TECHNOLOGY FOCUS - ORGANIC CHEMISTRY - Preferred Process: When the step (a) is performed in the presence of oxygen, then the amount of free oxygen is less than 10 (preferably 1, more preferably less than 0.5)%, or (preferably greater than 1, more preferably 2-8)% of the stoichiometric amount of oxygen to completely combust the feed material. The step (a) is optionally performed in the presence of added steam. The added steam is present in an amount of less than 50 (preferably less than 10)% of the stoichiometric amount of water to completely convert the feed material to carbon monoxide and hydrogen. A first amount of steam is present from initial moisture in the carbon-containing feed material, a second amount of steam is added during step (a), and the combined first amount and second amount of steam is less than or greater than the stoichiometric amount of water to completely convert the feed material to carbon monoxide and hydrogen. When the step (b) is performed in the presence of oxygen, then the amount of free oxygen is less than 25 (preferably less than 10, or 10-20)% of the stoichiometric amount of oxygen to completely combust the carbon contained in the solid phase produced in step (a). The step (b) is performed in the presence of steam, where an initial ratio of free oxygen to steam (O2/H2O) in step (b) is less than about 1 (preferably less than 0.5, or is 0.01-0.2). The step (a) is performed in the presence of a first amount of free oxygen that is 0.1-10 (preferably less than 1)% of the stoichiometric amount of oxygen to completely combust the feed material, and the step (b) is performed in the presence of a second amount of free oxygen that is 0.1-25 (preferably less than 10)% of the stoichiometric amount of oxygen to completely combust the carbon contained in the solid phase produced in step (a). The process (M1) further involves the substeps of: (i) measuring the composition of the gas phase and/or the solid phase, (ii) determining a suitable amount of free oxygen based on predicted partial oxidation of at least some of the composition to syngas, and (iii) introducing a gas containing the suitable amount of free oxygen. The step (a) is performed in the presence of a catalyst. The catalyst present during step (a) is selected from potassium, potassium hydroxide, and/or potassium carbonate. The step (b) is performed in the presence of a catalyst. The catalyst present during step (b) is selected from nickel, cobalt, rhodium, and/or their oxides. The residence times of the gas phase and the solid phase in step (a) are different. The gas phase is removed, at least in part, during step (a). The devolatilization unit is a multiple-stage unit in which both the gas phase and solid phase pass through at least one stage of the devolatilization unit and at least a portion of the gas phase is removed from the devolatilization unit prior to the final stage. The free oxygen is added to the first stage only. Different amounts of oxygen are added across the multiple stages of the devolatilization unit. The oxygen is added to the devolatilization unit prior to removal of at least a portion of the gas phase. After at least a portion of the gas phase is removed, oxygen is added to the devolatilization unit. A first amount of oxygen is added prior to removal of at least a portion of the gas phase, and a second amount of oxygen is added after removal of at least a portion of the gas phase. The first amount of oxygen is greater than the second amount of oxygen. Prior to step (b), the solid phase is combined with gas removed during step (a). The process further involves introduction of at least one inert gas after removal of at least a portion of the gas phase. The presence of free oxygen decreases the ratio of hydrogen to carbon monoxide in the syngas, compared to the ratio of hydrogen to carbon monoxide produced by the same method in the absence of oxygen. The ratio of hydrogen to carbon monoxide is about 0.75-1.5 (preferably 1-1.3). The process temperature in the devolatilization unit is greater than 900 degrees F at least at one point during step (a). The maximum process temperature in the devolatilization unit is less than 1400 degrees F. The process temperature in the heated reaction vessel is greater than 1400 degrees F at least at one point during step (b). The maximum process temperature in the heated reaction vessel is less than 2200 degrees F. The process further involves: (i) introducing a stream produced in step (a) to a reactor configured with an input for a gas comprising oxygen, where at least some of the stream is partially oxidized to produce additional syngas; and (ii) introducing at least some of a stream produced in step (b) to a reactor configured with an input for a gas comprising oxygen, where at least some of the stream is partially oxidized to produce additional syngas. EXAMPLE - No suitable example is given.