II. Electrodeposition/Removal of Nickel in a Spouted Electrochemical Reactor

Grimshaw, Pengpeng; Calo, J.M.; Shirvanian, Pezhman; Hradil, G.

doi:10.1021/ie200669b

Cited by 21 publications

(47 citation statements)

References 42 publications

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“…16 As shown in Figures 2 and 3, for co-electrodeposition, copper generally behaved as previously, except with a much more rapid net removal rate. Nickel behavior, however, was more complex, such that the maximum net electrodeposition rate occurred at about pH 4.…”

Section: Resultssupporting

confidence: 72%

“…where the subscripts are: 1 = copper; 2 = nickel; and 3 = hydrogen , respectively; z i , i i and C i are the corresponding charge, cathodic current density, and bulk phase concentration; F is Faraday's constant; k j is the electrochemical reduction rate constant, which depends on the electrode overpotential according to the Tafel approximation; 15,16,21 k L is the mass transfer coefficient given by Pickett 22 for a single layer packed bed electrode, and a is the interfacial surface area per unit volume. The resultant mass balances for the two metal cations are:…”

Section: Co-electrodeposition Modelmentioning

confidence: 99%

“…Also, it is assumed that the metal displacement reaction is first order in the copper cation concentration, C 1 , with the rate constant k d , and the k ci are the apparent corrosion rate constants for the two metals, which are zeroth order in the metal cation concentration, and first order in DO and [H + ]. 15,16,23 …”

Section: Co-electrodeposition Modelmentioning

confidence: 99%

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III. Co-electrodeposition/Removal of Copper and Nickel in a Spouted Electrochemical Reactor

Grimshaw

Calo

Hradil

2011

Ind. Eng. Chem. Res.

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Results are presented of an investigation of co-electrodeposition of copper and nickel from acidic solution mixtures in a cylindrical spouted electrochemical reactor. The effects of solution pH, temperature, and applied current on metal removal/recovery rate, current efficiency, and corrosion of the deposited metals from the cathodic particles were examined under galvanostatic operation. The quantitative and qualitative behavior of co-electrodeposition of the two metals from their mixtures differs significantly from that of the individual single metal solutions. This is primarily attributed to the metal displacement reaction between Ni0 and Cu2+. This reaction effectively reduces copper corrosion, and amplifies that for nickel (at least at high concentrations). It also amplifies the separation of the deposition regimes of the two metals in time, which indicates that the recovery of each metal as a relatively pure deposit from the mixture is possible. It was also shown that nitrogen sparging considerably increases the observed net electrodeposition rates for both metals – considerably more so than from solutions with just the single metals alone. A numerical model of co-electrodeposition, corrosion, metal displacement, and mass transfer in the cylindrical spouted electrochemical reactor is presented that describes the behavior of the experimental copper and nickel removal data quite well.

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Section: Resultssupporting

confidence: 72%

Section: Co-electrodeposition Modelmentioning

confidence: 99%

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III. Co-electrodeposition/Removal of Copper and Nickel in a Spouted Electrochemical Reactor

Grimshaw

Calo

Hradil

2011

Ind. Eng. Chem. Res.

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“…Besides, the literature related to nickel electrowinning was largely reported [19,20]. Electrodeposition of nickel ions from acidic solution in a cylindrical spouted electrochemical reactor was also reported [21]. Generally, anodic oxidation of organic complexes was characterized by a relatively low current efficiency.…”

Section: Introductionmentioning

confidence: 99%

Simultaneous destruction of Nickel (II)-EDTA with TiO2/Ti film anode and electrodeposition of nickel ions on the cathode

Zhao

Guo

et al. 2014

Applied Catalysis B: Environmental

101

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a b s t r a c tEthylenediaminetetraacetic acid (EDTA) forms stable complexes with toxic metals such as nickel. A combined photocatalytic-electrochemical system using TiO 2 /Ti plate as anode and stainless steel as cathode achieves the simultaneous decomplexation of Ni-EDTA and recovery of nickel. Ni-EDTA was efficiently destroyed in photoelectrocatalytic process in comparison with individual photocatalytic and electrooxidation process. At 60 min, removal efficiencies of Ni-EDTA were 75%, 12%, and 5%, respectively. At 180 min, the removal efficiency of Ni-EDTA in the photocatalysis and electrolysis processes is only 21% and 18%, respectively. By contrast, nearly 90% Ni-EDTA is removed in the photoelectrocatalytic process. The recovery percentage of nickel was determined to be 45%, 21%, and 5% in the photoelectrocatalysis, electrolysis, and photocatalysis process, respectively. The deposition of nickel ions at the cathode was confirmed by scanning electron microscopy analysis and the nickel species were identified via X-ray photoelectron spectra as nickel with zero value. The removal of Ni-EDTA and recovery of nickel ions increased with the current density and favored at acid conditions. Intermediates detected using a capillary electrophoresis and a high performance liquid chromatography includes Ni-NTA, glycine, maleic acid, glycolic acid, formic acid, acetic acid, oxalic acid, and oxamic acid were identified. The decomplexation pathway of Ni-EDTA was proposed.

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“…Electrochemical reaction over the electrode surface is influenced by the operational parameters including electrolyte concentration, electrolyte initial pH, metal ion initial concentration and applied electrical current density which have been studied or optimized by several researchers (Grimshaw et al 2011;Kaminari et al 2007;Rana et al 2004).…”

Section: Introductionmentioning

confidence: 99%

Improvement of cadmium ion electrochemical removal from dilute aqueous solutions by application of multi-stage electrolysis

Baghban

Mehrabani-Zeinabad

Moheb

2014

Int. J. Environ. Sci. Technol.

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Improvement of cadmium ion electrochemical removal from dilute aqueous solutions in a spouted bed reactor was investigated. Enlargement of cathode surface area from 1,000 to 1,500 cm 2 resulted in a decrease of nearly 30 % in both of the process time and the specific energy consumption. Application of a three-stage electrolysis process for a solution containing initial concentration of 270 ppm cadmium ion, resulted in the removal of 99.9 % cadmium ion in 135 min with the specific energy consumption of 2.29 kWh/kg, 23 % less than the value of a single-stage process. For a solution with cadmium ion initial concentration of 180 ppm, 99.9 % of cadmium ion was removed in 135.5 min by application of a two-stage electrolysis process, while the specific energy consumption was 2.82 kWh/kg, 30 % less than that of a single-stage process. For a solution with cadmium ion initial concentration of 90 ppm, 99.5 % of cadmium ion was removed in 100.2 min with the specific energy consumption of 3.78 kWh/kg in a single-stage electrolysis process.

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II. Electrodeposition/Removal of Nickel in a Spouted Electrochemical Reactor

Cited by 21 publications

References 42 publications

III. Co-electrodeposition/Removal of Copper and Nickel in a Spouted Electrochemical Reactor

III. Co-electrodeposition/Removal of Copper and Nickel in a Spouted Electrochemical Reactor

Simultaneous destruction of Nickel (II)-EDTA with TiO2/Ti film anode and electrodeposition of nickel ions on the cathode

Improvement of cadmium ion electrochemical removal from dilute aqueous solutions by application of multi-stage electrolysis

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