NOVELTY - Producing fermented product involves introducing fuel stream having reformable fuel into anode of molten carbonate fuel cell, and/or internal reforming element associated with the anode; introducing cathode inlet stream having CO2 and O2 into cathode of the fuel cell; forming electricity within the fuel cell; separating from the anode exhaust H2-containing stream (485), and/or syngas-containing stream; processing biomass to form fermentation product and fermentation exhaust; and distilling the fermentation product.    USE - For producing a fermented product, where the fermentation product comprises ethanol (claimed).    ADVANTAGE - The process uses no external energy source and emits CO2 only derived from biological processes. The CO2 separation scheme is added at any of various points, such as after the anode and/or after all the CO2 streams are combined. This stage provides pure CO2 output stream for sequestration and/or for some other use. In this configuration, the overall plant CO2 emissions, from a life-cycle basis, is negative (less than zero net CO2 produced), as biologically derived CO2 is removed for sequestration with proportionally fewer (without any) external carbon-based fuel inputs.    DETAILED DESCRIPTION - Producing fermented product involves introducing a fuel stream comprising a reformable fuel into an anode of a molten carbonate fuel cell, and/or internal reforming element associated with the anode; introducing a cathode inlet stream comprising CO2 and O2 into a cathode of the fuel cell; generating electricity within the molten carbonate fuel cell; separating from the anode exhaust an H2-containing stream (485), and/or a syngas-containing stream; processing biomass to produce at least one fermentation product and a fermentation exhaust; and distilling the fermentation product, at least some heat for distillation is provided by heat exchange with the anode exhaust, combustion of the syngas-containing stream, combustion of the H2-containing stream, electric heating using the electricity generated within the molten carbonate fuel cell. The method further involves at least one of the following: the cathode inlet stream comprises at least a portion of the fermentation exhaust; the processing step is done in the presence of H2O separated from the anode exhaust, H2O separated from the syngas-containing stream, and/or H2O separated from the H2-containing stream; the reformable fuel comprises a portion of the fermentation product, the reformable fuel optionally containing at least 50 vol.% of the fermentation product, the portion of the fermentation product optionally is a distilled portion of the fermentation product having a water to carbon ratio of 1.5:1 to 3:1; the processing step involves separating fermentable biomass portion from non-fermentable biomass portion, the non-fermentable biomass portion is processed in at least one thermal, chemical, and/or thermochemical process in the presence of at least a portion of the H2-containing gas stream, and/or at least a portion of the syngas-containing stream; an amount of the reformable fuel introduced into the anode of the fuel cell, and/or the internal reforming element associated with the anode of the fuel cell, provides a reformable fuel surplus ratio of at least 2; a reformable hydrogen content of reformable fuel introduced into the anode of the fuel cell, and/or the internal reforming element associated with the anode of the fuel cell, is at least 50% greater than an amount of hydrogen oxidized to generate electricity; an electrical efficiency for the fuel cell is 10-40%, and a total fuel cell efficiency for the fuel cell is at least 55%; the fuel cell is operated at a thermal ratio of 0.25-1.5; a ratio of net moles of syngas in the anode exhaust to moles of CO2 in a cathode exhaust is at least 2, and optionally less than or equal to 40; a fuel utilization in the anode of the fuel cell is less than or equal to 50%, and a CO2 utilization in the cathode is at least 60%; the fuel cell is operated at a first operating condition to generate electrical power and at least 100 mW/cm2 of waste heat, the first operating condition providing a current density of at least 150 mA/cm2, and an effective amount of an endothermic reaction is performed to maintain a temperature differential between the anode inlet and an anode outlet of less than or equal to 80 degrees C; the fuel cell is operated at a voltage of 0.60-0.67 Volts, the fuel cell optionally is operated at a fuel utilization of less than or equal to 65%; the cathode inlet stream comprises at least a portion of a combustion turbine exhaust, at least a portion of the anode exhaust is recycled into the anode; the cathode inlet stream comprises at least a portion of a combustion turbine exhaust, at least a portion of the anode exhaust is used as an anode recycle fuel for a combustion zone (415) of the combustion turbine, an optional second fuel stream for the combustion zone of the combustion turbine optionally comprising at least 30 vol.% CO2 and/or at least 35 vol.% of a combination of CO2 and inerts; the cathode inlet stream comprises at least a portion of a combustion turbine exhaust, at least a first portion of the anode exhaust is used as an anode recycle fuel for a combustion zone of the combustion turbine, and at least a second portion of the anode exhaust is recycled into the anode of the fuel cell; the cathode inlet stream comprises at least a portion of a combustion turbine exhaust, the cathode inlet stream comprising at least 20 vppm of NOx, and a cathode exhaust comprising less than about half of the NOx content of the cathode inlet stream.    DESCRIPTION OF DRAWING(S) - The figure shows a schematic view of an integrated system including introduction of both CO2-containing recycled exhaust gas and H2 or CO from the fuel cell.    Compressor (402)    Shaft (404)    Expander (406)    Oxygen source (411)    Combustion zone (415)    Carbon dioxide containing stream (422)    Recycled exhaust gas (498)