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Electroplating heavy metal ion back-bath sodium removing process

A technology of heavy metal ions and electroplating process, which is applied in the direction of ion exchange water/sewage treatment, electrolysis process, electrolysis components, etc. It can solve the problems of poor corrosion resistance, loose coating, affecting the quality of electroplating coating, etc., and achieve low free acid content , the effect of low sodium ion content

Active Publication Date: 2021-12-07
南京昆腾化工科技有限公司 +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

In the prior art, heavy metal ions and water in electroplating wastewater can be recovered through ion exchange. The water can be directly reused in the electroplating line, and the heavy metal ions can also be reused in the electroplating line after further concentration. However, the heavy metal ion solution separated by the existing ion exchange technology contains Higher concentration of sodium ions and free acids; as the reuse time increases, sodium ions and free acids will continue to accumulate in the electroplating bath, too high sodium ions will cause loose coatings, poor corrosion resistance, and too high free acids It will affect the pH of the electroplating solution, etc., which will seriously affect the quality of the electroplating coating

Method used

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  • Electroplating heavy metal ion back-bath sodium removing process

Examples

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Embodiment 1

[0012] This embodiment relates to a process for removing sodium from electroplating heavy metal ions back into the tank, comprising the following steps: collecting copper-containing rinsing wastewater from the electroplating production line, Cu 2+ Concentration 102mg / L, after filtration, Cu 2+ The wastewater ions enter the 110 sodium type weakly acidic cation exchange resin column for ion exchange, and the sodium type weakly acidic cation exchange resin column is saturated to adsorb Cu 2+ After ions are cleaned, first dilute with 0.75% H 2 SO 4 Countercurrent elution was performed as the eluent, the elution volume was 1.75 times the column volume, and the elution rate was 0.65 times the column volume / h; after that, 10% H 2 SO 4 For the countercurrent elution of the eluent, the elution flow rate volume is 2.5 times the column volume / h, and the Cu-containing 2+ The ion effluent is concentrated and returned to the electroplating process line for use.

[0013] Cu in this exam...

Embodiment 2

[0024] The present embodiment specifically comprises the following steps: collecting nickel-containing rinsing waste water from the electroplating production line, Ni 2+ Concentration 118mg / L, after filtration, Ni 2+ The waste water enters the 116 sodium type weakly acidic cation exchange resin column for ion exchange, and the 116 sodium type weakly acidic cation exchange resin column is saturated to adsorb Ni 2+ After ions are cleaned, first dilute with 0.5% H 2 SO 4 Countercurrent elution was performed as the eluent, the elution volume was 1.5 times the column volume, and the elution rate was 0.5 times the column volume / h; after that, 10% H 2 SO 4 For the countercurrent elution of the eluent, the elution flow rate volume is 2 times the column volume / h, and the Ni-containing 2+ The ion effluent is concentrated and returned to the electroplating process line for use.

[0025] Ni in this example 2+ Ionic effluent, Ni 2+ Concentration 30g / L, Na + <1mg / L, pH 6.5.

Embodiment 3

[0033] This embodiment specifically includes the following steps: collecting zinc-containing rinsing wastewater from the electroplating production line, Zn 2+ Concentration 121mg / L, after filtration, Zn 2+ The ionic wastewater enters the D152 sodium type weakly acidic cation exchange resin column for ion exchange, and the D152 sodium type weakly acidic cation exchange resin column is saturated to adsorb Zn 2+ After ion cleaning, first dilute with 1% H 2 SO 4 Countercurrent elution was performed as the eluent, the elution volume was 2 times the column volume, and the elution rate was 0.75 times the column volume / h; after that, 10% H 2 SO 4 For the countercurrent elution of the eluent, the elution flow rate volume is 3 times the column volume / h, and the collected Zn-containing 2+ The ion effluent is concentrated and returned to the electroplating process line for use.

[0034] In this example Zn 2+ Ionic effluent, Zn 2+ Concentration 31g / L, Na + <1mg / L, pH 6.5.

[0035]...

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Abstract

The invention relates to an electroplating heavy metal ion back-tank sodium removing process, which comprises the following steps: collecting electroplating heavy metal ion wastewater, carrying out rough filtration and fine filtration, and enabling a heavy metal ion solution to pass through a sodium type weak acid cation exchange resin column to exchange and adsorb heavy metal ions; and after the adsorption is saturated, eluting the cation exchange column by dilute acid and concentrated acid respectively, collecting effluent of heavy metal ions, and concentrating and returning theeffluent of heavy metal ions to an electroplating process line for use. The method can greatly reduce the concentration of sodium ions and free acid in the bath return liquid, and meets the use stability of electroplating heavy metal ions in the bath return.

Description

technical field [0001] The invention relates to a technology in the field of electroplating heavy metals and water recovery, in particular to a process for removing sodium by electroplating heavy metal ions back into the tank. Background technique [0002] The electroplating industry is one of the industries with serious environmental pollution, especially the pollution of heavy metal wastewater. The existing electroplating heavy metal wastewater is mainly treated by flocculation and sedimentation at the end of the electroplating line, resulting in a large amount of hazardous waste sludge, resulting in a large waste of resources and high treatment costs; the effluent of this terminal treatment technology contains particulate matter and contains relatively high High salt concentration can easily cause membrane fouling, resulting in low efficiency of subsequent membrane separation water recovery and reduced membrane life. [0003] The existing technology has developed a varie...

Claims

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Application Information

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IPC IPC(8): C02F9/04C02F1/42C25D21/18C02F101/20C02F103/16
CPCC02F1/42C02F1/001C25D21/18C02F2103/16C02F2101/20C02F2001/425C02F2303/14C02F2303/16Y02P10/20
Inventor 袁华周保学袁玥文李金花
Owner 南京昆腾化工科技有限公司
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