本研究目的是建立一套亞硝化/厭氧氨氧化反應器系統，可以在較短的水力停留時間下(< 0.2天，因為台灣大部分工廠的可用地狹小)處理含高濃度氨氮且變異大的工業製程廢水。
　　本研究方法首先進行實驗室規模反應器系統的連續流實驗[包括：雙槽式好氧及無氧固定床反應器系統(30 L×2)、單槽式複合載體(移動床+固定床)反應器系統(10 L)，以及顆粒化污泥床反應器(20 L)]，進行亞硝化及厭氧氨氧化程序處理人造廢水及實際工業廢水中的氨氮，並比較雙槽式與單槽式系統，以及不同反應器形式的功能表現。之後基於實驗室規模研究的基礎，進而設計模場規模的雙槽式反應器[包括亞硝化固定床反應器(3 m3)+厭氧氨氧化顆粒污泥反應器(1 m3)]系統，並進行連續流處理實際煉焦廢水三級處理水的功能驗證，同時利用食品廠的甲烷化顆粒污泥作為厭氧氨氧化反應槽的植種源，測試轉植成厭氧氨氧化顆粒污泥的可行性。
　　本研究在實驗室連續流實驗結果中，發現單槽式系統因為雙層生物膜結構(外層為好氧氨氧化菌，內層為厭氧氨氧化菌)與其複雜的生化動力特性(氧在外層進行硝化反應而被耗盡後，產生的亞硝酸與氨氮繼續穿透至生物膜內層進行厭氧氨氧化反應)，使得容積轉化速率在單槽式系統 (0.2–0.3 kg N m−3 d−1)相對低於雙槽式系統(亞硝化0.6–1.4 kg N m−3 d−1; 厭氧氨氧化0.4–0.8 kg N m−3 d−1)。另外，針對厭氧氨氧化反應器形式的比較，發現固定床反應器，雖然可以在三個月內將容積轉化速率由0.1 kg N m−3 d−1提升至0.4–0.6 kg N m−3 d−1(因不織布載體具有較高的比表面積吸附大量污泥，大幅提升污泥停留時間)，但是在這之後容積轉化速率僅維持在0.6–0.7 kg N m−3 d−1，推論為固定式的載體造成流體的停滯效應，使得較弱的剪應力減少了生物膜表面的切削程度(厚的生物膜質傳較差，限制了容積轉化速率的提升)；而顆粒化污泥床雖然至少需要約一年以上的時間才能形成顆粒化污泥，並且將容積轉化速率提升至1.0 kg N m−3 d−1以上，然而維持在適當的控制條件下(液相亞硝酸氮維持在50 mg L−1以下，水力停留時間小於0.2天)，可逐步將容積轉化速率提升至2.0 kg N m−3 d−1以上，顯示顆粒污泥同樣具有極高的比表面積，不但能延長污泥停留時間，並且維持相對優於固定床或移動床的質傳，因此顯示採用雙槽式系統及顆粒污泥床作為厭氧氨氧化反應器，較適合高負荷(>1 kg N m−3 d−1)、高流量(HRT < 0.2天)或可用地面積小的工廠。
　　本研究模場驗證中，直接採用甲烷化顆粒污泥作為植種源(可減少需要至少一年才能由膠羽形成顆粒污泥的過程)，以連續流實驗處理含高氮的煉焦廢水三級處理水，結果厭氧氨氧化反應槽最大容積負荷速率及最大總氮去除效率可分別達到1.0 kg N m−3 d−1及90%以上。另外在Anammox污泥顆粒粒徑分佈分析發現218天污泥顆粒平均粒徑由0.77–0.98 mm，至513天總平均粒徑增加至1.83–1.9 mm，顯示較大的顆粒並非原先植入的污泥顆粒，而是透過厭氧顆粒轉植成Anammox顆粒過程重新形成較大的污泥顆粒，同時由污泥顆粒外觀由黑色轉為磚紅色，確實可驗證Anammox菌的特徵明顯增加，因此利用厭氧顆粒當作植種源，確實有助於啟動Anammox顆粒污泥反應器。

This study is mainly conducted to develop a nitration-anammox reactor system that can be use to remove nitrogen from industrial wastewater with a low hydraulic retention time (HRT) below 0.2 day.
In this study, continuous-flow experiments using lab-scale nitritation-anammox reactor systems, including a two-stage aerobic and anoxic fixed-bed reactor system (30 L×2), an one-stage hybrid biofilm-carrier reactor system (10 L) and a granular- sludge reactor (20 L) were first undertaken to explore their capability for removing nitrogen from synthetic wastewater and actual industrial wastewaters. Also, the performance of two-stage and one-stage reactor system, as well as of different type of reactors was discussed. After the afore-said lab-scale experiments had been completed, a pilot-scale two-stage reactor system was designed and used to evaluate the performance treating tertiary effluent of coking wastewater. Meanwhile, the methano- genic granules were selected as the seed to start up the anammox reactor in order to directly obtain anammox granules.
The results of lab-scale experiments indicated that a volumetric conversion rate (0.2–0.3 kg N m−3 d−1) of one-stage system was apparently lower than that of two- reactor system (nitritation: 0.6–1.4 kg N m−3 d−1; anammox: 0.4–0.8 kg N m−3 d−1). This is mainly because the volumetric conversion rate was governed by a complex bio-kinetics of two-layer structure biofilm in the one-stage reactor system. In reactor choice, although the volumetric loading rate of the fixed-bed reactor could increase from 0.1 kg N m−3 d−1 to 0.4–0.5 kg N m−3 d−1 within first 3 months [extending solid retention time (SRT) by using non-woven carriers with high specific surface], after that the volumetric loading rate of the fixed-bed reactor could not improve anymore and only kept at 0.5–0.6 kg N m−3 d−1. A possible explanation is that the fixed carriers resulted in a stagnating effect, leading a weak shear stress to detach biofilm (higher diffusion resistance occurs in a thicker biofilm and limits the increase of the volumetric loading rate); In contrast, although the formation of granular sludge in the granular-sludge reactor generally required to spend at least one year increasing the volumetric conversion rate above 1.0 kg N m−3 d−1, with favorable operating conditions (bulk NO2−-N concentration below 50 mg L−1, HRT < 0.2 d), the volumetric conversion rate of granular-sludge reactor could be gradually increased to above 2.0 kg N m−3 d−1. It is indicated that granular sludge reactor possesses not only a sufficient SRT, but also a better mixing rather than the fixed-bed reactor. Thus, the granular-sludge reactor can be a promising alternative to be employed in industrial wastewaters (high nitrogen loading rate, low HRT and insufficiently available footprint).
In pilot evaluation, a two-stage process of nitritation (3-m3) and anammox (1-m3) was undertaken to explore its capability for removing nitrogen from tertiary effluent of coking wastewater. Moreover, methanogenic granules were selected as the seed to start up the anammox reactor in order to directly obtain anammox granules (to avoid a long period for granulation and start-up). Results showed that the anammox reactor was successfully started up with volumetric loading rate of 1.0 kg N m−3 d−1 and nitrogen removal efficiency of 89%, respectively. According to the analysis of size diameter and distribution, average granule size of 0.77–0.98 mm at day 218 grew to 1.83–1.9 mm at day 513. The nuclei of a large proportion of anammox granules retained part of the original seed biomass. Anammox biofilm attached to the surfaces of methanogenic granule and turned red, meanwhile new anammox granules were formed (smaller, not smooth and rounded). The findings of this study are expected to develop strategies of shorter start-up and more stable operation of anammox reactor.

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