초록

The invention provides methods, apparatus and chemical systems for making vinyl acetate from ethylene, oxygen, and acetic acid.

대표청구항 ▼

What is claimed is: 1. A method of making vinyl acetate, comprising: providing a reaction channel comprising a catalyst-containing reaction zone; passing ethylene, acetic acid and dioxygen into the reaction channel; wherein the ethylene, acetic acid and dioxygen react to form vinyl acetate monomer;

What is claimed is: 1. A method of making vinyl acetate, comprising: providing a reaction channel comprising a catalyst-containing reaction zone; passing ethylene, acetic acid and dioxygen into the reaction channel; wherein the ethylene, acetic acid and dioxygen react to form vinyl acetate monomer; wherein at least 30% of the ethylene is converted to products; wherein at least 95% of the ethylene that is converted to products, is converted to vinyl acetate monomer or carbon dioxide; wherein the ethylene selectivity to carbon dioxide is 10% or less; wherein at least 60% of the dioxygen is converted to products; and wherein at least 40% of the acetic acid is converted to products; and wherein the above-described conversions and selectivities are obtained in a single pass through the reaction channel; and wherein the reaction zone is adjacent to a heat exchanger; and further wherein the reaction zone has a ratio of heat transfer surface area to reaction zone volume of 1.6 cm-1 or greater. 2. The method of claim 1 wherein the contact time of dioxygen in the reaction zone is 500 ms or less. 3. The method of claim 1 wherein the catalyst comprises Pd. 4. The method of claim 3 wherein the catalyst further comprises Au. 5. The method of claim 1 wherein the reaction zone is a microchannel reaction zone. 6. The method of claim 5 further comprising a step of removing heat into a microchannel heat exchanger that is disposed adjacent to the reaction zone. 7. The method of claim 1 comprising the step of staging dioxygen into the reaction channel. 8. The method of claim 1 further comprising a step of recycling unreacted feeds back into the reaction channel. 9. The method of claim 1 wherein at least 40% of the ethylene and at least 70% of the acetic acid are converted to products. 10. The method of claim 1 wherein the ethylene selectivity to carbon dioxide is 15% or less. 11. The method of claim 1 wherein the molar ratio of ethylene to dioxygen entering the reaction channel is 6:1 or less, and the concentration of dioxygen is at least 10% by mole, and the selectivity of ethylene to carbon dioxide is 15% or less. 12. The method of claim 1 wherein at least one of ethylene, acetic acid, and dioxygen are added in a staged fashion into at least two points along the length of the reaction channel. 13. The method of claim 1 wherein the reaction channel is a microchannel having at least one dimension of 2 mm or less. 14. The method of claim 13 comprising a plurality of reaction microchannels arranged in a array of microchannels. 15. The method of claim 14 wherein the array of microchannels is in thermal contact with a plurality of adjacent heat exchange microchannels. 16. The method of claim 1 wherein the reaction channel is cylindrical. 17. The method of claim 1 wherein the reaction zone is adjacent to a heat exchanger; and further wherein the reaction zone has a ratio of heat transfer surface area to reaction zone volume of greater than 2.0 cm-1. 18. The method of claim 1 wherein the reaction zone is adjacent to a heat exchanger; and further wherein the reaction zone has a ratio of heat transfer surface area to reaction zone volume of 1.6 cm-1 to 200 cm-1. 19. The method of claim 14 comprising 3 alternating interleaved layers, comprising, in order: coolant: reaction: coolant: reaction: coolant: reaction. 20. The method of claim 19 wherein the reaction channel has a height of 0.05 to 2 mm. 21. The method of claim 1 wherein the reaction channel has a surface-to-volume ratio of at least 10 cm2 of channel internal surface area per cubic centimeter of internal channel volume. 22. The method of claim 1 wherein the reaction channel comprises plural porous sections disposed along the length of the reaction channel; and wherein a reactant is added to the reaction channel through the porous sections. 23. The method of claim 22 wherein the reaction channel is a tube in a tubular reactor, and comprising a porous section on the periphery of the channel near a connection with a tube sheet. 24. The method of claim 1 wherein the catalyst comprises Au and more than 2 wt % Pd. 25. The method of claim 24 wherein the catalyst comprises a silica, alumina, silica-alumina, titania, or zirconia support. 26. The method of claim 1 wherein the catalyst is a thin layer or rim-type catalyst, and wherein the catalyst comprises at least 12 wt % Pd. 27. The method of claim 1 wherein catalyst is intermittently disposed in reaction zones in a continuous reaction channel and wherein a reactant is added through orifices in between reaction zones so that there is mixing but substantially no catalyzed reaction between reaction zones. 28. The method of claim 1 wherein the ethylene to dioxygen ratio in the reaction channel is 4:1 or less. 29. The method of claim 28 wherein the O2 concentration in the reaction channel is at least 8%. 30. The method of claim 28 wherein the ratio of gaseous recycle to fresh feed is 1:1 or less. 31. The method of claim 29 wherein the contact time is 500 ms or less. 32. The method of claim 30 wherein dioxygen is added in the form of air. 33. The method of claim 29 wherein the reaction channel has an inlet and pressure at the inlet is in the range of 1 to 20 bar. 34. The method of claim 1 wherein temperature in the reaction zone is at least 130�� C. and the temperature over at least 50% of the length of the reaction zone varies by less than 5�� C. 35. The method of claim 34 wherein the temperature in the reaction zone is in the range of 140-200�� C. 36. The method of claim 1 wherein the per pass conversion of dioxygen is at least 90%. 37. A method of making vinyl acetate, comprising: providing a reaction channel comprising a catalyst-containing reaction zone; passing ethylene, acetic acid and dioxygen into the reaction channel; wherein the molar ratio of ethylene to dioxygen is 6:1 or less, and the concentration of dioxygen is at least 10% by mole; wherein the ethylene, acetic acid and dioxygen react to form vinyl acetate monomer and carbon dioxide; wherein at least 95% of the ethylene that is converted to products is converted to vinyl acetate monomer or carbon dioxide; wherein the ethylene selectivity to carbon dioxide is 10% or less; wherein at least 30% of the ethylene is converted to products; wherein at least 20% of the oxygen is converted to products; and wherein the selectivity to carbon dioxide is 15% or less; and wherein the above-described conversions and selectivities are obtained in a single pass through the reaction channel; and wherein the reaction zone is adjacent to a heat exchanger; and further wherein the reaction zone has a ratio of heat transfer surface area to reaction volume of greater than 2.0 cm-1. 38. The method of claim 37 wherein the contact time of ethylene in the reaction zone is 500 ms or less. 39. The method of claim 37 wherein the catalyst comprises Pd and further comprises Au and potassium acetate. 40. The method of claim 37 wherein at least 60% of the dioxygen and at least 40% of the acetic acid are converted to products. 41. The method of claim 37 wherein the reaction channel has at least one dimension of 17 mm or less. 42. The method of claim 41 wherein the reaction channel is a tube in a tubular reactor, and comprising a porous section on the periphery of the channel near a connection with a tube sheet. 43. The method of claim 37 wherein the catalyst comprises Au and more than 4 wt % Pd. 44. The method of claim 41 wherein the catalyst comprises at least 4 wt % Pd. 45. The method of claim 37 wherein the ratio of gaseous recycle to fresh feed is 2:1 or less. 46. The method of claim 37 wherein the reaction channel has an outlet and pressure at the outlet is in the range of 1 to 20 bar. 47. The method of claim 46 wherein temperature in the reaction zone is at least 130�� C. and the temperature over at least 50% of the length of the reaction zone varies by less than 5�� C. 48. The method of claim 37 wherein the reaction channel has at least one dimension of 10 mm or less. 49. A method of making vinyl acetate, comprising: providing a reaction channel comprising a catalyst-containing reaction zone; passing ethylene, acetic acid and dioxygen into the reaction channel; wherein the ethylene, acetic acid and dioxygen react to form vinyl acetate monomer; wherein at least 30% of the ethylene is converted to products; wherein at least 95% of the ethylene that is converted to products, is converted to vinyl acetate monomer or carbon dioxide; wherein the ethylene selectivity to carbon dioxide is 10% or less; wherein at least 60% of the oxygen and at least 40% of the acetic acid are converted to products; and wherein the above-described conversions and selectivities are obtained in a single pass through the reaction channel and wherein the reaction zone is adjacent to a heat exchanger; and further wherein the reaction zone has a ratio of heat transfer surface area to reaction zone volume of 1.6 cm-1 to 200 cm-1. 50. The method of claim 49 wherein the catalyst further comprises at least 2 wt % Pd and wherein the catalyst further comprises Au. 51. The method of claim 49 comprising the step of staging ethylene into the reaction channel. 52. The method of claim 49 wherein at least 40% of the ethylene and at least 70% of the acetic acid are converted to products. 53. The method of claim 49 wherein the molar ratio of ethylene to dioxygen entering the reaction channel is 6:1 or less, and the concentration of dioxygen is at least 10% by mole. 54. The method of claim 49 wherein the catalyst is a thin layer or rim-type catalyst, and wherein the catalyst comprises at least 10 wt % Pd. 55. The method of claim 54 wherein catalyst is intermittently disposed in reaction zones in a continuous reaction channel and wherein a reactant is added through orifices in between reaction zones so that there is mixing but substantially no catalyzed reaction between reaction zones. 56. The method of claim 55 wherein the ethylene to dioxygen ratio in the reaction channel is 4:1 or less. 57. The method of claim 56 wherein the O2 concentration in the reaction channel is at least 8%. 58. The method of claim 56 wherein the ratio of ethylene:acetic acid:dioxygen is in the range of 6:3:1 and 2:2:1. 59. A process for the production of vinyl acetate monomer, passing ethylene, acetic acid, and dioxygen into a reaction channel, wherein the reaction channel comprises a reaction zone containing a catalyst; reacting the ethylene, acetic acid, and dioxygen over the catalyst to form VAM; wherein the partial pressure of acetic acid when calculated on the basis of the total feed to the reactor exceeds the dewpoint pressure of acetic acid at the reaction temperature; wherein at least 30% of the ethylene is converted to products; wherein at least 95% of the ethylene that is converted to products, is converted to vinyl acetate monomer or carbon dioxide; wherein the ethylene selectivity to carbon dioxide is 10% or less; wherein at least 60% of the dioxygen is converted to products; and wherein at least 40% of the acetic acid is converted to products; and wherein the above-described conversions and selectivities are obtained in a single pass through the reaction channel; and wherein the reaction zone is adjacent to a heat exchanger; and further wherein the reaction zone has a ratio of heat transfer surface area to reaction zone volume of greater than 2.0 cm-1. 60. The process of claim 59 wherein the reaction zone is less than 2 meters in length. 61. The process of claim 59 wherein the reaction zone is a microchannel reaction zone. 62. The method of claim 59 comprising the step of staging acetic acid into the reaction channel. 63. The method of claim 59 wherein the molar ratio of ethylene to dioxygen entering the reaction channel is 6:1 or less, and the concentration of dioxygen is at least 10% by mole, and the selectivity of ethylene to carbon dioxide is 15% or less. 64. The method of claim 59 wherein the catalyst comprises Pd and further comprising a step of removing heat into a microchannel heat exchanger that is disposed adjacent to the reaction zone; and wherein acetic acid is added in a staged fashion into at least two points along the length of the reaction channel. 65. The method of claim 62 wherein catalyst is intermittently disposed in reaction zones in a continuous reaction channel and wherein a reactant is added through orifices in between reaction zones so that there is mixing but substantially no catalyzed reaction between reaction zones. 66. A process for the production of vinyl acetate monomer, passing ethylene, acetic acid, and dioxygen into a reaction channel, wherein the reaction channel comprises a reaction zone containing a catalyst; reacting the ethylene, acetic acid, and dioxygen over the catalyst to form VAM; wherein at least one of ethylene, acetic acid, and dioxygen are added in a staged fashion into at least two points along the length of the reaction channel; wherein at least 30% of the ethylene is convened to products; wherein at least 95% of the ethylene that is converted to products, is converted to vinyl acetate monomer or carbon dioxide; wherein the ethylene selectivity to carbon dioxide is 10% or less; wherein at least 60% of the dioxygen is convened to products; and wherein at least 40% of the acetic acid is converted to products; and wherein the above described conversions and selectivities are obtained in a single pass through the reaction channel; and wherein the reaction zone is adjacent to a heat exchanger; and further wherein the reaction zone has a ratio of heat transfer surface area to reaction zone of greater than 2.0 cm-1. 67. The process of claim 66 wherein the reaction zone has an inlet and an outlet and the linear velocity of gas is greater at the outlet of the reaction zone than it is at the inlet to the reaction zone. 68. The process of claim 66 wherein the reaction zone is a microchannel reaction zone. 69. The process of claim 68 wherein the reaction zone has an inlet and an outlet and the mass flow rate of gas is greater at the outlet of the reaction zone than it is at the inlet to the reaction zone. 70. The method of claim 66 wherein the molar ratio of ethylene to dioxygen entering the reaction channel is 6:1 or less, and the concentration of dioxygen is at least 10% by mole. 71. The method of claim 66 wherein the catalyst is a thin layer or rim-type catalyst, and wherein the catalyst comprises at least 4 wt % Pd. 72. The method of claim 29 wherein the ratio of ethylene:acetic acid:dioxygen is in the range of 6:3:1 and 2:2:1. 73. The method of claim 37 wherein the reaction zone is a microchannel reaction zone. 74. The method of claim 39 further comprising a step of removing heat into a microchannel heat exchanger that is disposed adjacent to the reaction zone. 75. The method of claim 37 comprising the step of staging dioxygen into the reaction channel. 76. The method of claim 49 wherein the reaction channel is a microchannel having at least one dimension of 2 mm or less. 77. The method of claim 71 comprising a plurality of reaction microchannels arranged in an away of microchannels. 78. The method of claim 77 wherein the array of microchannels is in thermal contact with a plurality of adjacent heat exchange microchannels. 79. The method of claim 49 wherein the reaction zone is adjacent to a heat exchanger; and further wherein the reaction zone has a ratio of heat transfer surface area to reaction zone volume of greater than 2.0 cm-1. 80. The method of claim 49 wherein the reaction channel has a height of 0.05 to 2 mm. 81. The method of claim 49 wherein the reaction channel has a surface-to-volume ratio of at least 10 cm2 of channel internal surface area per cubic centimeter of internal channel volume. 82. The method of claim 49 wherein the reaction channel comprises plural porous sections disposed along the length of the reaction channel; and wherein a reactant is added to the reaction channel through the porous sections. 83. The method of claim 49 wherein the reaction channel is a tube in a tubular reactor, and comprising a porous section on the periphery of the channel near a connection with a tube sheet. 84. The method of claim 66 wherein catalyst is intermittently disposed in reaction zones in a continuous reaction channel and wherein a reactant is added through orifices in between reaction zones so that there is mixing but substantially no catalyzed reaction between reaction zones. 85. The method of claim 1 wherein temperature in the reaction zone is at least 130�� C. and the temperature over at least 50% of the length of the reaction zone varies by less than 5�� C.