臺灣博碩士論文加值系統

摘要

由於石油蘊藏量有限，及燃燒化石燃料造成的CO2排放過量的問題，促進了生質燃料的研究。流體化床燃燒爐可處理多種形態燃料與低NOx排放特性，而在燃燒生質燃料的研究上佔有一席之地。本研究將針對生質燃料之氮氧化物排放做一探討。
本研究係於一總高4.6 m之渦旋式流體化床燃燒爐中進行，其乾舷區內徑為0.75 m，氣泡床區為0.8 m × 0.4 m之矩形。以木屑做為燃料，矽砂為床質，探討不同操作條件對於燃燒爐中各區段氮氧化物分布及出口排放濃度之影響。實驗之主要操作參數為：床溫、過量空氣、配風比與床溫控制方式。
研究結果顯示，大部分NO與N2O於飛濺區生成，可歸因於木屑揮發物含量高達70% 以上之故，隨後在二次風注入混合區與乾舷區進行還原。各操作條件下，N2O之出口排放濃度極小，可考慮忽略。NO之排放濃度：隨床溫之增加而增加；當過量空氣小於40%，隨過量空氣增加而增加，但過量空氣大於40%，反而隨之下降；在靜床高20 cm之條件下，NO之排放有一最低值；以床內噴水控溫，噴水量大時，NO之排放濃度將明顯高於以熱傳管控溫。
木屑之熱值不低，易於燃燒，所產生之氮氧化物排放亦低於環保法規，應為一不錯之生質燃料選擇。

ABSTRACT

In this study, all the experiments were carried out in a pilot scale vortexing fluidized bed combustor of 0.75 m I.D. and 4.6 m in height. Sawdust was used as the fuel, and silica sand was employed as the bed material.
The effects of various operating conditions on NOx and N2O emissions were investigated, and the main operating parameters studied were bed temperature, excess air, and the method of bed temperature control.
The experiment results show that most formation of NOx and N2O take place in splashing zone, and then reduce in secondary air injection zone and freeboard. This is due to high volatile matter content of sawdust. Under each different operating condition, the N2O emissions are very small, and it can consider to be ignored. The NOx emission increases with the bed temperature. The NOx emission increases with excess air ratio from 10% to 40%, but the contrary result was found at a higher excess air ratio. At the static bed height of 20 cm, there is a lowest NOx emission. In addition, the amount of NOx is more with the method of water injection than heat transfer tube in bed temperature control.
Sawdust burns easily, and its heating value achieves above 3000 kcal/kg. Furthermore, the nitrogen oxides emissions from sawdust combustion conform to the environmental protection regulations. Thus sawdust could be a good choice for biofuel.

目錄

中文摘要…………………………………………………………………i
英文摘要…………………………………………………………………ii
誌謝……………………………………………………………………iii
目錄……………………………………………………………………iv
圖目錄…………………………………………………………………vii
表目錄……………………………………………………………………x
第一章 緒論…………………………………………………………1
第二章 文獻回顧……………………………………………………2
2-1 氮氧化物之特性…………………………………………3
2-2 氮氧化物對人體及環境之影響………………………5
2-2-1 氮氧化物對人體之影響……………………………5
2-2-2 一氧化氮對環境之影響……………………………5
2-2-3 氧化亞氮對環境之影響……………………………6
2-3 氮氧化物之來源與生成…………………………………8
2-3-1 一氧化氮之來源與生成……………………………8
2-3-2 二氧化氮之來源與生成……………………………13
2-3-3 氧化亞氮之來源與生成……………………………16
2-3-4 一氧化氮與氧化亞氮之關聯性……………………20
2-4 流體化床中操作變數對氮氧化物之影響………………23
2-4-1 過量空氣……………………………………………23
2-4-2 床溫…………………………………………………23
2-4-3 二次空氣……………………………………………24
2-4-4 床高…………………………………………………25
2-5 燃料性質對氮氧化物之影響……………………………26
2-5-1 木屑燃燒之氮氧化物排放…………………………26
2-5-2 氮含量……………………………………………26
2-5-3 揮發物含量…………………………………………27
2-5-4 粒徑…………………………………………………27
2-5-5 組成…………………………………………………27
2-6 氮氧化物之減量技術……………………………………30
2-6-1 一氧化氮之減量技術………………………………30
2-6-2 氧化亞氮之減量技術………………………………32
第三章 實驗設備及操作方法………………………………………34
3-1 實驗設備………………………………………………34
3-1-1 渦旋式流體化床焚化爐主體………………………34
3-1-2 進料系統……………………………………………35
3-1-3 送風及預熱系統……………………………………38
3-1-4 煙道氣處理系統及熱能回收設備…………………40
3-2 進料性質與製備…………………………………………41
3-2-1 燃料…………………………………………………41
3-2-2 床質…………………………………………………41
3-2-3 進料量之校正………………………………………42
3-3 操作方法及實驗變數……………………………………44
3-3-1 開爐…………………………………………………44
3-3-2 實驗操作變數………………………………………45
3-3-3 採樣方法……………………………………………45
第四章 結果與討論…………………………………………………48
4-1 溫度與氣態污染物分佈…………………………………48
4-1-1 溫度分佈………………………………………………………48
4-1-2 氮氧化物分佈………………………………………50
4-1-3 一氧化碳分佈………………………………………53
4-2 操作變數對氣態污染物排放之影響……………………55
4-2-1 床溫效應……………………………………………55
4-2-2 過量空氣效應………………………………………57
4-2-3 配風比效應…………………………………………60
4-2-4 靜床高效應…………………………………………67
4-2-5 控溫方式之效應……………………………………70
4-3 燃料中含氮物質之討論…………………………………72
第五章 結論…………………………………………………………76
符號說明………………………………………………………………78
參考文獻………………………………………………………………79
附錄A…………………………………………………………………87
附錄B…………………………………………………………………89
附錄C…………………………………………………………………91
附錄D…………………………………………………………………91
作者自述………………………………………………………………97
圖目錄

Figure 2-1 Scheme of reaction for prompt NOx .…………………11
Figure 2-2 Scheme of conversion of fuel-nitrogen …………………13
Figure 2-3 Reaction path diagram illustrating the re-action mechanism by which fuel-N is converted to NO, N2O and N2. ………22
Figure 3-1 The scheme of the process and status of the fluidized bed combustion system. ………………………………………35
Figure 3-2 Schematic diagram of the vortexing fluidized bed combustor…………………..……………………………36
Figure 3-3 Top view for the tangential secondary air injection in the vortexing fluidized bed combustor. ………….……………38
Figure 3-4 Size distribution of the bed material. …………………42
Figure 4-1 Temperature distributionin the vortexing fluidized bed combustor with various excess air (bed temperature = 700℃； Q1 = stoichiometric air). ……………………48
Figure 4-2 Figure 4-2 NO concentration at various distances above the distributor (bed temperature = 700℃； Q1 = stoichiometric air). ……………………………………………………50
Figure 4-3 N2O concentration at various distances above the distributor (bed temperature = 700℃； Q1 = stoichiometric air). ……………………………………………………51
Figure 4-4 CO concentration at various distances above the distributor (bed temperature = 700℃； Q1 = stoichiometric air). ……………………………………………………53
Figure 4-5 Effect of the bed temperature on NOx and N2O emission (excess air ratio = 60%；Q1 = stoichiometric air； Q2 = 60% stoichiometric air). ……………………………………55
Figure 4-6 Effect of the bed temperature on CO emission (excess air ratio = 60%；Q1 = stoichiometric air； Q2 = 60% stoichiometric air). ……………………………………57
Figure 4-7 Effect of the excess air ratio on NOx and N2O emission (bed temperature = 700℃； Q1 = stoichiometric air). ……………………………………………………58
Figure 4-8 Effect of the excess air ratio on CO emission (bed temperature = 700℃； Q1 = stoichiometric air). ………60
Figure 4-9 Effect of the primary/total air ratio on NOx and N2O emission (bed temperature = 700℃； excess air ratio = 40%). …………………………………………………61
Figure 4-10 Effect of the primary/total air ratio on CO emission (bed temperature = 700℃； excess air ratio = 40%). …………62
Figure 4-11 Effect of the primary/total air ratio on NOx and N2O emission (bed temperature = 700℃； excess air ratio = 60%). ……………………………………………………64
Figure 4-12 Effect of the primary/total air ratio on CO emission (bed temperature = 700℃； excess air ratio = 60%). …………65
Figure 4-13 Effect of the static bed height on NOx and N2O emission (bed temperature = 700℃； excess air ratio = 60%； Q1 = stoichiometric air； Q2 = 60% stoichiometric air). ……67
Figure 4-14 Effect of the static bed height on CO emission (bed temperature = 700℃； excess air ratio = 60%； Q1 = stoichiometric air； Q2 = 60% stoichiometric air). ………68
Figure 4-15 Effect of the different bed temperature control on NOx and N2O emission (excess air ratio = 60%； Q1 = stoichiometric air； Q2 = 60% stoichiometric air). ………………………70
Figure 4-16 The main ways of conversion of N-containing compound in FBC. ………………………………………………….71
Figure C-1 Calibration curve of sawdust. ……………………………90


表目錄

Table 2-1 Equilibrium constants for the formation of NO (N2 + O2 � 2NO) …………………………………………………16
Table 2-2 Equilibrium constants for the formation of NO2 (NO + 1/2 O2 � NO2) ……………………………………………….16
Table 3-1 The properties of fuel …………………………………41
Table 3-2 The experimental conditions ……………………………46
Table 4-1 Comparison with previous investigations of FBC on NOx and N2O emission …………………………………………73

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