In a first stage of a methane conversion system, at least some methane (CH.sub.4) in an input gas flow stream can be converted into C.sub.2 hydrocarbons, hydrogen gas (H.sub.2), and aromatics to provide a first processed stream. The conversion can be direct non-oxidative methane conversion (DNMC). At least some of the aromatics can be removed from the first processed stream to provide a second processed stream. In a second stage of the methane conversion system, at least some of the H.sub.2 can be removed from the second processed stream to provide a recycle stream. The recycle stream can be returned to the first stage of the methane conversion system for further conversion of methane and removal of aromatics and H.sub.2 products.

A method of converting cellulosic feedstock to bio coal. The cellulosic feedstock in a carrier of process fluid is introduced within a conduit having substantially linear portions connected by curved portions creating a serpentine structure. The substantially linear portions are surrounded by tubular sleeves creating annular spaces between the tubular sleeves and substantially linear portions for carrying a high temperature fluid for transferring thermal energy to the cellulosic feedstock and process fluid. The cellulosic feedstock is maintained in an oxygen-free environment. The method is continuous as the cellulosic feedstock in process fluid is subjected to a plurality of mixing elements characterized as having no edges perpendicular to the longitudinal axes of the plurality of substantially linear segments and which are sized and positioned within the plurality of substantially linear segments such no mixing elements are in contact with one another resulting in an open region of travel for fluids passing from the conduit inlet to conduit outlet.

The present invention relates to a process for the preparation of a zeolitic material, as well as to a catalyst per se as obtainable or obtained according to said process. Furthermore, the present invention relates to the use of the zeolitic material, in particular as a catalyst.

Fuel mixed in water is combusted in a reactor having an internal operating pressure and temperature greater than 3200 psi and greater than 374 C., where the combustion of the fuel is exothermic. Air and fuel are pressurized for introduction into the reactor to a pressure greater than the internal operating pressure using energy generated from the combustion of the fuel, and the pressurized air and the pressurized fuel are injected into the reactor. Pressurized water from the reactor is injected into a drive water column that is partially filled with water to increase a pressure of the drive water column, and water at a temperature less than 100 C. is injected into the reactor to replace water from the reactor that is injected into the drive water column. Pressurized water from the drive water column is used to drive a hydroelectric drive system to produce electrical power.

A water gas shift (WGS) reactor system includes a housing; a reaction tube disposed in the housing, wherein a reaction channel is defined within the reaction tube and a cooling fluid channel is defined between the housing and the reaction tube; a catalyst disposed in the reaction channel, the catalyst configured to catalyze a hydrogen generation reaction; and a heat transfer material disposed in the reaction channel.

A method of manufacturing synthesis gas by catalytic partial oxidation can prevent formation of hot spots from taking place when driving mixture gas to pass through a catalyst-filled layer at high velocity. The method comprises converting mixture gas of source gas containing lower hydrocarbons and oxidative gas containing oxygen into synthesis gas containing hydrogen and carbon monoxide as main components thereof by causing mixture gas to flow through a fixed bed catalyst layer arranged in a reactor. The method of manufacturing synthesis gas by catalytic partial oxidation is conducted such that the mixture gas is made to flow to the catalyst layer under the condition that the Reynolds number does not exceed 20 at the inlet of the catalyst layer.

The invention relates to an apparatus (1) for producing pseudoionone and hydroxy pseudoionone. It suggests an apparatus (1) comprising first and second substantially vertically oriented reactor chambers oriented such that components flow through the first and second reactor chambers in different directions, wherein the first reactor chamber (13) is configured to receive a first component feed (C1) containing a first aqueous mixture through an inlet (15), and to produce a second aqueous mixture, and wherein the apparatus (1) comprises a mixing device (17) positioned downstream of the first component feed inlet (15) and configured to add a second component feed (C2) to the first component feed (C1) when the second aqueous mixture has formed, and the second reactor chamber (23) is configured to receive the first and second component feeds unified in the mixing device (17) from the first reactor chamber (13) and to produce a third aqueous mixture from the first and second aqueous mixtures. The invention further suggests a method and a use for producing pseudoionone and hydroxy pseudoionone.

A fuel reforming device includes a combustion part including a burner; an exhaust part configured to circulate an exhaust gas that is generated from the combustion part; and a reactor that is configured to generate hydrogen from a raw material by absorbing heat from the exhaust gas circulating in the exhaust part. The reactor includes a heat storage member that is configured to absorb the heat from the exhaust gas during operation of the combustion part, store the absorbed heat, and provide the absorbed heat to the reactor.

A mixing reactor (1), the reactor comprising a body (2) having a first inlet (3), a second inlet (5) and an outlet (4), in which there is an inner passage (6) through the body (2) from the first inlet (3) at a first end (12) of the body (2) to the outlet (4) at a second end of the body (2) along a length of the body (2), the inner passage (6) having a side wall (17) along the length, and an outer passage (7) closer to a surface (14) of the body (2) than the inner passage (6), the outer passage (7) running from the second inlet (5) at the second end, travelling through the body (2) along the length and meeting the inner passage (6) at a junction (11) at the first end, the outer passage (7) joining the inner passage (6) through the side wall (17) at the junction (11). Such a mixing reactor can be used for producing particles such as nanoparticles or Metal-Organic frameworks. Furthermore, we disclose a cascade of such reactors and a method of using such reactors to mix fluids, typically but non-exclusively so as to produce such particles.

A reaction apparatus for use in solid carbon production includes a reactor shell defining a reactor inlet and a reactor outlet. Concentric cylinders or substantially parallel plates of catalytic material are disposed within the reactor shell and are structured and adapted to expose at least one contact surface to gaseous reactants. Another apparatus includes a removable cartridge comprising a plurality of substantially parallel plates of catalytic material disposed within the reactor shell. A system for use in carbon nanotube production may include any such reactor and a solids recovery means for removing carbon nanotubes from the reactor.