reactor height.
12. The method according to claim 9 wherein the process comprises multiple stages and in which each stage may have one or more reactors, and wherein the inlet gas superficial velocity is at least 20 cm/sec and syngas per pass conversion in each reactor is between 35% and 75%.
13. The method according to claim 12 wherein the overall syngas conversion is at least 90%.
14. The method according to claim 9 wherein the mole ratio of hydrogen to carbon monoxide in the syngas is greater than 0.5:1.
15. The method according to claim 9 wherein the mole ratio of hydrogen to carbon monoxide in the syngas is between about 0.67:1 and about 2.5:1.
16. The method according to claim 9 wherein the Fischer-Tropsch reactor system produces hydrocarbons comprising C 1 to C 80+ hydrocarbons.
17. The method according to claim 9 wherein the catalyst comprises a supported or precipitated cobalt catalyst.
18. The method according to claim 1 wherein the volume productivity of the catalytic system is at least 350 gHC/kg.cat/hr.
19. The method according to claim 9 wherein the volume productivity of the catalytic system is at least 350 gHC/kg.cat/hr.