含氮類污染物常見於光電半導體、石油煉製、煉焦、肥料和食品等工業之製程廢水及廢氣排放，對於生物具有毒性且對人體具有致癌性及致基因突變性。本研究旨在探討以自製之奈米級催化劑處理含氮類污染物，並進行其氣液相反應機制之研究。由於銅觸媒活性中心的研究，長期以來爭議不斷，至今仍無法明確獲知銅的活性中心到底為何。因此，要闡明奈米級銅觸媒對含氮類污染物的催化活性，就必須瞭解觸媒表面的物理性質與化學組成特性。本研究成果主要內容可歸納為下列四大部份。
在添加奈米級Cu-La-Ce複合金屬觸媒濕式氧化程序催化液相氨方面主要可包括下列幾點：（1）奈米級Cu-La-Ce（7:2:1）複合金屬觸媒對氨（簡稱NH3）轉化率之提昇效果顯著。（2）NH3之轉化率隨反應溫度之提高而增加，但是卻隨進流液空間流速的增加而降低。（3）添加觸媒之濕式氧化反應速率隨水溶液之初始pH值升高而增大，在鹼性條件（pH = 12.0）下水溶液之NH3轉化率可達到95.0%。（4）當提昇壓力至4.0 MPa，則NH3之轉化率可達95.0%以上，顯然提供氧氣可幫助NH3在高溫下之分解效能。（5）由X光粉末繞射分析（簡稱XRD）結果出現的氧化銅（CuO）、三氧化二鑭（La2O3）和二氧化鈰（CeO2）特性波峰。此三種晶相所產生的協合效應是Cu-La-Ce複合金屬觸媒活性極佳的最主要原因之一。由傅立葉轉換紅外線光譜（簡稱FTIR）及擴散反射式紫外－可見光光譜儀（簡稱UV-Vis）分析結果，推測Cu-La-Ce複合金屬觸媒濕式氧化反應機制可能是由CuO所主導，且觸媒可利用對氧的化學吸附來進行氧化反應。（6）由解析型掃描穿透式電子顯微鏡（簡稱AEM）及穿透式電子顯微鏡（簡稱TEM）分析結果，顯示觸媒大多是圓形顆粒聚集狀，且顆粒多集中在奈米尺寸範圍內。由X光成份分析系統（簡稱EDS）及元素X光影像（簡稱Mapping）分析結果證實Cu、La及Ce確實為觸媒的主要組成成份。
在添加奈米級Cu-ACF觸媒濕式氧化程序催化液相氨方面主要可包括下列幾點：（1）銅的載量對Cu-ACF觸媒在處理效率上為一重要的因素，當銅載量在5%時，即足以維持銅在+2價的狀態所致，而+2價的銅乃具有將水溶液中NH3催化成N2之能力。（2）在溫度463 K及濃度400 mg L-1下操作，NH3之最佳轉化率可達99%，顯示Cu-ACF觸媒也具有極佳之活性。（3）添加觸媒對NH3之轉化率隨反應溫度之提高而增加，但是N2之選擇率卻隨反應溫度的增加而降低。（4）添加觸媒對NH3之轉化率隨氧氣分壓之提高而增加。（5）由比表面積分析儀（簡稱BET）、FTIR及元素分析儀（簡稱EA）分析結果證實活性碳纖維（ACF）具有較高的比表面積及表面含氧官能基，因而具有較多的活性位址的特性，可均勻分散金屬，以增加金屬的反應活性。由XRD繞射分析結果出現的CuO和ACF特性波峰顯示CuO晶相與ACF擔體所產生的協合效應為Cu-ACF觸媒活性極佳的最主要原因之一。由FTIR及UV-Vis分析結果，推測Cu-ACF觸媒濕式氧化反應機制可能是由CuO及ACF所共同主導。（6）由金相顯微實驗進一步觀察碳纖維的表面型態，可得知碳纖維的鍛燒溫度與表面含氧官能基是決定氧化銅在碳纖維上沉積是否均勻的重要因素。由AEM及TEM分析結果，顯示觸媒含銅的奈米纖維管微結構為一細長狀的中空管狀碳層結構所構成，且內徑多集中在奈米尺寸範圍內。由EDS及X光螢光分析（簡稱XRF）分析結果證實Cu及P元素為觸媒的主要組成成份。
添加奈米級Cu-Ce複合金屬觸媒氣相氨選擇性催化方面主要可包括下列幾點：（1）在573 K的反應溫度下，Cu-Ce（6:4）複合金屬觸媒對NH3具有極佳之轉化率。（2）NH3之初始濃度愈高，其轉化率愈低，推測可能係因中間產物無法有效被分解而逐漸累積在氣相中所致。（3）由XRD繞射分析結果出現的CuO和CeO2特性波峰。此兩種晶相所產生的協合效應是Cu-Ce複合金屬觸媒活性極佳的最主要原因之一。由BET及EA成分分析結果證實Cu-Ce複合金屬觸媒具有較高的比表面積及表面氧空洞的生成，因而具有較多的活性位址的特性，可增加金屬的反應活性。由FTIR及UV-Vis分析結果，推測Cu-Ce雙功能複合金屬觸媒選擇性催化反應機制可能是由CuO和CeO2所主導。（4）由AEM及TEM分析結果，顯示觸媒大多是圓形顆粒聚集狀，且顆粒多集中在奈米尺寸範圍內。由EDS及Mapping分析結果證實Cu及Ce為觸媒的主要組成成份。
添加奈米級Pt-Pd-Rh陶瓷觸媒氣相氨選擇性催化方面主要可包括下列幾點：（1）Pt-Pd-Rh陶瓷觸媒轉化率在623 K時，NH3之轉化率可達99%。以不同濃度（500~1000 ppm）之NH3進行選擇性催化氧化（SCO）處理程序，結果顯示NH3之初始濃度愈高，其被去除之比率愈低。（2）Pt-Pd-Rh陶瓷觸媒氧化不同濃度NH3（500~1000 ppm）時會產生少量的NO、NO2及大量的N2。（3）由陶瓷擔體觸媒的金相顯微測試結果顯示，NH3之初始濃度愈高，陶瓷擔體的劣化程度就愈高，相對所產生的沉積物量也愈多，且氧化鋁塗覆層因受熱而產生剝落及燒結的現象也相當明顯。（4）由XRD繞射分析結果出現的鉑（Pt）、氧化鈀（PdO）、銠（Rh）及CeO2特性波峰。此四種晶相所產生的複合金屬協合效應是Pt-Pd-Rh陶瓷觸媒活性極佳的最主要原因之一。由FTIR及UV-Vis分析結果，推測Pt-Pd-Rh陶瓷觸媒選擇性氧化反應機制可能是由PdO及CeO2所主導。（5）由EDS、XRF及Mapping分析結果證實Pt、Pd及Rh確實為觸媒的主要組成成份，並均勻分散在含Mg-Al-Si陶瓷擔體的表面上。

Ammonia is one of valuable chemicals, which are commonly used, in various industrial factors. It is also a typical pollutant, and has a long-term impact on human health for its toxicity characteristics. This study investigated the reaction mechanism of gas-liquid phase in oxidation of ammonia in WAO and SCO processes over copper catalysts. As for lack of the research on activated center of copper catalyst for a long time, it was still not exactly unknown what center was going on affecting activity. Therefore, we conducted the physical and chemical properties on surface of catalyst to realize conversion/activity in oxidation of ammonia over nanoscale copper catalyst.
Achievements in oxidation of liquid phase ammonia in WAO process over nanoscale Cu-La-Ce catalysts are as follows: (1) The raising on conversion of ammonia is significantly by adding the molar ratio 7:2:1 of Cu-La-Ce catalyst. (2) The higher temperature the higher conversion, and the increasing space velocity of influent the lower conversion. (3) The reaction rate in WAO process over 7:2:1 catalyst increases with initial pH increasing of solution, 95% conversion of ammonia can be achieved under alkalinity condition. (4) Oxygen supply can promote the decomposition of ammonia at high temperature, above 95% conversion of ammonia can be achieved when total pressure raises at 4.0 MPa. (5) The characteristic peaks of CuO, La2O3 and CeO2 showed from XRD tests indicate the coordination by three peaks probably causes the excellent activity in Cu-La-Ce catalysts; UV-Vis and FTIR analysis results show CuO species dominates the reaction mechanism of liquid phase of WAO process over Cu-La-Ce catalyst which can be used to adsorb the oxygen atom in proceeding the oxidation of ammonia. (6) AEM and TEM analysis results show the outlook of catalyst sites are almost nearly circular and its particle sizes are concentrated in range of nanoscale level; and by EDS and Mapping tests proof elements of Cu, La and Ce are indeed the major components in this catalyst.
Achievements in oxidation of liquid phase ammonia in WAO process over nanoscale Cu-ACF catalysts are as follows: (1) The dose of copper on activated carbon fiber support (denoted by ACF) is important in treatment efficiency of pollutants removal; adding at least 5% of copper dosage which can maintain Cu to be a state of +2, it has the catalytic capacity to convert the ammonia in solution. (2) The optimal conversion obtained in 99% under 463 K and 400 mg/l, shows Cu-ACF is also an alterative catalyst. (3) The higher temperature the higher conversion, and the lower nitrogen is. (4) The higher oxygen pressure the higher conversion. (5) From analysis results of BET, FTIR and EA show ACF support has high BET surface area and oxygen-containing function groups, it causes an increasing activity of metal in reaction for the higher activated sites and metal dispersed uniformly on ACF; XRD tests indicate the coordination by CuO and ACF probably causes the excellent activity over Cu-ACF catalysts; UV-Vis and FTIR analysis results show species CuO and ACF both dominate the reaction mechanism of liquid phase of WAO process over Cu-ACF catalyst. (6) AEM and TEM analysis results show the outlook of catalyst sites are almost Nearly long narrowed tube and its diameters are concentrated in range of nanoscale level; and by EDS and XRF (Mapping) tests proof elements of Cu and P are indeed the major components in this catalyst.
Achievements in oxidation of gas phase ammonia in SCO process over nanoscale Cu-Ce catalysts are as follows: (1) The great conversion over Cu-Ce catalyst (molar ratio 6:4) obtained under 463 K and 400 mg/l. (2) The higher initial concentration of ammonia the lower conversion is probably due to the intermediates out of completely decomposed in catalytic reaction. (3) From analysis results of BET and EA show this catalyst have high BET surface area and empty hole of oxygen-containing on surface, it causes an increasing activity of metal in reaction for the higher activated sites; XRD tests indicate the coordination by CuO and CeO2 probably causes good activity over Cu-Ce catalysts; UV-Vis and FTIR analysis results show species CuO and CeO2 both dominate the reaction mechanism of gas phase of ammonia in SCO process over Cu-CeO2 catalyst. (4) AEM and TEM analysis results show the outlook of catalyst sites are almost nearly circular and its particle sizes are concentrated in range of nanoscale level; and by EDS and Mapping tests proof elements of Cu and Ce are indeed the major components in this catalyst.
Achievements in oxidation of gas phase ammonia in SCO process over nanoscale Pt-Pd-Rh catalyst coated on ceramics are as follows: (1) The 99% conversion over this catalyst can be obtained at 623 K; the higher initial concentration of ammonia ranging from 500 to 1000 mg/l the lower conversion is found. (2) The large amount of N2 and minor amount of NO and NO2 are found in the products after this reaction. (3) XRD tests indicate the coordination by Pt, PdO, Rh and CeO2 probably causes the excellent activity over this catalyst; UV-Vis and FTIR analysis results show species PdO and CeO2 both dominate the reaction mechanism of gas phase of ammonia in SCO process over Pt-Pd-Rh catalyst. (4) AEM and TEM analysis results show the higher initial concentration the higher aged the ceramic support, and the wider sintering of Al2O3 coating layer is. (5) By EDS, XRF and Mapping tests proof elements of Pt, Pd and Rh are indeed the major components dispersed on this ceramic catalyst.

論文授權書
學位論文審定書
中文摘要 I
英文摘要 VI
致謝 XI
總目錄 i
表目錄 .vi
圖目錄 vii
第一章 緒論 1
1-1 研究緣起與目的 1
1-2 研究內容及目的 6
第二章 文獻回顧 9
2-1 含氮類污染物用途及污染來源 9
2-2 含氮類污染物之物理及化學特性 11
2-3 含氮類污染物之廢水處理法 17
2-3-1 濕式氧化法 18
2-3-2 超臨界濕式氧化法 26
2-3-3 觸媒濕式氧化法 29
2-4 選擇性觸媒氧化法 34
2-5 觸媒載體 37
2-5-1 活性碳纖維 38
2-5-2 陶瓷多孔體 44
2-6 奈米材料的觸媒性質 49
第三章 研究方法 52
3-1 實驗設備 52
3-1-1 半批次式觸媒濕式氧化程序處理設備 52
3-1-2 連續式異相觸媒濕式氧化程序處理設備 54
3-1-3 異相觸媒氣相催化程序處理設備 56
3-2 奈米觸媒製備裝置 58
3-3 奈米觸媒製備方法 58
3-4 實驗藥品與儀器 59
3-4-1 實驗水樣 59
3-4-2 實驗氣體及藥品 59
3-4-3 實驗儀器 61
3-5 分析設備及裝置 62
3-5-1 比表面積分析儀 63
3-5-2 粒徑分析儀 63
3-5-3 元素分析儀 63
3-5-4 熱重及熱差分析 64
3-5-5 X光粉末繞射分析 65
3-5-6 X光螢光分析 65
3-5-7 擴散反射式紫外－可見光光譜儀 66
3-5-8 傅立葉轉換紅外線光譜與調減全反射式傅立葉轉
換紅外線光譜分析 66
3-5-9 金相組織觀察 67
3-5-10 掃描式電子顯微鏡 67
3-5-11 穿透式電子顯微鏡 68
第四章 濕式氧化程序催化液相氨之結果與討論 70
4-1 奈米級Cu-La-Ce複合金屬觸媒之處理效能 70
4-1-1 Cu-La-Ce複合金屬觸媒篩選 70
4-1-2 Cu-La-Ce複合金屬觸媒之特性分析 82
4-1-3 添加Cu-La-Ce複合金屬觸媒對WAO處理效能
之影響 97
4-1-4 觸媒填充量對WAO處理效能之影響 106
4-1-5 溫度對WAO處理效能之影響 108
4-1-6 pH值對WAO處理效能之影響 120
4-1-7 氧氣分壓力對WAO處理NH3效能之影響 133
4-1-8 NH3初始濃度對WAO處理效能之影響 147
4-1-9 觸媒長時間穩定測試 151
4-2 奈米級Cu-ACF觸媒之之處理效能 168
4-2-1 Cu-ACF觸媒篩選 168
4-2-2 添加Cu-ACF觸媒對WAO處理效能之影響 199
4-2-3 溫度對WAO處理效能之影響 203
4-2-4 氧氣分壓力對WAO處理效能之影響 206
4-2-5 NH3初始濃度對WAO處理效能之影響 209
4-2-6 觸媒長時間穩定測試 209
第五章 氣相氨選擇性催化之結果與討論 216
5-1 奈米級Cu-Ce複合金屬觸媒之處理效能 216
5-1-1 Cu-Ce複合金屬觸媒篩選 216
5-1-2 添加Cu-Ce複合金屬觸媒對SCO處理效能
之影響 237
5-1-3 溫度及氧氣濃度對SCO處理效能之影響 241
5-1-4 溫度對SCO處理效能之影響 243
5-1-5 氧氣濃度對SCO處理效能之影響 252
5-1-6 觸媒長時間穩定測試 260
5-2 奈米級Pt-Pd-Rh陶瓷觸媒之處理效能 278
5-2-1 Pt-Pd-Rh陶瓷觸媒之特性分析 278
5-2-2 添加Pt-Pd-Rh陶瓷觸媒對SCO處理效能之影響 297
5-2-2-1 溫度效應對添加Pt-Pd-Rh陶瓷觸媒處理
之影響 297
5-2-2-2 氧氣濃度對SCO處理NH3效能之影響 302
5-2-2-3 初始濃度對添加Pt-Pd-Rh陶瓷觸媒處理
效能之影響 304
5-2-3 添加Pt-Pd-Rh陶瓷觸媒處理NH3對產物選擇率
之影響 311
第六章 結論與建議 316
6-1 結論 316
6-1-1 添加奈米級Cu-La-Ce複合金屬觸媒於濕式
氧化程序催化液相氨 316
6-1-2 添加奈米級Cu-ACF觸媒於濕式氧化程序催
化液相氨 317
6-1-3 添加奈米級Cu-Ce複合金屬觸媒於氣相氨選擇
性催化 319
6-1-4 添加奈米級Pt-Pd-Rh陶瓷觸媒於氣相氨選擇
性催化 320
6-2 建議 321

參考文獻 323
附錄 個人簡介 374

表 目 錄
Table 2-1 The various forms of oxidation and reduction states of compounds of nitrogen in the water/soil environment. 13
Table 2-2 Toxicity of nitrogenous compounds and their oxidation
by-products. 16
Table 2-3 Application of cordierite cellular ceramic substances.. 46
Table 4-1 BET area and texture properties of catalysts after
different treatments.. 84
Table 4-2 Surface composition analysis of the test catalyst.. 88
Table 4-3 Product selectivity from ammonia oxidation using
copper-lanthanum-cerium composite catalyst at different
temperature in a continuous trickle-bed reactor. 114
Table 4-4 The first-order reaction equation over the Cu/La/Ce
(7/2/1) composite catalyst under various pressures.. 136
Table 4-5 The first-order reaction equation without catalyst under
various pressures.. 137
Table 4-6 Equations of the WO of ammonia solution in Figure
4-21. 138
Table 4-7 Energy of activation and frequency factor for the wet
oxidation of ammonia solution. 143
Table 4-8 BET area and texture properties of ACF.. 176
Table 4-9 Surface composition analysis of the test catalyst.. 186
Table 4-10 Surface elements composition analysis and atomic ratios
of the test catalyst... 187
Table 5-1 Surface composition analysis of the test catalyst... 227
Table 5-2 Surface composition analysis of the cordierite
compositions... 284

圖 目 錄
Figure 1-1 Schematic representation of research structure. 8
Figure 2-1 A schematic survey on the transformation and
distribution of N compounds in various reservoirs
of the environment. 12
Figure 2-2 Flow diagram of a WO process. 19
Figure 2-3 The pathway for destruction of organic compound by
WAO. 22
Figure 2-4 Distribution of ammonia and ammonium ion with pH
in aqueous solution.. 27
Figure 2-5 Optical photograph of uncoated activated carbon fibers
（ACFs）. 40
Figure 2-6 Optical photograph of Cu-ACF catalyst before calcined.
The blue-white particle is the result of the copper
adsorption, and indicates copper oxide crystals
formed on the surface.. 40
Figure 2-7 The surface function group of ACF. 43
Figure 2-8 Thermal expansion coefficients (298~1273 K) of
extruded cordierite compositions in relation to
stoichiometry.. 47
Figure 2-9 Optical photograph of a monolithic catalyst showing:
(a) cordierite cellular ceramic, (b) noble metal-
catalyzed gamma alumina washcoat, and (c)
open cellular channel.. 48
Figure 3-1 Schematic diagram of the wet oxidation setup. 53
Figure 3-2 Schematic diagram of the catalytic wet oxidation
employed to carry out the ammonia oxidation
over catalyst in a trickle-bed reactor.. 55
Figure 3-3 The schematic diagram of the catalytic oxidation
employed to carry out the ammonia oxidation
over catalyst of the tubular fixed-bed reaction
(TFBR) system.. 57
Figure 4-1 Effect of various calcinations temperature on the
Cu/La/Ce composite catalysts for the conversion
of NH3 in a batch reactor.. 71
Figure 4-2 Changes of specific surface area of Cu/La/Ce (7:2:1)
composite catalysts of various calcinations
temperature in a batch reactor after lifetime
reaction.. 73
Figure 4-3 Adsorption and desorption isotherms diagram of the
various metal content of Cu/La/Ce composite
catalysts.. 75
Figure 4-4 FTIR pattern of various calcinations temperature on the
Cu/La/Ce catalyst.. 77
Figure 4-5 A UV-Vis absorption spectra of the various calcinations
temperature on the Cu/La/Ce composite
catalysts in a batch reactor.. 79
Figure 4-6 Changes in particle sizes distribution with various
calcinations temperature on the Cu/La/Ce
composite catalysts.. 81
Figure 4-7 Thermal gravimetric analysis (TGA) diagram of
Cu/La/Ce (7:2:1) catalyst. 83
Figure 4-8 Changes in adsorption and desorption isotherms
diagram of the Cu/La/Ce (7:2:1) composite
catalysts showing: (a) fresh, (b) after 72 hours
activity test in a batch reactor.. 86
Figure 4-9 SEM with dot mapping photographs result of various
contents on the fresh Cu/La/Ce (7:2:1) catalyst.
(a) Original magnification: × 3000, (b) Cu,
(c) La and (d) Ce.. 89
Figure 4-10 SEM with dot mapping photographs result of various
contents on the Cu/La/Ce (7:2:1) catalyst after
activity test. (a) Original magnification: × 3000,
(b) Cu , (c) La and (d) Ce.. 90
Figure 4-11 SEM photograph that shows of Cu/La/Ce (7/2/1)
composite catalysts that is (a) fresh and (b)
after activity test.. 92
Figure 4-12 AEM photograph and selected-area electron diffraction
(SAED) analysis of the fresh Cu-La-Ce (7:2:1)
catalyst. (a) Original magnification: × 300,000,
(b) Original magnification: × 300,000 and (c) EDS
analysis of (b).. 94
Figure 4-13 FTIR pattern of various metal content on ammonia
removal of the catalytic wet oxidation over the
Cu/La/Ce composite catalysts in a batch reactor.. 96
Figure 4-14 A UV-Vis absorption spectra of metal content on
ammonia removal of the catalytic wet oxidation
over the composite catalysts in a batch reactor.. 98
Figure 4-15 Changes in particle sizes distribution with various metal
content on ammonia removal of the catalytic wet
oxidation over the composite catalysts.. 99
Figure 4-16 Effect of metal content on ammonia removal of the
catalytic wet oxidation over the Cu/La composite
catalysts in a batch reactor. 101
Figure 4-17 Effect of metal content on ammonia removal of the
catalytic wet oxidation over the Cu/Ce composite
catalysts in a batch reactor.. 102
Figure 4-18 Effect of metal content on ammonia removal of the
catalytic wet oxidation over the Cu/La/Ce composite
catalysts in a batch reactor.. 103
Figure 4-19 XRD pattern of the Cu/La/Ce (7/2/1) composite
catalysts. (a) fresh, (b) after activity test.. 105
Figure 4-20 Effect of various catalyst content on ammonia removal
of the catalytic wet oxidation over the Cu/La/Ce
composite catalysts in a batch reactor. 107
Figure 4-21 Effect of temperature on the wet oxidation of the
ammonia solution.. 109
Figure 4-22 Effect of reaction temperature and liquid hourly space
velocity on removal of the catalytic wet oxidation of
ammonia solution over the Cu/La/Ce (7:2:1)
composite catalysts in a continuous trickle-bed
reactor.. 112
Figure 4-23 Gaseous nitrogen oxides in the trickle-bed reactor.. 118
Figure 4-24 Effect of reaction temperature of the XRD pattern over
the Cu/La/Ce (7:2:1) catalysts.. 119
Figure 4-25 pH fluctuation of the wet oxidation of the ammonia
solution.. 121
Figure 4-26 Effect of pH on the decomposition of ammonia during
the wet oxidation process.. 122
Figure 4-27 Distribution of ammonia and ammonium ion with pH
in aqueous solution.. 123
Figure 4-28 Effect of liquid flow rate and pH on ammonia
conversion at 503 K in the trickle-bed reactor.. 125
Figure 4-29 Effect of pH on the decomposition of NH3 profiles
during both the catalytic and the noncatalytic wet
oxidations of ammonia solution at 503 K in the
trickle-bed reactor.. 126
Figure 4-30 Plot of the resultant pH with NO2- and NO3- formation
during the noncatalytic wet oxidations of ammonia
solution at 503 K in the trickle-bed reactor.. 127
Figure 4-31 NO2- and NO3- formation at 503 K in the trickle-bed
reactor.. 129
Figure 4-32 Plot of the resultant pH with NO2- and NO3- formation
at 423 K in the trickle-bed reactor.. 130
Figure 4-33 Plot of the resultant pH with NO2- and NO3- formation
at 473 K in the trickle-bed reactor.. 131
Figure 4-34 Plot of the resultant pH with NO2- and NO3- formation
at 503 K in the trickle-bed reactor.. 132
Figure 4-35 Effect of reaction pressure on the wet oxidation of the
ammonia solution.. 134
Figure 4-36 Effect of temperature and wet oxidation of the ammonia
solution. (a) noncatalytic; (b) catalyzed by
Cu/La/Ce.. 139
Figure 4-37 Plot ln k vs. T-1on wet oxidation of the ammonia
solution. (a) first step; (b) second step.. 140
Figure 4-38 Plot ln k vs. T-1on catalyst wet oxidation of the
ammonia solution. (a) first step; (b) second step.. 141
Figure 4-39 Effect of reaction pressure on ammonia removal of
the catalytic wet oxidation over the Cu/La/Ce
(7:2:1) composite oxide catalyst in a continuous
trickle-bed reactor.. 145
Figure 4-40 Effect of the initial concentration of ammonia in the
solution on the decomposition of ammonia during
the wet oxidation process.. 148
Figure 4-41 Effect of initial concentration on ammonia removal of
the catalytic wet oxidation over the Cu/La/Ce
(7:2:1) composite oxide catalyst in a continuous
trickle-bed reactor.. 150
Figure 4-42 Effect of liquid flow rate on ammonia conversion and
by-products selectivity at 503 K in the trickle-bed
reactor.. 152
Figure 4-43 NH3 removal profiles during both the catalytic (over
the Cu/La/Ce（7:2:1） composite catalyst ) and
the noncatalytic wet oxidations of ammonia
solution.. 154
Figure 4-44 Effect of the reaction time on Cu/La/Ce (7:2:1)
composite catalysts in a continuous trickle-bed
reactor.. 155
Figure 4-45 FTIR pattern of the Cu/La/Ce (7:2:1) composite
catalysts. (a) fresh, (b) after activity test.. 158
Figure 4-46 ATR pattern of the Cu/La/Ce (7:2:1) catalyst. (a) fresh,
(b) after activity test.. 160
Figure 4-47 A UV-Vis absorption spectra of the fresh and aged
Cu/La/Ce composite catalysts in a batch reactor.. 161
Figure 4-48 Changes in particle sizes distribution of the Cu/La/Ce
(7/2/1) composite catalysts showing: (a) fresh, (b)
after 72 hours activity test.. 163
Figure 4-49 (TEM photograph and selected-area electron diffraction
(SAED) analysis on the Cu/La/Ce
(7:2:1) catalyst in a batch reactor. (a) Fresh and (b) after activity test... 164
Figure 4-50 TEM photograph and selected-area electron diffraction
(SAED) analysis on the Cu/La/Ce (7:2:1) catalyst in
the trickle-bed reactor. (a) Fresh and (b) after
activity test.. 165
Figure 4-51 Effect of various calcinations temperature on the Cu-
ACF catalysts for the conversion of NH3 in a
continuous trickle-bed reactor.. 167
Figure 4-52 NH3 oxidation reaction mechanism during the catalytic
(over the Cu/La/Ce（7:2:1） composite catalyst ) of ammonia solution.. 169
Figure 4-53 Optical photographs of the Cu-ACF catalyst by various
calcining temperatures (a) 473 K, (b) 573 K,
(c) 673 K and (d) 773 K.. 171
Figure 4-54 Effect of various copper loading on the Cu-ACF
catalyst for the conversion of NH3.. 174
Figure 4-55 FTIR spectra of the ACF. 177
Figure 4-56 FTIR-ATR spectra of the ACF. 179
Figure 4-57 UV-Vis absorption spectra on ammonia removal of
the catalytic wet oxidation of (a) fresh and (b) after
activity test catalyst. 181
Figure 4-58 The particle sizes distribution of activated carbon
fibers (ACFs). 183
Figure 4-59 TGA-DTA curve of the Cu-ACF catalyst. 184
Figure 4-60 SEM photograph of the fresh activated carbon fiber
substrate by (a) fracture surface and (b) fiber
surface. 190
Figure 4-61 Optical photographs of the Cu-ACF catalyst of (a)
cleaned activated carbon fiber before impregnation,
(b) before calcined, (c) after calcined and (d) aged
activated carbon fiber for the conversion of NH3.. 191
Figure 4-62 TEM photograph and elected-area electron diffraction
(SAED) analysis of the Cu-ACF catalyst. (a) before
calcined, (b) after calcined and (c) after activity
test.. 193
Figure 4-63 The Crystallography of the CuO.. 196
Figure 4-64 AEM photograph of the fresh Cu-ACF catalyst. (a)
Original magnification × 25,000, (b) Original
magnification × 500,000 and (c) EDS analysis of
(b).. 197
Figure 4-65 AEM photograph of the fresh Cu-ACF catalyst. (a)
Original magnification × 50,000, (b) Original
magnification × 500,000 and (c) EDS analysis of
(b).. 198
Figure 4-66 Effect of liquid flow rate on ammonia conversion and
N2 selectivity at 463 K in the trickle-bed reactor.. 200
Figure 4-67 XRD pattern of the Cu-ACF catalyst of (a) cleaned
activated carbon fiber before impregnation, (b) before
calcined, (c) after calcined and (d) aged activated
carbon fiber for the conversion of NH3.. 202
Figure 4-68 Effect of reaction temperature on removal of the
catalytic wet oxidation of ammonia solution over
the Cu-ACF catalysts in a continuous trickle-bed
reactor.. 204
Figure 4-69 Effect of reaction pressure on ammonia removal of
the catalytic wet oxidation over the Cu-ACF
catalyst in a continuous trickle-bed reactor.. 207
Figure 4-70 Effects of initial concentration on the conversion in
oxidation of ammonia over Cu-ACF catalyst.. 210
Figure 4-71 NH3 removal profiles during the catalytic (over the
Cu-ACF catalyst ) of ammonia solution.. 211
Figure 4-72 FTIR pattern of the Cu-ACF catalysts. (a) before
calcined, (b) after calcined and (c) after activity
test.. 214
Figure 4-73 NH3 oxidation reaction mechanism during the catalytic
(over the Cu-ACF catalyst ) of ammonia solution.. 215
Figure 5-1 BET of the various metal content of Cu/Ce composite
catalysts.. 217
Figure 5-2 Adsorption and desorption isotherms diagram of the
various metal content of Cu/Ce composite
catalysts.. 219
Figure 5-3 FTIR pattern of various metal content on the Cu/Ce
catalyst for the conversion of NH3.. 220
Figure 5-4 UV-Vis absorption spectra of the metal content on the
Cu/Ce catalyst for the conversion of NH3.. 222
Figure 5-5 Changes in particle sizes distribution of the various
metal content on the Cu/Ce catalyst for the
conversion of NH3.. 223
Figure 5-6 Thermal gravimetric analysis (TGA) diagram of Cu/Ce
(6:4) catalyst for the conversion of NH3.. 225
Figure 5-7 SEM with dot mapping photographs result of various
contents on the fresh Cu/Ce (6:4) catalyst. (a)
Originalmagnification: × 3000, (b) Cu and (c)
Ce.. 228
Figure 5-8 SEM with dot mapping photographs result of various
contents on the fresh Cu/Ce (6:4) catalyst after
activity test. (a) Original magnification: × 3000,
(b) Cu and (c) Ce.. 229
Figure 5-9 SEM photograph of (a) fresh and (b) after activity test
on the Cu/Ce (6:4) catalyst for the conversion
of NH3.. 231
Figure 5-10 AEM photograph and elected-area electron diffraction
(SAED) analysis of the fresh Cu/Ce (6:4) catalyst.
(a) Original magnification: × 300,000, (b) Original
magnification: × 300,000.. 232
Figure 5-11 HRTEM photograph of lattice image of various
magnifications on the fresh Cu/Ce (6:4) catalyst. (a)
Original magnification by Fig. 5-10 (a-1): × 500,000,
(b) Original magnification by Fig. 5-10 (a-2): ×
500,000 and (c) EDS analysis of (b).. 233
Figure 5-12 HRTEM photograph of lattice image of the fresh Cu/Ce
(6:4) catalyst. (a) Original magnification by Fig. 5-10
(a-3): × 500,000, (b) Original magnification by Fig.
5-10 (a-4): × 500,000 and (c) EDS analysis of (b).. 234
Figure 5-13 HRTEM photograph of lattice image and elected-area
electron diffraction (SAED) analysis of the fresh
Cu/Ce (6:4) catalyst. (a) Original magnification by
Fig. 5-10 (b-5): × 500,000, (b) Original magnification
by Fig. 5-10 (b-6): × 500,000.. 235
Figure 5-14 Effect of various NH3 concentrations on the Cu/Ce
(6:4) catalyst for the conversion of NH3.. 238
Figure 5-15 XRD pattern of the various metal content on the Cu/Ce
catalyst for the conversion of NH3.. 240
Figure 5-16 Effect of the oxygen concentration on the Cu/Ce (6:4)
catalyst for the conversion of NH3.. 242
Figure 5-17 Effect of the oxygen content with reaction rates on the
Cu/Ce (6:4) catalyst for the conversion of NH3.. 245
Figure 5-18 Effect of space velocity on the Cu/Ce (6:4) catalyst for
the conversion of NH3 as function of temperature.. 246
Figure 5-19 Effect of empty bed residence time (EBRT) on the
Cu/Ce (6:4) catalyst for the conversion of NH3 as
function of temperature. 248
Figure 5-20 Scheme illustrating the mechanism of the NO-NH3
reaction over Cu-based catalyst in the presence of
oxygen proposed... 251
Figure 5-21 Effect of various NH3 concentrations on the Cu/Ce (6:4)
catalyst for the conversion of NH3.. 253
Figure 5-22 Effect of various ammonia concentrations with reaction
rates on the Cu/Ce (6:4) catalyst for the conversion
of NH3.. 255
Figure 5-23 Relationship of the ammonia conversion, N2 yield, and
NO yield at various temperatures over the Cu/Ce
(6:4) catalyst.. 256
Figure 5-24 Relationship of the ammonia conversion, N2 yield, and
NO yield at various temperatures over the Cu/Ce
(6:4) catalyst.. 257
Figure 5-25 Relationship of the ammonia conversion, N2 yield, and
NO yield at various temperatures over the Cu/Ce
(6:4) catalyst.. 258
Figure 5-26 Relationship of the ammonia conversion, N2 yield, and
NO yield at various temperatures over the Cu/Ce (6:4) catalyst. 259
Figure 5-27 Effect of the reaction time on the Cu/Ce (6:4) catalyst
for the conversion of NH3.. 261
Figure 5-28 Effect of reaction temperature with changes of specific surface area on the Cu/Ce catalyst for the conversion of
NH3.. 263
Figure 5-29 Adsorption and desorption isotherms diagram of the
Cu/Ce (6:4) composite catalysts. (a)fresh and (b)
aged.. 266
Figure 5-30 XRD pattern of (a) fresh and (b) after activity test on
the Cu/Ce (6:4) catalyst.. 267
Figure 5-31 FTIR pattern of the Cu/Ce (6:4) composite catalysts.
(a) fresh, (b) after activity test. 269
Figure 5-32 ATR pattern of the Cu/Ce (6:4) catalyst. (a) fresh, (b)
after activity test.. 271
Figure 5-33 UV-Vis absorption spectra of (a) fresh and (b) after
activity test Cu/Ce (6:4) catalyst.. 272
Figure 5-34 Changes in particle sizes distribution of the Cu/Ce
(6:4) composite catalysts. (a) fresh, (b) after 72
hours activity test. 274
Figure 5-35 TEM photograph of various magnifications on the
fresh Cu/Ce (6:4) catalyst. (a) Original magnification:
× 100,000, (b) Original magnification: × 150,000, (c)
Original magnification: × 205,000 and (d) selected-
area electron diffraction (SAED) analysis of (c). 275
Figure 5-36 TEM photograph of various magnifications on the Cu/Ce
(6:4) catalyst after activity test. (a) Original
magnification: × 62,000, (b) Original magnification:
× 100,000, (c) Original magnification: × 150,000
and (d) selected-area electron diffraction (SAED)
analysis of (c).. 276
Figure 5-37 FTIR pattern of the (a) fresh, (b) after activity test
and (c) cordierite monolith of Pt-Pd-Rh cordierite
monolith catalyst for the conversion of NH3.. 279
Figure 5-38 UV-Vis absorption spectra of (a) fresh and (b) after
activity test Pt-Pd-Rh cordierite monolith
catalyst.. 280
Figure 5-39 TGA-DTA curve of the cordierite monolith. 281
Figure 5-40 TGA-DTA curve of the Pt-Pd-Rh cordierite monolith
catalyst.. 282
Figure 5-41 SEM with dot mapping photographs result of various
contents on the ceramic support. (a) Original
ceramic support, (b) Mg , (c) Al and (d) Si.. 285
Figure 5-42 SEM with dot mapping photographs result of various
contents on the fresh Pt-Pd-Rh cordierite monolith
catalyst. (a) Original magnification: × 60, (b) Mg,
(c) Al and (d) Si.. 286
Figure 5-43 SEM with dot mapping photographs result of various
contents on the fresh Pt-Pd-Rh cordierite monolith
catalyst. (a) Original magnification: × 60, (b) Pt,
(c) Pd and (d) Rh.. 287
Figure 5-44 Optical photographs of cross-sectional areas of various
magnifications on the fresh Pt-Pd-Rh cordierite
monolith catalyst.. 289
Figure 5-45 SEM photographs of various magnifications on the
fresh cordierite monolith. (a) Original magnification:
× 50, (b) Original magnification: × 1,000, (c) Original
magnification: × 3,000 and (d) Original magnification:
× 5,000.. 290
Figure 5-46 STEM photograph of a fresh Pt-Pd-Rh cordierite
monolith catalyst. Original magnification: ×
10,000. 292
Figure 5-47 TEM photograph and elected-area electron diffraction
(SAED) analysis of the fresh Pt-Pd-Rh cordierite
monolith catalyst. (a) fresh catalyst by original
magnification: × 81,000, (b) after activity test by
original magnification: × 81,000, (c) after activity
test by original magnification: × 100,000 and (d)
after activity test by original magnification: ×
100,000. 293
Figure 5-48 AEM photograph of the fresh Pt-Pd-Rh cordierite
monolith catalyst. (a) Original magnification ×
80,000, (b) Original magnification × 500,000 and
(c) EDS analysis of (b).. 295
Figure 5-49 AEM photograph and elected-area electron diffraction
(SAED) analysis of the fresh Pt-Pd-Rh cordierite
onolith catalyst. (a) Original magnification ×
80,000, (b) Original magnification × 500,000 and
(c) EDS analysis of (b).. 296
Figure 5-50 Effect of the oxygen concentration on the Pt-Pd-Rh
cordierite monolith catalyst for the conversion
of NH3. 298
Figure 5-51 XRD pattern of the Pt-Pd-Rh cordierite monolith
catalysts. (a) cordierite monolith, (b) fresh and
(c) after activity test. 301
Figure 5-52 Effect of space velocity on the Pt-Pd-Rh cordierite
monolith catalyst for the conversion of NH3 as
function of temperature.. 303
Figure 5-53 Effect of various NH3 concentrations on the Pt-Pd-Rh
cordierite monolith catalyst for the conversion
of NH3.. 305
Figure 5-54 Optical photographs of various magnifications on the
fresh Pt-Pd-Rh cordierite monolith for the conversion
of NH3. The dark area is the result of the NH3
adsorption, and indicates oxide crystals formed on the
surface.. 306
Figure 5-55 Optical photographs of various magnifications on the
fresh Pt-Pd-Rh cordierite monolith for the conversion
of NH3. The green area is the result of the NH3
adsorption, and indicates oxide crystals formed
on the surface.. 307
Figure 5-56 Optical photographs of various magnifications on the
fresh Pt-Pd-Rh cordierite monolith for the conversion
of NH3. The green and red areas are the result of
the NH3 adsorption, and indicates oxide crystals
formed on the surface.. 308
Figure 5-57 Optical photographs of various magnifications on the
fresh Pt-Pd-Rh cordierite monolith for the conversion
of NH3. The green area is the result of the NH3
adsorption, and indicates oxide crystals formed on
the surface. 309
Figure 5-58 Relationship of the ammonia conversion, N2, NO and
NO2 yield at various temperatures over the Pt-Pd-Rh
cordierite monolith catalyst.. 312
Figure 5-59 Relationship of the ammonia conversion, N2, NO and
NO2 yield at various temperatures over the Pt-Pd-Rh
cordierite monolith catalyst.. 313
Figure 5-60 Relationship of the ammonia conversion, N2, NO and
NO2 yield at various temperatures over the Pt-Pd-Rh
cordierite monolith catalyst.. 314
Figure 5-61 Relationship of the NH3 conversion, N2, NO and NO2
yield at various temperatures over the Pt-Pd-Rh
cordierite monolith catalyst.. 315

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