TECHNOLOGY FOCUS - INORGANIC CHEMISTRY - Preferred Components: The SMR catalyst comprises La, Pt, Fe, Ni, Ru, Rh, In, Ir, W, and/or their oxide. The SMR catalyst further comprises MgO, Al2O3, SiO2 and/or TiO2. The combustion catalyst comprises Pd, Pr, Pt, Rh, Ni, Cu, and/or their oxides; and further comprises Al2O3, SiO2, and/or MgO. The Fischer-Tropsch catalyst comprises at least one Co, Fe, Ni, Ru, Re, Os, and/or their oxides; or at least one metal selected from Group IA, IIA, IIIB or IIB of the Periodic Table and/or their oxides, lanthanide metal and/or their oxides, actinide metal and/or their oxide. The SMR catalyst, combustion catalyst and/or Fischer-Tropsch catalyst is in the form of particulate solids.    TECHNOLOGY FOCUS - INSTRUMENTATION AND TESTING - Preferred Components: The SMR process microchannel has at least one heat transfer wall and the heat flux for heat exchange within the SMR microchannel reactor is 0.01-500 watts per square centimeter of surface area of the heat transfer walls; has a first part (where the temperature is 150-400 degrees C), and a second part downstream of the first part (where the temperature is 600-1000 degrees C); has at least one heat transfer wall and the heat flux for heat exchange within the Fischer-Tropsch microchannel reactor is 0.01-500 watts per square centimeter of surface area of the heat transfer walls. The SMR catalyst, combustion catalyst and/or Fischer-Tropsch catalyst is coated on interior walls of the channels, grown on interior walls of the channels, or coated on a fin structure; is supported on a support structure having a flow-by configuration, flow-through configuration, or serpentine configuration; is supported on a support structure having the configuration of a foam, felt, wad and/or fin; or is supported a support on a structure in the form of a fin assembly comprising at least one fin.    TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: The process (M1) further involves: flowing the third intermediate product in a second Fischer-Tropsch microchannel reactor in contact with at least one second Fischer-Tropsch catalyst to form a second Fischer-Tropsch product comprising at least one higher molecular weight hydrocarbons; flowing the SMR feed and steam in a pre-reformer to convert at least some of the higher molecular weight hydrocarbons in the SMR feed to methane (where the pre-reformer being upstream of the SMR microchannel reactor or being integrated with the SMR microchannel reactor and being heated by heat from the combustion channels); and flowing the SMR feed and steam in the SMR process microchannels at a first temperature in a first part of the SMR process microchannels to convert at least some of the higher molecular weight hydrocarbons in the SMR feed to methane (where the resulting product comprises a modified SMR feed comprising methane), and flowing the modified SMR feed in a second part of the SMR process microchannels at a second temperature to convert the modified SMR feed to the first intermediate product. The third intermediate product contacts the second Fischer-Tropsch catalyst in the second Fischer-Tropsch process microchannel; and transfers heat from the second Fischer-Tropsch process microchannel to a heat exchange fluid in the second heat exchange channel. The SMR feed is derived from a natural gas feed, and a tail gas is formed in the Fischer-Tropsch microchannel reactor (where at least part of the tail gas being combined with the natural gas feed); is derived from a natural gas feed, and process water is formed in the Fischer-Tropsch microchannel reactor (where at least a portion of the process water being combined with the natural gas feed); is derived from a natural gas feed, and process water which is formed in the Fischer-Tropsch microchannel reactor and which is combined with the natural gas feed, and tail gas which is formed in the Fischer-Tropsch microchannel reactor and at least part of the tail gas is combined with the natural gas feed; is derived from a natural gas feed, and a tail gas is formed in the second Fischer-Tropsch microchannel reactor (where at least part of the tail gas being combined with the natural gas feed); is derived from a natural gas feed, and a tail gas is formed in the Fischer-Tropsch microchannel reactor (where the tail gas comprises H2, CO, CO2 and at least one hydrocarbon, the tail gas flows through an H2 separator to provide a carbon rich tail gas and an H2 rich tail gas, the carbon rich tail gas being combined with the natural gas feed, the H2 rich tail gas being used as a fuel); is derived from a natural gas feed, and a tail gas is formed in the Fischer-Tropsch microchannel reactor (where the tail gas comprises H2, N2, CO, CO2 and at least one hydrocarbon, the tail gas flows through an H2 separator to provide a carbon rich tail gas and H2 rich tail gas, the carbon rich tail gas comprises N2, the carbon rich tail gas flows through a nitrogen separator, where N2 is separated from the carbon rich tail gas, the carbon rich tail gas being combined with the natural gas feed, the H2 rich tail gas being used as a fuel); is derived from a natural gas feed, and a tail gas is formed in the Fischer-Tropsch microchannel reactor and at least part of the tail gas is combined with the natural gas feed (where at least part of the tail gas being compressed prior to being combined with the natural gas feed). The staged addition channels are positioned adjacent to the combustion channels (where the oxygen source of oxygen flowing through to the staged addition channels into the combustion channels). The tail gas is formed in the Fischer-Tropsch microchannel reactor (where the tail gas comprises N2, the tail gas flows through a nitrogen separator, where N2 is separated from the tail gas). The pressure in the second Fischer-Tropsch process microchannels is different than the pressure in the Fischer-Tropsch process microchannels. The second intermediate product is compressed prior to second step. The Fischer-Tropsch product is further processed using hydrocracking, hydroisomerizing or dewaxing. The H2 is separated from the first intermediate product using temperature swing adsorption, pressure swing adsorption and/or membranes. The temperature swing adsorption and/or pressure swing adsorption, membranes is used to separate the carbon rich tail gas from the H2 rich tail gas; is used to separate the N2 from the tail gas; is used to separate H2 from the tail gas and to separate N2 from the carbon rich tail gas. The process (M1) involves use of at least one multi-stream heat exchanger which provide for exchange of heat between the SMR feed and first intermediate product, and H2 and the oxygen or source of oxygen of the combustion reaction mixture and the combustion exhaust. Preferred Components: The Fischer-Tropsch product formed in second step further comprises a gaseous mixture comprising CO and H2. The gaseous mixture is separated from the Fischer-Tropsch product. The separated gaseous mixture comprises a third intermediate product. The second Fischer-Tropsch microchannel reactor comprises several second Fischer-Tropsch process microchannels and several second heat exchange channels. The second Fischer-Tropsch process microchannels contains at least one second Fischer-Tropsch catalysts. The natural gas feed, process water and tail gas are combined in a saturator. The saturator is upstream of the SMR microchannel reactor. The SMR feed comprises at least one higher molecular weight hydrocarbons. The combustion exhaust comprises a vapor and a liquid comprising water. The vapor is separated from the liquid in a vapor-liquid separator. The heat exchange fluid in the heat exchange channels is at least partially vaporized in the heat exchange channels. The Fischer-Tropsch product comprises at least one paraffin and/or at least one 5-100C olefin. The ratio of olefins to paraffins is 0.01-0.8. The natural gas is used in the formation of the SMR feed (where the percent of carbon in the Fischer-Tropsch product relative to carbon in the natural gas is 50-70%; or the overall percent of carbon in the first and second Fischer-Tropsch products relative to carbon in the natural gas is at least 75%). The Fischer-Tropsch product and/or second Fischer-Tropsch product is hydrocracked in a hydrocracker operated in series with the Fischer-Tropsch microchannel reactor and/or second Fischer-Tropsch microchannel reactor. EXAMPLE - No suitable example given.