TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Components: The produced mixture contains condensable hydrocarbons with an API gravity of at least 25degrees; 0.05 wt.% ammonia; non-condensable hydrocarbons; hydrogen sulfide (H2S); carbon dioxide (CO2); and the average carbon number less than 30. The ammonia is used to produce fertilizer. The non-condensable and condensable hydrocarbons contain 0.1-15 wt.% olefins. The non-condensable hydrocarbons have an ethene to ethane molar ratio of 0.001-0.15. The condensable hydrocarbons contain less than 1 wt.% nitrogen when calculated on an atomic basis, 5-30 wt.% oxygen containing compounds, 20 wt.% aromatic compounds, less than 5 wt.% multi-rings aromatics with more than two rings, less than 0.3 wt.% asphaltenes, 5-30 wt.% cycloalkanes, and hydrogen.The oxygen containing compounds comprises phenols. The hydrogen is greater than 10 and less than 80 vol.% of the non-condensable component. The synthesis gas generating fluid comprises liquid water or steam, or water and CO2, or water and hydrocarbons having carbon numbers less than 5 or greater than 4. The heat transfer fluid comprises steam.    TECHNOLOGY FOCUS - CHEMICAL ENGINEERING - Preferred Method: Superposition of heat from at least the two heat sources pyrolyzes at least some hydrocarbons within the selected section of the formation. The controlling step includes maintaining a temperature within the selected section in a pyrolysis temperature range, and recirculating a portion of hydrogen from the mixture into the formation. A pressure and a temperature are controlled within at least a majority of the selected section. The pressure is controlled as a function of temperature or vice versa. It is controlled within at least the majority of the selected section with a valve coupled to at least one of the heat sources, or coupled to a production well (825) located in the formation. It is changed within the formation to inhibit production of hydrocarbon from the formation having carbon numbers greater than 25.The H2 is provided to the heated section to hydrogenate hydrocarbons within the section. The portion of the section is heated with heat from hydrogenation. The heat is controlled so that an average heating rate of the section is less than 1degreesC/day during pyrolysis. It is controlled to yield greater than 60 wt.% condensable hydrocarbons, as measured by a Fischer Assay. The producing step includes producing the mixture in the production well, where at least 7 heat sources are positioned in the formation for each well.The providing step includes heating a selected volume (V) of the hydrocarbon containing formation from the heat sources, where the formation has an average heat capacity (Cv), and heating the section such that a thermal conductivity of at least a portion of the section is greater than 0.5 W/(mdegreesC). The heating pyrolyzes at least some hydrocarbons within the selected volume of the formation. It is controlled so that the mixture can be produced from the formation as a vapor. The heating energy/day (Pwr) provided to the volume is equal to or less than Pwr which is calculated by the equation: Pwr=hasteriskVasteriskCvasteriskrhob, where h is an average heating rate of the formation, rhob is a formation bulk density, and the heating rate is less than 10degreesC/day.The allowing step includes transferring heat by conduction, and increasing the permeability of the majority of the section to greater than 100 millidarcy or uniformly increasing the permeability of the majority of the section. The partial pressure of H2 is measured when the mixture is at the production well. A portion of the produced condensable hydrocarbons is hydrogenated with at least a portion of the produced hydrogen. Three or more heat sources are located in the formation in a unit of heat sources comprising a triangular pattern. The units are repeated over an area of the formation to form a repetitive pattern of units. The produced mixture is separated into a gas stream and a liquid stream. The liquid stream is separated into an aqueous stream and a non-aqueous stream. Portion of the H2S and the CO2 are separated from the non-condensable hydrocarbons, respectively.A wellbore of the production well is heated to inhibit condensation of the mixture within the wellbore. The pressure is maintained within the formation above 2 bar absolute to inhibit production of fluids with carbon numbers greater than 25. The pressure is controlled within the formation from atmospheric pressure to 100 bar, as measured at a wellhead of the well, to control an amount of or the API gravity of condensable hydrocarbons within the produced mixture. The pressure is reduced to increase production of condensable hydrocarbons or to decrease the API gravity and where the pressure is increased to increase production of non-condensable hydrocarbons or to reduce the API gravity. The permeability of the section is greater than 100 millidarcy when the temperature to allow synthesis gas generation within the formation is achieved.The method of in situ synthesis gas production includes monitoring a composition of the produced synthesis gas; controlling heating of the section and provision of the synthesis gas generating fluid to maintain the composition of the produced synthesis gas within a selected range comprising a ratio of H2 to CO of 2:1; maintaining a pressure within the formation during synthesis gas generation; and passing produced synthesis gas through a turbine to generate electricity. A portion of the CO2 reacts with carbon in the formation to generate CO. The synthesis gas is removed from a producer well equipped with the heating source. A portion of the heating source adjacent to a synthesis gas producing zone operates at constant temperature (preferably 700degreesC) to promote production of the synthesis gas having selected composition.At least a portion of the hydrocarbons are subjected to a reaction within the section to increase a concentration of the generated synthesis gas or to increase an energy content of the synthesis gas removed from the formation. At least a portion of carbon-containing material in the first portion is removed from the formation. It is used in a metallurgical application comprising steel manufacturing. Electricity is generated from the synthesis gas using a fuel cell. The CO2 is separated from a fluid exiting the fuel cell. A portion of the separated CO2 is stored within a spent section of the formation. At least a portion of the produced synthesis gas is converted to condensable hydrocarbons using a Fischer-Tropsch synthesis process, to methanol or gasoline, or to methane using a catalytic methanation process.A ratio of H2 to N2 (nitrogen) of 3:1 (preferably 2.8:1-3.2:1) is provided to the ammonia synthesis gas process. At least a portion of the N2 rich stream is used to condense hydrocarbons with 4 or more carbon atoms from a pyrolyzation fluid (807). The air is separated by cryogenic distillation. At least a portion of the ammonia is provided to a urea synthesis process to produce urea.The produced mixture has a partial pressure of H2 within the mixture greater than 0.5 bar. The minimum pyrolysis temperature is 270degreesC. The temperature to alloy synthesis gas generation ranges from 400-1200degreesC.    TECHNOLOGY FOCUS - MECHANICAL ENGINEERING - Preferred Components: The heat sources comprises electrical heaters (803), surface burners, flameless distributed combustors, or natural distributed combustors. The wellbore comprises a heater element configured to heat the formation adjacent to the wellbore. The conduit comprises orifices configured to provide the oxidizing fluid into the opening, or critical flow orifices configured to control a flow of the oxidizing fluid comprising air, thus controlling an oxidation rate of the formation. The conduit is further configured to be cooled with the oxidizing fluid such that the conduit is not heated by oxidation, or further configured to remove an oxidation product such that the oxidation product transfers heat to the oxidizing fluid.The oxidizing fluid is configured to generate heat in the reaction zone, so that the oxidizing fluid is transported through the reaction zone by diffusion. The system includes a center conduit within the conduit, a conductor in a second conduit or an insulated conductor within the opening, a heat exchanger configured to heat the oxidizing fluid, and overburden casing coupled to the opening and disposed in an overburden of the formation. The center conduit is configured to provide the oxidizing fluid into the opening during use. The second conductor is configured to heat at least the portion of the formation during application of an electrical current to the conductor. The overburden casing is further positioned in cement, and comprises steel. A packing material is positioned at a junction of the overburden casing and the opening. A flow rate of the oxidizing fluid is equal to a flow rate of the oxidation product in the conduit.    TECHNOLOGY FOCUS - ELECTRICAL POWER AND ENERGY - Preferred Component: The fuel cell is a molten carbonate fuel cell, or a solid oxide fuel cell.