Process for removal of alkynes and/or dienes from an olefin stream

• US 20070004946A1
• Filed: 09/07/2006
• Published: 01/04/2007
• Est. Priority Date: 03/28/2003
• Status: Active Grant

• Current Assignee: David Lumgair, Keith Kuechler
• Original Assignee: David Lumgair, Keith Kuechler
• Inventors: Lumgair, David, Kuechler, Keith
• Granted Patent: US 7,378,562 B2
• Time in Patent Office: Days
• US Class Current: 585/265
• CPC Class Codes: C07C 1/20 starting from organic compounds containing only oxygen atoms as heteroatoms
• CPC Class Codes: C07C 11/04 Ethylene
• CPC Class Codes: C07C 11/06 Propene
• CPC Class Codes: C07C 7/163 by hydrogenation
• CPC Class Codes: C07C 7/167 for removal of compounds containing a triple carbon-to-carbon bond
• CPC Class Codes: C10G 45/32 Selective hydrogenation of the diolefin or acetylene compounds
• CPC Class Codes: C10G 45/40 containing platinum group metals or compounds thereof
• CPC Class Codes: C10G 65/06 at least one step being a selective hydrogenation of the diolefins
• CPC Class Codes: Y02P 30/20 using bio-feedstock
• CPC Class Codes: Y02P 30/40 Ethylene production

Abstract

The present invention is a process for removing alkynes and/or dienes from an olefin product stream withdrawn from an oxygenate-to-olefins reactor. The process comprises hydrogenating a first olefin stream that has alkynes and/or dienes in the presence of excess hydrogen and a first hydrogenation catalyst. The hydrogenation of the first olefin stream produces a second olefin stream that has unreacted hydrogen. The second olefin stream is contacted with a second hydrogenation catalyst producing a third olefin stream. The third olefin stream has low levels of hydrogen and alkynes and/or dienes.

Claims

1-46. -46. (canceled)

47. A process for making a polyolefin product from an oxygenate feed stream, the process comprising the steps of:

(a) contacting the oxygenate feed stream with a molecular sieve catalyst in an oxygenate-to-olefin reactor thereby producing a first olefin stream having olefins selected from the group comprising ethylene, propylene and mixtures thereof and byproducts selected from the group consisting of alkynes, dienes and mixtures thereof, wherein there is about 200 mppm or less of byproducts for every mole of olefins in the first product stream;

(b) adding hydrogen to the first olefin stream, wherein the mole ratio of hydrogen to byproducts in the first product stream is about 1.05;

1 or higher;

(c) hydrogenating the first olefin stream in the presence of a first hydrogenation catalyst producing a second olefin stream comprising prime olefins and unreacted hydrogen;

(d) contacting the second olefin stream with a second hydrogenation catalyst producing a third olefin stream, wherein the third olefin stream has about 10 mppm or less hydrogen based upon the composition of the third olefin stream; and

(e) converting the prime olefins from the third olefin stream to the polyolefin product.

48. The process of claim 47, wherein at least a portion of the hydrogen is from a hydrogen source stream having about 98 mol. % or more hydrogen based upon the composition of the hydrogen source stream.

49. The process of claim 48, wherein a combined stream of the first olefin stream and the hydrogen source stream has about 500 mppm or less methane based upon the composition of the combined stream.

50. The process of claim 48, wherein a combined stream of the first olefin stream and the hydrogen source stream has about 1 mppm or less CO based upon the composition of the combined stream.

51. The process of claim 48, wherein a combined stream of the first olefin stream and the hydrogen source stream has about 1 mppm or less CO₂ based upon the composition of the combined stream.

52. The process of claim 47, wherein from about 1.5 moles to about 10 moles of hydrogen are present for every mole of byproducts in the first olefin stream.

53. The process of claim 48, wherein the hydrogen source stream is from a source selected from the group comprising pipeline hydrogen, hydrogen from reformed naphtha, hydrogen from refinery streams, hydrogen from bottled sources, hydrogen from water electrolysis reactors, hydrogen from refinery streams and hydrogen from decomposition of oxygenates.

54. The process of claim 47, wherein the first olefin stream is heated to a temperature ranging from about 100°

F. (38°

C.) to about 250°

F. (121°

C.)

55. The process of claim 47, wherein the step of (a) hydrogenating occurs at a pressure ranging from about 50 psia (344 kPaa) to about 400 psia (2760 kPaa).

56. The process of claim 47, wherein the first catalyst and second catalyst are an elemental Group VIII metal catalysts.

57. The process of claim 47, wherein the first catalyst and second catalyst are elemental palladium catalyst.

58. The process of claim 47, wherein the first olefin stream contains about 98 mol. % or more olefin based upon the composition of the first olefin stream.

59. The process of claim 47, wherein the first olefin stream comprises about 90 mol. % or more ethylene based upon the composition of the first olefin stream.

60. The process of claim 47, wherein the byproducts include acetylene and the first olefin stream comprises about 50 mppm or less byproducts based upon the composition of the first olefin stream.

61. The process of claim 47, wherein the first olefin stream comprises about 90 mol. % or more propylene based upon the composition of the first olefin stream.

62. The process of claim 47, wherein the byproducts are selected from the group comprising methyl acetylene, propadiene and mixtures thereof and the first olefin stream comprises about 50 mppm or less byproducts based upon the composition of the first olefin stream.

63. The process of claim 47, wherein the temperature of the second olefin stream ranges from about 100°

F. (38°

C.) to about 250°

F. (121°

C.)

64. The process of claim 47, wherein the step of (b) contacting occurs at a pressure ranging from about 50 psia (344 kPaa) to about 400 psia (2760 kPaa).

65-113. -113. (canceled)