A heat and hydrogen generation device comprising a burner combustion chamber (3), a burner (7) for feeding fuel and air into the burner combustion chamber (3), and a reformer catalyst (4). The target value of the O.sub.2/C molar ratio of air and fuel which are made to react in the burner combustion chamber (3) is preset as the target O.sub.2/C molar ratio. The actual O.sub.2/C molar ratio at the time of warm-up operation is estimated from the rate of temperature rise of the reformer catalyst (4) etc., when performing warm-up operation. When the estimated actual O.sub.2/C molar ratio deviates from the target O.sub.2/C molar ratio at the time of warm-up operation, the ratio of feed between the amount of feed of air for burner combustion and the amount of feed of fuel for burner combustion is corrected, in a direction making the estimated actual O.sub.2/C molar ratio approach the target O.sub.2/C molar ratio at the time of warm-up operation.

Hydrogen generation assemblies and methods of generating hydrogen are disclosed. In some embodiments, the method may include receiving a feed stream in a fuel processing assembly of the hydrogen generation assembly; and generating a product hydrogen stream in the fuel processing assembly from the received feed stream. Generating a product hydrogen stream may, in some embodiments, include generating an output stream in a hydrogen generating region from the received feed stream, and generating the product hydrogen stream in a purification region from the output stream. The method may additionally include receiving the generated product hydrogen stream in a buffer tank of the hydrogen generation assembly; and detecting pressure in the buffer tank via a tank sensor assembly. The method may further include stopping generation of the product hydrogen stream in the fuel processing assembly when the detected pressure in the buffer tank is above a predetermined maximum pressure.

Process for the production of synthesis gas from hydrocarbon feed containing higher hydrocarbons comprising bypassing a portion of the hydrocarbon feed around a first pre-reforming stage and passing the pre-reformed and bypassed portions through at least a second pre-reforming stage.

The present disclosure is directed to a hydrogen production system for creating and extracting hydrogen gas. The hydrogen production system contains a reactor vessel into which a solution and a metallic or semi-metal material may be placed. The solution is added to the reactor vessel contains both water and a caustic. When contacting the metallic or semi-metal material within the reactor vessel a chemical reaction occurs. The chemical reaction creates hydrogen gas as well as heat and other byproducts. The hydrogen gas may then flow through a hydrogen extraction point located on the reactor vessel for collection or operational use.

A plant and process for producing a hydrogen rich gas are provided, said process comprising the steps of: reforming a hydrocarbon feed in a reforming step thereby obtaining a synthesis gas comprising CH.sub.4, CO, CO.sub.2, H.sub.2 and H.sub.2O; shifting said synthesis gas in a shift configuration including a high temperature shift step; removal of CO.sub.2 upstream hydrogen purification unit, such as a pressure swing adsorption unit (PSA), and recycling off-gas from hydrogen purification unit and mix it with natural gas upstream prereformer feed preheater, prereformer, reformer feed preheater or ATR or shift as feed for the process.

Disclosed herein are systems and methods for producing synthesis gas (syngas) using bio-oil. In some embodiments, syngas is produced by steam reforming bio-oil. In some embodiments, the bio-oil is provided in liquid form. In some embodiments at least some of the liquid bio-oil is transitioned into droplet form when entering a reformer for steam-reforming. In some embodiments, the reformer produces a gas stream comprising syngas, which may be fed to a furnace (e.g., direct reducing furnace, shaft furnace) for reducing iron ore to iron. In some embodiments, the amount of oxygen provided to the reformer is regulated based on an equivalence ratio (ER) corresponding to moles of oxygen fed to the reformer divided by moles of oxygen necessary to achieve stoichiometric combustion of the bio-oil, wherein an exemplary ER value is from about 0.1 to about 0.6.

A system configured for and a method includes introducing a carbonaceous feedstock to a gasifier unit to produce a syngas stream. In addition, the system configured for and the method includes passing the syngas stream to a catalytic reactor unit that is configured to facilitate an exothermic catalytic reaction by use of the syngas stream to produce a heated syngas stream having a greater temperature than the syngas stream. Further, the system configured for and the method includes transferring heat into a carbon-dioxide-containing (CO.sub.2-containing) stream of a power production unit utilizing of the heated syngas stream, where the power production unit is configured to circulate the CO.sub.2-containing stream to produce electrical power.

A feed gas reforming system is provided. The system includes a reformer configured to receive feed gas and supply water and to produce and discharge mixed gas including hydrogen, a pressure swing absorber (PSA) configured to receive the mixed gas and to refine and discharge hydrogen gas, a feed gas supply unit configured to control the supply amount of feed gas, a supply water supply unit configured to control the supply amount of supply water, a hydrogen gas supply unit configured to control the amount of hydrogen gas, and a control unit configured to control the flow rate of hydrogen gas, to control the feed gas supply unit based on the pressure of the discharged hydrogen gas, and to control the supply water supply unit based on the flow rate of feed gas.

Hydrogen generation assemblies, hydrogen purification devices, and their components are disclosed. In some embodiments, the devices may include a permeate frame with a membrane support structure having first and second membrane support plates that are free from perforations and that include a plurality of microgrooves configured to provide flow channels for at least part of the permeate stream. In some embodiments, the assemblies may include a return conduit fluidly connecting a buffer tank and a reformate conduit, a return valve assembly configured to manage flow in the return conduit, and a control assembly configured to operate a fuel processing assembly between run and standby modes based, at least in part, on detected pressure in the buffer tank and configured to direct the return valve assembly to allow product hydrogen stream to flow from the buffer tank to the reformate conduit when the fuel processing assembly is in the standby mode.

A hydrogen generator includes a reformer that generates a hydrogen-containing gas from a source gas and reforming water, a condensed water channel through which condensed water flows, a circulating water channel through which circulating water flows, an ion exchange resin filter provided to the circulating water channel and deionizing the circulating water, a reservoir tank including a first reservoir provided to the condensed water channel and a second reservoir provided to the circulating water channel, a first communicator through which the first and second reservoirs are in communication with each other, and a reforming water channel that extends from a junction of the circulating water channel and supplies the circulating water as reforming water to the reformer. The pressure in the inner space of the first reservoir is maintained to be the same as the pressure in the inner space of the second reservoir.