A method of producing liquid fuel and/or chemicals from a carbonaceous material entails combusting a conditioned syngas in pulse combustion heat exchangers of a steam reformer to help convert carbonaceous material into first reactor product gas which includes carbon monoxide, hydrogen, carbon dioxide and other gases. A portion of the first reactor product gas is transferred to a hydrogen reformer into which additional conditioned syngas is added and a reaction carried out to produce an improved syngas. The improved syngas is then subject to one or more gas clean-up steps to form a new conditioned syngas. A portion of the new conditioned syngas is recycled to be used as the conditioned syngas in the pulse combustion heat exchangers and in the hydrocarbon reformer. A system for carrying out the method include, a steam reformer, a hydrocarbon reformer, first and second gas-cleanup systems, a synthesis system and an upgrading system.

The invention relates to a process for the combined production of hydrogen and carbon dioxide from a hydrocarbon mixture, in which the residual gas of a PSA H.sub.2 (12) is separated by permeation in order to reduce the hydrocarbon content thereof and the hydrocarbon-purified gas is separated at a low temperature to produce a carbon dioxide-rich liquid (22).

The present invention relates to a gas/liquid oligomerization reactor with successive zones of variable diameter. The invention also relates to a process for the oligomerization of ethylene using a gas/liquid oligomerization reactor with successive zones of variable diameter.

The present invention relates to a gas/liquid oligomerization reactor with successive zones of variable diameter. The invention also relates to a process for the oligomerization of ethylene using a gas/liquid oligomerization reactor with successive zones of variable diameter.

A flow reactor can promote a reaction under appropriate temperature management, can precent reaction fluid or generated gas from being trapped in a heat transmission part, can be disassembled for easy cleaning, and to which a coating or lining can be applied. This flow reactor is provided with two flow paths, a reaction flow path and a second flow path, in a space formed between an inner cylinder and an outer cylinder that are concentric. A spiral heat transmission body is disposed between the inner cylinder and the outer cylinder, and the spiral heat transmission body has a substantially triangular cross-sectional shape in an axial cross-sectional view. The spiral heat transmission body partitions the space into the reaction flow path and the second flow path, and heat is exchanged via the spiral heat transmission body between a reaction fluid F1 flowing through the reaction flow path and a heat medium F2 flowing through the second flow path.

A flow reactor can promote a reaction under appropriate temperature management, can precent reaction fluid or generated gas from being trapped in a heat transmission part, can be disassembled for easy cleaning, and to which a coating or lining can be applied. This flow reactor is provided with two flow paths, a reaction flow path and a second flow path, in a space formed between an inner cylinder and an outer cylinder that are concentric. A spiral heat transmission body is disposed between the inner cylinder and the outer cylinder, and the spiral heat transmission body has a substantially triangular cross-sectional shape in an axial cross-sectional view. The spiral heat transmission body partitions the space into the reaction flow path and the second flow path, and heat is exchanged via the spiral heat transmission body between a reaction fluid F1 flowing through the reaction flow path and a heat medium F2 flowing through the second flow path.

A device for loading pellets into reactor tubes includes a portable loading box with a bottom wall defining an opening, a loading tube projecting downwardly from the opening, and a movable dam for dividing said loading box into separate chambers.

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 process comprises polymerizing an olefin monomer in a loop reactor in the presence of a catalyst and a diluent, and producing a slurry comprising solid particulate olefin polymer and diluent. The Biot number is maintained at or below about 3.0 within the loop reactor during the polymerizing process. The slurry in the loop reactor forms a slurry film having a film coefficient along an inner surface of the reactor wall, and the film coefficient is less than about 500 BTU.Math.hr.sup.−1.Math.ft.sup.−2.Math.° F..sup.−1.