System and method for producing high-purity vanadium pentoxide powder

Patent metadata

Field	Value
Publication number	US-10099939-B2
Application number	US-201615547075-A
Country	US
Kind code	B2
Filing date	Jan 28, 2016
Priority date	Jan 30, 2015
Publication date	Oct 16, 2018
Grant date	Oct 16, 2018

Abstract

The present invention provides a system and method for producing high-purity vanadium pentoxide powder. Industrial grade vanadium pentoxide is converted to vanadium oxytrichloride by low temperature fluidizing chlorination, wherein chlorinating gas is preheated via heat exchange between fluidizing gas and chlorination flue gas, and an appropriate amount of air is added to enable a part of carbon powder to combust so as to achieve a balanced heat supply during the chlorination, thereby increasing the efficiency of chlorination and ensuring good selectivity in low temperature chlorination. The vanadium oxytrichloride is purified by rectification, and then subjected to fluidized gas phase hydrolyzation and fluidized calcination, thereby producing a high-purity vanadium pentoxide product and a by-product of hydrochloric acid solution. The system and method have advantages of favorable adaptability to raw material, no discharge of contaminated wastewater, low energy consumption in production, low operation cost, stable product quality, etc.

First claim

What is claimed is:

1. A system for producing high-purity vanadium pentoxide powder, comprising a feeding device, a low temperature chlorination fluidized bed, a rectification and purification device, a gas phase hydrolyzation fluidized bed, a calcination fluidized bed, a tail gas washing absorber, an induced draft fan and a chimney;
wherein the feeding device comprises an industrial grade vanadium pentoxide hopper, an industrial grade vanadium pentoxide screw feeder, a carbon powder hopper and a carbon powder screw feeder;
the low temperature chlorination fluidized bed comprises a chlorination bed feeder, a chlorination fluidized bed body, a chlorination bed cyclone separator, a flue gas heat exchanger, a flue gas condenser, a chlorination bed acid-seal tank and a chlorination bed spiral slag-discharging device;
the rectification and purification device comprises a distilling still, a rectifying column, a distillate condenser, a reflux liquid collecting tank, a silicon-containing vanadium oxytrichloride storage tank, a rectification section acid-seal tank, a high-purity vanadium oxytrichloride condenser, and a high-purity vanadium oxytrichloride storage tank;
the gas phase hydrolyzation fluidized bed comprises a hydrolyzation bed air purifier, a hydrolyzation bed gas heater, a vanadium oxytrichloride nozzle, a gas phase hydrolyzation fluidized bed body, a hydrochloric acid tail gas absorber, and a hydrolyzation bed discharger;
the calcination fluidized bed comprises a calcination bed air purifier, a calcination bed gas heater and a calcination fluidized bed body;
wherein a feed outlet at the bottom of the industrial grade vanadium pentoxide hopper is connected with a feed inlet of the industrial grade vanadium pentoxide screw feeder; a feed outlet at the bottom of the carbon powder hopper is connected with a feed inlet of the carbon powder screw feeder; and a feed outlet of the industrial grade vanadium pentoxide screw feeder and a feed outlet of the carbon powder screw feeder are both connected with a feed inlet of the chlorination bed feeder through a pipeline;
a feed discharge opening of the chlorination bed feeder is connected with a feed inlet at the upper part of the chlorination fluidized bed body through a pipeline; a gas inlet at the bottom of the chlorination bed feeder is connected with a nitrogen gas source main pipe through a pipeline; the chlorination bed cyclone separator is provided at the center of the top of the expansion section of the chlorination fluidized bed body; a gas outlet at the top of the chlorination bed cyclone separator is connected with a hot flue gas inlet of the flue gas heat exchanger through a pipeline; a cold flue gas outlet of the flue gas heat exchanger is connected with a gas inlet of the flue gas condenser through a pipeline; a gas outlet of the flue gas condenser is connected with a gas inlet of the chlorination bed acid-seal tank through a pipeline; a gas outlet of the chlorination bed acid-seal tank is connected with a gas inlet of the tail gas washing absorber through a pipeline; a slag-discharge opening at the lower part of the chlorination fluidized bed body is connected with a feed inlet of the chlorination bed spiral slag-discharging device through a pipeline; a gas inlet at the bottom of the chlorination fluidized bed body is connected with a hot gas outlet of the flue gas heat exchanger through a pipeline; and a cold gas inlet of the flue gas heat exchanger is connected with a chlorine gas source main pipe, the nitrogen gas source main pipe and a compressed air main pipe through pipelines, respectively;
a liquid outlet at the bottom of the flue gas condenser is connected with a feed inlet of the rectifying column through a pipeline; a steam outlet of the distilling still is connected with a steam inlet of the rectifying column through a pipeline; a backflow inlet of the distilling still is connected with a liquid reflux outlet at the bottom of the rectifying column through a pipeline; a gas outlet at the top of the rectifying column is connected with a gas inlet of the distillate condenser through a pipeline; a liquid outlet of the distillate condenser is connected with a liquid inlet of the reflux liquid collecting tank through a pipeline; a reflux liquid outlet of the reflux liquid collecting tank is connected with a reflux liquid inlet at the top of the rectifying column through a pipeline; a feed discharge opening of the reflux liquid collecting tank is connected with an inlet of the silicon-containing vanadium oxytrichloride storage tank through a pipeline; an exhaust gas outlet of the silicon-containing vanadium oxytrichloride storage tank is connected with a gas inlet of the rectification section acid-seal tank through a pipeline; a gas outlet of the rectification section acid-seal tank is connected with a gas inlet of the tail gas washing absorber through a pipeline; a rectificate outlet of the rectifying column is connected with a gas inlet of the high-purity vanadium oxytrichloride condenser through a pipeline; a liquid outlet of the high-purity vanadium oxytrichloride condenser is connected with a liquid inlet of the high-purity vanadium oxytrichloride storage tank through a pipeline; and an underflow outlet is provided at the bottom of the distilling still;
a gas inlet of the hydrolyzation bed air purifier is connected with the compressed air main pipe through a pipeline; a gas outlet of the hydrolyzation bed air purifier is connected with a gas inlet of the hydrolyzation bed gas heater, a gas inlet of the vanadium oxytrichloride nozzle, and a gas inlet at the bottom of the hydrolyzation bed discharger through pipelines, respectively; a combustion-supporting wind inlet and a fuel inlet of a combustion nozzle of the hydrolyzation bed gas heater are respectively connected with the compressed air main pipe and a fuel main pipe through pipelines; the gas inlet of the hydrolyzation bed gas heater is connected with a ultrapure water main pipe through a pipeline; a gas outlet of the hydrolyzation bed gas heater is connected with a gas inlet at the bottom of the gas phase hydrolyzation fluidized bed body through a pipeline; a liquid outlet of the high-purity vanadium oxytrichloride storage tank is connected with a vanadium oxytrichloride inlet of the vanadium oxytrichloride nozzle through a pipeline; a gas outlet at the top of the expansion section of the gas phase hydrolyzation fluidized bed body is connected with a gas inlet of the hydrochloric acid tail gas absorber through a pipeline; a hydrochloric acid solution outlet is provided at the bottom of the hydrochloric acid tail gas absorber; a gas outlet of the hydrochloric acid tail gas absorber is connected with a gas inlet of the tail gas washing absorber through a pipeline; a feed outlet at the upper part of the gas phase hydrolyzation fluidized bed body is connected with a feed inlet of the hydrolyzation bed discharger through a pipeline; and a feed discharge opening of the hydrolyzation bed discharger is connected with a feed inlet at the upper part of the calcination fluidized bed body through a pipeline;
a gas inlet of the calcination bed air purifier is connected with the compressed air main pipe through a pipeline; a gas outlet of the calcination bed air purifier is connected with a gas inlet of the calcination bed gas heater through a pipeline; a combustion-supporting wind inlet and a fuel inlet of a combustion nozzle of the calcination bed gas heater are respectively connected with the compressed air main pipe and the fuel main pipe through pipelines; a gas outlet of the calcination bed gas heater is connected with a gas inlet at the bottom of the calcination fluidized bed body through a pipeline; a gas outlet at the top of the calcination fluidized bed body is connected with a gas inlet at the bottom of the gas phase hydrolyzation fluidized bed body through a pipeline; and a feed discharge openin

Assignees

• Inst Process Eng Cas
• Beijing Zhongkaihongde Tech Co Ltd
• Beijing Zhongkaihong De Tech Co Ltd

Inventors

• Fan Chuanlin
• Zhu Qingshan
• Mu Wenheng
• Liu Jibin
• Wang Cunhu
• Ban Qixun

Classifications

• B01J6/004

  using hot gas streams in which the material is moved · CPC title

• B01J2219/00166

  controlling the residence time inside the reactor vessel · CPC title

• C01G31/04

  Halides · CPC title

• Y02E60/36

  Hydrogen production from non-carbon containing sources, e.g. by water electrolysis · CPC title

• C01G31/02 Primary

  Oxides · CPC title