Current work deals with the treatment of leachate nanofiltration concentrate which was exposed to ultrafiltration membrane treatment following anaerobic biological process and nitrification–dentrification process before. Advanced electrocoagulation processes [electro-Fenton (EF) and electro-persulfate (EF)] were applied to the wastewater characterized by high inert COD content arising from resistant organic matter. Response surface methodology and central composite design were employed for modeling and optimizing the processes. Adequacy of the model was examined by application of variance analysis that verified the conformity of experimental and predicted data. Under statistically obtained optimized conditions for COD removal (H 2 O 2 /COD ratio 1.42, current 2.27 A, pH 2.9, and reaction time 30.3 min for EF; and S 2 O 8 −2 /COD ratio 1.72, current 1.26 A, pH 5.0 and reaction time 34.8 min for EP processes), predicted COD removal efficiencies were determined to be 67.1% and 72.6% for EF and EP treatments, respectively. By performing experimental sets for validation, 60.8% and 71.4% COD removals through EF and EP processes were obtained under these conditions. NF concentrate COD fractions were also determined before and after treatment processes. Soluble COD fraction increased from 71.4 to 83.2% and 87.7% whereas biodegradable COD fraction increased from 12.2 to 19.2% and 32.5% after EF and EP processes, respectively. Results of the study showed that both EF and EP processes were efficient alternatives for leachate NF concentrate treatment but EP process can be preferred due to lower energy consumption. Electro-Fenton and Electro-Persulfate processes were applied for inert COD removal from leachate nanofiltration concentrate. Response surface methodology approach using Central Composite Design was employed for modelling. Under statistically optimized conditions 60.8% and 71.4% COD removals through EF and EP processes were obtained. Biodegradable COD fraction increased and insoluble COD fraction was significantly converted to soluble fraction. Total cost of EF process (5.0 €/ m 3 ) was found to be higher than that of and EP process (2.8 €/ m 3 ).

中文翻译：

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使用中心复合设计通过电芬顿和电过硫酸盐工艺处理浓缩渗滤液

目前的工作涉及处理渗滤液纳滤浓缩液，该浓缩液经过厌氧生物工艺和硝化-反硝化工艺后经过超滤膜处理。先进的电凝聚工艺[电芬顿 (EF) 和电过硫酸盐 (EF)] 被应用于废水，其特征是由抗性有机物产生的高惰性 COD 含量。响应面方法和中心复合设计被用于建模和优化过程。通过应用方差分析来检查模型的充分性，该分析验证了实验数据和预测数据的一致性。在统计获得的优化 COD 去除条件下（H 2 O 2 /COD 比为 1.42，电流为 2.27 A，pH 2.9，EF 的反应时间为 30.3 分钟；S 2 O 8 -2 /COD 比为 1.72，电流 1.26 A、pH 5.0 和反应时间 34.8 分钟（EP 工艺），预计 EF 和 EP 处理的 COD 去除效率分别为 67.1% 和 72.6%。通过进行实验组验证，在这些条件下通过 EF 和 EP 工艺获得了 60.8% 和 71.4% 的 COD 去除率。NF 浓缩物 COD 分数也在处理过程之前和之后确定。在 EF 和 EP 工艺后，可溶性 COD 分数从 71.4% 增加到 83.2% 和 87.7%，而可生物降解 COD 分数分别从 12.2% 增加到 19.2% 和 32.5%。研究结果表明，EF 和 EP 工艺都是渗滤液 NF 浓缩物处理的有效替代方案，但由于能耗较低，EP 工艺可能是首选。电芬顿和电过硫酸盐工艺用于从渗滤液纳滤浓缩物中去除惰性 COD。使用中央复合设计的响应面方法被用于建模。在统计优化的条件下，通过 EF 和 EP 工艺获得了 60.8% 和 71.4% 的 COD 去除率。可生物降解的 COD 部分增加，不溶性 COD 部分显着转化为可溶部分。发现 EF 工艺的总成本 (5.0 €/ m 3 ) 高于 EP 工艺 (2.8 €/ m 3 )。可生物降解的 COD 部分增加，不溶性 COD 部分显着转化为可溶部分。发现 EF 工艺的总成本 (5.0 €/ m 3 ) 高于 EP 工艺 (2.8 €/ m 3 )。可生物降解的 COD 部分增加，不溶性 COD 部分显着转化为可溶部分。发现 EF 工艺的总成本 (5.0 €/ m 3 ) 高于 EP 工艺 (2.8 €/ m 3 )。