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Calcification roasting clinker counter-flow acid pickling vanadium extracting method

A technology of calcification roasting and countercurrent acid is applied in the direction of improving process efficiency, which can solve the problems of low vanadium extraction rate and low vanadium product quality, and achieve the effects of high concentration, fast and efficient leaching, and high vanadium product quality.

Active Publication Date: 2019-02-15
CHENGDU ADVANCED METAL MATERIALS IND TECH RES INST CO LTD +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0007] Aiming at the defects of relatively low vanadium extraction rate and low vanadium product quality in the field of vanadium extraction in the prior art, the present invention provides a method for countercurrent acid leaching of vanadium with high vanadium extraction rate and good product quality

Method used

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  • Calcification roasting clinker counter-flow acid pickling vanadium extracting method

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0045] First-stage leaching: Add 200 g of calcified roasted clinker (TV=8.66%) to the mixed solution of pH=2.6, 150 mL of the first-stage filtrate and 350 mL of the second-stage leaching liquid, and use sulfuric acid to control the system pH=2.8-3.0 under stirring conditions , control the temperature at 50°C and leaching for 45 minutes, filter the first-stage leachate and filter residue, measure TV=33.87g / L, P=0.02g / L in the first-stage leachate, the pH of the first-stage leachate is 3.1; =7 times of washing with water, the pH of the first stage filtrate is 3.5;

[0046] Second-stage leaching: After washing, the filter residue is leached with the mixed solution of the third-stage leachate + third-stage filtrate with a pH of 1.42, and filtered to obtain the second-stage leachate with pH = 2.5;

[0047] The third stage leaching: add the filter residue to pH=0.7, 200mL reuse water for leaching the third stage leaching, stir and react for 10 minutes and then filter, the pH of the ...

Embodiment 2

[0050] The first stage leaching: to pH = 2.8, the first stage filtrate 12m 3 and the second level leachate 6m 3 Add 6t of calcified roasted clinker (TV=8.66%) to the mixed solution, control the system pH=2.8-3.0 with sulfuric acid under stirring conditions, control the temperature at 41°C for 60 minutes, and filter to obtain the first-stage leachate and filter residue. TV=32.67g / L, P=0.02g / L in the first-stage leachate, the pH of the first-stage leachate is 3.05; the filter residue is washed with reused water at pH=6.78, and the pH of the first-stage filtrate is 3.41;

[0051] Second-stage leaching: After washing, the filter residue is leached with a third-stage leachate with a pH of 1.6, and filtered to obtain a second-stage leachate with a pH of 2.7;

[0052] The third stage leaching: filter residue is added to pH=1.4, 7m 3 The third-stage leaching was carried out with recycled water, and the pH of the third-stage leachate was 1.6 after stirring and reacting for 10 minutes...

Embodiment 3

[0055] The first stage leaching: to pH = 2.7, the first stage filtrate 12m 3 and the second level leachate 6m 3 Add 6.5t of calcified roasted clinker (TV=8.12%) to the mixed solution, use sulfuric acid to control the system pH=2.8-3.0 under stirring conditions, and control the temperature to 56°C for 60 minutes of leaching, and filter to obtain the first-stage leachate and filter residue, measured TV=34.35g / L, P=0.02g / L in the first-stage leachate, the pH of the first-stage leachate is 2.94; the filter residue is washed with pH=7 reuse water, and the pH of the first-stage filtrate is 2.98;

[0056] Second-stage leaching: After washing, the filter residue is leached with a third-stage leachate with a pH of 1.45, and filtered to obtain a second-stage leachate with a pH of 2.5;

[0057] The third stage leaching: filter residue is added to pH=1.0, 7m 3The third-stage leaching was carried out with reused water, stirred and reacted for 7 minutes, and then filtered. The pH of the t...

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Abstract

The invention belongs to the technical field of vanadium extraction and particularly relates to a calcification roasting clinker counter-flow acid pickling vanadium extracting method. To solve technical problems, the calcification roasting clinker counter-flow acid pickling vanadium extracting method is provided. The method comprises the following steps that a, clinker and primary filter liquor and / or secondary lixivium are mixed, sulfuric acid is added for leaching, the pH of a primary leaching process system is controlled to be 2.8-3.5, solid-liquid separation is performed to obtain primarylixivium and solids, and washing is performed to obtain primary filter liquor and solids; b, the solids are subjected to leaching by adopting tertiary lixivium or / and tertiary filter liquor, and the pH of a second leaching terminal system is controlled to be 1.8-3.5, and solid-liquid separation is performed to obtain secondary lixivium and solids; and c, the solids are subjected to leaching, the pH of a third leaching terminal system is controlled to be 1.4-2.2, solid-liquid separation is performed to obtain tertiary lixivium and solids, and washing is performed to obtain tertiary filter liquor and vanadium extracting tailings. The method provided by the invention has the advantages of high leaching vanadium extracting rate and low cost.

Description

technical field [0001] The invention belongs to the technical field of vanadium oxide extraction, and in particular relates to a method for extracting vanadium by countercurrent acid leaching of calcified roasted clinker. Background technique [0002] After the vanadium slag is calcified and roasted, the low-priced vanadium in the slag (in V 3+ , V 4+ Mainly) gradually oxidized and calcified into calcium vanadate (manganese) compounds, such as CaV 2 o 6 , Ca 2 V 2 o 7 , Ca 3 V 2 o 8 , MnCaV 2 o 7 etc. In the laboratory, the leaching temperature is 50-60°C and the leaching pH value is 2.8-3.2, and the dissolution rate of vanadium can reach about 88%. [0003] However, the vanadium dissolution and leaching rate in the on-site production process is low. The main reasons are: firstly, the on-site leaching temperature is difficult to meet the process requirements, especially when there are no insulation measures on site, the leaching temperature control is only determi...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C22B3/08C22B34/22
CPCC22B3/08C22B34/22Y02P10/20C22B3/00
Inventor 何文艺彭毅李明陈燕叶露
Owner CHENGDU ADVANCED METAL MATERIALS IND TECH RES INST CO LTD
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