1320085 玖、發明說明： 【發明所屬之技術領域】 本發明係關於一種物質之燃燒方法及其系統，尤其是 關於一種可燃物質經氣化後轉換成氣態可燃氣之燃燒方法 及其系統。 【先前技術】 _ 當今人類取得能源的方式之一係藉由燃燒可燃物以產 生熱能’其所追求的目標在於燃燒過程中提高熱能的利用 效率並降低因燃燒所產生的污染物。 理論上若要求高的熱效率，過剩反應氣體（excess oxidant ’如純氧、空氣等）的量越低越好，以降低過剩反應 氣體所衍生的排氣熱損。但過低的過剩反應氣體量易導致 燃料燃燒不完全，不僅造成燃料的損失，也會導致如碳氫 化合物(HC)、一氧化碳(c〇)等污染物的產出。另外，理論 _ 絕熱溫度隨過剩反應氣體量的增加而降低，高熱值的燃料 在過低的過剩反應氣體量下燃燒極易因高溫而產生出大量 的氮氧化物(NOx)。 舉例來說，當燃料(如天然氣、燃油、粉煤等）極易與 反應氣體混合時，為降低排氣熱損，往往給予較低的過剩 助燃空氣，但燃燒產物的溫度較高，導致氮氧化物污染物 的產出。 當燃料(例如塊煤或廢棄物等）不易與反應氣體混合 時，為使燃料充分燃燒，往往供給大量的過剩氣體量，因 5 1320085 了排氣熱損與降低了熱效率。例如焚化爐為使廢棄 物月b充分的燃燒，一般反應氣體量至少達到理論需氧量的 兩倍。 另外，燃燒過程所產生的飛灰往往含有一些有害物 質，若要降低污染性與提高材料再利用的可行性，=須要 使飛灰炼融形成融渣，燃燒溫度需提高至灰份炼點以上， (二般約達1300〜15〇〇。〇。在此高溫下，若同時存在氧氣與 氮氣將會產出氮氧化物(NOx)污染物。 • ?廢棄物焚化爐為例，為使廢棄物充分燃燒，必須供 給大里的助燃空氣，因此燃燒排氣的溫度（約8〇〇〜1〇〇〇。〇 無法達到使飛灰炫融的溫度。若要使飛灰炼融，必須在焚 化爐後設置熔融爐，加入額外的輔助燃料，以提高燃燒產 物的皿度。此-方式需要額外的外來能源，同時也因操作 在過剩空氣存在的情況下，衍生出大量的氮氧化物污染。 習知技術的燃燒模式在熱效率與降低污染物之間往往 無法兼顧。因此，有必要提供一種物質之燃燒方法及其系 φ 統，以改善先前技術所存在的問題。 【發明内容】 本發明之目的係在提供一種物質之燃燒方法，可在極 低的過剩反應氣體量下達到高燃燒效率與高熱效率。 本發明之另一目的係在使可燃物的飛灰得以高溫熔 融，且不會因高溫產生氮氧化物污染物。 本發明之又一目的係在提供一種物質之燃燒系統， 在極低的過剩反應氣體量下達到高燃燒效率與高熱效率。 6 1320085 為達成上述之目的，本發明之物質之燃燒方法包括下 列步驟：將物質於低於其理論需氧量下加入第一反應氣 體，以產生底灰與第一產物，第一產物包括第一氣態物質 與飛灰；將第一產物於低於其理論需氧量下加入第二反應 氣體，以提高第一產物之溫度至飛灰之熔點以上，以產生 熔渣以及第二產物，第二產物包括第二氣態物質；將第二 產物至少進行一次熱回收，以及將第二產物至少進行一次 氧化燃燒，以達成第二產物實質上充分燃燒。其中，最後 φ 一步驟之過程中不會使氮氧化物大量產生。 為達成上述之目的，本發明之物質燃燒系統包括氣化 爐、熔融爐、至少一熱回收裝置，以及至少一反應氣體供 應裝置。其中，氣化爐係將物質於低於其理論需氧量下加 入第一反應氣體，以產生底灰與第一產物，第一產物包括 第一氣態物質與飛灰。熔融爐係將第一產物於低於其理論 需氧量下加入第二反應氣體，以提高第一產物之溫度至飛 灰之熔點以上，以產生熔渣以及第二產物，第二產物包括 Φ 第二氣態物質。至少一熱回收裝置用以進行熱回收。至少 一反應氣體供應裝置用以達成第二產物實質上充分燃燒， 且不會使氮氧化物大量產生。 【實施方式】 為能讓貴審查委員能更瞭解本發明之技術内容，特舉 較佳具體實施例說明如下。 以下請一併參考圖1至圖2關於本發明之第一實施例。 圖1係某物質（熱值LHV約3,300 kcal/kg)之燃燒產物溫度與 7 Ί 320085 _________ \ - ΨΗ^： ^：· - . — .....r_，一 反應氣體當量比之關係圖。圖2係本發明之物質之燃燒系統 1之不意圖。 請先參考圖1。於圖1之關係圖中，橫轴表示反應氣體 當量比’反應氣體當量比為實際反應氣體量與理論需氧量 的比值(ER)。縱軸表示燃燒產物的溫度，以攝氏溫度表示。 當ER=1時表示實際反應氣體量等於理論需氧量，燃燒產物 的溫度可達到最高的理論燃燒溫度。當ER<1時表示供給的 反應氣體量小於理論需氧量’此時燃料無法完全燃燒，燃 # 燒產物的溫度隨ER的增加而增加。當ER>1時表示實際反應 氣體量大於理論需氧量，此時過剩的反應氣體會使燃燒產 物的溫度降低’燃燒產物的溫度隨ER增加而降低。 圖1共有三條曲線，表示某可燃物質在不同狀態下燃燒 產物與ER的關係圖，其中最上方的曲線代表此一可燃物在 絕熱狀態的溫度曲線，第二條曲線代表第一條曲線經熱回 收裝置降低燃燒產物溫度後的溫度曲線，第三條曲線代表 第二條曲線再次經熱回收裝置降低燃燒產物溫度後的曲 • 線。圖中Q1、Q2、Q3、Q4與Q5分別表示A點之前、A點至 B點之間、B點至C點之間、D點至E點之間’以及ρ點至G點 之間所獲得之反應氣體量。圖中所示之斜線區域表示氮氧 化物生成區，此區域形成於高溫有氧的環境下。 接著請一併參考圖1與圖2，其中圖1之a點至〇點與圖2 之A點至G點係為完全對應之關係。本發明可處理各類可燃 物質’包括固態、液態及氣態可燃物。不同性質的物質經 由適當的燃料進料器81輸送進入氣化爐10。舉例來說，輸 送固體燃料的燃料進料器81可為螺旋輸送器，輸送液體及 1320085 氣態燃料的燃料進料器81可為喷嘴。氣化爐10位於圖2相對 應的位置在A點至B點之間，其可為各種形式的爐床，舉例 來說，氣化爐10可為流體化床。 將固態或液態的可燃物在ER<1的情況下，藉由反應氣 體供應裝置41加入Q1的反應氣體（如氧氣、空氣、水蒸氣 等）後，達到圖1與圖2中的A點。其反應的過程為：物質 的其中一部分氧化並釋放出化學能，同時因高溫將無法氧 化的物質裂解轉換成氣態物質。如圖1所示，當所給予的反 φ 應氣體Q1越高時，產物的溫度也會越高，可視可燃物的性 質調整Q1以控制進入氣化爐10的反應溫度。一般來說，進 入氣化爐10(進入A點）之溫度介於500°C至900°C之間。物質 經氣化爐10作用後產生底灰與第一產物，第一產物包括第 一氣態物質與飛灰。物質經氣化後大部分轉換成低分子量 的氣體，如CO、C02、H2、H20、CH4、N2等，以及小部份 的焦油（Tar)、未燃碳及灰份等。這些物質會隨氣流的方向 流出氣化爐10，而部分較大型的未燃碳及不可燃物（如金 φ 屬、砂石等）會留在氣化爐10的底部。殘留的大型未燃碳會 繼續與注入的反應氣體（Q1)繼續反應，轉換成氣態物質， 或直到隨燃燒產物流出氣化爐10為止。無法反應的不可燃 物質（統稱為底灰）在此高溫的情況下可有效的與可燃物質 分離，可於氣化爐10底部排出，接著經震動篩選機82及磁 選機83分選後分別存於儲存槽84、85，較細的物質大多為 床砂可循環再使用，其餘粒徑較大的物質可利用適當的分 選設備，例如磁選機及渦電流分選機等設備，將燃料中所 含的金屬物質分選出來。由於此狀態下處於缺氧的環境 9 1320085 k 中，這些金屬物質不易氧化成金屬氧化物，極具回收價值。 其他剩餘的不可燃物質係非金屬的無機物，亦可回收當成 級配再利用。 如圖2所示，在氣化爐10的末端（位於A點至B點之間靠 近B點部份）可藉由反應氣體供應裝置42送入適量的反應氣 體(Q2)，此時部份氣態可燃物會與注入的反應氣體進一步 反應，可提高生成物的溫度。並可有效的將高分子量的氣 態物質、焦油及未燃碳等物質進一步轉化成低分子量氣態 • 的型式。此時為避免灰份軟化在爐壁上結渣，氣化爐10内 的溫度通常保持在5〇〇°c至1〇〇〇。〇之間。 一接著將氣化爐1〇出口（於圖2之3點）的高溫可燃氣體導 入高溫之熔融爐20。熔融爐20位於圖2相對應的位置在B點 至C點之間’可燃氣體進入熔融爐20後可於其上方藉由反應 氣體供應裝置4 3 (位於圖2之B點至C點之間）注入適量的反 應氣體(Q3) ’利用控制注入的反應氣體量，可控制溶融爐 2〇的溫度，將反應後的產物溫度提高到灰份溶點以上(如圖 鲁y之C點），以產生料以及第二產物，第二產物包括第二氣 匕物質此V驟有別於先前技術中燃燒炼融爐操作於過剩 氣體的情況下（圖1之C’點）。當燃料具有-定的熱值（約 2,000 kcal/kg卩上）時，以空氣當反應氣體可控制炼融爐 在ER<1的隋况下達到飛灰熔點以上的溫度，飛灰等固態污 染物可因此被熔融形成灰份產物（例如溶潰）。請參考圖卜 =本實施例中’為了達到飛灰熔點以上的溫度，將溫度升 冋至C點，此時之值約為〇 6，溫度約為。相較於 驾知技術’則到達圖，點，此時ER值約為i 4，溫度約 10 1320085BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and system for burning a substance, and more particularly to a method and system for converting a combustible substance into a gaseous combustible gas after gasification. [Prior Art] _ One of the ways in which human beings obtain energy by burning combustibles to generate thermal energy' is aimed at improving the efficiency of heat utilization and reducing the pollutants generated by combustion during combustion. Theoretically, if high thermal efficiency is required, the lower the amount of excess reactive gas (excess oxidant' (such as pure oxygen, air, etc.), the better, in order to reduce the heat loss of the exhaust gas derived from the excess reaction gas. However, the excessively low amount of excess reaction gas tends to cause incomplete combustion of the fuel, which not only causes loss of fuel, but also leads to the production of pollutants such as hydrocarbon (HC) and carbon monoxide (c〇). In addition, the theoretical _ adiabatic temperature decreases as the amount of excess reaction gas increases, and a high calorific value fuel is highly prone to generate a large amount of nitrogen oxides (NOx) due to high temperatures at an excessively low amount of excess reaction gas. For example, when fuel (such as natural gas, fuel oil, pulverized coal, etc.) is easily mixed with the reaction gas, in order to reduce the heat loss of the exhaust gas, a lower excess combustion air is often given, but the temperature of the combustion product is higher, resulting in nitrogen. The production of oxide contaminants. When fuel (e.g., lump coal or waste, etc.) is not easily mixed with the reaction gas, a large amount of excess gas is often supplied for the fuel to be fully combusted, and the exhaust heat loss and the thermal efficiency are lowered due to 5 1320085. For example, the incinerator generally burns the waste month b, and the amount of the reaction gas is at least twice the theoretical oxygen demand. In addition, the fly ash produced by the combustion process often contains some harmful substances. If the pollution is to be reduced and the feasibility of material reuse is improved, the fly ash needs to be smelted to form slag, and the combustion temperature needs to be increased above the ash point. (Normally 1300~15〇〇.〇. At this high temperature, if both oxygen and nitrogen are present, nitrogen oxide (NOx) pollutants will be produced. • Waste incinerators, for example, The material is fully combusted and must be supplied with combustion air in the large area. Therefore, the temperature of the exhaust gas is burned (about 8 〇〇 to 1 〇〇〇. 〇 can not reach the temperature that makes the fly ash melt. If the fly ash is to be condensed, it must be incinerated. A furnace is placed behind the furnace to add additional auxiliary fuel to increase the degree of combustion products. This method requires additional external energy and is also contaminated with a large amount of nitrogen oxides due to the presence of excess air. The combustion mode of the prior art often fails to balance thermal efficiency with reducing pollutants. Therefore, it is necessary to provide a method for burning a substance and its system to improve the problems of the prior art. SUMMARY OF THE INVENTION The object of the present invention is to provide a method for burning a substance which can achieve high combustion efficiency and high heat efficiency at an extremely low excess reaction gas amount. Another object of the present invention is to make fly ash of combustibles. It is melted at a high temperature and does not generate nitrogen oxide contaminants due to high temperature. Another object of the present invention is to provide a combustion system for a substance which achieves high combustion efficiency and high thermal efficiency at an extremely low excess reaction gas amount. 6 1320085 To achieve the above object, the method of burning a substance of the present invention comprises the steps of: adding a substance to a first reaction gas below its theoretical oxygen demand to produce a bottom ash and a first product, the first product comprising a first gaseous state a substance and fly ash; adding the first product to the second reaction gas below its theoretical oxygen demand to increase the temperature of the first product above the melting point of the fly ash to produce slag and the second product, the second product Including a second gaseous substance; at least one heat recovery of the second product, and at least one oxidative combustion of the second product to achieve a second product Fully burnt in quality. Among them, the nitrogen oxide is not generated in a large amount during the last step of φ. To achieve the above object, the material combustion system of the present invention comprises a gasifier, a melting furnace, at least one heat recovery device, and At least one reaction gas supply device, wherein the gasification furnace adds the substance to the first reaction gas below its theoretical oxygen demand to produce bottom ash and the first product, the first product comprising the first gaseous substance and the fly ash The melting furnace adds the first product to the second reaction gas below its theoretical oxygen demand to increase the temperature of the first product above the melting point of the fly ash to produce slag and a second product, the second product comprising Φ second gaseous substance. At least one heat recovery device is used for heat recovery. At least one reaction gas supply device is used to achieve substantially full combustion of the second product without causing a large amount of nitrogen oxides to be generated. The technical content of the present invention will be better understood by the reviewing committee, and the preferred embodiments are described below. Hereinafter, please refer to FIG. 1 to FIG. 2 together with respect to the first embodiment of the present invention. Figure 1 is a graph showing the relationship between the combustion product temperature of a substance (heat value LHV of about 3,300 kcal/kg) and 7 Ί 320085 _________ \ - ΨΗ^: ^:· - . -- ....r_, a reaction gas equivalent ratio . Figure 2 is a schematic representation of the combustion system 1 of the material of the present invention. Please refer to Figure 1 first. In the diagram of Fig. 1, the horizontal axis indicates the reaction gas equivalent ratio 'reaction gas equivalent ratio" is the ratio (ER) of the actual reaction gas amount to the theoretical oxygen demand. The vertical axis represents the temperature of the combustion products, expressed in degrees Celsius. When ER = 1, the actual amount of reaction gas is equal to the theoretical oxygen demand, and the temperature of the combustion product can reach the highest theoretical combustion temperature. When ER < 1 indicates that the amount of the supplied reaction gas is smaller than the theoretical oxygen demand', the fuel cannot be completely burned at this time, and the temperature of the burned product increases as the ER increases. When ER >1 indicates that the actual amount of reactant gas is greater than the theoretical oxygen demand, then excess reaction gas will lower the temperature of the combustion product. The temperature of the combustion product decreases as ER increases. Figure 1 has three curves, which show the relationship between combustion products and ER of a combustible substance under different conditions. The uppermost curve represents the temperature curve of the combustible in adiabatic state, and the second curve represents the first curve. The recovery device reduces the temperature profile of the combustion product temperature, and the third curve represents the curve of the second curve after the combustion product temperature is again reduced by the heat recovery device. In the figure, Q1, Q2, Q3, Q4 and Q5 represent the point before point A, point A to point B, point B to point C, point D to point E, and point ρ to point G, respectively. The amount of reaction gas obtained. The hatched area shown in the figure indicates a nitrogen oxide generating region which is formed in a high temperature aerobic environment. Next, please refer to FIG. 1 and FIG. 2 together, wherein the point a to the point of FIG. 1 and the point A to point G of FIG. 2 are in a perfect correspondence relationship. The present invention is capable of treating a wide variety of combustible materials, including solid, liquid, and gaseous combustibles. Substances of different nature are transported into the gasifier 10 via a suitable fuel feeder 81. For example, the fuel feeder 81 that delivers solid fuel can be a screw conveyor, and the fuel feeder 81 that delivers liquid and 1320085 gaseous fuel can be a nozzle. The gasifier 10 is located at a corresponding position in Fig. 2 between point A and point B, which may be various types of hearths, for example, the gasifier 10 may be a fluidized bed. In the case of ER < 1 in the case of ER < 1, the reaction gas (e.g., oxygen, air, water vapor, etc.) of Q1 is added by the reaction gas supply means 41 to reach point A in Figs. 1 and 2. The reaction process is: a part of the substance oxidizes and releases chemical energy, and at the same time, the non-oxidizable substance is cleaved into a gaseous substance due to the high temperature. As shown in Fig. 1, when the imparted anti-φ gas Q1 is higher, the temperature of the product is higher, and Q1 can be adjusted depending on the nature of the combustible material to control the reaction temperature entering the gasification furnace 10. Generally, the temperature entering the gasifier 10 (going to point A) is between 500 ° C and 900 ° C. The substance is passed through the gasifier 10 to produce bottom ash and a first product, the first product comprising the first gaseous material and fly ash. Most of the substances are converted into low molecular weight gases such as CO, CO 2 , H 2 , H 20 , CH 4 , N 2 , etc., as well as a small portion of tar (Tar), unburned carbon and ash. These materials will flow out of the gasifier 10 in the direction of the gas stream, and some of the larger unburned carbon and incombustibles (such as gold genus, sand, etc.) will remain at the bottom of the gasifier 10. The residual large unburned carbon continues to react with the injected reaction gas (Q1), is converted to a gaseous substance, or until it exits the gasifier 10 with the combustion products. The incombustible non-flammable substances (collectively referred to as bottom ash) can be effectively separated from the combustible materials at the high temperature, can be discharged at the bottom of the gasification furnace 10, and then separately sorted by the vibration screening machine 82 and the magnetic separator 83. In the storage tanks 84, 85, most of the finer materials can be recycled for the bed sand, and the other materials with larger particle size can be used in the fuel by using appropriate sorting equipment, such as a magnetic separator and an eddy current sorter. The metal substances contained are sorted out. Due to the oxygen-deficient environment in this state, 9 1320085 k, these metal substances are not easily oxidized into metal oxides, which is extremely valuable for recycling. Other remaining non-combustible substances are non-metallic inorganic substances, which can also be recycled and reused. As shown in Fig. 2, at the end of the gasification furnace 10 (between the point A and the point B and the portion near the point B), an appropriate amount of the reaction gas (Q2) can be supplied by the reaction gas supply unit 42, at this time, The gaseous combustibles react further with the injected reaction gas to increase the temperature of the product. It can effectively convert high molecular weight gaseous substances, tar and unburned carbon into a low molecular weight gaseous form. At this time, in order to prevent ash formation on the furnace wall by ash softening, the temperature in the gasification furnace 10 is usually maintained at 5 ° C to 1 Torr. Between 〇. Next, the high-temperature combustible gas at the outlet of the gasifier 1 (point 3 in Fig. 2) is introduced into the high-temperature melting furnace 20. The melting furnace 20 is located at a corresponding position in Fig. 2 between point B and point C. After the combustible gas enters the melting furnace 20, it can be passed over the reaction gas supply device 4 3 (between point B and point C of Fig. 2). Injecting an appropriate amount of reactive gas (Q3) 'Using the amount of reactive gas injected to control, the temperature of the molten furnace can be controlled to increase the temperature of the product after the reaction to above the ash melting point (C point of Figure y). In order to produce a material and a second product, the second product includes a second gas enthalpy material which is different from the prior art in which the combustion smelting furnace operates on excess gas (point C' in FIG. 1). When the fuel has a constant calorific value (about 2,000 kcal/kg 卩), the reaction gas can control the temperature of the smelting furnace to reach a temperature above the melting point of the fly ash under the condition of ER<1, and solid waste such as fly ash. The material can thus be melted to form an ash product (e.g., melt). Please refer to Fig. 2 = In this embodiment, in order to reach the temperature above the melting point of the fly ash, the temperature is raised to point C, and the value is about 〇 6, and the temperature is about. Compared to the driving technique, the graph arrives at the point where the ER value is about i 4 and the temperature is about 10 1320085.
°在相同的滞留時間下’因反應氣體量的不同， 爐20的體積不栽前技術之燃舰融爐的一 外，習知技術會產生氮氧化物(如圖1之斜線所 不品二二C，點即位於此區域中），但本發明之方法不僅不會 j生氮氧化物，其他高分子量的有機物質也會因此高溫: ，匕成低分子量的第二產物。熔融的灰份熔渣則可經由熔 融爐20下方的熔渣出口 86流至其下方的冷卻水槽87，可經 冷卻後排出再利用。在熔渣出口 86處可注入適量的反應氣 體即可提升此處的溫度，無需如先前技術需提供額外的燃 料’使熔渣得以順利流出熔融爐2〇。在熔融爐2〇内的溫度 通常保持在1〇〇〇。〇至16〇〇。〇之間。 須注意的是，在氣化爐10的末端亦可不設置反應氣體 供應裝置42’而僅藉由位於熔融爐2〇的反應氣體供應裝置 43將所需的反應氣體一次加到所需的量。 經由熔融爐20的產物（位於圖1的c點）係為高溫可燃氣 體產物，此時若繼續給予反應氣體，使其充分燃燒，則將 會進入氮氧化物生成區。因此，為了避免產生氮氧化物， 接著將第二產物至少進行一次熱回收，以及將第二產物至 少進行一次氧化燃燒，以達成第二產物實質上充分燃燒。 此過程係透過控制溫度或控制供氧量來達成不會使氮氧化 物大量產生之目的。其中最後一次進行氧化燃燒時係供給 足夠之反應氣體，使該第二產物實質上充分燃燒。以下針 對此過程作進一步說明。 將第二產物利用熱回收裝置吸收其顯熱，以達到降低 溫度的目的。經降低溫度後的可燃氣體（位於圖1的1)點）再 1320085 * 藉由反應氣體供應裝置給予適量的反應氣體（Q4)，將可燃 氣體所含的可燃部份進一步氧化，同時將其化學能轉換成 燃燒產物的顯熱，因而使燃燒產物的溫度提高（位於圖1的E 點）。 此時，若ER值已略大於1時，表示供給的反應氣體已 足夠燃料充分燃燒，且溫度仍低於氮氧化物生成區時，此 時即完成本發明之所有步驟。於其後接續利用習知技術的 熱回收裝置回收燃燒產物中的顯熱。但若經由反應氣體供 φ 應裝置44給予適量的反應氣體後，ER值仍小於1，且溫度 接近氮氧化物生成區時，若持續加入反應氣體使其完全燃 燒，將使燃燒產物的溫度達到氮氧化物生成的溫度（如第二 條曲線之頂點），此時需再次進行吸收可燃氣體的顯熱，經 降低其溫度後（如圖1的F點）再導入適量的反應氣體的步 驟。重複此二步驟，直到燃燒產物的實際反應氣體量大於 理論需氧量時，可燃成份完全燃燒，此時雖有過剩氧氣存 在，惟其溫度已低於氮氧化物產生的溫度（如圖1的G點）， φ 如此即可避免氮氧化物的產生。 於本實施例中，於圖1之C點狀態下，經由熱回收裝置 31後成為圖1中的D點狀態，再經反應氣體供應裝置44後， 成為於圖1之E點狀態，然其ER值仍小於1，此時若持續加 入反應氣體，將使燃燒產物達到氮氧化物生成的溫度，因 此，接著將可燃氣體經另一熱回收置32吸收可燃氣體的顯 熱，降低其溫度（如圖1之E點降溫至F點），接著再藉由反應 氣體供應裝置45導入適量的反應氣體(Q5)，使燃燒產物進 一步氧化釋出化學能以提高溫度，達到圖1之G點。此時， 1 1320085 由於高溫氣體燃料與反應氣體極易混合，因此可使燃燒產 物在極低的過剩反應氣體下達到完全燃燒。於本實施例 中，最終燃燒產物的過剩氣體量僅約10%，因此可有效的 降低過剩反應氣體的熱排放損失，其熱效率與傳統燃燒模 式G’點相同，但本發明之方法無傳統燃燒模式會產氮氧化 物污染物的缺點。 須注意的是，上述熱回收裝置與反應氣體供應裝置， 可視實際需要設置兩組（如圖2之第一實施例）、僅設置一 φ 組，或設置三組以上。熱回收裝置與反應氣體供應裝置設 置的數量與待處理之物質特性有關。 另須注意的是，上述進行熱回收與進行氧化燃燒的步 驟除先後進行外，亦可同時進行吸熱與燃燒，此時熱回收 裝置與反應氣體供應裝置係整合為同一裝置。可同時進行 吸熱與燃燒之裝置亦可設置兩個以上，其設置的數量與待 處理之物質特性有關。 接著請參考圖2。本發明之物質之燃燒系統1包括氣 • 化爐10、熔融爐20、熱回收裝置31、32以及反應氣體供 應裝置44, 45。其中氣化爐10可將於低於可燃物質理論需 氧體量下加入第一反應氣體，以產生底灰與第一產物，第 一產物包括第一氣態物質與飛灰。熔融爐20可將第一產物 於低於其理論需氧量下加入第二反應氣體，以提高第一產 物之溫度至飛灰之熔點以上，以產生熔渣與第二產物，第 二產物包括第二氣態物質。熱回收裝置31、32可降低第二 產中氣態物質之溫度。反應氣體供應裝置44、45可加入反 1320085 應氣體使第二產物中的可燃氣態物質進一步燃燒，以提升 溫度。藉由熱回收裝置31、32與反應氣體供應裝置44、 45，將第二產物至少進行一次熱回收，以及將第二產物至 少進行一次氧化燃燒，以達成第二產物實質上充分燃燒。 此過程係透過控制溫度或控制供氧量來達成不會使氮氧化 物大量產生之目的。其中最後一次進行氧化燃燒時係供給 足夠之反應氣體，使該第二產物實質上充分燃燒。由於各 • 個裝置所能產生的功效與說明相同於上述有關物質之燃燒 方法之各個步驟，因此不再贅述。 須注意的是，上述熱回收裝置與反應氣體供應裝置， 可視實際需要設置兩組（如圖2之實施例）、僅設置一組，或 設置三組以上。熱回收裝置與反應氣體供應裝置設置的數 量與待處理之物質特性有關。 每組之熱回收裝置與反應氣體供應裝置，除先後設置 外，亦可整合為一體。如圖3所示，為本發明之物質之燃燒 ® 系統之第二實施例示意圖。與第一實施例不同的是，本實 施例具有可同時進行熱回收與氧化燃燒之裝置50。舉例來 說，裝置50之結構可為反應氣體供應裝置的周圍同時具有 可進行熱回收之水冷壁或鍋爐管。須注意的是，裝置50亦 可設置兩個以上，裝置50設置的數量與待處理之物質特性 有關。 综合上述，本案之可燃物質之燃燒熱利用方法及其系 統，係利用在缺乏氧氣存在的情況下使灰份熔融，避免氮 14 1320085 * 氧化物及戴奥辛等污染物的產生，以及使可燃物質進一步 轉化成低分子量的可燃氣態物質，低分子量的可燃氣態物 質與反應氣體極易混合的特性，當氣體燃料處於高溫的情 況下，逐步使其燃燒，不僅可使物質有效地完全燃燒，當 過剩反應氣體產生時，其燃燒產物的溫度亦可降至氮氧化 物的產生的溫度以下。因此可達到高的熱效率與有效控制 污染物產出的目的。 綜上所陳，本發明無論就目的、手段及功效，在在均 Φ 顯示其迥異於習知技術之特徵。惟須注意，上述實施例僅 為例示性說明本發明之原理及其功效，而非用於限制本發 明之範圍。任何熟於此項技藝之人士均可在不違背本發明 之技術原理及精神下，對實施例作修改與變化。本發明之 權利保護範圍應如後述之申請專利範圍所述。 【圖式簡單說明】 圖1係某物質之燃燒產物溫度與反應氣體當量比之關係圖。 • 圖2係本發明之物質之燃燒系統之第一實施例示意圖。 圖3係本發明之物質之燃燒系統之第二實施例示意圖。 【元件代表符號說明】 物質之燃燒熱利用系統1 氣化爐10 熔融爐20 熱回收裝置31、32 1320085 反應氣體供應裝置41、42、43、44、45 裝置50 燃料進料器81 震動篩選機82 磁選機83 儲存槽84、85 熔渣出口 86 冷卻水槽87° Under the same residence time, because of the difference in the amount of reaction gas, the volume of the furnace 20 is not the technology of the former ship-fired furnace, the conventional technology will produce nitrogen oxides (as shown in Figure 1 Two C, the point is located in this region), but the method of the present invention not only does not produce nitrogen oxides, but other high molecular weight organic substances are also high in temperature: 匕 into a second product of low molecular weight. The molten ash slag can be discharged to the cooling water tank 87 below it via the slag outlet 86 below the melting furnace 20, and can be cooled and discharged for reuse. An appropriate amount of reactant gas can be injected at the slag outlet 86 to increase the temperature there without the need to provide additional fuel as required by the prior art to allow the slag to flow smoothly out of the furnace. The temperature in the crucible 2 is usually maintained at 1 Torr. 〇 to 16〇〇. Between 〇. It is to be noted that the reaction gas supply means 42' may not be provided at the end of the gasification furnace 10 and the required reaction gas may be added to the required amount only once by the reaction gas supply means 43 located in the melting furnace 2''. The product passing through the melting furnace 20 (located at point c in Fig. 1) is a high-temperature combustible gas product, and if the reaction gas is continuously supplied to be fully combusted, it will enter the nitrogen oxide generating region. Therefore, in order to avoid the generation of nitrogen oxides, the second product is then subjected to at least one heat recovery, and the second product is subjected to at least one oxidative combustion to achieve substantially complete combustion of the second product. This process achieves the goal of not producing large amounts of nitrogen oxides by controlling the temperature or controlling the amount of oxygen supplied. The last time the oxidative combustion is carried out, sufficient reaction gas is supplied to substantially fully combust the second product. The following pin further explains this process. The second product is absorbed by the heat recovery device to absorb its sensible heat for the purpose of lowering the temperature. The combustible gas (at the point of 1 in Fig. 1) after the temperature is lowered) 1320085 * The flammable portion contained in the combustible gas is further oxidized by chemical gas supply means to give an appropriate amount of the reaction gas (Q4) while chemically oxidizing It can be converted into sensible heat of the combustion products, thus increasing the temperature of the combustion products (located at point E in Figure 1). At this time, if the ER value is slightly larger than 1, it means that all of the steps of the present invention are completed when the supplied reaction gas is sufficiently fuel-burned and the temperature is still lower than the nitrogen oxide generating zone. The sensible heat in the combustion products is then recovered using a heat recovery unit of the prior art. However, if an appropriate amount of reaction gas is supplied to the φ device 44 via the reaction gas, the ER value is still less than 1, and when the temperature is close to the nitrogen oxide generating region, if the reaction gas is continuously added to completely burn, the temperature of the combustion product is reached. The temperature at which nitrogen oxides are formed (such as the apex of the second curve), at which point the sensible heat of the flammable gas is absorbed again, and after the temperature is lowered (point F in Fig. 1), an appropriate amount of the reaction gas is introduced. Repeat these two steps until the actual amount of reaction gas of the combustion product is greater than the theoretical oxygen demand, the combustible component is completely burned. At this time, although excess oxygen exists, the temperature is lower than the temperature generated by the nitrogen oxide (see Figure G). Point), φ can avoid the generation of nitrogen oxides. In the present embodiment, in the state of point C in Fig. 1, the state of point D in Fig. 1 is passed through the heat recovery device 31, and after passing through the reaction gas supply device 44, it becomes the state of point E in Fig. 1, but The ER value is still less than 1. If the reaction gas is continuously added, the combustion product will reach the temperature at which the nitrogen oxides are formed. Therefore, the flammable gas is then absorbed by another heat recovery unit 32 to absorb the sensible heat of the combustible gas, thereby lowering the temperature ( As shown in Fig. 1, the temperature is lowered to point F, and then an appropriate amount of the reaction gas (Q5) is introduced by the reaction gas supply device 45 to further oxidize the combustion product to release the chemical energy to raise the temperature to reach the point G of Fig. 1. At this time, 1 1320085, because the high-temperature gas fuel is extremely easy to mix with the reaction gas, the combustion product can be completely burned under extremely low excess reaction gas. In the present embodiment, the amount of excess gas of the final combustion product is only about 10%, so that the heat emission loss of the excess reaction gas can be effectively reduced, and the thermal efficiency is the same as the conventional combustion mode G' point, but the method of the present invention has no conventional combustion. Modes can produce shortcomings of nitrogen oxide contaminants. It should be noted that the above-mentioned heat recovery device and the reaction gas supply device may be provided with two groups (as in the first embodiment of FIG. 2), only one φ group, or three or more groups, as needed. The number of heat recovery devices and reactive gas supply devices is related to the properties of the material to be treated. It should also be noted that the above steps of performing heat recovery and oxidative combustion may be carried out simultaneously with heat absorption and combustion, and the heat recovery device and the reaction gas supply device are integrated into the same device. There are also two or more devices that can simultaneously perform heat absorption and combustion, and the number of settings is related to the characteristics of the substance to be treated. Then please refer to Figure 2. The combustion system 1 of the substance of the present invention includes a gasification furnace 10, a melting furnace 20, heat recovery devices 31, 32, and reaction gas supply devices 44, 45. The gasifier 10 can add a first reaction gas below the theoretical oxygen demand of the combustible material to produce a bottom ash and a first product, the first product comprising the first gaseous material and fly ash. The melting furnace 20 can add the first product to the second reaction gas below its theoretical oxygen demand to increase the temperature of the first product above the melting point of the fly ash to produce slag and the second product, the second product comprising The second gaseous substance. The heat recovery units 31, 32 reduce the temperature of the gaseous material in the second production. The reaction gas supply means 44, 45 may be added to the anti- 1320085 gas to further combust the combustible gas in the second product to raise the temperature. The second product is subjected to at least one heat recovery by the heat recovery means 31, 32 and the reaction gas supply means 44, 45, and the second product is subjected to at least one oxidative combustion to achieve substantially complete combustion of the second product. This process achieves the goal of not producing large amounts of nitrogen oxides by controlling the temperature or controlling the amount of oxygen supplied. The last time the oxidative combustion is carried out, sufficient reaction gas is supplied to substantially fully combust the second product. Since the functions and descriptions of each device are the same as those of the combustion method of the above-mentioned related substances, they will not be described again. It should be noted that the above-mentioned heat recovery device and the reaction gas supply device may be provided with two sets (as in the embodiment of Fig. 2), only one set, or three or more sets as needed. The number of heat recovery devices and reactive gas supply devices is related to the properties of the material to be treated. The heat recovery unit and the reaction gas supply unit of each group can be integrated into one unit. Figure 3 is a schematic view of a second embodiment of the Combustion ® system of the material of the present invention. Unlike the first embodiment, this embodiment has means 50 for simultaneously performing heat recovery and oxidative combustion. For example, the structure of the apparatus 50 may be a water wall or a boiler tube that is capable of heat recovery while surrounding the reaction gas supply unit. It should be noted that more than two devices 50 may be provided, and the number of devices 50 is set in relation to the characteristics of the material to be treated. In summary, the combustion heat utilization method and system of the combustible material in the present invention utilizes the ash melting in the absence of oxygen to avoid the generation of pollutants such as nitrogen 14 1320085 * oxides and dioxin, and further flammable substances. It is converted into a low molecular weight flammable substance, and the low molecular weight flammable substance is easily mixed with the reaction gas. When the gas fuel is at a high temperature, it is gradually burned, which not only enables the substance to be completely burned completely, but also when the reaction is excessive. When the gas is generated, the temperature of the combustion products may also fall below the temperature at which the nitrogen oxides are generated. Therefore, high thermal efficiency and effective control of pollutant production can be achieved. In summary, the present invention, regardless of its purpose, means, and efficacy, exhibits characteristics that are different from conventional techniques. It is to be noted that the above-described embodiments are merely illustrative of the principles of the invention and its advantages, and are not intended to limit the scope of the invention. Modifications and variations of the embodiments can be made by those skilled in the art without departing from the spirit and scope of the invention. The scope of the protection of the present invention should be as described in the scope of the patent application to be described later. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a graph showing the relationship between the temperature of a combustion product of a substance and the equivalent ratio of a reaction gas. • Figure 2 is a schematic illustration of a first embodiment of a combustion system for a substance of the present invention. Figure 3 is a schematic illustration of a second embodiment of a combustion system for a substance of the present invention. [Description of Component Symbols] Combustion Heat Utilization System of Substance 1 Gasification Furnace 10 Melting Furnace 20 Heat Recovery Device 31, 32 1320085 Reaction Gas Supply Device 41, 42, 43, 44, 45 Device 50 Fuel Feeder 81 Vibration Screening Machine 82 magnetic separator 83 storage tank 84, 85 slag outlet 86 cooling sink 87