本實驗使用鐵作為電解的電極板，藉由電混凝(EC)及電Fenton法(ECF)程序處裡電鍍廢水。由於電鍍廢水具有高導電度(> 11 mS/cm)及低pH值(< 2)的特性，適合使用EC及ECF程序來去除水中重金屬及有機污染物。在此實驗中探討了不同的實驗參數對重金屬和有機物的去除效果，包括反應時間，初始pH和電流密度。
在反應時間為四分鐘、電流密度為24.15 mA / cm2的條件下，可以完全去除金屬污染物，但化學需氧量(COD)只有40％能被去除。而在固定理論的鐵添加劑量下，增加電流密度並不會影響金屬及COD的去除效率，反而需要更多的能量消耗。例如:比較電流密度4.83mA / cm 2、反應時間20分鐘及電流密度77.29mA / cm 2、反應時間1.25分鐘，兩種條 件下，前者所消耗的能量為1.69kWh / m3、後者為13.4kWh / m3，高電流密度下能量消耗明顯更多。在污泥方面，低電流條件下，產生褐色的氫氧化鐵污泥(Fe (OH)3)，而在高電流條件下產生的污泥為綠色的氫氧化亞鐵(Fe(OH)2)。氫氧化亞鐵具有對水較高的溶解度，會嚴重影響處理後的水質。
EC程序在對COD的處理上較為不足，進而採用ECF程序來補足。在H2O2/Fe（II）莫耳比為5的情況下，ECF對COD的去除率達到67％以上， 符合台灣EPA的排放標準(COD < 100 mg/L)。此時若增加電流密度， COD的去除率會略為下降。

Electrocoagulation (EC) and Electrochemical Fenton (ECF) processes using iron electrodes were employed to treat electroplating wastewater. The wastewater is suitable for the EC and ECF treatment due to high in conductivity (>11 mS/cm) and low in pH (~2). Different experiment parameters were investigated including electrolytic time, initial pH, and current density on the removal of heavy metals and organic. A completed removal of metal contaminants was achieved, whereas only 40% of chemical oxygen demand was removed with the electric current density of 24.15 mA/cm2 and electrolytic time of 4 min. At the fixed theoretical iron dose, the increase of current density had no improvement in removal efficiency but increased energy usage. The energy consumption was approximate 1.69 kWh/m3 at a current density of 4.83 mA/cm2 and a reaction time of 20 min but it dramatically increased to 13.4 kWh/m3 at a current density of 77.29 mA/cm2 and a reaction time of 1.25 min. Under the low current condition, a brown color sludge was produced, which is associated with ferric hydroxide. On the contrary, a greenish color sludge was created under the high current condition, suggesting the formation of ferrous hydroxide. Ferrous hydroxide with a relatively high solubility profoundly impacted the treated water quality. The ECF process was employed to overcome the low COD removal of the EC process. At the H2O2:Fe(II) molar ratio of 5, the ECF achieved > 67% of COD removal and met the regulatory COD level of 100 mg/L. At the fixed H2O2:Fe(II) molar ratio of 5, increasing current density resulted in the slight decrease of COD removal.

Table of content
Abstract:	I
List of Figure	V
List of Table	VIII
Chapter 1 Introduction	1
1.1 Study background	1
1.2 Study objectives	4
1.3 Research scope	4
Chapter 2 Background information	5
2.1 Electroplating wastewater	5
2.2 Heavy metals removal methods for plating wastewater	6
2.2.1 Adsorption	6
2.2.2 Coagulation-flocculation	8
2.2.3 Membrane filtration	9
2.2.4 Electrodialysis	10
2.2.5 Ion-exchange	11
2.3 Electrocoagulation	13
2.3.1 Fundamental of electrocoagulation	13
2.3.2 Factors affecting electrocoagulation	16
2.4 Electrochemical-Fenton process	21
Chapter 3 Material and methods	25
3.1 Wastewater characteristics	25
3.2 Experimental set-up and procedures	26
3.2.1 Electrochemical cell	26
3.2.2 Electrocoagulation process	26
3.2.3 Electrochemical-Fenton process	27
3.3 Analysis methods	29
Chapter 4 Results and Discussions	31
4.1 Electrocoagulation process	31
4.1.1 Effect of coagulant dosage	31
4.1.2 Effect of current density	34
4.1.3 Effect of initial pH	38
4.2 Electrochemical-Fenton process	43
4.2.1 Effect of H2O2:Fe(II) ratios	43
4.2.2 Effect of current	47
Chapter 5 Conclusions and suggestions	49
5.1 Conclusions	49
5.2 Recommendations	50
Reference	51

 
List of Figure
Figure 1. Schematic framework of functional cation exchange resin: (a) resin immersed in an aqueous solution containing B+ cation and X- anions and (b) cation exchange resin in equilibrium with aqueous solution of B+ cations and X- anions [28].	11
Figure 2. Schematic diagram of bench-scale electrocoagulation process [45].	13
Figure 3. Attractive and repulsive potential energy that result when two particles are brought together [48].	16
Figure 4. The standard redox potential of iron and aluminium	18
Figure 5. Percent of Fe ions precipitation as a function of pH for Fe(II) and Fe(III) ions using chemical equilibrium software, Mineql+ (version Mineql+ 4.6). Total ferrous and ferric concentration added 10-3 M.	19
Figure 6. Schematic representation of different categories of electro-Fenton process based on Fenton's reagent: (A) Electro-Fenton process; (B) Fered-Fenton process; (C) Electrochemical-Fenton process.	24
Figure 7. Schematic diagram of EC process	27
Figure 8. Schematic diagram of ECF process.	28
Figure 9. The removal efficiency vs. reaction time. Experiment condition: initial pH = 7; stirring rate = 100 rpm; current density = 24.15 mA/cm2.	32
Figure 10. The standard redox potential of various metal ions.	33
Figure 11. (A) Sludge settling after EC process vs. reaction times. (B) The percentage of Fe(II) in sludge and final pH as a function of reaction time. Experiment condition: initial pH = 7; stirring rate = 100 rpm; current density = 24.15 mA/cm2.	34
Figure 12. Contaminants removal under different current vs. current density. Experiment condition: fixed iron dosage 174 mg/L; initial pH = 7; stirring rate = 100 rpm.	36
Figure 13. Energy consumption vs. current density. Experiment condition: fixed iron dosage 174 mg/L; initial pH = 7; stirring rate = 100 rpm.	37
Figure 14. Sludge quality under various current density. Experiment condition: fixed iron dosage 174 mg/L; initial pH = 7; stirring rate = 100 rpm.	37
Figure 15. (A) Contaminants removal vs. initial pH. (B) Fe(II) concentration in solution. Experiment condition: fixed iron dosage 174 mg/L; stirring rate = 100 rpm; current density = 24.15 mA/cm2.	40
Figure 16. (A) Sludge settling after EC with various initial pH values. (B) The percentage of Fe(II) in the sludge and final pH as a function of initial pH values. Experiment condition: fixed iron dosage 174 mg/L; stirring rate = 100 rpm; current density = 24.15 mA/cm2.	41
Figure 17. Precipitation pH of ferrous hydroxide as a function of total ferrous concentration added (Modeled by Mineql+ chemical equilibrium modeling program).	42
Figure 18. Current efficiency under different initial pH, fixed dosage 174 mg/L, current density 24.15 mA/cm2.	43
Figure 19. (A) Effect of H2O2:Fe(II) molar ratios on the removal efficiencies for fixed theoretical Fe dosage of 174 mg/L. (B) Ni removal using chemical coagulation process; Fe(II) and Fe(III) as coagulant; pH 7.	45
Figure 20. H2O2 efficiency vs. H2O2 dose on the COD removal by oxidation	47
Figure 21. Effect of current on the contaminants removal efficiency. Experiment condition: fixed theoretical Fe dosage of 174 mg/L; H2O2:Fe(II) molar ratio = 5:1; mechanic mixing; electrode area was around 20.7 cm2.	48
 
List of Table
Table 1. Electroplating wastewater characteristic [1, 27]	6
Table 2. Classification electro-Fenton process [59]	22
Table 3. The characteristics of electroplating wastewater	25

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