The present invention relates to an apparatus for dissolving lithium salt powder which is used in preparation of a liquid electrolyte for a lithium ion battery, and more specifically, to an apparatus for dissolving lithium salt powder, which includes: a reactor 10 configured to supply an electrolyte solution; a powder hopper configured to supply lithium salt powder; a dissolution chamber 30 configured to forcibly mix the electrolyte solution and the lithium salt powder; and a powder supply pipe 40 configured to connect the powder hopper 20 and the dissolution chamber 30, wherein a hopper standing frame 70 is installed around the powder hopper 20, the hopper standing frame 70 is detachably loaded on a hopper vibrating unit 80, and a powder outlet 22 of the powder hopper 20 is connected to the powder supply pipe 40 by a vibration-proof connection pipe 23.

Steam may be generated using an apparatus that creates shockwaves in a supersonic gaseous vortex. The apparatus includes a chamber configured to receive, pressurize, and heat fuel gas and/or oxygen containing gas. One or more inlets positioned at a first end of the chamber and arranged to emit fuel gas, oxygen containing gas, or water as one or more jet streams tangentially to an internal surface of the chamber may create a gaseous vortex rotating about a longitudinal axis within the chamber. The inlet(s) may include one or more inlet nozzles structured to accelerate the one or more fuel gas, oxygen-containing gas, or water to a supersonic velocity and adjustably control frequency of shockwaves emitted into the gaseous vortex. Water can be injected into the chamber to stabilize internal chamber temperature where it may be converted into steam. An outlet may be configured to emit product gases and/or steam from the chamber.

A fluid treatment apparatus is described. The fluid treatment apparatus includes: (i) a pulverizer designed to pulverize solids present in a fluid flow to produce pulverized solids admixed with the fluid flow; (ii) a rotatable shaft for rotating the pulverized solids and the fluid flow; (iii) a restrictor or filter for retaining a first portion of the pulverized solids, and allowing a second portion of pulverized solids and a second portion of the fluid flow to pass therethrough; and (iv) a first recirculating line configured to receive the first portion of the pulverized solids and a first portion of the fluid flow that did not pass through the restrictor or the filter.

The present invention provides efficient reaction conditions by clarifying a relationship between a contact time and an optimum particle diameter etc. in a method for reacting a reaction object with a liquid containing the reaction object being in contact with a granular porous body. The upper limit D (mm) of the particle diameter of the granular porous body is determined from D=0.556LN (T)+0.166 in a column flow method in non-circulation type, and determined from D=0.0315T+0.470 in the column flow method in a circulation type and a shaking method. The contact time T (seconds) is given by a value obtained by dividing the volume (m.sup.3) of the granular porous body by the flow rate (m.sup.3/second) of the liquid in the column flow method in non-circulation type, given by a value obtained by multiplying the fluid flow time (seconds) of the liquid by a volume ratio obtained by dividing the volume of the granular porous body by the volume of the liquid in the column flow method in a circulation type, and given by a value obtained by multiplying the volume ratio by the elapsed time (seconds) after addition of the granular porous body in the liquid in the shaking method.

The present invention provides efficient reaction conditions by clarifying a relationship between a contact time and an optimum particle diameter etc. in a method for reacting a reaction object with a liquid containing the reaction object being in contact with a granular porous body. The upper limit D (mm) of the particle diameter of the granular porous body is determined from D=0.556LN (T)+0.166 in a column flow method in non-circulation type, and determined from D=0.0315T+0.470 in the column flow method in a circulation type and a shaking method. The contact time T (seconds) is given by a value obtained by dividing the volume (m.sup.3) of the granular porous body by the flow rate (m.sup.3/second) of the liquid in the column flow method in non-circulation type, given by a value obtained by multiplying the fluid flow time (seconds) of the liquid by a volume ratio obtained by dividing the volume of the granular porous body by the volume of the liquid in the column flow method in a circulation type, and given by a value obtained by multiplying the volume ratio by the elapsed time (seconds) after addition of the granular porous body in the liquid in the shaking method.

An apparatus for fluidizing particles present as a particle bed and, optionally, objects included in the particle bed comprises at least one vertically movably supported container that defines a processing space for receiving the particle bed; an oscillation generator by which the container can be set into a vertical oscillation during operation; and a control unit for setting the frequency and/or amplitude of the vertical oscillation.

A method of loading a catalyst includes providing a catalyst loading apparatus having an optically transparent tube removably coupled to a metal tube and a horizontal divider having a shaft coupled to a plate, the horizontal divider positioned within the optically transparent tube, the metal tube or at least partially within both. The method also includes adding a first inert material to the optically transparent tube, adding a catalyst into the optically transparent tube, adding a second inert material to the optically transparent tube, inserting a distal end of a leveling device having a shaft and a disc into the catalyst loading apparatus from the top surface of the optically transparent tube, contacting the disc of the leveling device against the second layer comprising the catalyst; and displacing at least the horizontal divider into the metal tube.

A method of loading a catalyst includes providing a catalyst loading apparatus having an optically transparent tube removably coupled to a metal tube and a horizontal divider having a shaft coupled to a plate, the horizontal divider positioned within the optically transparent tube, the metal tube or at least partially within both. The method also includes adding a first inert material to the optically transparent tube, adding a catalyst into the optically transparent tube, adding a second inert material to the optically transparent tube, inserting a distal end of a leveling device having a shaft and a disc into the catalyst loading apparatus from the top surface of the optically transparent tube, contacting the disc of the leveling device against the second layer comprising the catalyst; and displacing at least the horizontal divider into the metal tube.

The present disclosure provides a reactor and a method for the production of high purity silicon granules. The reactor includes a reactor chamber; and the reaction chamber is equipped with a solid feeding port, auxiliary gas inlet, raw material gas inlet, and exhaust gas export. The reaction chamber is also equipped with an internal gas distributor; a preheating unit; and an external exhaust gas processing unit connected between the preheating unit and a gas inlet. The reaction chamber is further equipped with a surface finishing unit, a heating unit, and a dynamics-generating unit. The reaction occurs through decomposition of silicon-containing gas in a densely stacked, high purity granular silicon layer reaction bed in relative motion, and uses the exhaust gas for heating. The present invention achieves a large-scale, efficient, energy-saving, continuous, low-cost production of high purity silicon granules.

The present disclosure provides a reactor and a method for the production of high purity silicon granules. The reactor includes a reactor chamber; and the reaction chamber is equipped with a solid feeding port, auxiliary gas inlet, raw material gas inlet, and exhaust gas export. The reaction chamber is also equipped with an internal gas distributor; a preheating unit; and an external exhaust gas processing unit connected between the preheating unit and a gas inlet. The reaction chamber is further equipped with a surface finishing unit, a heating unit, and a dynamics-generating unit. The reaction occurs through decomposition of silicon-containing gas in a densely stacked, high purity granular silicon layer reaction bed in relative motion, and uses the exhaust gas for heating. The present invention achieves a large-scale, efficient, energy-saving, continuous, low-cost production of high purity silicon granules.