A method for producing a synthetic fuel from hydrogen and carbon dioxide comprises extracting hydrogen molecules from hydrogen compounds in a hydrogen feedstock to produce a hydrogen-containing fluid stream; extracting carbon dioxide molecules from a dilute gaseous mixture in a carbon dioxide feedstock to produce a carbon dioxide containing fluid stream; and processing the hydrogen and carbon dioxide containing fluid streams to produce a synthetic fuel. At least some thermal energy and/or material used for at least one of the steps of extracting hydrogen molecules, extracting carbon dioxide molecules, and processing the hydrogen and carbon dioxide containing fluid streams is obtained from thermal energy and/or material produced by another one of the steps of extracting hydrogen molecules, extracting carbon dioxide molecules, and processing the hydrogen and carbon dioxide containing fluid streams.

A process for producing a catalytically active multielement oxide comprising the elements Mo, W, V and Cu, wherein at least one source of the elemental constituents W of the multielement oxide is used to produce an aqueous solution, the resultant aqueous solution is admixed with sources of the elemental constituents Mo and V of the multielement oxide, drying of the resultant aqueous solution produces a powder P, the resultant powder P is optionally used to produce geometric shaped precursor bodies, and the powder P is or the geometric shaped precursor bodies are subjected to thermal treatment to form the catalytically active composition, wherein the aqueous solution used for drying comprises from 1.6% to 5.0% by weight of W and from 7.2% to 26.0% by weight of Mo, based in each case on the total amount of aqueous solution.

A process for producing direct reduced iron (“DRI”) from iron ore and biomass in a single stage fluidised bed includes injecting (a) iron ore, (b) gaseous oxygen and (c) a solid reductant including biomass into a reaction zone of the fluidized bed operating in a temperature range of 750-850#C and reducing iron ore and forming DRI in the fluidized bed and discharging DRI having a metallisation of at least 70% from the fluidised bed.

A method for the conversion of a carbonaceous material. The method comprising the steps of providing a carbonaceous material, providing a hot powder material and contacting the carbonaceous material and the powder material in an atmosphere configured to no more than partially oxidize carbon to CO.sub.2. The carbonaceous material is at least a partial converted into volatiles. The volatiles are separated from the additional components by specific gravity.

A process for producing a highly calcined and uniformly calcined product from a feedstock. The process comprising the steps of grinding the feedstock to powder, preheating the powder, and calcining the powder in a reactor plant that comprises a number of reactor segments in which a flash calciner is used in each progressive reactor segment to incrementally react the powder by raising the temperature in each segment. The last segment may be a high-temperature reactor that has a controlled residence time and temperature that may allow controlled finishing of the calcination process to achieve a desired degree of calcination and sintering of the product; and cooling of the product.

The present invention discloses a continuous calcination vessel which can be used to prepare calcined chemically-treated solid oxides from solid oxides and chemically-treated solid oxides. A process for the continuous preparation of calcined chemically-treated solid oxides is also provided. Calcined chemically-treated solid oxides disclosed herein can be used in catalyst compositions for the polymerization of olefins.

Process for manufacturing a lithiated transition metal oxide, said process comprising the steps of (a) mixing at least one lithium salt and a precursor selected from transition metal oxides, transition metal oxyhydroxides, transition metal hydroxides, and transition metal carbonates, (b) pre-calcining the mixture obtained in step (a) at a temperature in the range of from 300 to 700° C., and (c) calcining the pre-calcined mixture according to step (b) in a multi-stage fluidized bed reactor at a temperature in the range of from 550° C. to 950° C., wherein the temperatures in step (b) and (c) are selected in a way that step (c) is being performed at a temperature higher than that of step (b).

The present disclosure relates to a method for chemically modifying particles of a bicarbonate salt in a co-rotating twin-screw extruder and chemically modified bicarbonate particles prepared therefrom. The present disclosure also relates to a method for controlling an amount of carbonate salt formed during chemical modification of bicarbonate salt particles.

A catalyst comprising a microporous crystalline metallosilicate having a Constraint Index of 12, or 10, or 8, or 6 or less, a binder, a Group 1 alkali metal or a compound thereof and/or a Group 2 alkaline earth metal or a compound thereof, a Group 10 metal or a compound thereof, and, optionally, a Group 11 metal or a compound thereof; wherein the catalyst is calcined in a first calcining step before the addition of the Group 10 metal or compound thereof and optionally the Group 11 metal or compound thereof; and wherein the first calcining step includes heating the catalyst to first temperatures of greater than 500° C.; and wherein the catalyst is calcined in a second calcining step after the addition of the Group 10 metal or compound thereof and optionally the Group 11 metal or compound thereof wherein the second calcining step includes heating the catalyst to temperatures of greater than 400° C.

Systems and methods are provided for production of carbon nanotubes and H.sub.2 using a reaction system configuration that is suitable for large scale production. In the reaction system, a substantial portion of the heat for the reaction can be provided by using a heated gas stream. Optionally, the heated gas stream can correspond to a heated H.sub.2 gas stream. By using a heated gas stream, when the catalyst precursors for the floating catalyst—chemical vapor deposition (FC-CVD) type catalyst are added to the gas stream, the gas stream can be at a temperature of 1000° C. or more. This can reduce or minimize loss of catalyst precursor material and/or deposition of coke on sidewalls of the reactor. Additionally, a downstream portion of the reactor can include a plurality of flow channels of reduced size that are passed through a heat exchanger environment, such as a shell and tube heat exchanger. This can provide cooling of the gas flow after catalyst formation to allow for carbon nanotube formation, while also reducing the Reynolds number of the flow sufficiently to provide laminar flow within the region where carbon nanotubes are formed.