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.

The present invention relates to a method for dehydrogenating an alkane, the method including: a step of feeding into dehydrogenation reactors a feed gas stream containing a hydrocarbon to be dehydrogenated, hydrogen, and steam and performing dehydrogenation, wherein the dehydrogenation step is repeated in five or more sets, the dehydrogenation reactors have two parallel-connected reaction material heaters configured to heat the feed gas stream which is fed into each of the dehydrogenation reactors, and the steam is fed separately to the individual reactors for five or more sets of dehydrogenation steps; and a step of cooling and compressing a production gas stream resulting from the previous step, quenching the compressed product gas stream by passage through a cooling box, separating and purifying the product gas stream having passed through the cooling box, and recovering a product.

A hydrocarbon stream is combusted within a reactor to produce soot and syngas. Sub-stoichiometric combustion of the hydrocarbon stream within the reactor converts at least 10% of the carbon in the hydrocarbon stream into soot. The syngas is mixed with a steam stream to produce a hydrogenation feed stream. A shift reactor converts at least a portion of the carbon monoxide and steam to carbon dioxide and hydrogen to produce a shifted gas stream. Water is separated from the shifted gas stream to produce a dehydrated gas stream. The dehydrated gas stream is separated to produce a hydrogen product stream and a recycle stream. The recycle stream is recycled to the reactor.

The present invention relates to a thermochemical reactor system for a temperature swing cyclic process with integrated heat recovery comprising at least two modules, wherein each module comprises at least one chemical reaction zone (CRZ) and at least one thermal energy storage unit (TES), wherein the at least two modules are operationally connected for at least one heat transfer fluid (HTF) for transporting heat between the two modules, wherein each chemical reaction zone (CRZ) comprises at least one reacting material that undergoes in a reversible manner an endothermic reaction at temperature T.sub.endo and an exothermic reaction at temperature T.sub.exo, wherein T.sub.endo and T.sub.exo differ from each other, wherein the at least one reacting material is provided in at least one encapsulation within each of the chemical reaction zones (CRZ) such that a contact of the reacting material and the at least one heat transfer fluid is avoided. The present invention relates further to a method for operating such a reactor system.

A multi-tubular chemical reactor (400) includes an igniter (435) for the initiation of gas phase exothermic reaction within the gas phase reaction zones (409) of the tubular reactor units (408). A method of carrying out a gas phase exothermic reaction within the multi-tubular chemical reactor comprising: introducing gaseous reactants into a tubular reactor unit (408); initiating with radiant heat an exothermic reaction of the gaseous reactants within the reactor unit; and transferring heat produced by the exothermic reaction occurring within the gas phase reaction zone of the reactor unit to the gas phase reaction zone of one or more adjacent reactor units (408), thereby initiating an exothermic reaction within at least one adjacent reactor unit (408) until in such manner an exothermic reaction has been initiated in each of the plurality of spaced-apart reactor units (408).

The invention relates to hydrocarbon pyrolysis, to equipment and materials useful for hydrocarbon pyrolysis, to processes for carrying out hydrocarbon pyrolysis, and to the use of hydrocarbon pyrolysis for, e.g., hydrocarbon upgrading.

A system for promoting endothermic conversions includes a first and second portion, a first and second supply, a first outlet, and a heat exchanger. The first portion defines a first inner volume containing an oxygen transfer agent. The first supply contains a reducing agent and is fluidly connected to the first inner volume. The first outlet conveys one or more of carbon dioxide, water, and an unsaturated hydrocarbon from the first inner volume. The second portion and the heat exchanger positioned within the second portion define a second inner volume containing reduced oxygen transfer agent. The second supply contains an oxidizing agent fluidly connected to the second inner volume. The heat exchanger also defines a third inner volume segregated from the second inner volume, and the heat exchanger is configured to transfer heat resulting from the oxidation of the reduced oxygen transfer agent to the third inner volume.

Methods comprising: evaporating a catalyst source to produce a catalyst gas; condensing the catalyst gas to produce a catalyst vapor comprising catalyst droplets suspended in a gas phase; and contacting the catalyst vapor with a hydrocarbon gas to catalyze a decomposition reaction of the hydrocarbon gas into hydrogen gas and carbon. And, systems comprising: a catalyst source evaporator that provides a first stream to a reactor; a hydrocarbon source that provides a second stream to the reactor; a cooling column coupled to the reactor via a third stream comprising hydrogen, catalyst liquid, solid carbon, optionally catalyst gas, and optionally unreacted hydrocarbon gas such that the cooling column receives the third stream from the reactor; and wherein the cooling column has effluent streams that include (a) a fourth stream that comprises hydrogen and optionally catalyst gas and (b) a fifth stream that comprises catalyst liquid.

A continuous chemical reactor may include a primary reaction unit and at least one secondary reaction unit. The primary reaction unit has a stirring device and a first temperature regulating device, and a feed inlet provided at an upper portion thereof. The secondary reaction unit is sleeved outside the primary reaction unit, and a reaction chamber is formed therebetween. By adding reaction materials to the primary reaction unit via the feed inlet and adjusting the temperature of the reaction materials by the first temperature regulating device, the reacted materials enter the reaction chamber, and the heat generated in the reaction chamber can be used to adjust the temperature of the materials in the primary reaction unit to more effectively use the heat, and the product after reaction can be discharged from a discharge hole at the lower end of the secondary reaction unit, thereby achieving continuous production.

A dual utilization liquid and gaseous fuel CPOX reformer that includes reaction zones for the CPOX reforming of liquid and gaseous reformable fuels. A reforming method is also provided. The method comprises reforming a first gaseous reformable reaction mixture comprising oxygen-containing gas and vaporized liquid fuel and before or after this step, reforming second gaseous reformable reaction mixture comprising oxygen-containing gas and gaseous fuel to produce a hydrogen-rich reformate.