TH12237B - Selective hydrogenation of highly unsaturated compounds in a hydrocarbon stream. - Google Patents

Abstract

Reveal the hydrogenation process Selectively of diolefin and acetylenic compounds In the liphatic hydro stream Carbon with a lot of olefins Selective hydrogenation was obtained at 40–300 ํ under low hydrogen pressure in the range of approximately 0.1 psi to below 70 psi at 0 - 350 psig in column reactors. Distilled with a hydrogenation catalyst Which will act as a component Of a refined structure such as a supported Pdo Inserted in a tube A basket of wire mesh. Without any hydrogenation of olefins

Claims (78)

1. The process for the selective hydrogenation of highly unsaturated compounds consists of the following steps: (a) feeding (1) a stream of hydrocarbons containing highly unsaturated compounds, including di-olefins and acetylene, and (2) a stream containing hydrogen into the distillation column reactor; (b) counter-flow in the said distillation column reactor at a hydrogen partial pressure that yields a range of at least approximately 0.1 psi to less than 70 psi; (i) contact of the said stream in the distillation reaction region with a hydrogenation catalyst prepared to serve as one of the distillation structures, by selectively hydrogenating a portion of the highly unsaturated compounds with hydrogen to produce less unsaturated hydrocarbons in the reaction mixture in the vapor/liquid phase; and (ii) separation of the olefins produced by such selective hydrogenation from the reaction mixture by fractional distillation in the distillation structure while prepared for the partial condensation of hydrocarbons containing olefins and highly unsaturated hydrocarbon compounds. 2. The process of claim 1 where the hydrocarbon stream consists of aliphatic compounds containing 3-9 carbon atoms. 3. The process of claim 1 whereby the aforementioned hydrocarbon stream contains a principal amount of normal olefins that have been separated as products of the aforementioned hydrogenation. 4. The process of claim 1 where the hydrocarbon in question has a WHSV in the range of 0.1-35. 5. Procedure of claim 2, where the upper pressure of the distillation column reactor is in the range of 0 - 350 psig. 6. Procedure of Claim 1 where the partial pressure of hydrogen is less than 50 psig. 7. The process of claim 6, where the partial pressure of hydrogen is less than 10 psia. 8. The process of claim 7, where the partial pressure of hydrogen is less than 7 psia. 9. The process of claim 5, where the partial pressure of hydrogen is less than 50 psia. 10. The process of claim 9, where the partial pressure of hydrogen is less than 10 psia. 11. The process of claim 10, where the partial pressure of hydrogen is less than 7 psia. 12. Procedure of Claim 1, whereby the hydrogenation catalyst contains a metal or a compound of Group VIII metal as the basic component of the catalyst. 13. The process of claims 12, where the said catalyst consists of Pd. 14. The process of claim 5, where the upper pressure is in the range of 50 - 150 psia. 15. The process of claim 1 consists of the following steps: (a) feeding (1) a first stream containing olefins, diolefins, and acetylenyl hydrocarbon compounds; and (2) a second stream containing hydrogen into the distillation column reactor at the feed site; (b) counterflow in the aforementioned distillation column reactor under a partial hydrogen pressure of approximately 0.1 psi to less than 50 psi; (i) contact of these streams with the prepared hydrogenation catalyst distillation site, which will serve as a distillation structure, by the major reaction of all diolefins and acetylenyl compounds with hydrogen to produce less unsaturated hydrocarbons in the partial liquid phase of the reaction mixture; and (ii) separation of the olefins present in the first stream and any olefins produced by hydrogenation from the reaction mixture by fractional distillation as prepared. For the partial condensation of hydrocarbons containing olefins, di-olefins, and acetylenenic hydrocarbon compounds in the distillation reaction area. 16. The process of claim 15, whereby the initial stream is fed into the lower end of the distillation reaction area, or fed below that end. 17. The process of claim 15, by feeding the various streams into the reactor, the distillation column, in a separate manner. 18. The process of claim 15, whereby the first and second streams are mixed before entering the aforementioned distillation column reactor. 19. The process of claim 15 where the hydrocarbon stream consists of aliphatic compounds with 3–9 carbon atoms. 20. The process of claim 19, where the said hydrocarbon stream consists of C3 components. 21. The process of claim 19, where the hydrocarbon stream consists of the C4 segment. 22. The process of claim 19, whereby the said hydrocarbon stream consists of the C5 segment. 23. The process of claim 19, where the hydrocarbon stream consists of the C6 segment. 24. The process of claim 19, whereby the first and second streams are combined before being fed into the column distillation reactor. 25. The process of claim 15 whereby the hydrogenation catalyst consists of a metal or a compound of a Group VIII metal as the basic component of the catalyst. 26. The process of claim 25 whereby the catalyst for such hydrogenation consists of 0.1 - 5.0% by weight of palladium oxide on an alumina extruder. 27. The process of claim 15, where the top pressure of the column distillation reactor is between 240 and 315 psig. 28. The process of claims 27, where the first stream consists of propylene. 29. The process of claim 15 whereby the distillation structure consists of a cylindrical, semi-solid, flexible open-mesh wire mesh packed with a finely hydrogenated catalytic substance. 30. The process of claim 15 also consists of steps (c) the separation of the olefins already separated from step (b), (ii) along with any unreacted hydrogen and alkanes from the reaction column of the distillation as the above substance. 31. The process of claim 15, whereby the column distillation reactor operates at an overpressure between 0 and 250 psig. 32. The procedure for claim 31, where the above pressure is in the range of 50 - 150 psig. 33. The process of claim 15, where the temperature within the distillation reaction area is in the range of 40 - 300 °F. 34. The process of claim 33, where the temperature within the distillation reaction area is in the range of 110 - 270 °F. 35. The process of claim 15, in which all diolefins and acetylinic compounds were significantly excluded from the said hydrocarbon stream. 36. The process of claim 15, where the initial stream has a WHSV in the range of 0.1 - 35. 37. The process of claim 16, whereby the hydrogenation catalyst contains a metal or a compound of Group VIII metals as the basic component of the catalyst. 38. The process of claim 37 where the catalyst for such hydrogenation consists of 0.1 - 50% by weight of palladium oxide on an alumina extruded material. 39. The process of claim 37, whereby the aforementioned column distillation reactor operated at an upper pressure in the range of 0 and 250 psig. 40. The process described in claim 39 involves a distillation reaction temperature in the range of 40 - 300 °F. 41. Procedure of claim 40 where the pressure is in the range of 50 - 150 psig. 42. The process described in claim 41 involves a distillation reaction temperature ranging from 110 to 270°F. 43. The process of claim 42, where the partial pressure of hydrogen is in the range of 0.1 - 10 psia. 44. The process of claim 43 involves internal reflux in the range of 0.5-5 L/D. 45. The process of claim 15 where the highly unsaturated compounds have been significantly hydrogenated in their entirety. 46. The process of claim 1, where the upper fraction containing condensed hydrocarbons is separated from the column reactor, almost all of the condensed hydrocarbons are condensed and returned to the distillation column reactor in a reflux manner. 47. The process of claim 13, in which the Catalyst has Silver. 48. The process of claim 38, in which the Catalyst has money. 49. The process for the selective hydrogenation of highly unsaturated compounds consists of the following steps: (a) feeding (1) a stream of highly unsaturated hydrocarbons containing diolefins and (2) a stream containing hydrogen into the distillation column reactor; (b) counter-flow in the said distillation column reactor at a hydrogen partial pressure that yields a range of at least approximately 0.1 psi to less than 70 psi; (i) contact of the said stream in the distillation reaction region with a hydrogenation catalyst prepared to serve as one of the distillation structures, by selectively hydrogenating a portion of the highly unsaturated compounds with hydrogen to produce less unsaturated hydrocarbons in the reaction mixture in the vapor/liquid phase; and (ii) separation of the olefins produced by such selective hydrogenation from the reaction mixture by fractional distillation in the distillation structure while prepared for the condensation of a portion of the hydrocarbons containing olefins and highly unsaturated hydrocarbons. 50. The process of claim 47 where the hydrocarbon stream consists of aliphatic compounds with 3–9 carbon atoms. 51. The process of claim 47 whereby the said hydrocarbon stream contains a principal amount of normal olefins that have been separated as products of such hydrogenation. 52. The process of claim 49 where the hydrocarbons in question have a WHSV in the range of 0.1-35. 53. Procedure of claim 50, where the overhead pressure of the distillation column reactor is in the range of 0 - 350 psig. 54. The procedure of claim 49, where the partial pressure of hydrogen is less than 50 psia. 55. The process of claim 54, where the partial pressure of hydrogen is less than 10 psia. 56. Procedure of claim 54 where the partial pressure of hydrogen is less than 7 psig. 57. The procedure of claim 53, where the partial pressure of hydrogen is less than 50 psia. 58. The process of claim 57 where the partial pressure of hydrogen is less than 10 psia. 59. The process of claim 58 where the partial pressure of hydrogen is less than 7 psia. 60. The process of claim 49 whereby the hydrogenation catalyst consists of a metal or a compound of a Group VIII metal as the basic component of the catalyst. 61. The process of claim 60, in which the said catalyst consists of Pd. 62. The process of claim 53, where the upper pressure is in the range of 50 - 150 psia. 63. The process of claim 61, in which the Catalyst has money. 64. The process for the selective hydrogenation of highly unsaturated compounds consists of the following steps: (a) feeding (1) a stream of highly unsaturated hydrocarbons, including acetylene, and (2) a stream containing hydrogen into the distillation column reactor; (b) counter-flow in the said distillation column reactor at a hydrogen partial pressure that yields a range of at least approximately 0.1 psi to less than 70 psi under distillation conditions in which a vapor and liquid phase are present; (i) contact of the said stream in the distillation region with a hydrogenation catalyst prepared to serve as one of the distillation structures, by selectively hydrogenating a portion of the highly unsaturated compounds with hydrogen to produce less unsaturated hydrocarbons in the reaction mixture in the vapor/liquid phase; and (ii) separation of the olefins produced by such selective hydrogenation from the reaction mixture by fractional distillation in the distillation structure while prepared for the partial condensation of hydrocarbons containing the olefins and highly unsaturated hydrocarbon compounds. 65. The process of claim 64, where the hydrocarbon stream consists of aliphatic compounds containing 3–9 carbon atoms. 66. The process of claim 64 where the said hydrocarbon stream consists of a principal amount of normal olefins that have been separated as products of such hydrogenation. 67. The process of claim 64 where the hydrocarbons in question have a WHSV in the range of 0.1-35. 68. The process of claim 65, where the overhead pressure of the distillation column reactor is in the range of 0 - 350 psig. 69. The procedure of claim 66, where the partial pressure of hydrogen is less than 50 psig. 70. The procedure of claim 69, where the partial pressure of hydrogen is less than 10 psia. 71. The process of claim 70, where the partial pressure of hydrogen is less than 7 psia. 72. The procedure of claim 68, where the partial pressure of hydrogen is less than 50 psia. 73. The process of claim 72, where the partial pressure of hydrogen is less than 10 psia. 74. The process of claim 73, where the partial pressure of hydrogen is less than 7 psia. 75. The process of claim 65 whereby the hydrogenation catalyst contains a metal or a compound of Group VIII metal as the basic component of the catalyst. 76. The process of claims 75, in which the said catalyst consists of Pd. 77. The process of claim 68 where the upper pressure is in the range of 50 - 150 psia. 78. The process of claim 76, in which the Catalyst has money.