New Jersey Institute of Technology

Evonik Degussa Gmbh

Orion Engineered Carbons Gmbh

Degussa Aktiengesellschaft

Evonik Carbon Black Gmbh

Juergen Flesch

Kai Schumacher

Robert Pfeffer

Jose A Quevedo

Volker Hamm

Roland Schilling

Dieter Kerner

Harald Alff

Martin Moerters

Matthias Schmitt

Thomas Schiener

Marcus Von Twistern

Methods and systems for enhancing fluidization of nanoparticle and/or nanoagglomerates and for mixing and blending nanoparticle/nanoagglomerate systems at the nanoscale are provided. A fluidization chamber is provided with a fluidizing medium (e.g., a fluidizing gas) directed in a first fluidizing direction, e.g., upward into and through a bed containing a volume of nanoparticles and/or nanopowders. A second source of air/gas flow is provided with respect to the fluidization chamber, the secondary air/gas flow generally being oppositely (or substantially oppositely) directed relative to the fluidizing medium. Turbulence created by the secondary gas flow, e.g., a jet from a micro jet nozzle, is advantageously effective to aerate the agglomerates and the shear generated by the jet is advantageously effective to break apart nanoagglomerates and/or reduce the tendency for nanoagglomerates to form or reform. A downwardly directed source of secondary gas flow located near the main gas distributor leads to full fluidization of the entire amount of powder in the column. In addition, the oppositely directed fluid flow facilitates powder circulation within the fluidization chamber, thereby enhancing fluidization and mixing/blending results.

Fluidized mixing and blending of nanopowders with secondary gas flow

Methods and systems for enhancing fluidization of nanoparticle and/or nanoagglomerates are provided. A fluidization chamber is provided with a fluidizing medium directed in a first fluidizing direction, e.g., upward into and through a bed containing a volume of nanoparticles and/or nanopowders. A second source of air/gas flow is provided with respect to the fluidization chamber, the secondary air/gas flow generally being oppositely directed relative to the fluidizing medium. Turbulence created by the secondary gas flow is advantageously effective to aerate the agglomerates and the shear generated by the jet is advantageously effective to break apart nanoagglomerates and/or reduce the tendency for nanoagglomerates to form or reform. A downwardly directed source of secondary gas flow located near the main gas distributor leads to full fluidization of the entire amount of powder in the column. The oppositely directed fluid flow facilitates powder circulation within the fluidization chamber, thereby enhancing fluidization results.

Fluidized bed systems and methods including micro-jet flow

Aluminum oxide powder in the form of aggregates of primary-particles, which has a BET surface area of from 10 to 90 m2/g and comprises as crystalline phases, in addition to gamma-aluminum oxide and/or theta-aluminum oxide, at least 30% of delta-aluminum oxide. It is prepared by vaporizing aluminum chloride and burning the vapor together with hydrogen and air, the ratio of primary air/secondary air being 0.01 to 2, the exit speed vof the reaction mixture from the burner being at least 10 m/s, the lambda value being 1 to 4, the gamma value being 1 to 3 and the value of gamma*v/lambda being greater than or equal to 55. Dispersion comprising the aluminum oxide powder. Coating composition comprising the dispersion.

Aluminium oxide powder, dispersion and coating composition

Process for removing halide compounds adhering to finely divided metal oxide particles by means of steam, wherein the metal oxide particles are applied to the upper part of an upright column and migrate downwards by means of gravity, the steam is applied at the bottom end of the column, the metal oxide particles and the steam are fed counter-currently, the metal oxide particles freed of halide residues are removed at the base of the column, steam and halide residues are removed at the head of the column, wherein the column is heated in such a manner that the temperature difference T&#x2212;Tbetween the lower part and the upper part of the column is at least 20&#xb0; C. and a maximum temperature of 500&#xb0; C. prevails in the column, and the metal oxide particles have a residence time in the column of from 1 second to 30 minutes.

Purification of finely divided, pyrogenically prepared metal oxide particles

Pyrogenically produced silicon dioxide powder in the form of aggregates of primary particles having a BET surface area of 200&#xb1;25 m/g, wherein the aggregates display an average surface area of 7000 to 12000 nm, an average equivalent circle diameter (ECD) of 80 to 100 nm and an average circumference of 850 to 1050 nm. It is produced by a pyrogenic process in which silicon tetrachloride and a second silicon component comprising HSiCl, HSiCl, HSiCl, CHSiCl, (CH)SiCl, (CH)SiCl and/or (n-CH)SiClare mixed with primary air and a combustion gas and burnt into a reaction chamber, secondary air also being introduced into the reaction chamber, and the feed materials being chosen such that an adiabatic flame temperature of 1570 to 1630&#xb0; C. is obtained. It can be used as a filler.

Pyrogenically produced silicon dioxide powder

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Rayong, Thailand

Juergen Flesch