Method for removing chlorine radicals and sulfate radicals in zinc hypoxide raw material

A technology of secondary zinc oxide and sulfate, applied in chemical instruments and methods, zinc oxide/zinc hydroxide, calcium/strontium/barium sulfate, etc., can solve the rising price of low-chlorine and low-sulfate raw materials and the reduction of electrowinning equipment Electric efficiency, pipeline blockage equipment efficiency, etc., to improve the added value of products, solve the enrichment of chloride and sulfate, and have the effect of strong operability

Pending Publication Date: 2021-08-24
江西思远再生资源有限公司
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  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

[0003] The types of raw materials used in wet leaching are various, and it is unavoidable that soluble sulfate radicals and chloride salts enter the leaching system. After entering the production system, chloride salts will continue to be enriched with the continuous entry of raw materials. Due to the chloride ion itself It is highly corrosive to metal equipment. At the same time, chlorine salts generally have a large solubility and are also very sensitive to temperature changes. Therefore, when the solution temperature fluctuates during the production process, it is easy to get out of the solution. Preci...

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  • Method for removing chlorine radicals and sulfate radicals in zinc hypoxide raw material

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Embodiment 1

[0037] Will contain Cu: 0.05g / L, Cd: 0.05g / L, Pb: 1.5g / L, Zn: 1.0g / L, SO 4 2- : 48g / L, Cl - : 200g / L, NH 4+ : 1L of 100g / L raffinate and 600mL of 1mol / L calcium chloride solution were mixed by pumping at the same time. The feeding time was 1 hour. After reacting for 1.0h at 50°C, stop stirring and age for 1.0h. Then the mixed solution is suction-filtered with a vacuum pump and a Buchner funnel to obtain calcium sulfate solid and calcium sulfate supernatant, and the obtained calcium sulfate solid is dried at 60° C. for 24 hours to obtain a dry calcium sulfate dihydrate by-product.

[0038] Detection of NH in solution 4+ The content is 98.6g / L, and 184.1g of lime is put into the supernatant of calcium sulfate through the lime feeding system for pre-deamination. Above 12.0, the temperature of ammonium distillation is 80°C, and the time of ammonium distillation is 180min. The obtained ammonia gas is collected through an ammonia gas absorption tower to obtain regenerated ammoni...

Embodiment 2

[0042] Will contain Cu: 0.10g / L, Cd: 0.02g / L, Pb: 1.6g / L, Zn: 1.2g / L, SO 4 2- : 60g / L, Cl - : 196g / L, NH 4+ : 1L of 108g / L raffinate and 750mL of 1mol / L calcium chloride solution were mixed by pumping at the same time. The feeding time was 1 hour. After reacting for 1.0h at 60°C, stop stirring and age for 1.0h. Then the mixed solution is suction-filtered with a vacuum pump and a Buchner funnel to obtain calcium sulfate solid and calcium sulfate supernatant, and the obtained calcium sulfate solid is dried at 60° C. for 24 hours to obtain a dry calcium sulfate dihydrate by-product.

[0043] Detection of NH in solution 4+The content is 105.6g / L, and 197.1g of lime is put into the supernatant of calcium sulfate through the lime feeding system for pre-deamination. Above 12.0, the temperature of ammonium distillation is 85°C, and the time of ammonium distillation is 120min. The obtained ammonia gas is collected through an ammonia gas absorption tower to obtain regenerated ammoni...

Embodiment 3

[0047] Will contain Cu: 0.08g / L, Cd: 0.04g / L, Pb: 1.1g / L, Zn: 1.7g / L, SO 4 2- : 30g / L, Cl - : 200g / L, NH 4+ : 1L of 110g / L raffinate and 375mL of 1mol / L calcium chloride solution were mixed by pumping at the same time. The feeding time was 1 hour. After reacting for 1.0h at 60°C, stop stirring and age for 1.0h. Then the mixed solution is suction-filtered with a vacuum pump and a Buchner funnel to obtain calcium sulfate solid and calcium sulfate supernatant, and the obtained calcium sulfate solid is dried at 60° C. for 24 hours to obtain a dry calcium sulfate dihydrate by-product.

[0048] Detection of NH in solution 4+ The content is 106.3g / L, and 198.4g of lime is put into the supernatant of calcium sulfate through the lime feeding system for pre-deamination. Above 12.0, the temperature of ammonium distillation is 85°C, and the time of ammonium distillation is 180min. The obtained ammonia gas is collected through an ammonia gas absorption tower to obtain regenerated ammon...

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Abstract

The invention discloses a method for removing chlorine radicals and sulfate radicals in a zinc hypoxide raw material, which comprises the following steps: A, mixing and reacting raffinate containing chlorine radicals, sulfate radicals, ammonium radicals and a small amount of metal ions with a calcium chloride solution to obtain mixed turbid liquid, and carrying out solid-liquid separation on the mixed turbid liquid to obtain calcium sulfate solid and calcium sulfate supernate; B, drying the calcium sulfate solid to obtain calcium sulfate dihydrate; C, adding lime into the calcium sulfate supernatant through a lime feeding system, and carrying out pre-deamination to obtain a deamination liquid; and D, pumping the deamination liquid into a deamination tower, carrying out steam stripping deamination on the deamination liquid, and collecting obtained ammonia gas through an ammonia gas absorption tower to obtain regenerated ammonia water. The method for removing the chlorine radicals and the sulfate radicals in the zinc hypoxide raw material adopts the structure, is simple in process, short in flow and high in operability, can solve the problem of enrichment of the chlorine radicals and the sulfate radicals in the zinc hypoxide raw material comprehensively recovered by a traditional process, and reduces the production cost.

Description

technical field [0001] The invention relates to the technical field of hydrometallurgy, in particular to a method for removing chloride radicals and sulfate radicals in secondary zinc oxide raw materials. Background technique [0002] In hydrometallurgy, the mainstream process of raw material leaching is acid leaching. However, acidic leaching requires high acidity, and a large amount of non-target metals will also be leached into the solution. In the subsequent purification process, metal ions such as Fe ions in conventional treatment will form colloids, making the solution basically impossible to filter Or replacement purification consumes a large amount of acid. Therefore, more and more companies start to use chlorine salt leaching. The obvious advantage of ammonium salt leaching is that iron ions will not be leached out of the solution, and the solution can maintain a high pH value. During replacement purification, the consumption of replacement products can be signifi...

Claims

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Application Information

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IPC IPC(8): C01F11/46C01F11/28C01C1/10C01C1/02C01G9/02C22B19/20C22B7/02
CPCC01F11/46C01F11/28C01C1/10C01C1/022C01C1/026C01G9/02C22B19/24C22B19/26C22B7/02C22B7/008C01P2006/80Y02P10/20
Inventor 董飘平蒋航宇刘宇豪赵尹
Owner 江西思远再生资源有限公司
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