초록 ▼

A gas-agitated multiphase reactor system with multiple reaction zones comprising gas-liquid or gas-liquid-solid mixtures that can maximize the production rate while allowing better control of the temperature distribution and better control of the liquid and solid phases in the reactors. Still more p

A gas-agitated multiphase reactor system with multiple reaction zones comprising gas-liquid or gas-liquid-solid mixtures that can maximize the production rate while allowing better control of the temperature distribution and better control of the liquid and solid phases in the reactors. Still more particularly, this invention relates to a method for operating a pair of linked gas-agitated slurry reaction zones such that the hydrodynamic behavior and reactor performance of such reactor system are improved compared to that of a conventional slurry bed reactor.

대표청구항 ▼

1. A method for producing hydrocarbonaceous products from synthesis gas in a multiphase catalytic system, comprising:(a) providing a reactor system comprising separate first and second reaction zones, each reaction zone comprising a liquid phase and a solid phase containing a catalyst, the first and

1. A method for producing hydrocarbonaceous products from synthesis gas in a multiphase catalytic system, comprising:(a) providing a reactor system comprising separate first and second reaction zones, each reaction zone comprising a liquid phase and a solid phase containing a catalyst, the first and second reaction zones being in fluid communication with each other via a lower fluid flow passage and an upper fluid flow passage, said each flow passage having an inlet and an outlet;(b) feeding a first gas comprising H 2 and CO into the bottom of said first reaction zone and a second gas comprising H 2 and CO into the bottom of second reaction zone such that the superficial gas velocity in the first reaction zone is greater than the superficial gas velocity in the second reaction zone and a pressure differential exists across at least said lower fluid flow passage; and(c) creating a liquid circulation from the first reaction zone through the upper fluid flow passage to the second reaction zone and from the second reaction zone through the lower fluid flow passage to the first reaction zone by said pressure differential; and(d) controlling the liquid circulation to achieve a desired liquid circulation velocity. 2. The method according to claim 1 wherein the superficial gas velocity in the first reaction zone is between 17 and 60 cm/sec. 3. The method according to claim 1 wherein the superficial gas velocity in the first reaction zone is between 2 cm/s and 45 cm/s greater than the superficial gas velocity in the second reaction zone. 4. The method according to claim 3 wherein the superficial gas velocity in the second reaction zone is between 15 and 58 cm/s. 5. The method according to claim 1 wherein step (d) comprises adjusting the difference in superficial gas velocities between the two reaction zones. 6. The method according to claim 1 wherein step (d) comprises using a valve in at least one of said fluid flow passages. 7. The method according to claim 1 wherein step (d) results in a slurry circulation velocity between 0.5 and 20 cm/s. 8. The method according to claim 1 wherein step (d) includes selecting the gas superficial velocities for the first and second reaction zones such that slurry flows up through the first reaction zone, into the second reaction zone through the upper fluid flow passage, down through the second reaction zone and into the first reaction zone via the lower fluid passage. 9. The method according to claim 1, further including maintaining fluid circulation between the first and second reaction zones substantially continuously during operation. 10. The method according to claim 1 wherein circulation between the first and second reaction zones is intermittent. 11. The method according to claim 1 wherein the first gas and the second gas have the same molar ratio of hydrogen to carbon monoxide. 12. The method according to claim 1 wherein the first gas and the second gas have different molar ratios of hydrogen to carbon monoxide. 13. The method according to claim 1 wherein the reactor system contains a Fischer-Tropsch catalyst. 14. The method according to claim 1, further including removing water from the reactor system. 15. The method according to claim 1, further including converting a portion of said first and second gases to hydrocarbonaceous products. 16. The method according to claim 15, further including removing hydrocarbonaceous products from the reactor system.