Advances in dehydrogenation catalysis

• US 6,700,028 B2
• Filed: 05/07/2002
• Issued: 03/02/2004
• Est. Priority Date: 08/27/1999
• Status: Expired due to Term

• Current Assignee: Indorama Ventures Oxides, LLC
• Original Assignee: Huntsman Petrochemical LLC (Huntsman Corporation)
• Inventors: Dyroff, David R.
• Primary Examiner(s): Dang, Thuan D.
• Application Number:
  US10/140,178
• Publication Number:
  US 20020183580A1
• Time in Patent Office: 665 Days
• Field of Search: 585/660, 585/661, 585/662, 585/663
• US Class Current: 585/660
• CPC Class Codes: B01J 23/40 of the platinum group metals
• CPC Class Codes: B01J 35/31 Density
• CPC Class Codes: B01J 35/32 Bulk density
• CPC Class Codes: B01J 35/615 100-500 m2/g
• CPC Class Codes: B01J 35/635 0.5-1.0 ml/g
• CPC Class Codes: B01J 35/647 2-50 nm
• CPC Class Codes: B01J 35/651 50-500 nm
• CPC Class Codes: B01J 35/66 Pore distribution
• CPC Class Codes: C07C 11/02 Alkenes
• CPC Class Codes: C07C 2521/04 Alumina
• CPC Class Codes: C07C 2523/42 Platinum
• CPC Class Codes: C07C 2523/44 Palladium
• CPC Class Codes: C07C 2523/46 Ruthenium, rhodium, osmium or iridium
• CPC Class Codes: C07C 5/3337 of the platinum group

Abstract

Provided herein are processes for the dehydrogenation of hydrocarbons using new supported catalysts. A process according to the invention employs new catalysts that possess a unique pore size distribution which provides a favorable balance of selectivity, activity, and thermal stability. A process according to the invention includes regeneration of the new catalysts. Detergent range paraffins may be converted to monoolefins using the new catalysts with fewer unwanted by-products being formed during the dehydrogenation.

Claims

1. A process for forming an olefin by dehydrogenation of a hydrocarbon which comprises the steps of:

a) providing a hydrocarbon;

b) providing a catalyst comprising a primary catalytic component that comprises one or more elements selected from the group consisting of;

platinum, rhodium, iridium, palladium, ruthenium, and osmium deposited on a solid support comprising porous alumina, wherein said regenerable catalyst has a surface area greater than 100 m²/g, a volume of pores with diameters below 60 Angstrom units that is less than 0.05 cm³/g, a volume of pores with diameters in the range of 60-350 Angstrom units that is greater than 0.50 cm³/g, and wherein the volume of pores with diameters in the range of 60-350 Angstrom units is greater than about 70% of the total contained pore volume; and

c) contacting said catalyst with said hydrocarbon under conditions effective to cause dehydrogenation of said hydrocarbon to produce an olefin.

2. A process according to claim 1 in which the hydrocarbon is a paraffin.

3. A process according to claim 2 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

4. A process according to claim 1 in which the hydrocarbon comprises at least one unsaturated hydrocarbon.

5. A process according to claim 4 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons are present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

6. A process according to claim 1 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

7. A process according to claim 1 in which the hydrocarbon comprises a mixture of hydrocarbons in which unsaturated hydrocarbons comprise at least 50.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

8. A process according to claim 1 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

9. A process according to claim 1 in which said catalyst is disposed within a reactor wherein the reactor includes:

a) an inlet portion to which a raw material stream comprising a gaseous hydrocarbon is fed;

b) a means for maintaining the catalyst in a substantially stationary position; and

c) an outlet portion where effluent gases comprising at least one olefin exit said reactor.

10. A process according to claim 9 in which the hydrocarbon comprises at least one paraffin.

11. A process according to claim 10 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

12. A process according to claim 9 in which the hydrocarbon comprises an unsaturated hydrocarbon.

13. A process according to claim 9 in which the hydrocarbon comprises a saturated hydrocarbon.

14. A process according to claim 12 in which the hydrocarbon comprises a mixture of hydrocarbons wherein said unsaturated hydrocarbon is present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

15. A process according to claim 9 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

16. A process according to claim 9 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

17. A process according to claim 9 further comprising the step of:

d) recovering a paraffin from said effluent gases.

18. A process according to claim 9 further comprising the step of:

d) recovering a monoolefin from said effluent gases.

19. A process according to claim 9 further comprising the steps of:

d) recovering a monoolefin from said effluent gases to provide a stripped effluent stream that contains a lower percentage of monoolefins than said effluent gases; and

e) re-directing said stripped effluent stream to said inlet portion.

20. A process as in claim 19 further comprising the step of adding a gaseous hydrocarbon to the stripped effluent stream prior to the step of re-directing said stripped effluent stream to said inlet portion.

21. A process according to claim 9 wherein said raw material stream includes hydrogen in an effective amount for maintaining said catalyst in an active state.

22. A process according to claim 21 wherein the hydrogen to hydrocarbon mole ratio is within the range of 0.3 to 1.9.

23. A process according to claim 9 wherein the hydrocarbon is a paraffin and further comprising the steps of:

d) recovering unreacted paraffins from said effluent; and

e) re-directing said unreacted paraffins to said inlet portion of said reactor.

24. A process according to claim 10 further comprising the steps of:

d) recovering unreacted paraffins from said effluent;

e) mixing fresh paraffins with said unreacted paraffins to form a mixture; and

f) feeding said mixture to said inlet portion.

25. A process according to claim 1 further comprising the step of:

regenerating said catalyst.

26. A process according to claim 9 further comprising the step of:

regenerating said catalyst.

27. A process according to claim 25 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.

28. A process according to claim 26 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.

29. A process for forming an olefin by dehydrogenation of a hydrocarbon which comprises the steps of:

a) providing a hydrocarbon;

b) providing a catalyst comprising;

i) a primary catalytic component that comprises one or more elements selected from the group consisting of;

platinum, rhodium, iridium, palladium, ruthenium, and osmium deposited on a porous alumina catalyst support, and

ii) an acidity control component comprising at least one element selected from the group consisting of the alkali metals and the alkaline earth metals deposited upon said support,

wherein said catalyst has a surface area greater than 100 m²/g, a volume of pores with diameters below 60 Angstrom units that is less than 0.05 cm³/g, a volume of pores with diameters in the range of 60-350 Angstrom units that is greater than 0.50 cm³/g, and wherein the volume of pores with diameters in the range of 60-350 Angstrom units is greater than about 70% of the total contained pore volume; and

c) contacting said catalyst with said hydrocarbon under conditions effective to cause dehydrogenation of said hydrocarbon to produce an olefin.

30. A process according to claim 29 in which the hydrocarbon is a paraffin.

31. A process according to claim 30 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

32. A process according to claim 29 in which the hydrocarbon comprises at least one unsaturated hydrocarbon.

33. A process according to claim 32 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons are present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

34. A process according to claim 29 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

35. A process according to claim 29 in which the hydrocarbon comprises a mixture of hydrocarbons in which unsaturated hydrocarbons comprise at least 50.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

36. A process according to claim 29 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

37. A process according to claim 29 in which said catalyst is disposed within a reactor wherein the reactor includes:

a) an inlet portion to which a raw material stream comprising a gaseous hydrocarbon is fed;

b) a means for maintaining the catalyst in a substantially stationary position; and

c) an outlet portion where effluent gases comprising at least one olefin exit said reactor.

38. A process according to claim 37 in which the hydrocarbon comprises at least one paraffin.

39. A process according to claim 38 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

40. A process according to claim 37 in which the hydrocarbon comprises an unsaturated hydrocarbon.

41. A process according to claim 37 in which the hydrocarbon comprises a saturated hydrocarbon.

42. A process according to claim 40 in which the hydrocarbon comprises a mixture of hydrocarbons wherein said unsaturated hydrocarbon is present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

43. A process according to claim 37 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

44. A process according to claim 37 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

45. A process according to claim 37 further comprising the step of:

d) recovering a paraffin from said effluent gases.

46. A process according to claim 37 further comprising the step of:

d) recovering a monoolefin from said effluent gases.

47. A process according to claim 37 further comprising the steps of:

d) recovering a monoolefin from said effluent gases to provide a stripped effluent stream that contains a lower percentage of monoolefins than said effluent gases; and

e) re-directing said stripped effluent stream to said inlet portion.

48. A process as in claim 47 further comprising the step of adding a gaseous hydrocarbon to the stripped effluent stream prior to the step of re-directing said stripped effluent stream to said inlet portion.

49. A process according to claim 37 wherein said raw material stream includes hydrogen in an effective amount for maintaining said catalyst in an active state.

50. A process according to claim 49 wherein the hydrogen to hydrocarbon mole ratio is within the range of 0.3 to 1.9.

51. A process according to claim 37 wherein the hydrocarbon is a paraffin and further comprising the steps of:

d) recovering unreacted paraffins from said effluent; and

e) re-directing said unreacted paraffins to said inlet portion of said reactor.

52. A process according to claim 38 further comprising the steps of:

d) recovering unreacted paraffins from said effluent;

e) mixing fresh paraffins with said unreacted paraffins to form a mixture; and

f) feeding said mixture to said inlet portion.

53. A process according to claim 29 further comprising the step of:

regenerating said catalyst.

54. A process according to claim 37 further comprising the step of:

regenerating said catalyst.

55. A process according to claim 53 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.

56. A process according to claim 54 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.

57. A process for forming an olefin by dehydrogenation of a hydrocarbon which comprises the steps of:

a) providing a hydrocarbon;

b) providing a catalyst comprising;

i) a primary catalytic component that comprises one or more elements selected from the group consisting of;

platinum, rhodium, iridium, palladium, ruthenium, and osmium deposited on a porous alumina catalyst support, and

ii) an activator component comprising one or more elements selected from the group consisting of;

scandium, titanium, vanadium, chromium, manganese, iron, cobalt, nickel, copper, zinc, yttrium, zirconium, niobium, molybdenum, silver, lanthanum, hafnium, tantalum, tungsten, rhenium, and gold deposited upon said support,

wherein said catalyst has a surface area greater than 100 m²/g, a volume of pores with diameters below 60 Angstrom units that is less than 0.05 cm³/g, a volume of pores with diameters in the range of 60-350 Angstrom units that is greater than 0.50 cm³/g, and wherein the volume of pores with diameters in the range of 60-350 Angstrom units is greater than about 70% of the total contained pore volume; and

c) contacting said catalyst with said hydrocarbon under conditions effective to cause dehydrogenation of said hydrocarbon to produce an olefin.

58. A process according to claim 57 in which the hydrocarbon is a paraffin.

59. A process according to claim 58 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

60. A process according to claim 57 in which the hydrocarbon comprises at least one unsaturated hydrocarbon.

61. A process according to claim 60 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons are present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

62. A process according to claim 57 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

63. A process according to claim 57 in which the hydrocarbon comprises a mixture of hydrocarbons in which unsaturated hydrocarbons comprise at least 50.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

64. A process according to claim 57 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

65. A process according to claim 57 in which said catalyst is disposed within a reactor wherein the reactor includes:

a) an inlet portion to which a raw material stream comprising a gaseous hydrocarbon is fed;

b) a means for maintaining the catalyst in a substantially stationary position; and

c) an outlet portion where effluent gases comprising at least one olefin exit said reactor.

66. A process according to claim 65 in which the hydrocarbon comprises at least one paraffin.

67. A process according to claim 66 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

68. A process according to claim 65 in which the hydrocarbon comprises an unsaturated hydrocarbon.

69. A process according to claim 65 in which the hydrocarbon comprises a saturated hydrocarbon.

70. A process according to claim 68 in which the hydrocarbon comprises a mixture of hydrocarbons wherein said unsaturated hydrocarbon is present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

71. A process according to claim 65 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

72. A process according to claim 65 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

73. A process according to claim 65 further comprising the step of:

d) recovering a paraffin from said effluent gases.

74. A process according to claim 65 further comprising the step of:

d) recovering a monoolefin from said effluent gases.

75. A process according to claim 65 further comprising the steps of:

d) recovering a monoolefin from said effluent gases to provide a stripped effluent stream that contains a lower percentage of monoolefins than said effluent gases; and

e) re-directing said stripped effluent stream to said inlet portion.

76. A process as in claim 75 further comprising the step of adding a gaseous hydrocarbon to the stripped effluent stream prior to the step of re-directing said stripped effluent stream to said inlet portion.

77. A process according to claim 65 wherein said raw material stream includes hydrogen in an effective amount for maintaining said catalyst in an active state.

78. A process according to claim 77 wherein the hydrogen to hydrocarbon mole ratio is within the range of 0.3 to 1.9.

79. A process according to claim 65 wherein the hydrocarbon is a paraffin and further comprising the steps of:

d) recovering unreacted paraffins from said effluent; and

e) re-directing said unreacted paraffins to said inlet portion of said reactor.

80. A process according to claim 66 further comprising the steps of:

d) recovering unreacted paraffins from said effluent;

e) mixing fresh paraffins with said unreacted paraffins to form a mixture; and

f) feeding said mixture to said inlet portion.

81. A process according to claim 57 further comprising the step of regenerating said catalyst.

82. A process according to claim 65 further comprising the step of:

regenerating said catalyst.

83. A process according to claim 81 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.

84. A process according to claim 82 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.

85. A process for forming an olefin by dehydrogenation of a hydrocarbon which comprises the steps of:

a) providing a hydrocarbon;

b) providing a catalyst comprising;

i) a primary catalytic component that comprises one or more elements selected from the group consisting of;

platinum, rhodium, iridium, palladium, ruthenium, and osmium deposited on a porous alumina catalyst support;

ii) an activator component comprising one or more elements selected from the group consisting of;

scandium, titanium, vanadium, chromium, manganese, iron, cobalt, nickel, copper, zinc, yttrium, zirconium, niobium, molybdenum, silver, lanthanum, hafnium, tantalum, tungsten, rhenium, and gold deposited upon said support; and

iii) an acidity control component comprising at least one element selected from the group consisting of the alkali metals and the alkaline earth metals deposited upon said support,

wherein said catalyst has a surface area greater than 100 m²/g, a volume of pores with diameters below 60 Angstrom units that is less than 0.05 cm³/g, a volume of pores with diameters in the range of 60-350 Angstrom units that is greater than 0.50 cm³/g, and wherein the volume of pores with diameters in the range of 60-350 Angstrom units is greater than about 70% of the total contained pore volume; and

c) contacting said catalyst with said hydrocarbon under conditions effective to cause dehydrogenation of said hydrocarbon to produce an olefin.

86. A process according to claim 85 in which the hydrocarbon is a paraffin.

87. A process according to claim 86 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

88. A process according to claim 85 in which the hydrocarbon comprises at least one unsaturated hydrocarbon.

89. A process according to claim 88 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons are present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

90. A process according to claim 85 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

91. A process according to claim 85 in which the hydrocarbon comprises a mixture of hydrocarbons in which unsaturated hydrocarbons comprise at least 50.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

92. A process according to claim 85 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

93. A process according to claim 85 in which said catalyst is disposed within a reactor wherein the reactor includes:

a) an inlet portion to which a raw material stream comprising a gaseous hydrocarbon is fed;

b) a means for maintaining the catalyst in a substantially stationary position; and

c) an outlet portion where effluent gases comprising at least one olefin exit said reactor.

94. A process according to claim 93 in which the hydrocarbon comprises at least one paraffin.

95. A process according to claim 94 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

96. A process according to claim 93 in which the hydrocarbon comprises an unsaturated hydrocarbon.

97. A process according to claim 93 in which the hydrocarbon comprises a saturated hydrocarbon.

98. A process according to claim 96 in which the hydrocarbon comprises a mixture of hydrocarbons wherein said unsaturated hydrocarbon is present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

99. A process according to claim 93 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

100. A process according to claim 93 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

101. A process according to claim 93 further comprising the step of:

d) recovering a paraffin from said effluent gases.

102. A process according to claim 93 further comprising the step of:

d) recovering a monoolefin from said effluent gases.

103. A process according to claim 93 further comprising the steps of:

d) recovering a monoolefin from said effluent gases to provide a stripped effluent stream that contains a lower percentage of monoolefins than said effluent gases; and

e) re-directing said stripped effluent stream to said inlet portion.

104. A process as in claim 103 further comprising the step of adding a gaseous hydrocarbon to the stripped effluent stream prior to the step of re-directing said stripped effluent stream to said inlet portion.

105. A process according to claim 93 wherein said raw material stream includes hydrogen in an effective amount for maintaining said catalyst in an active state.

106. A process according to claim 105 wherein the hydrogen to hydrocarbon mole ratio is within the range of 0.3 to 1.9.

107. A process according to claim 93 wherein the hydrocarbon is a paraffin and further comprising the steps of:

d) recovering unreacted paraffins from said effluent; and

e) re-directing said unreacted paraffins to said inlet portion of said reactor.

108. A process according to claim 94 further comprising the steps of:

d) recovering unreacted paraffins from said effluent;

e) mixing fresh paraffins with said unreacted paraffins to form a mixture; and

f) feeding said mixture to said inlet portion.

109. A process according to claim 85 further comprising the step of:

regenerating said catalyst.

110. A process according to claim 93 further comprising the step of:

regenerating said catalyst.

111. A process according to claim 109 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.

112. A process according to claim 110 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.

113. A process for forming an olefin by dehydrogenation of a hydrocarbon which comprises the steps of:

a) providing a hydrocarbon;

b) providing a catalyst comprising;

i) a primary catalytic component that comprises platinum deposited on a porous alumina catalyst support;

ii) an activator component comprising one or more elements selected from the group consisting of;

copper, silver, and gold present in an amount between 0.10% and 5.00% by weight based on the total weight of the and catalyst, including every hundredth percentage therebetween, deposited upon said support; and

iii) an acidity control component comprising at least one element selected from the group consisting of the alkali metals and the alkaline earth metals present in an amount between 0.001% and 1.000% by weight based on the total weight of the catalyst, including every thousandth percentage therebetween, deposited upon said support,

wherein said catalyst has a surface area greater than 100 m²/g, a volume of pores with diameters below 60 Angstrom units that is less than 0.05 cm³/g, a volume of pores with diameters in the range of 60-350 Angstrom units that is greater than 0.50 cm³/g, and wherein the volume of pores with diameters in the range of 60-350 Angstrom units is greater than about 70% of the total contained pore volume; and

c) contacting said catalyst with said hydrocarbon under conditions effective to cause dehydrogenation of said hydrocarbon to produce an olefin.

114. A process according to claim 113 in which the hydrocarbon is a paraffin.

115. A process according to claim 114 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

116. A process according to claim 113 in which the hydrocarbon comprises at least one unsaturated hydrocarbon.

117. A process according to claim 116 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons are present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

118. A process according to claim 113 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

119. A process according to claim 113 in which the hydrocarbon comprises a mixture of hydrocarbons in which unsaturated hydrocarbons comprise at least 50.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

120. A process according to claim 113 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

121. A process according to claim 113 in which said catalyst is disposed within a reactor wherein the reactor includes:

a) an inlet portion to which a raw material stream comprising a gaseous hydrocarbon is fed;

b) a means for maintaining the catalyst in a substantially stationary position; and

c) an outlet portion where effluent gases comprising at least one olefin exit said reactor.

122. A process according to claim 121 in which the hydrocarbon comprises at least one paraffin.

123. A process according to claim 122 in which the paraffin is straight chain or branched, and is a detergent-range paraffin.

124. A process according to claim 121 in which the hydrocarbon comprises an unsaturated hydrocarbon.

125. A process according to claim 121 in which the hydrocarbon comprises a saturated hydrocarbon.

126. A process according to claim 124 in which the hydrocarbon comprises a mixture of hydrocarbons wherein said unsaturated hydrocarbon is present in an amount of less than 25.00% on a mass basis based upon the total mass of the hydrocarbon.

127. A process according to claim 121 in which the hydrocarbon comprises a mixture of hydrocarbons wherein unsaturated hydrocarbons comprise at least 25.00% of the mixture on a mass basis based upon the total mass of the hydrocarbon.

128. A process according to claim 121 wherein said hydrocarbon comprises a straight chain detergent range paraffin.

129. A process according to claim 121 further comprising the step of:

d) recovering a paraffin from said effluent gases.

130. A process according to claim 121 further comprising the step of:

d) recovering a monoolefin from said effluent gases.

131. A process according to claim 121 further comprising the steps of:

d) recovering a monoolefin from said effluent gases to provide a stripped effluent stream that contains a lower percentage of monoolefins than said effluent gases; and

e) re-directing said stripped effluent stream to said inlet portion.

132. A process as in claim 131 further comprising the step of adding a gaseous hydrocarbon to the stripped effluent stream prior to the step of re-directing said stripped effluent stream to said inlet portion.

133. A process according to claim 121 wherein said raw material stream includes hydrogen in an effective amount for maintaining said catalyst in an active state.

134. A process according to claim 133 wherein the hydrogen to hydrocarbon mole ratio is within the range of 0.3 to 1.9.

135. A process according to claim 121 wherein the hydrocarbon is a paraffin and further comprising the steps of:

d) recovering unreacted paraffins from said effluent; and

e) re-directing said unreacted paraffins to said inlet portion of said reactor.

136. A process according to claim 122 further comprising the steps of:

d) recovering unreacted paraffins from said effluent;

e) mixing fresh paraffins with said unreacted paraffins to form a mixture; and

f) feeding said mixture to said inlet portion.

137. A process according to claim 113 further comprising the step of:

regenerating said catalyst.

138. A process according to claim 121 further comprising the step of:

regenerating said catalyst.

139. A process according to claim 137 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.

140. A process according to claim 138 wherein regenerating said catalyst includes heating the catalyst in an oxygen-bearing atmosphere to a temperature sufficient to cause at least a portion of any coke present on the surface of said catalyst to be oxidized.