Spent aromatization catalysts containing a transition metal and a catalyst support are selectively poisoned in the disclosed reforming methods, resulting in improvements in overall aromatics yield and selectivity.

The invention relates to a multitubular reactor for dehydrogenation of liquid phase alcohol dehydrogenation and a method of liquid phase alcohol dehydrogenation. Most of the alcohol dehydrogenation reaction is endothermic reaction, the reaction temperature is high and the equilibrium conversion rate is low.

An autothermal reforming catalytic structure for generating hydrogen gas from liquid hydrocarbons, steam and an oxygen source. The autothermal reforming catalytic structure includes a support structure and nanosized mixed metal oxide particles dispersed homogenously throughout the support structure.

An autothermal reforming catalytic structure for generating hydrogen gas from liquid hydrocarbons, steam and an oxygen source. The autothermal reforming catalytic structure includes a support structure and nanosized mixed metal oxide particles dispersed homogenously throughout the support structure.

Thermoneutral systems and methods for producing carbon monoxide (CO) and sulfur dioxide (SO.sub.2) are disclosed. The systems can include a first reaction zone and a second reaction zone, where heat generated in the first reaction zone is sufficient to drive a carbon dioxide gas (CO.sub.2(g)) and elemental sulfur gas (S(g)) reaction to produce a product stream that includes CO(g) and SO.sub.2(g).

Spent aromatization catalysts containing a transition metal and a catalyst support are selectively poisoned in the disclosed reforming methods, resulting in improvements in overall aromatics yield and selectivity.

An autothermal reforming catalytic structure for generating hydrogen gas from liquid hydrocarbons, steam and an oxygen source. The autothermal reforming catalytic structure includes a support structure and metal particles dispersed homogenously throughout the support structure.

An autothermal reforming catalytic structure for generating hydrogen gas from liquid hydrocarbons, steam and an oxygen source. The autothermal reforming catalytic structure includes a support structure and nanosized mixed metal oxide particles dispersed homogenously throughout the support structure.

The method serves for producing a horizontal through flow adsorber with two adsorbents which contains two immediately adjacent packings in a horizontal or vertical container. Between the two packings there is a vertical interface. In a step (a) a vertical dividing wall is positioned on the bottom of the adsorption bed and then on each side of the dividing wall one of the two adsorbents is charged up to a first height that does not exceed the upper edge of the separating ring. In the following step (b) the vertical dividing wall is displaced upwardly until the lower edge thereof is still placed in the existing packing. Then, on each side of the dividing wall one of the two adsorbents is charged up to a second height that does not exceed the upper edge of the displaced dividing wall. Finally, step (b) is repeated until a predetermined filling height is achieved. According to the invention, the vertical dividing wall is composed of at least three dividing wall modules (6.01) that extend only over a part of the length or of the periphery of the vertical dividing wall and are movable in a vertical direction independently of one another.

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.