本文主要研究橡膠產業排氣中硫化氫與異味物質之處理方法，探討之內容主要分為兩大部分。第一部分探討以生物洗滌法處理排氣中硫化氫的效能，並以活性污泥曝氣槽(W × L × H = 0.40 × 0.40 × 3.00 m)安裝2mm直徑的曝氣孔的散氣管用以處理氣態的硫化氫。此研究測試在進流氣體中硫化氫濃度(C0) 50–900 ppm、曝氣強度(Q/V) 0.083–0.50 m3 m-3 min-1、曝氣深度(H ) 0.5–3.0 m、活性污泥濃度(MLSS) 970–2,800 mg L-1的條件下硫化氫的去除能力與系統操作的穩定度。實驗結果顯示在不同操作狀況下，硫化氫去除效率分別在H為0.5 m達到96%，在H大於1.0 m時則大於98%。實驗結果亦指出在總硫負荷為0.047–0.148 kg S kg-1 MLSS d-1的狀況下，並沒有發生產生污泥膨化的問題。
第二部分之研究目的為去除橡膠產業排氣中的臭味成分。將樣品的橡膠粉末：熱塑性橡膠與熱固性橡膠分別置於維持在160°C及200°C的烘箱中加熱後產生臭氣，再將該氣體抽引後與新鮮空氣混合成為用以測試的模擬臭氣。製備的臭氣再與含有定量的臭氧的空氣預先混合後注入接觸系統。此系統由2個具有篩孔版之板層塔加以串連，而每一塔各自有4個1-L的單元所組成。藉由控制循環水的有無進行乾式與濕式的氧化反應。實驗結果顯示濕式氧化反應較乾式操作的效能為佳。試驗結果顯示，在進氣臭氧濃度4.0 ppm、THC濃度6.5-10.3 ppm (as methane)、溫度37.3 ℃、空塔停留時間(EBRT)為12秒及L/G為0.01m3/m3之操作條件下， VOC及臭味去除率分別達97及>90%。在相同的條件下，EBRT為11.4–14.5秒時，臭味濃度從1,738–3,090降低至31–98。活性碳於臭氧系統中不論在物理與化學上對於排氣中殘餘的VOCs、臭味混合物以及臭氧均有去除效果。經濟上的分析顯示處理每1000m3的橡膠業臭氣只需要US$ 0.16，故此臭氧反應程序值得推薦使用。

This dissertation consists of two parts on the treatment of hydrogen sulfide and odorants in gases emitted from rubber processing industry. In the first part, we study performance of removal hydrogen sulfide with bioscrubber. An activated sludge aeration tank (W × L × H = 0.40 × 0.40 × 3.00 m) with a 2 mm-orifice air sparger was used to treat gaseous hydrogen sulfide (H2S). The investigation tested the operational stability as well as how the removal ability of H2S was affected by influent H2S concentration (C0 = 50-900 ppm), aeration intensity (Q/V = 0.083-0.50 m3 m-3 min-1), liquid depth (H = 0.5-3.0 m), and mixed-liquor suspended solids concentration (MLSS = 970-2,800 mg L-1). Experimental results indicate that H2S removal efficiencies of 96% and over 98% were obtained with H = 0.5 m and H > 1.0 m in the cited operation conditions, respectively. Experimental results also indicate no sludge bulking problem occurred with total sulfide loadings of 0.047-0.148 kg S kg-1 MLSS d-1.
The second part aimed at the removal of odorous compounds in gases emitted from rubber processing industries. Simulated odorous gas for test was prepared by mixing fresh air and an odorous gas drawn from an oven in which a sample of rubber powder was kept either at 160°C (for a thermal plastic rubber) or 200°C (for a thermal setting rubber). The prepared odorous gas was then premixed with a definite amount of ozone-enriched air and introduced into a contact system. The contact system consists of two sieve-plate columns connected in series and each column has four 1-L chambers. Depending on with or without introducing circulating scrubbing water into the columns, the oxidation reaction could be either wet or dry one. Results indicate the wet oxidation got better performances than the dry one. The former got 97 and over 90% removal of VOCs (volatile organic compounds) and odorous intensity removal, respectively, with the operation conditions of initial ozone concentration 4.0 ppm, THC (total hydrocarbon) concentrations 6.5–10.3 ppm (methane equivalent), oxidation temperature 37.3°C, gas empty bed retention time (EBRT) 12 s, and liquid/gas rate ratio 0.01 m3/m3. With conditions similar to those cited above, odor concentration (dilutions to the threshold, D/T) in the test gas could be reduced from 1,738–3,090 to 31–98 with EBRTs of 11.4–14.5 s. Activated carbon is effective for both physical and chemical removals of residual VOCs, odorous compounds, and ozone in the effluent gas from the ozonation system. Economical analysis indicates that around US$ 0.16 is required for treating 1,000 m3 of the tested foul gas by the proposed ozonation process.

Table of Contents
謝誌 I
中文摘要 II
Abstract IV
Table of contents VI
List of Figures VIII
List of Tables X
Chapter1: Introduction ---------------------------------------------------1
Chapter2: Part 1
Biooxidation of Gaseous Hydrogen Sulfide in an Activated Sludge Tank
1. Introduction 13
2. Experimental methods and materials 15
2.1 Experimental setup 15
2.2 Media composition 18
2.3 Operation conditions and sequence 19
2.4 Analytical procedures 22
3. Results and discussion 22
3.1 Effects of superficial gas velocity and liquid depth 22
3.2 Effect of pH 26
3.3 Sludge settling property 27
4. Conclusions 28
5. Recommendations 29
6. Nomenclature 30

Chapter3: Part 2
Ozonation of Odorous Compounds in Gases Emitted from Rubber Processing Industries
1. Introduction 31
2. Materials and methods 34
2.1 Experimental Setup 34
2.2 Materials 36
2.3 Operations 36
2.4 Analytical 37
3. Results and Discussions 40
3.1 THC Removal 40
3.2 Reduction of Odor Intensity 45
3.3 Long-term Activated Carbon Adsorption Test 46
3.4 Odor Concentrations with the Dilution to Threshold (D/T) Method
51
3.5 Economic Analysis 52
4. Conclusion 53
5. Recommendations 54
Reference 55
作者簡歷與著作 62

List of Figures
Introduction
Figure 1. Typical Emulsion Process for Manufacturing Synthetic
Rubber 3
Figure 2. Processing rubber to prepare for product manufacture 4
Figure 3. Rubber manufacturing process 5
Figure 4. Tire manufacturing process 6
Figure 5. Typical rubber products manufacturing process pollution
outputs 8
Figure 6. Typical tire manufacturing process pollution outputs 9

Chapter2: Part 1
Biooxidation of Gaseous Hydrogen Sulfide in an Activated Sludge Tank
Figure 1. Schematic diagram of experimental system 17
Figure 2. Variations of H2S removal efficiency with superficial gas
velocities (Uo) at fixed influent H2S concentration Co and
liquid depth H (MLSS = 970-2800 mg L-1, pH = 5.7-7.6). 23
Figure 3. Variations of H2S removal efficiency with H at fixed Uo and Co
25
Figure 4. Effect of mixed-liquor pH on H2S removal efficiency at
H = 0.50 m (MLSS = 2150 mg L-1, pH = 7.62;
MLSS = 2380 mg L-1, pH = 4.82). 27

Chapter3: Part 2
Ozonation of Odorous Compounds in Gases Emitted from Rubber Processing Industries
Figure 1. Schematics of the experimental system. 35
Figure 2. THC (vented from the heated TSR) concentration and
removal efficiency in the dry ozonation test with
2a. [O3]o = 2.3 ppm and 2b. [O3]o = 4 ppm. 41
Figure 3. THC (vented from the heated TSR) concentration and
removal efficiency in the wet ozonation test with
3a. [O3]o = 2.6 ppm and 3b. [O3]o = 4 ppm. 42
Figure 4. THC (vented from the heated TPR) concentration and
removal efficiency in the wet ozonation test with
[O3]o = 4 ppm. 43
Figure 5. Odor removal efficiency in the course of ozonation. 45
Figure 6. THC (vented from the heated TSR) and ozone concentrations
for the long-term dry-ozonation test with [O3]o=4 ppm. 48
Figure 7. THC (vented from the heated TSR) and ozone concentrations
for the long-term wet-ozonation test with [O3]o=4 ppm. 50


List of Tables
Introduction
Table 1. H2S concentration of rubber manufactory 11
Table 2. H2S concentration of domestic and industry wastewater treatment
plant 11

Chapter2: Part 1
Biooxidation of Gaseous Hydrogen Sulfide in an Activated Sludge Tank
Table 1. Nutrition rate for sludge production 19
Table 2. Composition of nutrient solution for sulfide oxidation 19
Table 3. Operation conditions in experimental phase 2 21
Table 4. Sludge settling property before and after a 24-h sulfide loading
--------------------------------------------------------------------------- 28

Chapter3: Part 2
Ozonation of Odorous Compounds in Gases Emitted from Rubber Processing Industries
Table 1. Concentrations of VOCs compounds from heated rubber
exhaust (200°C) examined by GC. 40
Table 2. D/T ratios of the tested odorous gases. 52

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