Claims
- 1. A process for selectively forming nitroalkanes comprising contacting in a reaction zone in a homogeneous gas phase and at an elevated pressure of about 5 to 20 bars, a temperature of from about 100.degree. C. to about 500.degree. C. and a time of from 0.5 to 20 seconds, a C.sub.3 -C.sub.10 aliphatic ketone with nitrogen dioxide and recovering the formed nitroalkane compound.
- 2. The process of claim 1 wherein the reaction zone further contains oxygen, water or both.
- 3. The process of claim 1 wherein the ketones is selected from a C.sub.3 to C.sub.5, aliphatic ketone or mixtures thereof.
- 4. The process of claim 2 wherein the ketone is selected from a C.sub.3 to C.sub.5 aliphatic ketone or mixtures thereof.
- 5. The process of claim 1 wherein the ketone is represented by the formula: ##STR2## wherein R and R' each represent the same alkyl group.
- 6. The process of claim 2 wherein the ketone is represent by the formula: ##STR3## wherein R and R' each represent the same alkyl group.
- 7. The process of claim 5 wherein the ketone is acetone.
- 8. The process of claim 6 wherein the ketone is acetone.
- 9. The process of claim 1 wherein the process further comprises cooling the reaction zone effluent, separating the resulting liquid phase effluent from the non-condensed gaseous effluent and recovering any ketone and returning at least a portion of said ketone the reaction zone.
- 10. The process of claim 2 wherein the process further comprises cooling the reaction zone effluent, separating the resulting liquid phase effluent from the non-condensed gaseous effluent and recovering any ketone and returning at least a portion of said ketone to the reaction zone.
- 11. The process of claim 3 wherein the process further comprises cooling the reaction zone effluent, separating the resulting liquid phase effluent from the non-condensed gaseous effluent and recovering any ketone and returning at least a portion of said ketone to the reaction zone.
- 12. The process of claim 4 wherein the process further comprises cooling the reaction zone effluent, separating the resulting liquid phase effluent from the non-condensed gaseous effluent and recovering any ketone and returning at least a portion of said ketone to the reaction zone.
- 13. The process of claim 5 wherein the process further comprises cooling the reaction zone effluent, separating the resulting liquid phase effluent from the non-condensed gaseous effluent and recovering any ketone and returning at least a portion of said ketone to the reaction zone.
- 14. The process of claim 6 wherein the process further comprises cooling the reaction zone effluent, separating the resulting liquid phase effluent from the non-condensed gaseous effluent and recovering any ketone and returning at least a portion of said ketone to the reaction zone.
- 15. The process of claim 7 wherein the process further comprises cooling the reaction zone effluent, separating the resulting liquid phase effluent from the non-condensed gaseous effluent and recovering any ketone and returning at least a portion of said ketone to the reaction zone.
- 16. The process of claim 8 wherein the process further comprises cooling the reaction zone effluent, separating the resulting liquid phase effluent from the non-condensed gaseous effluent and recovering any ketone and returning at least a portion of said ketone to the reaction zone.
- 17. The process of claim 2 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 18. The process of claim 3 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 19. The process of claim 4 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 20. The process of claim 9 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 21. The process of claim 10 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 22. The process of claim 11 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 23. The process of claim 12 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 24. The process of claim 13 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 25. The process of claim 14 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 26. The process of claim 15 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
- 27. The process of claim 16 wherein the reaction zone pressure is from about 5 to 20 bars, temperature is from about 180.degree.-400.degree. C., the O.sub.2 to NO.sub.2 molar ratio is from about 0.05 to 1 and the NO.sub.2 to ketone molar ratio is from about 0.3 to 3.
Parent Case Info
This application is a continuation-in-part application of copending U.S. application Ser. No. 510,860, Filed July 5, 1983, now abandoned.
US Referenced Citations (6)
Non-Patent Literature Citations (3)
Entry |
Nitration Studies, Bachman et al., 35 J. Org. Chem., 4229, (1970). |
Vapor Phase Nitration of Aliphatic Ethers, Alcohols, Ketones and Carboxylic Acids, Hass et al., 76 JACS, 2692, (1954). |
Nitration of Gaseous Paraffins, Hass et al., 28 Ind. & Eng. Chem., 339. |
Continuation in Parts (1)
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Number |
Date |
Country |
Parent |
510860 |
Jul 1983 |
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