Disclosed is a method for preparing a material of plant origin rich in phenolic acids, including at least one metal, including: preparing a material of plant origin chosen from: aquatic plants; materials rich in tannins; materials rich in lignin; and obtaining a material of plant origin, rich in phenolic acids, in which the ratio of the intensity of the vibration band of the C═O bond of the COOH group and the intensity of each of the vibration bands the aromatic ring determined in FT-IR is between 0.5 and 4. The material of plant origin is brought into contact with an effluent including from 0.1 to 1000 mg/l of at least one metal, thus obtaining a material of plant origin rich in phenolic acids including from 1 to 30% by weight of at least one metal relative to the total weight of the material.

Processes for transforming an inert metal component into an active metal catalyst are provided. Apparatus and methods using active metal catalyst prepared according the process described herein are also provided.

A method for preparing an iron-based catalyst, the method including preparing iron ore particles by grinding iron ore; and impregnating the iron ore particles with a first metal and second metal, wherein the first metal is selected from copper, cobalt, or manganese, or a combination thereof, and the second metal is selected from an alkali metal or alkali earth metal, or a combination thereof.

The present invention relates to a process for preparing acrolein from propylene by catalytic gas phase oxidation with molecular oxygen (for example air). The invention further relates to the use of particular propylene-containing starting materials, for example refinery grade propylene, for preparation of acrolein.

A method for preparing a supported two-component metal oxide ozone catalytic oxidation catalyst for an advanced treatment of a petrochemical wastewater is provided. The supported two-component metal-oxide ozone catalytic oxidation catalyst is prepared from commercially-available active alumina balls by the steps of carrier activation, impregnating liquid preparation, carrier impregnation, catalyst roasting, and catalyst cleaning. The supported two-component metal oxide ozone catalytic oxidation catalyst has product stability, is reusable, and is of significance in application of ozone catalytic oxidation technologies as well as energy conservation and consumption reduction for petrochemical wastewater treatment plants.

A system and method of pre-purification of a feed gas stream is provided that is particularly suitable for pre-purification of a feed air stream in cryogenic air separation unit. The disclosed pre-purification systems and methods are configured to remove substantially all of the hydrogen, carbon monoxide, water, and carbon dioxide impurities from a feed air stream and is particularly suitable for use in a high purity or ultra-high purity nitrogen plant. The pre-purification systems and methods preferably employ two or more separate layers of hopcalite catalyst with the successive layers of the hopcalite separated by a zeolite adsorbent layer that removes water and carbon dioxide produced in the hopcalite layers.

A method of reducing a gaseous carbon oxide includes reacting a carbon oxide with a gaseous reducing agent in the presence of an intermetallic or carbide catalyst. The reaction proceeds under conditions adapted to produce solid carbon of various allotropes and morphologies, the selective formation of which can be controlled by means of controlling reaction gas composition and reaction conditions including temperature and pressure. A method for utilizing an intermetallic or carbide catalyst in a reactor includes placing the catalyst in a suitable reactor and flowing reaction gases comprising a carbon oxide with at least one gaseous reducing agent through the reactor where, in the presence of the catalyst, at least a portion of the carbon in the carbon oxide is converted to solid carbon and a tail gas mixture containing water vapor.

A process for preparing high molecular weight, branched, acyclic polyalkyleneamines comprising transaminating a reaction mixture that includes at least a first polyalkyleneamine component that contains at least two non-tertiary amine groups separated from one another by a ternary or higher carbon atom and a second polyalkyleneamine component having the formula wherein x, y, and z are the same or different and are integers of from 1 to 10; a, b, c, d, e, and f are the same or different and are H or hydrocarbyl of from 1 to 10 carbon atoms; A, B, C, D, E, are the same or different and are H or hydrocarbyl of from 1 to 10 carbon atoms; provided that at least two of the amine groups are primary or secondary. ##STR00001##

A continuous process for converting carbohydrates to ethylene and propylene glycol. The carbohydrates are mixed with water and passed through a reactor at a temperature that hydrolyzes the carbohydrate mixture at least partially to monosaccharides. The reactor has a first zone comprising a retro-aldol catalyst and a second zone comprising a reducing catalyst. The aldose is converted in the first zone into glycolaldehyde by the retro-aldol catalyst and the glycolaldehyde, in the presence of hydrogen, is converted to ethylene glycol in the second zone of the reactor. The reaction products are removed from the reactor and the ethylene glycol is recovered. The selectivity to propylene glycol can be enhanced via feeding ketose as the carbohydrate.

A honeycomb structure includes: a honeycomb structure body including a plurality of cells defined by a partition wall and serving as a through channel of fluid; and a plugging portion to alternately plug open end parts of the plurality of cells on one side as an inflow side of the exhaust gas and open end parts on the other side as an outflow side of the exhaust gas. The partition wall is loaded, on the side of the outflow cells, with an oxidation catalyst made of a transition metal oxide at least including Fe and Mn to oxidize NO gas or an oxidation catalyst made of a transition metal oxide loaded at CeO.sub.2 and at least including Fe and Mn to oxidize NO gas. The loading amount of the oxidation catalyst is 5.0 g/L or more and 50 g/L or less.