초록 ▼

Disclosed is a process for humidifying syngas to achieve a water to carbon monoxide molar ratio in the product syngas within a desired range and in which the molar ratio which can be varied over time in response to changes in downstream syngas requirements. The raw syngas is produced by reacting a c

Disclosed is a process for humidifying syngas to achieve a water to carbon monoxide molar ratio in the product syngas within a desired range and in which the molar ratio which can be varied over time in response to changes in downstream syngas requirements. The raw syngas is produced by reacting a carbonaceous material with oxygen, water, or carbon dioxide and can be combined with a diluent to produce a diluted syngas stream which can be cooled and contacted with liquid water to give a humidified syngas. The H2O:CO molar ratio of the humidified syngas may be adjusted in response to time-varying downstream syngas requirements by changing the amount and/or temperature of the diluent that is combined with the raw syngas stream, by adjusting quench and heat exchange conditions, or a combination thereof. The application of the process to the coproduction of chemicals and power are also disclosed.

대표청구항 ▼

I claim: 1. A process for the coproduction of power and chemicals, comprising: (a) reacting a carbonaceous material with an oxidant stream in a gasifier to produce a raw syngas stream comprising hydrogen, carbon monoxide, and carbon dioxide; (b) combining said raw syngas stream of step (a) with a d

I claim: 1. A process for the coproduction of power and chemicals, comprising: (a) reacting a carbonaceous material with an oxidant stream in a gasifier to produce a raw syngas stream comprising hydrogen, carbon monoxide, and carbon dioxide; (b) combining said raw syngas stream of step (a) with a diluent to produce a diluted syngas stream comprising about 10 to about 60 moles of said diluent per 100 moles of said raw syngas stream; (c) passing said diluted syngas stream of step (b) to a radiant heat exchanger to produce a cooled syngas stream; (d) contacting said cooled syngas stream of step (c) with liquid water to produce a humidified syngas stream; (e) passing said humidified syngas stream to a water-gas shift reactor to produce a shifted syngas stream comprising additional hydrogen and carbon dioxide during a period of off-peak power demand; (f) passing said shifted syngas stream from step (e) to a chemical process to produce a chemical product; and (g) passing said humidified syngas stream from step (d) to a power producing process to produce electricity during a period of peak power demand; wherein the amount of said diluent combined with said raw syngas stream in step(b) is chosen to give an H2O:CO molar ratio of about 1:1 to about 3:1 in said humidified syngas stream of step (d) and said H2:CO molar ratio varies in response to a downstream syngas requirement. 2. The process according to claim 1 wherein said carbonaceous material comprises coal or petroleum coke. 3. The process according to claim 1 wherein said oxidant stream comprises at least 85 volume % oxygen, based on the total volume of said oxidant stream. 4. The process according to claim 3 wherein said oxidant stream comprises at least 95 volume % oxygen. 5. The process according to claim 1 wherein the temperature of said diluent is lower than the temperature of said raw syngas stream. 6. The process according to claim 1 wherein the amount and/or temperature of said diluent in step (b) combined with said raw syngas stream varies in response to a syngas feedstock requirement for said water gas shift reactor, a fuel requirement for said power producing process, or a combination thereof. 7. The process according to claim 1 wherein said H2O:CO molar ratio in step (g) is chosen in response to a syngas feedstock requirement for said water gas shift reactor, a fuel requirement for said power producing process, or a combination thereof. 8. The process according to claim 1 wherein said diluent of step (b) comprises water, methane, ethane, propane, butane, recycled syngas, nitrogen, argon, helium, carbon dioxide, waste gases, combustion stack gases, or combinations thereof. 9. The process according to claim 8 wherein said diluent comprises water. 10. The process according to claim 1 further comprising generating steam in step (c). 11. The process according to claim 10 wherein the pressure of said steam generated in step (c) varies in response to a syngas feedstock requirement for said water gas shift reactor, a fuel requirement for said power producing process, or a combination thereof. 12. The process according to claim 1 wherein said raw syngas in step (a) has a temperature of about 1000 to about 2000�� C. 13. The process according to claim 1 wherein step (d) is carried in a water quench system having influent and effluent flows of water. 14. The process according to claim 13 wherein the amount of said influent and/or effluent flows of water varies in response to a syngas feedstock requirement for said water gas shift reactor, a fuel requirement for said power producing process, or a combination thereof. 15. The process according to claim 1 further comprising generating steam by recovering heat from said water-gas shift reactor. 16. The process according to claim 1 wherein said shifted syngas stream has a molar ratio of hydrogen to carbon monoxide of about 1:1 to about 20:1. 17. The process according to claim 15 wherein said chemical producing process comprises a methanol process. 18. The process according to claim 1 wherein said power producing process comprises a combined cycle system. 19. The process according to claim 1 wherein said chemical product comprises methanol, alkyl formates, dimethyl ether, oxo aldehydes, ammonia, methane, Fischer-Topsch products, or combinations thereof. 20. A process for the coproduction of power and methanol, comprising: (a) reacting coal, petroleum coke, or mixture thereof with an oxidant stream in a gasifier to produce a raw syngas stream comprising hydrogen, carbon monoxide, carbon dioxide, and sulfur containing compounds; (b) combining said raw syngas stream of step (a) with a diluent to produce a diluted syngas stream comprising about 10 to about 60 moles of said diluent per 100 moles of said raw synthesis gas; (c) passing said diluted syngas stream of step (b) to a radiant heat exchanger to produce a cooled syngas stream; (d) contacting said cooled syngas stream of step (c) with liquid water to produce a humidified syngas stream ; (e) passing said humidified syngas stream to a water-gas gas shift reactor to produce a shifted syngas stream having a molar ratio of hydrogen to carbon monoxide of about 1:1 to about 20:1 during a period of off-peak power demand; (f) contacting said shifted syngas stream with a catalyst effective for converting hydrogen and carbon monoxide into methanol; and (g) passing said humidified syngas stream from step (d) to a power producing process to produce electricity during a period of peak power demand; wherein the amount of said diluent combined with said raw syngas stream in step(b) is chosen to satisfy a target H2O:CO molar ratio of about 1:1 to about 3:1 in said humidified syngas stream of step (d) and said H2O:CO molar ratio varies in response to a downstream syngas requirement. 21. The process according to claim 20 wherein said target H2O:CO molar ratio is chosen in response said periods of peak and off peak power demand. 22. The process according to claim 21 further comprising generating steam in step (c) at a pressure chosen to satisfy said target H2O:CO molar ratio. 23. The process according to claim 20 wherein said shifted syngas stream has a molar ratio of hydrogen to carbon monoxide of about 1.5:1 to about 3:1. 24. The process according to claim 20 further comprising removing at least 95 mole percent of the total of said sulfur-containing compounds present in said shifted syngas streams from step (e). 25. The process according to claim 20 further comprising removing a portion of said carbon dioxide from said shifted syngas stream in step (e). 26. The process according to claim 20 wherein up to 100 volume percent of said shifted syngas stream of step (f) is contacted with said catalyst in a fixed bed methanol reactor. 27. The process according to claim 20 wherein up to 100 volume percent of said shifted syngas stream of step (f) is contacted with said catalyst in a liquid slurry phase methanol reactor. 28. The process according to claim 1 in which up to 100 volume percent of said humidified syngas stream in step (e) is passed to said water-gas shift reactor, up to 100 volume percent of said shifted syngas stream in step (f) is passed to said chemical process and, in step (g),up to 100 volume percent of said humidified syngas stream from step (d) is passed to said power producing process. 29. The process according to claim 20 in which up to 100 volume percent of said humidified syngas stream in step (e) is passed to said water-gas shift reactor, up to 100 volume percent of said shifted syngas stream in step (f) is contacted with said catalyst and, in step (g), up to 100 volume percent of said humidified syngas stream from step (d) is passed to said power producing process.