Disclosed is a method of operating an Alkaline Membrane Fuel Cell (AMFC) with direct ammonia feeding. The method may include providing AMFC comprising an anode inlet for receiving ammonia and a cathode inlet for receiving oxygen containing gas; operating the AMFC at an operation temperature of above 80° C.; providing the oxygen containing gas; to a cathode of the AMFC at a pressure above the equilibrium vapor pressure of water at the operation temperature; maintaining the pressure during the operation of the AMFC as to maintain water in substantially liquid phase near the cathode; and providing the ammonia to an anode of the AMFC.

The present disclosure relates generally to a carbon-neutral process for the generation of carbon-neutral hydrogen and carbon-neutral electricity. More specifically, the present disclosure relates to compositions, methods and apparatus employing a carbon-neutral process for generating electricity employing a liquid organic hydrogen carrier (LOHC) for supplying hydrogen for generating the carbon neutral electricity. The present disclosure also relates more specifically to carbon-neutral compositions consisting of liquid organic hydrogen carriers used for supplying hydrogen to generate electricity that may be regenerated in a carbon-neutral process using an apparatus with a net zero atmospheric emission of carbon oxides.

The present disclosure relates generally to a carbon-neutral process for the generation of carbon-neutral hydrogen and carbon-neutral electricity. More specifically, the present disclosure relates to compositions, methods and apparatus employing a carbon-neutral process for generating electricity employing a liquid organic hydrogen carrier (LOHC) for supplying hydrogen for generating the carbon neutral electricity. The present disclosure also relates more specifically to carbon-neutral compositions consisting of liquid organic hydrogen carriers used for supplying hydrogen to generate electricity that may be regenerated in a carbon-neutral process using an apparatus with a net zero atmospheric emission of carbon oxides.

A bimetallic catalyst alloy is provided for use in fuel cells, particularly in the oxidation of dimethyl ether in a direct dimethyl ether fuel cell.

A bimetallic catalyst alloy is provided for use in fuel cells, particularly in the oxidation of dimethyl ether in a direct dimethyl ether fuel cell.

An electrochemical energy conversion and storage system includes an electrochemical energy conversion device, such as a fuel cell that is in fluid communication with a hydrogen or electrically regenerable organic liquid fuel and an oxidant, for receiving, catalyzing and electrochemically oxidizing at least a portion of the fuel to generate electricity, a thus partially oxidized liquid fuel, and water. The liquid fuel includes six-membered ring cyclic hydrocarbons with functional group substituents, wherein the ring hydrogens may undergo an electrochemical oxidative dehydrogenation to the corresponding aromatic molecules. Comprising ring-substituent functional groups may also be electrochemically oxidized now with a potential incorporation of oxygen thus providing an additional capacity for energy storage. The partially oxidized spent liquid fuel may be electrically regenerated in situ with now an input of electricity and water to the device, generating oxygen as a by-product. Alternatively, the recovered spent fuel may be conveyed to a facility where it is reconstituted by catalytic hydrogenation or electrochemical hydrogenation processes.

An electrochemical energy conversion and storage system includes an electrochemical energy conversion device, such as a fuel cell that is in fluid communication with a hydrogen or electrically regenerable organic liquid fuel and an oxidant, for receiving, catalyzing and electrochemically oxidizing at least a portion of the fuel to generate electricity, a thus partially oxidized liquid fuel, and water. The liquid fuel includes six-membered ring cyclic hydrocarbons with functional group substituents, wherein the ring hydrogens may undergo an electrochemical oxidative dehydrogenation to the corresponding aromatic molecules. Comprising ring-substituent functional groups may also be electrochemically oxidized now with a potential incorporation of oxygen thus providing an additional capacity for energy storage. The partially oxidized spent liquid fuel may be electrically regenerated in situ with now an input of electricity and water to the device, generating oxygen as a by-product. Alternatively, the recovered spent fuel may be conveyed to a facility where it is reconstituted by catalytic hydrogenation or electrochemical hydrogenation processes.

Disclosed is a method of operating an Alkaline Membrane Fuel Cell (AMFC) with direct ammonia feeding. The method may include providing AMFC comprising an anode inlet for receiving ammonia and a cathode inlet for receiving oxygen containing gas; operating the AMFC at an operation temperature of above 80° C.; providing the oxygen containing gas; to a cathode of the AMFC at a pressure above the equilibrium vapor pressure of water at the operation temperature; maintaining the pressure during the operation of the AMFC as to maintain water in substantially liquid phase near the cathode; and providing the ammonia to an anode of the AMFC.

Disclosed is a method of operating an Alkaline Membrane Fuel Cell (AMFC) with direct ammonia feeding. The method may include providing AMFC comprising an anode inlet for receiving ammonia and a cathode inlet for receiving oxygen containing gas; operating the AMFC at an operation temperature of above 80° C.; providing the oxygen containing gas; to a cathode of the AMFC at a pressure above the equilibrium vapor pressure of water at the operation temperature; maintaining the pressure during the operation of the AMFC as to maintain water in substantially liquid phase near the cathode; and providing the ammonia to an anode of the AMFC.

Embodiments are directed to composite membranes having a microporous polymer structure, and an ion exchange material forming a continuous ionomer phase within the composite membrane. The continuous ionomer phase refers to absence of any internal interfaces in a layer of ionomer or between any number of layers coatings of the ion exchange material provided on top of one another. The composite membrane exhibits a haze change of 0% or less after being subjected to a blister test procedure. No bubbles or blisters are formed on the composite membrane after the blister test procedure. A haze value of the composite membrane is between 5% and 95%, between 10% and 90% or between 20% and 85%. The composite membrane may have a thickness of more than 17 microns at 0% relative humidity.