Disclosed are apparatuses, systems, methods, and devices for generating hydrogen pyrolysis of hydrocarbons (methane, diesel, JP8, etc.) in a reactor. The reactor includes multiple channels in parallel. A hydrocarbon flows in a channel and decomposes into hydrogen and carbon. Hydrogen gas flows out and some of the carbon will deposit on the channel wall. Once carbon deposition reaches a predetermined level, the hydrocarbon flow stops, and air or oxygen is caused to flow into the channels to oxidize carbon into carbon monoxide or carbon dioxide and supply heat to neighboring channels. Simultaneously, the hydrocarbon will flow into neighboring channels causing decomposition into hydrogen and carbon in the neighboring channels. When the carbon coating in the neighboring channels reaches a predetermined level, the gas flow is switched again to air or oxygen. In this way, each channel alternates between decomposing the hydrocarbon and oxidizing the deposited carbon.

Integrated plants and associated processes for producing ammonia and sulfuric acid have been developed comprising air separation and water electrolysis subsystems and which make surprisingly efficient use of the products from these subsystems (i.e. oxygen and nitrogen from the former and hydrogen and oxygen from the latter). The invention is particularly suitable for use as part of an integrated fertilizer production plant.

In some examples, hydrocarbon feed and a diluent such as steam are mixed, and heated. A vapor phase product and a liquid phase product can be separated from the heated mixture. The liquid phase product can be hydroprocessed to produce a first hydroprocessed product. A pitch and one or more hydrocarbon products can be separated from the first hydroprocessed product. The pitch can be contacted with a diluent to produce a pitch-diluent mixture. The pitch-diluent mixture can be hydroprocessed to produce a second hydroprocessed product. A hydroprocessor heavy product and a utility fluid product can be separated from the second hydroprocessed product. The diluent can be or include at least a portion of the utility fluid product. The vapor phase product can be steam cracked to produce a steam cracker effluent. A tar product and a process gas that can include ethylene and propylene can be separated from the steam cracker effluent.

A hybrid dehydrogenation reaction system includes: an acid aqueous solution tank having an acid aqueous solution; an exothermic dehydrogenation reactor including a chemical hydride of a solid state and receiving the acid aqueous solution from the acid aqueous solution tank for an exothermic dehydrogenation reaction of the chemical hydride and the acid aqueous solution to generate hydrogen; an LOHC tank including a liquid organic hydrogen carrier (LOHC); and an endothermic dehydrogenation reactor receiving the liquid organic hydrogen carrier from the LOHC tank and generating hydrogen through an endothermic dehydrogenation reaction of the liquid organic hydrogen carrier by using heat generated from the exothermic dehydrogenation reactor.

A catalytic reaction analysis dual reactor system and a method for measuring the catalytic activity of a catalyst by correcting for non-catalytic effects with the catalytic reaction analysis dual reactor system. The dual reactor system contains a first reactor comprising a first catalyst on a first catalyst support, and a second reactor comprising a second catalyst support, wherein the particle size and amount of the first catalyst and the second catalyst support are substantially the same, and the effect of the catalyst is isolated by correcting the result obtained from the first reactor containing the catalyst with the result obtained from the second reactor containing the catalyst support.

A method of determining multimodal polyethylene quality comprising the steps of (a) providing a multimodal polyethylene resin sample; (b) determining, in any sequence, the following: that the multimodal polyethylene resin sample has a melt index within 30% of a target melt index; that the multimodal polyethylene resin sample has a density within 2.5% of a target density; that the multimodal polyethylene resin sample has a dynamic viscosity deviation (% MVD) from a target dynamic viscosity of less than about 100%; that the multimodal polyethylene resin sample has a weight average molecular weight (M.sub.w) deviation (% M.sub.wD) from a target M.sub.w of less than about 20%; and that the multimodal polyethylene resin sample has a gel permeation chromatography (GPC) curve profile deviation (% GPCD) from a target GPC curve profile of less than about 15%; and (c) responsive to step (b), designating the multimodal polyethylene resin sample as a high quality resin.

In accordance with the present invention, there is provided a process for producing hydrogen and graphitic carbon from a hydrocarbon gas comprising: contacting at a temperature between 600° C. and 1000° C. the catalyst with the hydrocarbon gas to catalytically convert at least a portion of the hydrocarbon gas to hydrogen and graphitic carbon, wherein the catalyst is a low grade iron oxide.

Systems and methods are provided for improving the operation of groups of reverse flow reactors by operating reactors in a regeneration portion of the reaction cycle to have improved flue gas management. The flue gas from reactor(s) at a later portion of the regeneration step can be selectively used for recycle back to the reactors as a diluent/heat transport fluid. The flue gas from a reactor earlier in a regeneration step can be preferentially used as the gas vented from the system to maintain the desired volume of gas within the system. This results in preferential use of higher temperature flue gas for recycle and lower temperature flue gas for venting from the system. This improved use of flue gas within a reaction system including reverse flow reactors can allow for improved reaction performance while reducing or minimizing heat losses during the regeneration portion of the reaction cycle.

Methods and a reactor system for producing acetic acid in a selective oxidation (SO) reactor are provided. An example method includes providing a fresh feed stream to the SO reactor, wherein the fresh feed stream includes a light hydrocarbon feed stream, a carbon dioxide feed stream, and a steam feed stream. Acetic acid is formed in the SO reactor. An acetic acid product stream is separated from a reactor effluent stream in a scrubber. A recycle gas stream is obtained from the scrubber. At least a portion of the recycle gas stream is combined into the fresh feed stream to the SO reactor.

Described are a low temperature plasma reaction device and a hydrogen sulfide decomposition method. The reaction device includes: a first cavity; a second cavity, the second cavity being embedded inside or outside the first cavity; an inner electrode, the inner electrode being arranged in the first cavity; an outer electrode; and a barrier dielectric arranged between the outer electrode and the inner electrode. The hydrogen sulfide decomposition method includes: implementing dielectric barrier discharge at the outer electrode and the inner electrode of the low temperature plasma reaction device, introducing a raw material gas containing hydrogen sulfide into the first cavity to implement a hydrogen sulfide decomposition method, and continuously introducing a thermally conductive medium into the second cavity in order to control the temperature of the first cavity of the low temperature plasma reaction device.