Source: https://patents.justia.com/patent/9453165
Timestamp: 2019-09-21 22:21:36
Document Index: 780478542

Matched Legal Cases: ['Application No. 200480041082', 'Application No. 2004315214', 'Application No. 2004315214', 'Application No. 04', 'Application No. 2006', 'Application No. 2', 'Application No. 04', 'Application No. 2', 'Application No. 2006', 'Application No. 2006130871', 'Application No. 2010202533', 'Application No. 2010202533', 'Application No. 04814270', 'Application No. 2', 'Application No. 2006', 'Application No. 2006', 'Application No. 13160226', 'Application No. 04814270', 'Application No. 2', 'Application No. 15170565']

US Patent for Fischer-tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor Patent (Patent # 9,453,165 issued September 27, 2016) - Justia Patents Search
Justia Patents US Patent for Fischer-tropsch synthesis using microchannel technology and novel catalyst and microchannel reactor Patent (Patent # 9,453,165)
Apr 30, 2015 - Velocys, Inc.
A process for converting a reactant composition comprising H2 and CO to a product comprising at least one aliphatic hydrocarbon having at least about 5 carbon atoms comprises: flowing the reactant composition through a microchannel reactor in contact with a Fischer-Tropsch catalyst to convert the reactant composition to the product, the microchannel reactor comprising a plurality of process microchannels containing the catalyst; transferring heat from the process microchannels to a heat exchanger; and removing the product from the microchannel reactor; the process producing at least about 0.5 gram of aliphatic hydrocarbon having at least about 5 carbon atoms per gram of catalyst per hour; the selectivity to methane in the product being less than about 25%. A supported catalyst comprises Co, and a microchannel reactor comprises at least one process microchannel and at least one adjacent heat exchange zone.
flowing the reactant composition through a microchannel reactor in contact with a Fischer-Tropsch catalyst to convert the reactant composition to the product, the catalyst comprising Co supported on a support, the microchannel reactor comprising a plurality of process microchannels containing the catalyst;
the selectivity to methane in the product being less than about 25%; and
flowing a regenerating fluid through the process microchannels in contact with the catalyst, wherein the residence time for the regenerating fluid in the process microchannels is from about 0.01 to about 1000 seconds.
4. The process of claim 1 wherein the heat exchanger comprises a plurality of heat exchange channels.
7. The process of claim 4 wherein the heat exchange channels are made of a material comprising: steel; monel; inconel; aluminum; titanium; nickel; copper; brass; an alloy of any of the foregoing metals; a polymer; ceramics; glass; a composite comprising polymer and fiberglass; quartz; silicon; or a combination of two or more thereof.
8. The process of claim 1 wherein the microchannel reactor has an entrance and an exit, the product exits the microchannel reactor through the exit, the product being intermixed with unreacted components from the reactant composition, and at least part of the unreacted components from the reactant composition are recycled to the entrance to the microchannel reactor.
9. The process of claim 1 wherein the reactant composition enters the process microchannels and the product exits the process microchannels, the temperature of the reactant composition entering the process microchannels being within about 200° C. of the temperature of the product exiting the process microchannels.
10. The process of claim 1 wherein the mole ratio of H2 to CO in the reactant composition is in the range of about 0.8 to about 10.
11. The process of claim 1 wherein the reactant composition further comprises H2O, CO2, a hydrocarbon of 1 to about 4 carbon atoms, or a mixture of two or more thereof.
the heat exchanger comprises a plurality of heat exchange channels, the heat exchange channels containing a heat exchange fluid; and
the heat exchange fluid undergoes a phase change as it flows through the heat exchange channels.
13. The process of claim 1 wherein the heat exchanger comprises a plurality of heat exchange channels and an endothermic process is conducted in the heat exchange channels.
14. The process of claim 13 wherein the endothermic process comprises a steam reforming reaction or a dehydrogenation reaction.
the reactant composition and product flow through the process microchannels in a first direction, and the heat exchange fluid flows through the heat exchange channels in a second direction, the second direction being cross current, co-current or counter-current relative to the first direction.
16. The process of claim 1 wherein the heat exchanger contains a heat exchange fluid and the heat exchange fluid comprises air, steam, liquid water, carbon dioxide, gaseous nitrogen, a gaseous hydrocarbon or a liquid hydrocarbon.
17. The process of claim 1 wherein the catalyst further comprises Fe, Ni, Ru, Re, Os, or an oxide thereof, or a mixture of two or more thereof.
18. The process of claim 1 wherein the catalyst comprises a promoter selected from a metal from Group IA, IIA, IIIB or IIB of the Periodic Table or an oxide thereof, a lanthanide metal or oxide, an actinide metal or oxide, or a combination of two or more thereof.
19. The process of claim 1 wherein the catalyst comprises a promoter selected from the group consisting of Li, B, Na, K, Rb, Cs, Mg, Ca, Sr, Ba, Sc, Y, La, Ac, Ti, Zr, La, Ac, Ce or Th, or an oxide thereof, or a mixture of two or more thereof.
20. The process of claim 1 wherein the support is selected from alumina, zirconia, silica, aluminum fluoride, fluorided alumina, bentonite, ceria, zinc oxide, silica-alumina, silicon carbide, a molecular sieve, or a combination of two or more thereof.
21. The process of claim 1 wherein the catalyst comprises a refractory oxide support.
22. The process of claim 1 wherein the catalyst comprises a composition represented by the formula
23. The process of claim 1 wherein the catalyst has a Co loading of at least about 25% by weight.
24. The process of claim 23 wherein the catalyst further comprises Re, Ru or a mixture thereof.
25. The process of claim 1 wherein the catalyst comprises a catalytic metal and a support, the catalyst being made by the steps of:
26. The process of claim 25 wherein the composition comprising a catalytic metal comprises a cobalt nitrate solution and the support comprises alumina.
27. The process of claim 1 wherein the catalyst is washcoated on interior walls of the process microchannels, grown on interior walls of the process microchannels from solution, or coated in situ on a fin structure.
28. The process of claim 1 wherein the catalyst is supported by a support structure made of a material comprising an alloy comprising Ni, Cr and Fe, or an alloy comprising Fe, Cr, Al and Y.
29. The process of claim 1 wherein the catalyst is supported on a support structure having a flow-by configuration, a flow-through configuration, or a serpentine configuration.
30. The process of claim 1 wherein the catalyst is supported on a support structure having the configuration of a foam, felt, wad, fin, or a combination of two or more thereof.
31. The process of claim 1 wherein the catalyst comprises a fixed bed of particulate solids.
32. The process of claim 1 wherein the catalyst is supported on a support structure in the form of a fin assembly comprising at least one fin.
33. The process of claim 32 wherein the fin assembly comprises a plurality of parallel spaced fins.
34. The process of claim 32 wherein the fin has an exterior surface and a porous material overlies at least part of the exterior surface of the fin, the catalyst being supported by the porous material.
35. The process of claim 34 wherein the porous material comprises a coating, fibers, foam or felt.
36. The process of claim 32 wherein the fin has an exterior surface and a plurality of fibers or protrusions extend from at least part of the exterior surface of the fin, the catalyst being supported by the protrusions.
37. The process of claim 32 wherein the fin has an exterior surface and the catalyst is: washcoated on at least part of the exterior surface of the fin; grown on at least part of the exterior surface of the fin from solution; or deposited on at least part of the exterior surface of the fin using vapor deposition.
38. The process of claim 32 wherein the fin assembly comprises a plurality of parallel spaced fins, at least one of the fins having a length that is different than the length of the other fins.
39. The process of claim 32 wherein the fin assembly comprises a plurality of parallel spaced fins, at least one of the fins having a height that is different than the height of the other fins.
40. The process of claim 32 wherein the fin has a cross section having the shape of a square, a rectangle, or a trapezoid.
41. The process of claim 32 wherein the fin is made of a material comprising: steel; aluminum; titanium; iron; nickel; platinum; rhodium; copper; chromium; brass; an alloy of any of the foregoing metals; a polymer; ceramics; glass; a composite comprising polymer and fiberglass; quartz; silicon; or a combination of two or more thereof.
42. The process of claim 32 wherein the fin is made of an alloy comprising Ni, Cr and Fe, or an alloy comprising Fe, Cr, Al and Y.
43. The process of claim 32 wherein the fin is made of an Al2O3forming material or a Cr2O3 forming material.
44. The process of claim 1 wherein the process microchannels have a bulk flow path comprising about 5% to about 95% of the cross sections of such process m icrochannels.
45. The process of claim 1 wherein the contact time of the reactant composition and/or product with the catalyst is up to about 2000 milliseconds.
46. The process of claim 1 wherein the temperature of the reactant composition entering the process microchannels is in the range of about 150° C. to about 270° C.
47. The process of claim 1 wherein the pressure within the process microchannels is at least about 5 atmospheres.
48. The process of claim 1 wherein the space velocity for the flow of the reactant composition and product through the process microchannels is at least about 1000 hr−1.
49. The process of claim 1 wherein the pressure drop for the flow of the reactant composition and product through the process microchannels is up to about 10 atmospheres per meter of length of the process microchannels.
50. The process of claim 1 wherein
the heat exchange fluid flows through the heat exchange channels, the pressure drop for the heat exchange fluid flowing through the heat exchange channels being up to about 10 atmospheres per meter of length of the heat exchange channels.
51. The process of claim 1 wherein the conversion of CO is about 40% or higher.
52. The process of claim 1 wherein the yield of product is about 25% or higher.
53. The process of claim 1 wherein the conversion of CO is at least About 50%, the selectivity to methane in the product is about 15% or less, and the yield of product is at least about 35%.
54. The process of claim 1 wherein the catalyst is in the form of particulate solids, the median particle diameter of the particulate solids is in the range of about 1 to about 1000 μm.
55. The process of claim 1 wherein the product comprises hydrocarbons boiling at a temperature at or below about 350° C. at atmospheric pressure.
56. The process of claim 1 wherein the product comprises hydrocarbons boiling at or above a temperature of about 350° C. at atmospheric pressure.
57. The process of claim 1 wherein the product comprises a middle distillate.
58. The process of claim 1 wherein the product comprises at least one olefin.
59. The process of claim 1 wherein the product comprises a normal paraffin, isoparaffin, or mixture thereof.
60. The process of claim 1 wherein at least part of the product is further processed using hydrocracking, hydroisomerizing or dewaxing.
61. The process of claim 1 wherein at least part of the product is further processed to form a lubricating base oil or a diesel fuel.
62. The process of claim 1 wherein the process microchannels are vertically oriented, the reactant composition and product flow downwardly through the process microchannels.
63. The process of claim 1 wherein the regenerating fluid comprises hydrogen.
64. The process of claim 1 wherein the regenerating fluid comprises hydrogen and a diluent, the diluent comprising nitrogen, argon, helium, methane, carbon dioxide, steam, or a mixture of two or more thereof.
65. The process of claim 1 wherein the reactant composition comprises a product of a steam reforming process, autothermal reforming process, carbon dioxide reforming process, coal gasification process, or a combination of two or more thereof.
66. The process of claim 1 wherein the reactant composition comprises a product of a coal gasification process.
67. A process for converting a reactant composition comprising H2 and CO to a product comprising at least one aliphatic hydrocarbon having at least about 5 carbon atoms, the process comprising:
flowing the reactant composition through a microchannel reactor in contact with a Fischer-Tropsch catalyst to convert the reactant composition to the product, the catalyst comprising Co supported on a support, the microchannel reactor comprising a plurality of process microchannels containing the catalyst, the catalyst being in the form of a fixed bed of particulate solids, a median particle diameter of the particulate solids in the range of about 1 to about 1000 μm;
flowing a regenerating fluid through the process microchannel in contact with the catalyst.
68. The process of claim 67 wherein each process microchannel has an internal dimension of width or height of up to about 10 mm.
69. The process of claim 67 wherein the process microchannels are made of a material comprising: steel; monel; inconel; aluminum; titanium; nickel; copper; brass; an alloy of any of the foregoing metals; a polymer; ceramics; glass; a composite comprising a polymer and fiberglass; quartz; silicon; or a combination of two or more thereof.
70. The process of claim 67 wherein the microchannel reactor has an entrance and an exit, the product exits the microchannel reactor through the exit, the product being intermixed with unreacted components from the reactant composition, and at least part of the unreacted components from the reactant composition are recycled to the entrance to the microchannel reactor.
71. The process of claim 67 wherein the reactant composition enters the process microchannels and the product exits the process microchannels, the temperature of the reactant composition entering the process microchannels being within about 200° C. of the temperature of the product exiting the process microchannels.
72. The process of claim 67 wherein the mole ratio of H2 to CO in the reactant composition is in the range of about 0.8 to about 10.
73. The process of claim 67 wherein the reactant composition further comprises H2O, CO2, a hydrocarbon of 1 to about 4 carbon atoms, or a mixture of two or more thereof.
74. The process of claim 67 wherein the contact time of the reactant composition and/or product with the catalyst is up to about 2000 milliseconds.
75. The process of claim 67 wherein the temperature of the reactant composition entering the process microchannels is in the range of about 150° C. to about 270° C.
76. The process of claim 67 wherein the pressure within the process microchannels is at least about 5 atmospheres.
77. The process of claim 67 wherein the conversion of CO is about 40% or higher.
78. The process of claim 67 wherein the regenerating fluid comprises hydrogen.
79. The process of claim 67 wherein the regenerating fluid comprises hydrogen and a diluent, the diluent comprising nitrogen, argon, helium, methane, carbon dioxide, steam, or a mixture of two or more thereof.
80. The process of claim 67 wherein the reactant composition comprises a product of a steam reforming process, autothermal reforming process, carbon dioxide reforming process, coal gasification process, or a combination of two or more thereof.
81. The process of claim 67 wherein the reactant composition comprises a product of a coal gasification process.
82. The process of claim 1 wherein at least part of the product is hydrocracked.
83. The process of claim 67 wherein at least part of the product is hydrocracked.
84. A process for converting a reactant composition comprising H2 and CO to a product comprising at least one aliphatic hydrocarbon having at least about 5 carbon atoms, the process comprising:
hydrocracking at least part of the product.
85. The process of claim 84 wherein the heat exchanger comprises a plurality of heat exchange channels.
86. The process of claim 84 wherein the microchannel reactor has an entrance and an exit, the product exits the microchannel reactor through the exit, the product being intermixed with unreacted components from the reactant composition, and at least part of the unreacted components from the reactant composition are recycled to the entrance to the microchannel reactor.
87. The process of claim 84 wherein the reactant composition enters the process microchannels and the product exits the process microchannels, the temperature of the reactant composition entering the process microchannels being within about 200° C. of the temperature of the product exiting the process microchannels.
88. The process of claim 84 wherein the mole ratio of H2 to CO in the reactant composition is in the range of about 0.8 to about 10.
89. The process of claim 84 wherein the reactant composition further comprises H2O2, CO2, a hydrocarbon of 1 to about 4 carbon atoms, or a mixture of two or more thereof.
90. The process of claim 84 wherein
91. The process of claim 84 wherein the heat exchanger comprises a plurality of heat exchange channels and an endothermic process is conducted in the heat exchange channels.
92. The process of claim 91 wherein the endothermic process comprises a steam reforming reaction or a dehydrogenation reaction.
93. The process of claim 84 wherein
94. The process of claim 84 wherein the heat exchanger contains a heat exchange fluid and the heat exchange fluid comprises air, steam, liquid water, carbon dioxide, gaseous nitrogen, a gaseous hydrocarbon or a liquid hydrocarbon.
95. The process of claim 84 wherein the catalyst further comprises Fe, Ni, Ru, Re, Os, or an oxide thereof, or a mixture of two or more thereof.
96. The process of claim 84 wherein the catalyst comprises a promoter selected from a metal from Group IA, IIA, IIIB or IIB of the Periodic Table or an oxide thereof, a lanthanide metal or oxide, an actinide metal or oxide, or a combination of two or more thereof.
97. The process of claim 84 wherein the catalyst comprises a promoter selected from the group consisting of Li, B, Na, K, Rb, Cs, Mg, Ca, Sr, Ba, Sc, Y, La, Ac, Ti, Zr, La, Ac, Ce or Th, or an oxide thereof, or a mixture of two or more thereof.
98. The process of claim 84 wherein the support is selected from alumina, zirconia, silica, aluminum fluoride, fluorided alumina, bentonite, ceria, zinc oxide, silica-alumina, silicon carbide, a molecular sieve, or a combination of two or more thereof.
99. The process of claim 84 wherein the catalyst comprises a refractory oxide support.
100. The process of claim 84 wherein the catalyst comprises a composition represented by the formula
101. The process of claim 84 wherein the catalyst has a Co loading of at least about 25% by weight.
102. The process of claim 101 wherein the catalyst further comprises Re, Ru or a mixture thereof.
103. The process of claim 84 wherein the catalyst is supported by a support structure made of a material comprising an alloy comprising Ni, Cr and Fe, or an alloy comprising Fe, Cr, Al and Y.
104. The process of claim 84 wherein the catalyst is supported on a support structure having a flow-by configuration, a flow-through configuration, or a serpentine configuration.
105. The process of claim 84 wherein the catalyst is supported on a support structure having the configuration of a foam, felt, wad, fin, or a combination of two or more thereof.
106. The process of claim 84 wherein the catalyst comprises a fixed bed of particulate solids.
107. The process of claim 84 wherein the catalyst is supported on a support structure in the form of a fin assembly comprising at least one fin.
108. The process of claim 84 wherein the process microchannels have a bulk flow path comprising about 5% to about 95% of the cross sections of such process microchannels.
109. The process of claim 84 wherein the contact time of the reactant composition and/or product with the catalyst is up to about 2000 milliseconds.
110. The process of claim 84 wherein the temperature of the reactant composition entering the process microchannels is in the range of about 150° C. to about 270° C.
111. The process of claim 84 wherein the pressure within the process microchannels is at least about 5 atmospheres.
112. The process of claim 84 wherein the space velocity for the flow of the reactant composition and product through the process microchannels is at least about 1000 hr−1.
113. The process of claim 84 wherein the pressure drop for the flow of the reactant composition and product through the process microchannels is up to about 10 atmospheres per meter of length of the process microchannels.
114. The process of claim 84 wherein
115. The process of claim 84 wherein the conversion of CO is about 40% or higher.
116. The process of claim 84 wherein the yield of product is about 25% or higher.
117. The process of claim 84 wherein the conversion of CO is at least about 50%, the selectivity to methane in the product is about 15% or less, and the yield of product is at least about 35%.
118. The process of claim 84 wherein the catalyst is in the form of particulate solids, the median particle diameter of the particulate solids is in the range of about 1 to about 1000 μm.
119. The process of claim 84 wherein the product comprises hydrocarbons boiling at a temperature at or below about 350° C. at atmospheric pressure.
120. The process of claim 84 wherein the product comprises hydrocarbons boiling at or above a temperature of about 350° C. at atmospheric pressure.
121. The process of claim 84 wherein the product comprises a middle distillate.
122. The process of claim 84 wherein the product comprises at least one olefin.
123. The process of claim 84 wherein the product comprises a normal paraffin, isoparaffin, or mixture thereof.
124. The process of claim 84 wherein at least part of the product is further processed using hydroisomerizing or dewaxing.
125. The process of claim 84 wherein at least part of the product is further processed to form a lubricating base oil or a diesel fuel.
126. The process of claim 84 wherein the process microchannels are vertically oriented, the reactant composition and product flow downwardly through the process microchannels.
127. The process of claim 84 wherein subsequent to removing the product from the microchannel reactor, a regenerating fluid flows through the process microchannels in contact with the catalyst.
128. The process of claim 127 wherein the regenerating fluid comprises hydrogen.
129. The process of claim 127 wherein the regenerating fluid comprises hydrogen and a diluent, the diluent comprising nitrogen, argon, helium, methane, carbon dioxide, steam, or a mixture of two or more thereof.
130. The process of claim 84 wherein the reactant composition comprises a product of a steam reforming process, autothermal reforming process, carbon dioxide reforming process, coal gasification process, or a combination of two or more thereof.
131. The process of claim 84 wherein the reactant composition comprises a product of a coal gasification process.
132. The process of claim 1 wherein the microchannel reactor includes a header to provide a passageway for fluid to flow into the process microchannels and a footer to provide a passageway for fluid to flow out of the process microchannels, the regenerating fluid flowing from the header through the process microchannels to the footer.
133. The process of claim 1 wherein the microchannel reactor includes a header to provide a passageway for the reactant composition to flow into the process microchannels and a footer to provide a passageway for the reactant composition to flow out of the process microchannels, the regenerating fluid flowing subsequent to the flow of the reactant composition in an opposite direction to the flow of the reactant composition from the footer through the process microchannels to the header.
134. The process of claim 1 wherein the temperature of the regenerating fluid is in the range from about 50° C. to about 400° C.
135. The process of claim 1 wherein the pressure in the process microchannels during the regenerating step is in the range from about 1 to about 40 atmospheres.
136. The process of claim 67 wherein the residence time for the regenerating fluid in the process microchannels is from about 0.01 to about 1000 seconds.
137. The process of claim 67 wherein the microchannel reactor includes a header to provide a passageway for fluid to flow into the process microchannels and a footer to provide a passageway for fluid to flow out of the process microchannels, the regenerating fluid flowing from the header through the process microchannels to the footer.
138. The process of claim 67 wherein the microchannel reactor includes a header to provide a passageway for the reactant composition to flow into the process microchannels and a footer to provide a passageway for the reactant composition to flow out of the process microchannels, the regenerating fluid flowing subsequent to the flow of the reactant composition in an opposite direction to the flow of the reactant composition from the footer through the process microchannels to the header.
139. The process of claim 67 wherein the temperature of the regenerating fluid is in the range from about 50° C. to about 400° C.
140. The process of claim 67 wherein the pressure in the process microchannels during the regenerating step is in the range from about 1 to about 40 atmospheres.
4738948 April 19, 1988 Iglesia
5036032 July 30, 1991 Iglesia et al.
5382741 January 17, 1995 Astbury et al.
5733839 March 31, 1998 Epinoza et al.
6090742 July 18, 2000 Cultross
6121190 September 19, 2000 Zennaro et al.
6136868 October 24, 2000 Culross et al.
6156698 December 5, 2000 Iida et al.
6319872 November 20, 2001 Manzer et al.
6353035 March 5, 2002 Manzer et al.
6368997 April 9, 2002 Herron et al.
6476085 November 5, 2002 Manzer et al.
6491880 December 10, 2002 Gao et al.
7045486 May 16, 2006 Wang et al.
7084180 August 1, 2006 Wang
7722833 May 25, 2010 Wang et al.
7829602 November 9, 2010 Litt et al.
8188153 May 29, 2012 Wang
9006298 April 14, 2015 LeViness
9023900 May 5, 2015 Wang
20020048541 April 25, 2002 Schodel et al.
20020173556 November 21, 2002 Moore, Jr.
20020188031 December 12, 2002 Kibby
20030105171 June 5, 2003 Subramanian et al.
20150210606 July 30, 2015 LeViness
2002501430 January 2002 JP
2002126498 May 2002 JP
97/32687 December 1997 WO
98/55812 October 1998 WO
1096015 December 2001 WO
02064248 August 2002 WO
03/006149 January 2003 WO
WO 03/006149 January 2003 WO
03/099429 April 2003 WO
03078052 September 2003 WO
Schmidt (2014. Hydrocarbons. Ullmann's Encyclopedia of Industrial Chemistry. 1-74).
Post (“Diffusion Limitations in Fischer-Tropsch Catalysts” AIChE Journal, 35(7), 1989, p. 1107-1114).
Anderson; “The Fischer-Tropsch Synthesis”; Academic Press, Inc.; 1984, pp. 1-7.
Avila et al.; “Monolithic reactors for environmental applications A review on preparation technologies”; Chemical Engineering Journal 109 (2005); pp. 11-36.
Chaston; “The Oxidation of the Platinum Metals”; Platinum Metals Rev., 1975, 19, (4), pp. 135-140.
Deng et al.; “Characterisation of alumina scales on Fecralloy using impedance spectroscopy”; Thin Solid Films 516 (2008); pp. 5027-5031.
ERG Materials and Aerospace Corporation; “Metal Foam Introduction” (2010), http://www.ergaerospace.com/metal—foam.htm.
Gandhi et al.; “Automotive exhaust catalysis”; Journal of Catalysis 216 (2003); pp. 433-442.
Giroux et al.; “Monolithic structures as alternatives to particulate catalysts for the reforming of hydrocarbons for hydrogen generation”; Applied Catalysis B; Environmental 56 (2005); pp. 95-110.
Irandoust et al.; “Monolithic Catalysts for Nonautomobile Applications”; Catal. Rev.—Sci. Eng., 30(3), 341-392 (1988).
Queheillalt et al.; “Synthesis of open-cell metal foams by template directed vapor deposition”; J. Mater. Res., vol. 16, No. 4, Apr. 2001, pp. 1028-1036.
Chinese Office Action, Application No. 200480041082.9, issued Aug. 22, 2008.
Australian Office Action, Application No. 2004315214, dated Jun. 17, 2009.
Australian Office Action, Application No. 2004315214, dated Apr. 8, 2010.
Dohntec Ceramics Ltd.; “Corderite Honeycomb Monolith,” (2010); http://www.random-packing.com/product/27-cordierite-honeycomb-monolith-12-d3f5.
Catacel Corporation, “SMR catalyst Reaches 17,500 Hour Benchmark,” Thomas Net News, (2010), http://news.thomasnet.com/companystory/Catacel-s-Novel-SMR-Catalyst-Reaches-17-500- . . . .
Notice of Allowance, Chinese Application 200480041082.9, issued Jun. 5, 2009.
Issue Notification, U.S. Pat. No. 7,084,180, mailed Jul. 12, 2006.
Notice of Allowance, U.S. Appl. No. 10/766,297, mailed Mar. 31, 2006.
Office Action, U.S. Appl. No. 10/766,297, mailed Dec. 16, 2005.
Office Action, U.S. Appl. No. 10/766,297, mailed Sep. 21, 2005.
Issue Notification, U.S. Pat. No. 7,722,833, mailed May 5, 2010.
Notice of Allowance, U.S. Appl. No. 11/484,069, mailed Dec. 15, 2009.
Office Action, U.S. Appl. No. 11/484,069, mailed May 11, 2009.
Office Action, U.S. Appl. No. 11/484,069, mailed Jan. 28, 2009.
Office Action, U.S. Appl. No. 90/011,089, mailed Jan. 13, 2011.
Third-Party Requestor's Response to the Patent Owner's Statement, U.S. Appl. No. 90/011,089, filed Dec. 21, 2010.
Patent Owner's Statement in Response to Order Granting Request for Ex Parte Reexamination, U.S. Appl. No. 90/011,089, filed Oct. 22, 2010.
Office Action, U.S. Appl. No. 90/011,089, mailed Sep. 1, 2010.
Transmittal of Replacement Statement and Replacement 1449 Associated with Request for Ex Parte Reexamination, U.S. Appl. No. 90/011,089, filed Jul. 23, 2010.
Request for Ex Parte Reexamination Transmittal Form and Request for Ex Parte Reexamination of U.S. Pat. No. 7,084,180, filed Jul. 9, 2010.
Lekhal et al.; “Impact of Drying on the Catalyst Profile in Supported Impregnation Catalysts”; Chemical Engineering Science 56 (2001); 4473-4487.
Matlosz et al.; “Microreactors as Tools in Chemical Research”; Microreaction Technology; IMRET 5: Proceedings of the Fifth International Conference on Microreaction Technology. 2001.
Waku et al.; “Effects of O2 Concentration on the Rate and Selectivity in Oxidative Dehydrogenation of Ethane Catalyzed by Vanadium Oxide: Implications for O2 Staging and Membrane Reactors”; Ind. Eng. Chem. Res., 2003, 42, 5462-5466.
Stranges; “Germany's Synthetic fuel Industry 1927-45”; AIChE 2003 Spring National Meeting, New Orleans, LA, 2003.
Kuila; “Characterization of Alumina and Silica Sol-Gel Encapsulated Fe/Co/Ru Nanocatalysts in Microchannel Reactors for F-T Synthesis of Higher Alkanes”; Mat. Res. Soc. Synp. Proc. vol. 280, Materials Research Society; MRS Spring Meeting, San Francisco, CA, 2004.
Mazanec; “Microchannel technology for gas-to-liquids conversion”; PTQ, Oct. 2003; pp. 149-153.
Hoek; “The Shell Middle Distillate Synthesis Process—Facts, Technology and Perspective”; Presented at CatCon, Houston, TX, May 2003.
Office Action, U.S. Appl. No. 90/011,089, mailed Jun. 9, 2011.
European office action, Application No. 04 814 270.7-2014, dated Mar. 21, 2011.
Japanese Office Action, Application No. 2006-551076, dated Feb. 22, 2011.
Canadian Office Action, Application No. 2,552,283, dated Feb. 28, 2011.
U.S. Appl. No. 90/011,089; Litigation Search Report dated Sep. 13, 2011.
U.S. Appl. No. 90/011,089, Notice of Intent to Issue Ex Parte Reexamination Certificate mailed Sep. 26, 2011.
European Office Action, Application No. 04 814 270.7, dated Apr. 24, 2013.
Bennett et al.; “Microchannel cooled heatsinks for high average power laser diode arrays”; SPIE, vol. 1865; 1993; pp. 144-153.
Canadian Office Action, Application No. 2,552,283, dated Dec. 2, 2011.
Japanese Patent Office Notification of Reasons for Refusal, Application No. 2006-551076, mailed Sep. 13, 2011.
Japanese Application 2006-551076, Office Action Dated Sep. 4, 2012, English language translation.
European Application 04814270.7-2014, Office Action dated Mar. 21, 2011.
Russian Application 2006130871 (033542), Office Action dated Jul. 4, 2011, with English language translation.
Russian Application 2006130871 (033542), Office Action dated Feb. 7, 2008, with English language translation.
Jacobs et al.; “Fischer-Tropsch synthesis: support, loading, and promoter effects on reducibility of cobalt catalysts”; Applied Catalysis A: General 233; 2002; pp. 263-281.
Russian Office Action, Application No. 2006130871, received Sep. 19, 2012.
Australian Office Action, Application No. 2010202533, issued Oct. 17, 2012.
Australian Office Action, Application No. 2010202533, dated Oct. 19, 2011.
European Office Action, Application No. 04814270.7, dated Mar. 21, 2011.
Canadian Office Action, Application No. 2,552,283, dated Jul. 9, 2012.
Japanese Office Action, Application No. 2006-551076, dated Sep. 13, 2011.
Japanese Questioning, Application No. 2006-551076, mailed May 21, 2013.
Extended European Search Report, Application No. 13160226.0, dated May 7, 2013.
EP Communication purusant to ARticle 94(3) EPC, Application No. 04814270.7, dated Apr. 24, 2013.
Notice of Allowance, Canadian Patent Application No. 2,552,283, dated May 3, 2013.
Extended European Search Report, Applicatin No. 13160227.8, dated May 7, 2013.
European Search Report for corresponding Application No. 15170565.4 dated Nov. 17, 2015.
Patent Publication Number: 20150259609
Inventors: Yong Wang (Richland, WA), Anna Lee Tonkovich (Gilbert, AZ), Terry Mazanec (Solon, OH), Francis P. Daly (Delaware, OH), Dave VanderWiel (Brecksville, OH), Jianli Hu (Kennewick, WA), Chunshe Cao (Kennewick, WA), Charles Kibby (Benicia, CA), Xiaohong Li (Richland, WA), Michael D. Briscoe (Katy, TX), Nathan Gano (Dublin, OH), Ya-Huei Chin (Richland, WA)
Application Number: 14/700,197
Current U.S. Class: 252/466
International Classification: C10G 2/00 (20060101); B01J 23/75 (20060101); B01J 19/00 (20060101); B01J 37/03 (20060101); B01J 38/48 (20060101); B01J 35/04 (20060101); C10G 45/58 (20060101); C10G 47/00 (20060101); B01J 23/94 (20060101); B01J 37/02 (20060101); B01J 23/755 (20060101); B01J 23/83 (20060101); B01J 23/889 (20060101); B01J 23/89 (20060101); B01J 35/00 (20060101); B01J 35/10 (20060101); C10G 21/00 (20060101); C10L 1/08 (20060101); C10M 105/04 (20060101); B01J 38/58 (20060101);