200540372 九、發明說明： 【發明所屬之技術領域】 本發明係關於固態燃料氣化系統，更詳言之，係關於 利用固悲燃料的熱分解’而製造以氮及一氧化碳為主成分 之合成氣體的固態燃料氣化系統。 【先前技術】 已知有將廢塑膠、污泥、粉碎塵（shredder dust)、或 都市垃圾等有機廢棄物、或煤炭等低質固態燃料進行氣 ^匕’而將較面卡路里（高熱量）的合成氣體供應給發電設備 等的燃料氣化系統。本發明者曾開發出在此種氣化系統 中：利用％ 1 〇〇〇 C高溫空氣將固態燃料氣化熔融的燃料氣 化系統，並提案於日本專利特開2〇〇2_158885號等公報 中。 此方式的氣化系統係如第10圖與第u圖所示，具備 有將固態燃料氣化熔融的氣化爐。空氣加熱裝置係將⑽ C以上的尚皿空氣供應給氣化爐，而熱回收/氣體精製裝置 則係將氣化爐的粗氣體冷卻並加以精製。供應給氣化爐的 固悲燃料係利用尚溫空氣而氣化熔融並產生約10 0 0它的 高溫粗氣體，高溫粗氣體係便供應給熱回收/氣體精製裝 置。熱回收/氣體精製裝置係將高溫粗氣體冷卻且加二精 製，再將精製氣體供應給發電設備等。由熱回收/氣體精"製 裝置所回收的焦炭（熱分解後的碳化物）係利用焦炭再彳^2 機構（char recycle)導入於固態燃料供應管路中，並與固 態燃料一起供應給氣化爐。精製氣體的其中一部份將者作 315906 5 200540372 .空氣加熱用燃料而供應給空氣加熱裝置，空氣加熱裝置係 -利用精製氣體的燃燒熱而加熱空氣，再將高溫空氣供應給 .氣化爐。根據此種方式之氣化系統，因為粗氣體溫度屬於 非常高溫（約100(TC)，因而可獲得焦炭含量較少，且含較 多量的氫之粗氣體。 本發明者也開發出將利用固態燃料的熱分解而產生的 熱分解氣體，採用高溫水蒸氣進行改質，再將改質氣體供 應給發電設備等的燃料氣化系統，並提案於日本專利特開 * 2002-21 0444號等公報中。 此方式的氣化系統乃如第12圖與第13圖所示，具備 有將固態燃料進行熱分解的熱分解爐，而且具備有將熱分 解氣體利用高溫水蒸氣進行改質的改質爐。供應給熱分解 爐的固態燃料係在熱分解爐内施行熱分解，再將熱分解爐 中所產生溫度約300°C左右的熱分解氣體，供應給改質 爐。熱分解氣體便在改質爐中，與溫度約l〇〇〇°C的高溫水 φ 蒸氣混合而改質。為求防止因熱分解氣體中的碳化氫水蒸 氣改質反應（吸熱反應），而導致改質爐爐内溫度下降情況 發生，便將約1 〇〇〇°C的高溫空氣供應給改質爐，再從改質 爐中將約800°C左右的改質氣體供應給熱回收/氣體精製 裝置。熱回收/氣體精製裝置係將改質氣體冷卻並精製，再 將精製氣體供應給發電設備等。精製氣體其中一部份將供 應給空氣/水蒸氣加熱裝置，空氣/水蒸氣加熱裝置便利用 精製氣體的燃燒熱將空氣與水蒸氣加熱，再將溫度約1000 °C左右的高溫空氣與高溫水蒸氣供應給改質爐。 6 315906 200540372 根據此種方式之氣化系統，因為固態燃料係在熱分解 爐内坪留較長的時間，因此便可對較大尺寸的廢棄物等施、 行熱分解處理，且因為碳轉換率較高，並抑制煤份的產生，、 因而可省略焦炭再循環機構。此外，根據此種方式之氣化 系統，藉由更組合灰熔融燃燒爐，便可獲得抽出未混入焦 炭份的、j：容融灰等優點。 在上述具備氣化熔融型氣化爐（第1 〇圖及第丨丨圖）的 氣化系統，將有在燃料氣體中含較多量煤份的傾向，煤份 的產生特別在將塑膠廢棄物等固態燃料進行氣化的情況時 更加明顯。所以’如第1 0圖所示，氣化系統便需要具備將 焦炭份回收的焦炭再循環機構。此外，因為氣化爐中的固 態燃料在爐内滯留時間較短，因而頗難將較大尺寸的廢棄 物等進行氣化處理，所以便需要固態燃料的微粉碎處理等 前處理步驟與前處理設備。此外，此方式的氣化系統中， 精製氣體散熱量為1 000kcal/Nm3左右，僅能獲得散熱量較 低的合成氣體。 另一方面’根據具備熱分解爐與改質爐的上述氣化系 統（第12圖與第13圖），將可省略此種焦炭再循環機構， 且不需對較大型廢棄物等進行微粉碎而施行熱分解處理。 但是，為能將熱分解氣體中的焦油份完全改質，因而產生 必須將改質爐的爐内溫度維持於相當高的高溫（約1〇〇〇。〇 左右）而舄要將較多里的兩溫空氣導入於改質爐中。因而 將產生改質、精製後的精製氣體散熱量降低至約 l〇〇〇kcal/Nm3左右的問題。此外，此方式的精製氣體將含 315906 7 200540372 量氫的合成 ，便必須更 有較多量的曱烷。但是，因為頗難製造含有多 氣體，因而產生在欲製造含多量氫的合成氣^ 進一步改良氣化系統。 本發明之目的在於提供 且製造以氫與一氧化碳為主 固態燃料氣化系統。 【發明内容】 -種可省略焦炭再循環機構， 成分的高散熱量的合成氣體之200540372 IX. Description of the invention: [Technical field to which the invention belongs] The present invention relates to a solid fuel gasification system, and more specifically, it relates to the use of thermal decomposition of solid fuels to produce a synthetic gas composed mainly of nitrogen and carbon monoxide. Solid fuel gasification system. [Prior art] It is known to use waste plastics, sludge, shredder dust, organic waste such as municipal waste, or low-quality solid fuels such as coal to gasify the surface calories (high calories). The synthesis gas is supplied to a fuel gasification system such as a power generation facility. The inventors have developed a fuel gasification system for gasification and melting of solid fuel by using high temperature air at 10000C in this type of gasification system, and proposed it in Japanese Patent Laid-Open No. 2000_158885 and other publications . The gasification system of this embodiment is provided with a gasification furnace for gasifying and melting solid fuel, as shown in Figs. 10 and u. The air heating device supplies dish gas of ⑽C or more to the gasifier, while the heat recovery / gas refining device cools and purifies the crude gas from the gasifier. The solid fuel supplied to the gasification furnace uses the warm air to gasify and melt to produce about 100% of its high temperature crude gas. The high temperature crude gas system is supplied to the heat recovery / gas refining device. The heat recovery / gas refining device cools the high-temperature crude gas, performs refining, and supplies the refined gas to power generation equipment. The coke (thermally decomposed carbide) recovered by the heat recovery / gas refinery production unit is introduced into a solid fuel supply line using a coke recharging mechanism (char recycle) and supplied to the solid fuel together with the solid fuel. Gasifier. Part of the refined gas will be 315906 5 200540372. Air heating fuel is supplied to the air heating device. The air heating device is based on the combustion heat of the refined gas to heat the air, and then supplies high temperature air to the gasifier. . According to this type of gasification system, since the temperature of the crude gas is very high (about 100 (TC)), a crude gas having a small coke content and a large amount of hydrogen can be obtained. The inventors have also developed a solid gas The thermally decomposed gas generated by the thermal decomposition of fuel is reformed using high-temperature water vapor, and the reformed gas is supplied to fuel gasification systems such as power generation equipment, and has been proposed in Japanese Patent Laid-Open No. * 2002-21 0444 and other publications The gasification system in this mode is equipped with a thermal decomposition furnace that thermally decomposes solid fuel, as shown in Figs. 12 and 13, and a modification that uses a high-temperature water vapor to reform the thermal decomposition gas. Furnace. The solid fuel supplied to the thermal decomposition furnace is thermally decomposed in the thermal decomposition furnace, and then the thermal decomposition gas generated in the thermal decomposition furnace at a temperature of about 300 ° C is supplied to the reforming furnace. The thermal decomposition gas is in In the reforming furnace, it is mixed with high-temperature water φ steam having a temperature of about 1000 ° C to modify it. In order to prevent the reforming reaction (endothermic reaction) caused by the hydrocarbon water vapor in the thermal decomposition gas, the reforming furnace is caused. furnace When the internal temperature drops, high-temperature air of about 1000 ° C is supplied to the reforming furnace, and the reformed gas of about 800 ° C is supplied from the reforming furnace to the heat recovery / gas refining device. The recovery / gas refining device cools and refines the reformed gas, and then supplies the refined gas to power generation equipment, etc. Part of the refined gas will be supplied to the air / water vapor heating device. The air / water vapor heating device facilitates the use of refined gas. The heat of combustion heats air and water vapor, and then supplies high-temperature air and water vapor at a temperature of about 1000 ° C to the reforming furnace. 6 315906 200540372 A gasification system according to this method, because solid fuel is thermally decomposed. The furnace floor is left for a long time, so it can be used for thermal decomposition treatment of large-size waste, etc., and because the carbon conversion rate is high and the generation of coal is suppressed, the coke recycling mechanism can be omitted. In addition, according to the gasification system in this way, by more combining the ash melting combustion furnace, the advantages of extracting unmixed coke, j: capacity melting ash, etc. can be obtained. The gasification system of the melting type gasifier (Figure 10 and Figure 丨 丨) will tend to contain a large amount of coal in the fuel gas. The production of coal is particularly for the gasification of solid waste such as plastic waste. The situation of gasification is more obvious. Therefore, as shown in Fig. 10, the gasification system needs a coke recycling mechanism for recovering coke. In addition, the solid fuel in the gasification furnace has a short residence time in the furnace. Therefore, it is quite difficult to gasify a large-sized waste, etc., so pretreatment steps and pretreatment equipment such as pulverization of solid fuel are required. In addition, in this type of gasification system, the heat dissipation of the refined gas is About 1 000kcal / Nm3, only syngas with low heat dissipation can be obtained. On the other hand, according to the above-mentioned gasification system (Figures 12 and 13) equipped with a thermal decomposition furnace and a reforming furnace, this type of gas can be omitted. The coke recycling mechanism does not need to pulverize large wastes and the like to perform thermal decomposition treatment. However, in order to completely reform the tar content in the thermally decomposed gas, it is necessary to maintain the furnace temperature of the reforming furnace at a relatively high temperature (approximately 100.000). The two-temperature air is introduced into the reforming furnace. Therefore, a problem arises in that the heat radiation amount of the refined gas after the upgrading and refining is reduced to about 1,000 kcal / Nm3. In addition, the refined gas in this way will contain 315906 7 200540372 hydrogen for synthesis, and a larger amount of pinane is required. However, because it is difficult to produce a multi-gas containing gas, a synthesis gas containing a large amount of hydrogen is to be produced ^ The gasification system is further improved. An object of the present invention is to provide and manufacture a solid fuel gasification system mainly composed of hydrogen and carbon monoxide. [Summary of the Invention]-A kind of high-heat-synthesis synthetic gas that can omit the coke recycling mechanism
…者為這上述目的’乃經過一番鑽研 ，“ 眼於習知氣化系統中上述粗氣體：者 氮，便針對可製造含氮量較少之合成氣體 研究。結果，本發明者發現藉由_對熱 ^仃 而僅將_。^上的高溫水蒸氣供應給n工乳’ Γ態燃料熱分解，便產生含有較多二之：解Γ 體，便根據此見解而達成本發明。 …解孔 即，本發明固態燃料_介 解，而製造以氫與一氧化碳為主成八:、：：固態燃料熱分 料氣化系統中，其特徵為具備有成刀之&成氣體的固態燃 域）斷絕线供應的熱分解區域（不供應空氣至熱分解區 將熱分解區域的焦炭在辦燒 而產錢燒氣㈣焦_燒區=4存訂進行燃燒， 藉由燃燒氣體與水蒗翕問 的水蒸氣加'«置；’，、、_的熱父換’而將水蒸氣加熱 在上述焦炭燃燒區域與上述水蒸氣加熱裳置之間，淨 315906 8 200540372 化焦炭燃燒區域之燃燒氣體的除塵裝置；以及 · 使從除塵裝置朝水蒸氣加熱裝置送出之除塵後的燃燒、、 氣體進行燃燒，俾造成燃燒氣體溫度上升的燃燒氣體再熱、 用燃燒機構， 上述水蒸氣加熱裝置係具備有利用上述燃燒氣體與上 述水蒸氣間的熱交換，將水蒸氣加熱至6 0 0 °C以上的高溫 水蒸氣之熱交換器，高溫水蒸氣係供應給上述熱分解區 域，而將熱分解區域的固態燃料進行熱分解，俾在熱分解 區域中產生熱分解氣體。 @ 根據本發明之上述構造，固態燃料氣化系統係將焦炭 的燃燒熱當作熱能源，而將水蒸氣加熱至6 0 0 °C以上，再 利用600°C以上的高溫水蒸氣將固態燃料進行熱分解。斷 絕空氣供應的熱分解區域係除固態燃料供應部之外，其餘 均實質地封閉，供應給熱分解區域的熱源流體係實質上僅 由水蒸氣所構成，或者其成分的100%為水蒸氣。在熱分解 區域中將產生未含氮的熱分解氣體，亦將抑制煤份的產 鲁 生。熱分解區域中所殘留的焦炭將在焦炭燃燒區域中焚 燒。焦炭的燃燒熱係以經焦炭燃燒所產生的燃燒氣體為熱 媒體，而供應給水蒸氣加熱用熱交換器，可有效利用為供 水蒸氣加熱用的熱源。焦炭燃燒區域的燃燒氣體乃因為經 由除塵裝置而供應給熱交換器，因此燃燒氣體溫度便抑制 在800°C以下的溫度（除塵裝置淨化部的高溫極限）。但 是，根據本發明，經過淨化步驟的燃燒氣體，將利用燃燒 氣體再熱用燃燒機構進行二次燃燒或再燃燒，而溫度上 9 315906 200540372 -升。經溫度上升的燃燒氣體便在水蒸氣加熱機構中，將水 蒸氣加熱至高溫，高溫水蒸氣便如上述，供應給熱分解區 ，域。在熱分解區域中所產生的熱分解氣體將利用上述高溫 水蒸氣進行改質，而製得以氫與一氧化碳為主成分之較高 散熱量的合成氣體。 所以，根據本發明上述構造，因為焦炭將在焦炭燃燒 區域中進行燃燒，因而可省略焦炭再循環機構。以焦炭的 燃燒熱為熱能源並經加熱的高溫水蒸氣，將供應給斷絕空 * 氣供應的熱分解區域，因為固態燃料僅利用高溫水蒸氣進 行熱分解，因此在熱分解區域中將發生未含氮的熱分解氣 體。熱分解氣體更利用高溫水蒸氣進行改質，如此固態燃 料氣化系統便可製造以氫與一氧化碳為主成分的高散熱量 的合成氣體，並可供應給發電設備、氫製造設備等。 本發明之另一固態燃料氣化系統，係於將熱分解後較 難殘留焦炭的固態燃料進行熱分解，而製造以氫與一氧化 _ 碳為主成分之合成氣體的固態燃料氣化系統中，其特徵為 具備有： 斷絕空氣供應的熱分解區域； 使熱分解區域中經上述固態燃料熱分解而產生的熱分 解氣體，或該熱分解氣體經改質後的精製氣體進行燃燒， 而產生超過1 000°C燃燒氣體的燃燒機構；以及 藉由上述燃燒氣體與水蒸氣間的熱交換，而將上述水 蒸氣加熱的水蒸氣加熱裝置， 上述水蒸氣加熱裝置係具備利用上述燃燒氣體與上述 10 315906 200540372 水蒸氣間的熱交換，將水蒸氣加熱至600°C以上的高溫水 ， 蒸氣之熱交換器，該高溫水蒸氣係供應給上述熱分解區 、， 域，而將熱分解區域的固態燃料進行熱分解，俾在熱分解、 區域中產生熱分解氣體。 根據本發明上述構造，熱分解區域的熱分解氣體、或 熱分解氣體精製後的精製氣體，經利用燃燒機構而進行燃 燒，並產生高溫的燃燒氣體。藉由熱分解氣體或精製氣體 的燃燒所發生的燃燒氣體，便可未經淨化步驟，而直接馬 0 上導入於水蒸氣加熱裝置的熱交換器中。因此，燃燒氣體 的溫度便可設定於超過1000°C的高溫。僅將600°C以上的 高溫水蒸氣，供應給阻絕空氣供應的熱分解區域，結果在 熱分解區域中，便將產生未含氮，且含有較多量氫的熱分 解氣體，亦將抑制煤份的產生。在熱分解區域中所產生的 熱分解氣體經由高溫水蒸氣進行改質，便可製得以氫與一 氧化碳為主成分的較高散熱量的合成氣體。此種構造可使 用於採用燃燒後較難殘留焦炭之固態燃料，如生質燃料的籲 氣化系統。 所以，本發明固態燃料氣化系統係將燃燒後較難殘留 焦炭的固態燃料，僅利用高溫水蒸氣進行熱分解，並利用 熱分解氣體或精製氣體的燃燒，產生超過1 000°C的高溫燃 燒氣體。燃燒氣體係與水蒸氣進行熱交換，而將水蒸氣加 熱至600°C以上的高溫。固態燃料乃因為僅利用高溫水蒸 氣進行熱分解，因此便在熱分解區域中產生未含氮的熱分 解氣體。熱分解氣體更利用高溫水蒸氣進行改質，如此固 11 315906 200540372 料氣化系統便可製造以氫與—氧化碳為主成分的高散 ，1、、里的合成氣體’並可供應給發電設備 '氫製造設備等方 . 面0 【實施方式】 f發明的較佳實施形態中，上述焦炭燃燒區域係形成 '於，炭燃燒爐内。熱分解區域中所殘留的焦炭將被導入於 …从九’、k區域中’焦、炭焚化用的燃燒用$氣將供應給焦炭 燃燒區域。 ☆本發明的另-較佳實施形態，係採用兼用熱分解、焦 炭燃燒用的第1爐與第2爐。第1爐與第2爐分別具備有 熱分解區域兼焦炭燃燒區域作用的爐内區域。設有切換第 ^爐與第2爐運轉的切換機構，切換機構係在將高溫水蒸 氣供應給第1爐，且將燃燒用空氣供應給第2爐的第丨位 置，以及將燃燒用空氣供應給第丨爐，且將高溫水蒸氣供 應給第2爐的第2位置之間進行交替切換。在切換機構的 •第1位置，第1爐的爐内區域即產生熱分解區域的功能， 而第2爐的爐内區域則產生焦炭燃燒區域的功能。在切換 機構的第2位置，第1爐的爐内區域即產生焦炭燃燒區域 的功能’而第2爐的爐内區域則產生熱分解區域的功能。 根據此構造’在固態燃料進行熱分解後，爐床部分上所殘 留的焦炭’將利用燃燒用空氣繼續導入爐内而進行燃燒， 並產生高溫燃燒氣體。所以，便不需要設置焦炭燃燒專用 的焦厌燃燒爐’亦可省略設置從第1爐與第2爐中取出焦 炭’並移送往焦炭燃燒爐的焦炭供應管路。另外，第丨炒 315906 12 200540372 或第2爐係可為在將高溫水蒸氣供應給爐内之前，便將固 態燃料預先投入爐内的批次式（batch type)，亦可為在對、 第1爐或第2爐供應高溫水蒸氣之同時，將固態燃料供應-給爐内的連續供應式。 最好燃燒氣體再熱用燃燒機構係具有將部分合成氣體 及/或燃燒用空氣，添加於淨化後之燃燒氣體中的灌入部， 灌入部係例如由：燃燒氣體配管或風管，與合成氣體或燃 燒用空氣配管或風管的T型連接部所構成，或者由可將燃 燒氣體與合成氣體或燃燒用空氣進行混合的燃燒器所構 成。藉由合成氣體或燃燒用空氣的灌入，燃燒氣體便將再 燃燒或二次燃燒，燃燒氣體之溫度將上升。合成氣體之灌 入最好採取對焦炭燃燒區域供應充分燃燒用空氣的情況 (即，當焦炭在焦炭燃燒區域中實質完全燃燒，燃燒氣體含 較多量氧的情況），燃燒氣體便藉由合成氣體的添加而進行 再燃燒。當限制燃燒用空氣對焦炭燃燒區域之供應量的情 況（即，焦炭在焦炭燃燒區域中不完全燃燒，燃燒氣體含較 多量一氧化碳等的情況）時，燃燒用空氣便供應至灌入部， 再添加於燃燒氣體中。藉由燃燒用空氣的灌入，燃燒氣體 便將二次燃燒，燃燒氣體之溫度上升，而促進燃燒氣體中 的未燃成分之完全燃燒。亦可配合所需而將合成氣體與燃 燒用空氣二者均添加於燃燒氣體中。 本發明較佳實施形態中，氣化系統係具有導入上述熱 分解區域的熱分解氣體與高溫水蒸氣的改質爐，將60(TC 以上（最好900eC以上）的高溫空氣或氧氣，灌入於熱分解 13 315906 200540372 -氣體供應管路或改質爐中。當將氧氣灌入於熱分解氣體供 λ 應管路或改質爐中的情況時，亦可將常溫（相當於大氣的溫 .度）的氧灌入於熱分解氣體供應管路或改質爐中。熱分解氣 體、高溫水蒸氣、及高溫空氣（或氧）係在改質爐内進行混 合，熱分解氣體中的碳化氫（主要為焦油份）便將利用水蒸 氣改質反應，而被改質為以氫與一氧化碳為主成份的改質 氣體（合成氣體）。較佳情況乃改質氣體在後續精製步驟中 進行精製，並以精製氣體供應給發電設備、氫製造裝置等。 * 最好設置在對改質氣體進行精製之前予以冷卻的熱回收裝 置，供應給熱回收裝置的供應水便利用改質氣體的顯熱而 氣化為水蒸氣。此水蒸氣將供應給上述水蒸氣加熱裝置， 便如上述加熱成高溫水蒸氣。最好是部分的精製氣體供應 給空氣加熱裝置，將常溫空氣利用精製氣體的燃燒熱加熱 成上述高溫空氣。 根據本發明另一實施形態，上述高溫水蒸氣係具有 φ 900°C以上的溫度，將熱分解區域中的焦油份產生抑制最小 極限，並省略上述改質步驟。 最好將部分的精製氣體或熱分解氣體當作輔助燃料， 供應給焦炭燃燒區域，不足的焦炭燃燒熱便由精製氣體或 熱分解氣體的燃燒熱進行補充。藉此便將調節焦炭燃燒區 域的燃燒氣體溫度及/或流量，而控制供應給熱分解區域的 高溫水蒸氣溫度及/或流量。變化例亦可將焦炭燃燒區域高 溫化，將焦炭灰燼進行灰熔融。 以下，參照所附圖式，針對本發明較佳實施形態進行 14 315906 200540372 詳細說明。 、 第1圖係本發明第1實施形態之固態燃料氣化系統的、， 方塊流程圖。 - 固態燃料氣化系統係具備有：將產業廢棄物等固態燃 料進行熱分解的熱分解氣化爐；將溫度約100o°c的高溫水 蒸氣供應給熱分解氣化爐的水蒸氣加熱裝置；以及使從熱 分解氣化爐所排放出的焦炭進行燃燒的焦炭燃燒爐。水蒸 氣加熱裝置係利用高溫水蒸氣供應管路HS而連接於熱分 _ 解氣化爐。熱分解氣化爐連接著將固態燃料供應給熱分解 氣化爐的固態燃料供應管路L1，同時亦連接有將熱分解氣 化爐的焦炭供應給焦炭燃燒爐的焦炭供應管路L2。空氣供 應管路L3係連接於焦炭燃燒爐，燃燒氣體送出管路L4則 隔介高溫除塵裝置而連接於水蒸氣加熱裝置。介設於燃燒 氣體送出管路L4的高溫除塵裝置乃例如由可將燃燒氣體 淨化的高溫陶瓷過濾器所構成。空氣供應管路L3的分支管 路L30係在高溫除塵裝置與水蒸氣加熱裝置之間，連接於_ 燃燒氣體送出管路L4。 熱分解氣化爐係經由熱分解氣體供應送出管路L5而 連接於改質爐，改質爐係經由改質氣體供應送出管路L6 而連接於熱回收/氣體精製裝置。熱分解氣化爐的爐内區域 係除在初期時爐内所存在的空氣與氧、及於固態燃料供應 時隨固態燃料一起流入於爐内的少量空氣之外，均阻斷空 氣與氧的供應，對熱分解氣化爐的爐内區域中實質上僅供 應高溫水蒸氣。熱分解氣化爐的熱分解氣體係經由熱分解 15 315906 200540372 ，氣體供應送出管路L5而供應給改質爐，改質爐的改質氣體 -係經由改質氣體供應送出管路L6供應給熱回收/氣體精製 ，裝置。配合所需，部分的熱分解氣體則經由分支管路L9(虛 線所示）供應給焦炭燃燒爐。 熱回收/氣體精製裝置係連接著供水管路SW，同時連 接有水蒸氣供應管路L7上游端。水蒸氣供應管路L7下游 端係連結於水蒸氣加熱裝置。利用熱分解氣體的回收熱所 產生的水蒸氣則經由水蒸氣供應管路L7而供應給水蒸氣 * 加熱裝置。熱回收/氣體精製裝置係經由精製氣體送出管路 L8而連接於發電設備或氫製造設備。熱回收/氣體精製裝 置的精製氣體係當作燃料氣體或原料氣體供應給發電設備 或氫製造設備。精製氣體送出管路L8的第1分支管路L11 係連接於空氣加熱裝置，部分的精製氣體係當作空氣加熱 用燃料供應給空氣加熱裝置。空氣加熱裝置的高溫空氣供 應管路L10連接於熱分解氣體供應送出管路L5，約1000 φ °C的高溫空氣將被灌入於熱分解氣體供應送出管路L5 中。精製氣體送出管路L8的第2分支管路L12係連接於焦 炭燃燒爐。配合所需，部分的精製氣體則作為輔助燃料供 應給焦炭燃燒爐。更從精製氣體送出管路L8分支出第3 分支管路L13，第3分支管路L13下游端係在高温除塵裝 置與水蒸氣加熱裝置之間，連接於燃燒氣體送出管路L4。 將產業廢棄物等固態燃料供應給熱分解氣化爐，並投 入於熱分解氣化爐的爐内區域。系統外的輔助燃料供應設 備（未圖示）係將初期燃燒用燃料供應給焦炭燃燒爐的燃燒 16 315906 200540372 器（burner)設備，空氣供應管路L3所介設的供應風扇便將 ♦ 燃燒用空氣供應給焦炭燃燒爐。配合所需，將燃燒用空氣、， 預熱的空氣預熱裝置（未圖示），設於空氣供應管路L3中-間。藉由焦炭燃燒爐的燃燒動作，溫度約800°C左右的燃 燒氣體便從焦炭燃燒爐輸送給燃燒氣體送出管路L4。燃燒 氣體便經由高溫除塵裝置與燃燒氣體再熱用燃燒機構，供 應給水蒸氣加熱裝置。燃燒氣體再熱用燃燒機構係從系統 外的輔助燃料供應設備（未圖示）供應初期燃燒用燃料。 較低溫的水蒸氣（溫度約150至30(TC左右），係從系 @ 統外的處理蒸氣產生器（未圖示）等初期供應給水蒸氣加熱 裝置，並與焦炭燃燒爐的燃燒氣體進行熱交換，而加熱至 約1000°C左右的高溫。高溫水蒸氣係經由高溫水蒸氣供應 管路HS而供應給熱分解氣化爐。 熱分解氣化爐的爐内區域（熱分解區域）係斷絕空氣的 供應（在無供應空氣之狀態下進行熱分解），僅將水蒸氣加 熱裝置的高溫水蒸氣供應給熱分解氣化爐。從高溫水蒸氣籲 供應管路HS供應給熱分解氣化爐的高溫水蒸氣的溫度（供 應管路HS的出口溫度），設定於如1 000°C。熱分解氣化爐 的爐内壓力係設定於大氣壓（常壓）、或1至2氣壓。熱分 解區域的固態燃料係利用經導入於熱分解氣化爐之爐内的 高溫水蒸氣之熱，進行熱分解，藉由固態燃料的熱分解而 產生溫度約600°C左右的熱分解氣體。利用實質上僅依存 於高溫水蒸氣的固態燃料之熱分解，而在熱分解區域中所 產生的熱分解氣體，係未含氮，且以氫與一氧化碳為主成 17 315906 200540372 . 分，同時具有約600°C左右的溫度之熱分解氣體，僅不過 -含較少量焦油份而已。熱分解氣體便與熱分解氣化爐内的 λ .高溫水蒸氣，一起輸送給熱分解氣體供應送出管路L5。 系統外的輔助燃料供應設備（未圖示）係將初期燃燒用 燃料供應給空氣加熱裝置。空氣加熱裝置係利用燃料的燃 燒熱將相當於大氣溫度的空氣，加熱至約1 000°C的高溫， 將高溫空氣從高溫空氣供應管路L10灌入於熱分解氣體供 應送出管路L5中。高溫空氣的添加乃為彌補下一步驟（改 ® 質步驟）的改質反應所需要的熱，高溫空氣的添加量最好限 制於熱補給所需的最小限度的空氣量。 改質爐係由中空且無觸煤的反應容器所構成。熱分解 氣體供應送出管路L5的熱分解氣體、高溫水蒸氣、及高溫 空氣係灌入於改質爐的爐内區域中，並在改質爐的改質區 域中進行混合，熱分解氣體中的碳化氫（主要為焦油份）之 水蒸氣改質反應（吸熱反應），便在此混合過程中產生。熱 φ 分解氣體係藉由此種改質步驟，被改質為含有較多量氫與 一氧化碳的高卡路里氣體。改質區域乃因為同時進行高溫 空氣與熱分解氣體的放熱反應，因此溫度約800°C的改質 氣體（合成氣體）便供應給改質氣體供應送出管路L6。 改質氣體除含少量的水蒸氣之外，尚含有隨高溫空氣 的添加而供應給系統内的少量的氮。本實施例的變化例係 為防止此種氮的混入現象，亦可取代上述空氣加熱裝置改 為使用氧加熱裝置。此情況下，經氧加熱裝置而預熱的氧， 便從供應管路L10添加給熱分解氣體。變化例乃亦可將相 18 315906 200540372 當於大氣溫度的氧（常溫氧），從供應管路Ll4(虛線所 示），直接添加給熱分解氣體。 改質氣體供應送出管路L6的改質氣體（合成氣體）將 被導入於熱回收/氣體精製裝置中。熱回收/氣體精製裝置 係具備有利用改質氣體與供應水間的熱交換，而產生水蒸 氣的熱回收部，同時亦具備有將熱回收後的改質氣體進行 淨化的淨化部（滌氣器scrubber等）。擁有約800°C左右溫 度的高溫改質氣體，將與供應水進行熱交換而冷卻，供應 水氣化為水蒸氣，並輸送給水蒸氣供應管路L7。改質氣體 更進一步通過淨化部，淨化部則去除改質氣體中的水蒸氣 與固形份等。熱回收/氣體精製裝置的精製氣體便當作燃料 氣體，透過精製氣體送出管路L8供應給發電設備的氣渦輪 引擎（gas turbine engine)等，或者當作原料氣體供應給 氫製造設備。 部分的精製氣體將從第1分支管路Ll 1供應給空氣加 熱裝置。空氣加熱裝置係例如由曰本專利特開2002-158885號公報中所揭構造的空氣加熱裝置所構成。空氣加 熱裝置係將大約為大氣溫度的空氣，利用精製氣體的燃燒 熱加熱至約1 000°C，並供應給高溫空氣供應管路L10。配 合所需，部分的精製氣體則當作焦炭燃燒爐的輔助燃料， 並輸送給第2分支管路L12，然後供應給焦炭燃燒爐。 部分的精製氣體、或部分的空氣供應管路L3的燃燒用 空氣，係在高溫除塵裝置與水蒸氣加熱裝置之間，從分支 管路L13或分支管路L30灌入於燃燒氣體送出管路L4中。 19 315906 200540372 .亦可將精製氣體或燃料用空氣二者均灌入於燃燒氣體送出 ^管路L4中。精製氣體或燃燒用空氣的灌入部，係利用配管 _或風管的T形連接部、或燃燒氣體送出管路L4上所介設的 燃燒器而形成。 應供應給高溫除塵裝置的燃料氣體溫度，乃利用焦炭 燃燒爐的燃燒控制而規範於大約600至800°C左右的溫 度，但是燃燒氣體因為利用精製氣體（L13)及/或燃燒用空 氣（L30)的添加，進行再燃燒或二次燃燒，因此燃燒氣體溫 * 度將上升。所以，經導入水蒸氣加熱裝置中的燃燒氣體便 將擁有超過1000°C的溫度，如1 200°C的溫度。 第2圖與第3圖係表示本實施例中氣化系統之熱源構 造的方塊流程圖及概略構造圖。 在熱分解氣化爐的熱分解氣化反應呈穩定階段，便停 止從系統外的設備所進行的輔助燃料供應及水蒸氣供應。 氣化系統係如第2圖所示，將熱分解氣化爐的焦炭當作水 φ 蒸氣加熱用的熱能源，並切換為平常運轉。如第1圖所示， 在平常運轉時熱分解氣體的改質中所使用的空氣（或氧 氣），將利甩精製氣體的燃燒熱而加熱，供應水將與改質氣 體進行熱交換，而產生要供應給水蒸氣加熱裝置用的水蒸 氣。於是，平常運轉時，供水蒸氣加熱、空氣（或氧氣）加 熱、及供產生水蒸氣用的熱能源，係利用在熱分解氣化爐 1中所產生的焦炭與分解氣化而提供。即，氣化系統係將 熱分解氣化爐1的焦炭與熱分解氣體當作能量源而進行運 轉0 20 315906 200540372 如第3圖所示，熱分解氣化爐i係具備形成教分解區 =爐體:。。在爐體10下端形成有具備多數通氣孔的 爐床12。爐床12較適於採用經穿孔多數通氣孔的陶ή 固定床為佳。高溫水蒸氣供應管路阳與焦炭供應管路= 則連接於爐底部。固體燃料從固態燃料供應管路^ 分解區域η中，並堆積於爐床12上。熱分解氣化^ i ^ 從爐底部供應高溫水蒸氣的固定床式爐，熱分解區域U 乃除爐床上端所配置的固態燃料供應管路L1與敎分解 體供f送出管路L5的開口部之外’其餘部分均㈣。所 以’實質上完全斷絕外界空氣進入熱分解區域U。 水热氣加熱裝置3的高溫水蒸氣係從爐底部朝向上方 於爐内並通過爐床12的通氣孔而接觸於固態燃料 13，俾對固態燃料】3加熱。在阻絕线供應狀態的熱分解 區域11中固態燃料13僅利用高溫水蒸氣的供應而進行 …刀解，並產生熱分解氣體。為求能加速熱分解的反應速 度，最好將水蒸氣溫度設定於1〇〇(rc以上。熱分解區域u 的熱为解氣體與高溫水蒸氣，係流出至爐體上端所連接的 熱分解氣體供應送出管路L5，並供應給改質爐5。在熱分 解，體供應送出管路L5的熱分解氣體與高溫水蒸氣中，添 加而溫空氣供應管路L1〇的高溫空氣（或氧氣）^如虛線所 不，亦可將大約為大氣溫度的氧氣，從供應管路L14添加 於熱分解氣體供應送出管路中。 熱分解氣體、水蒸氣及空氣（或氧氣）將被導入於改質 爐5中’並在改質爐5中進行混合，熱分解氣體中的碳化 315906 200540372 •氫（。主要為焦油份）便被改質。所以，含較多量的氫與一氧 化碳的改質氣體（合成氣體）便輸送給改質氣體供應送出管 -路L6,並供應給熱回收/氣體精製裝置（第}圖）。^質燐5 最好使用如日本專利特開2002_2丨〇444號所揭示構造的*改 質爐。 利^固態燃才斗13的熱分解而所產生的焦炭，係從爐床 的通氣孔巾流下’並經由爐底區域巾所設置焦炭排放口 •=炭供應管路L2，而供應給焦炭燃燒爐卜焦炭燃燒爐 Z係具備有與熱分解氣化爐丨相同的構造。即，焦炭燃燒 、盧係八備有·形成焦炭燃燒區域21的爐體2 〇，以及具 備多數通氣孔的爐床22。爐床22最好使用穿孔有多數通 氣孔的陶究製固定床。空氣供應管㈣係連接於焦炭燃燒 爐2的爐底部，而燃燒氣體送出管路Μ則連接於焦炭燃燒 爐2的爐體上端。 i、應…焦炭燃燒爐2的焦炭，係堆積於爐床22上，空 •氣：應管路L3的燃燒用空氣則通過爐床22的通氣孔，朝 上口人向於焦炭燃燒區域21 0。焦炭燃燒爐2的爐溫利用隹 炭的燃燒而到達超過80(rc的溫度。溫度約6〇〇至8〇〇t& 右的燃燒氣體將輸送給燃燒氣體送出管路u的流通管路 配合所需’亦可將第2分支管路u2的精製氣體或分 支b路L9(虛線所不）的熱分解氣體，輔助性的供應給熱分 解區域11。 、燃燒氣體係通過高溫除塵裝置4,而去除燃燒氣體中 的私塵等。燃燒氣體係從高溫除塵裝置4輸送給流通管路 3】5906 22 200540372 L42。精製氣體及/或燃燒用空氣的灌入部40則連接於流通 管路L42。灌入部40係例如由相對於流通管路L42的分支-管路L13、L30之T形連接部，或連接著分支管路L13、L30 _ 的燃燒器所構成。燃燒氣體將在灌入部40中，與精製氣體 及/或燃燒用空氣進行混合，並進行再燃燒或二次燃燒。 在分支管路L13、L30中設有：控制對灌入部40所進 行精製氣體與燃燒用空氣之供應的控制闊45、46。控制閥 45、46係將精製氣體與燃燒用空氣的流量，控制成在灌入 部40中適當地進行燃燒氣體之再燃燒或二次燃燒的狀 態。例如當焦炭燃燒區域21的焦炭完全燃燒時，因為燃燒 氣體含有較多量的氧，因此控制閥4 5、4 6便主要將分支管 路L13的精製氣體供應給灌入部40。此外，當焦炭燃燒區 域21的焦炭不完全燃燒時，因為燃燒氣體含較多量的一氧 化碳，因此控制閥45、46便主要將分支管路L30的燃燒用 空氣供應給灌入部40。 燃燒氣體便利用灌入部40中的再燃燒或二次燃燒，而 溫度上升達超過1 000°C的高溫，並從流通管路L43供應給 水蒸氣加熱裝置3。燃燒氣體係如前述，將與水蒸氣進行 熱交換俾將水蒸氣加熱至高溫，而本身則將冷卻。冷卻後 的燃燒氣體係經由排氣管路釋放出於大氣中。 水蒸氣加熱裝置3係例如由具較高溫度效率的徑流式 (L jungstrom)熱交換器所構成，將水蒸氣供應管路L7的水 蒸氣加熱至約1 000°C左右的高溫，並輸送給高溫水蒸氣供 應管路HS。水蒸氣加熱裝置3亦可採用具備陶瓷蜂窩結構 23 315906 200540372… For this purpose ', after some research, "looking at the above-mentioned crude gas in the gasification system: Nitrogen, we will study the synthesis gas with a small nitrogen content. As a result, the inventor found that From _ to heat ^ 仃, only the high-temperature water vapor on _. ^ Is supplied to the n-phase milk 'Γ state fuel for thermal decomposition, which results in more than two: dissolve the Γ body, and based on this insight, the invention was made. ... Pore dissolving means that the solid fuel of the present invention _ mediates dissolution, and manufactures mainly hydrogen and carbon monoxide into eight :::: solid fuel thermal split gasification system, which is characterized by having & Solid-state combustion zone) The thermal decomposition zone (not supplying air to the thermal decomposition zone) does not supply air to the thermal decomposition zone. The coke in the thermal decomposition zone is burned and the gas is burned. The burned zone is burned by 4 deposits. The water vapor asks the water vapor and adds '«;; ,,, _'s hot parent to change', and heats the water vapor between the coke burning area and the water vapor heating device, net 315906 8 200540372 chemical coke burning area Dust removal device for combustion gases; and The combustion and gas after the dust removal sent by the dust removal device toward the water vapor heating device are combusted, and the combustion gas that causes the temperature of the combustion gas to rise is reheated, and a combustion mechanism is used. The water vapor heating device is provided with the use of the combustion gas and the water. Heat exchange between vapors, a heat exchanger that heats water vapor to high temperature water vapor above 600 ° C. The high temperature water vapor is supplied to the above thermal decomposition area, and the solid fuel in the thermal decomposition area is thermally decomposed. Thermal decomposition gas is generated in the thermal decomposition area. @ According to the above structure of the present invention, the solid fuel gasification system uses the combustion heat of coke as a thermal energy source, and heats water vapor to more than 600 ° C, and reuses 600 High-temperature water vapor at or above ° C decomposes the solid fuel. The thermal decomposition area that cuts off the air supply is essentially closed except for the solid fuel supply unit. The heat source flow system supplied to the thermal decomposition area is essentially composed of only water. It is composed of steam, or 100% of its composition is water vapor. In the thermal decomposition zone, a thermal decomposition gas that does not contain nitrogen will be generated. The production of coal is produced. The coke remaining in the thermal decomposition zone will be incinerated in the coke combustion zone. The combustion heat of coke is based on the combustion gas generated by the combustion of coke as a heat medium, and it is supplied to the water vapor for heat exchange. It can be effectively used as a heat source for heating the water supply steam. The combustion gas in the coke combustion area is supplied to the heat exchanger through the dust removal device, so the temperature of the combustion gas is kept below 800 ° C (the dust removal device purification section's High temperature limit). However, according to the present invention, the combustion gas after the purification step will use the combustion gas to reheat the combustion mechanism for secondary combustion or recombustion, and the temperature rises to 9 315906 200540372-liter. After the temperature rises, the combustion gas will In the water vapor heating mechanism, the water vapor is heated to a high temperature, and the high temperature water vapor is supplied to the thermal decomposition zone and the region as described above. The thermally decomposed gas generated in the thermally decomposed region will be modified by using the above-mentioned high-temperature water vapor to produce a synthetic gas with high heat dissipation capacity, which is composed mainly of hydrogen and carbon monoxide. Therefore, according to the above configuration of the present invention, since coke will be burned in the coke burning zone, the coke recycling mechanism can be omitted. The high-temperature water vapor that uses the heat of combustion of coke as a thermal energy source and is heated will be supplied to the thermal decomposition area that interrupts the supply of air * gas. Because solid fuel uses only high-temperature water vapor for thermal decomposition, undegraded areas will Thermal decomposition gas containing nitrogen. Pyrolysis gas is further modified with high-temperature water vapor, so that a solid fuel gasification system can produce a high-heat-synthesis synthetic gas containing hydrogen and carbon monoxide as main components, and can be supplied to power generation equipment and hydrogen manufacturing equipment. Another solid fuel gasification system of the present invention is a solid fuel gasification system for thermally decomposing solid fuels which are difficult to retain coke after thermal decomposition to produce a synthesis gas mainly composed of hydrogen and carbon monoxide. It is characterized by having: a thermal decomposition area that cuts off the air supply; and thermal decomposition gas generated by thermal decomposition of the solid fuel in the thermal decomposition area, or the refined gas after the thermal decomposition gas is reformed and burned to produce A combustion mechanism for a combustion gas exceeding 1 000 ° C; and a water vapor heating device for heating said water vapor by heat exchange between said combustion gas and water vapor, said water vapor heating device being provided with said combustion gas and said 10 315906 200540372 Heat exchange between water vapor, heating water vapor to high temperature water above 600 ° C, heat exchanger of steam, this high temperature water vapor is supplied to the above thermal decomposition zone, and The solid fuel undergoes thermal decomposition, and thorium generates thermally decomposed gas in the thermal decomposition, area. According to the above-mentioned structure of the present invention, the thermally decomposed gas in the thermally decomposed region, or the purified gas after the thermally decomposed gas is purified, is burned by a combustion mechanism, and a high-temperature combustion gas is generated. Combustion gas generated by the combustion of thermally decomposed gas or refined gas can be directly introduced into the heat exchanger of the water vapor heating device without purification step. Therefore, the temperature of the combustion gas can be set to a high temperature exceeding 1000 ° C. Only high-temperature water vapor above 600 ° C is supplied to the thermal decomposition area that blocks air supply. As a result, in the thermal decomposition area, thermal decomposition gas that does not contain nitrogen and contains a large amount of hydrogen will also be suppressed. The generation. The thermally decomposed gas generated in the thermally decomposed region is modified by high-temperature water vapor, so that a synthetic gas having a higher heat dissipation capacity, which is composed mainly of hydrogen and carbon monoxide, can be produced. This configuration can be used in a gasification system that uses solid fuels, such as biomass fuels, that are less likely to retain coke after combustion. Therefore, the solid fuel gasification system of the present invention is a solid fuel that is difficult to retain coke after combustion. It only uses high temperature water vapor to perform thermal decomposition, and uses the combustion of thermal decomposition gas or refined gas to generate high temperature combustion exceeding 1 000 ° C. gas. The combustion gas system exchanges heat with water vapor, and heats the water vapor to a high temperature above 600 ° C. Because solid fuel uses only high-temperature water vapor for thermal decomposition, thermal decomposition gas that does not contain nitrogen is generated in the thermal decomposition area. The thermal decomposition gas is further modified by high-temperature water vapor, so that the solid 11 315906 200540372 gasification system can produce high dispersion with hydrogen and carbon oxide as the main components. Equipment 'Hydrogen production equipment, etc. Surface 0 [Embodiment] In a preferred embodiment of the invention f, the coke combustion zone is formed in a carbon combustion furnace. The coke remaining in the thermal decomposition zone will be introduced into the combustion zone of the coke and char incineration of the coke and char from the nine and k zones and supplied to the coke combustion zone. ☆ Another preferred embodiment of the present invention uses the first furnace and the second furnace which are both used for thermal decomposition and coke combustion. The first furnace and the second furnace each have an in-furnace region which functions as a thermal decomposition region and a coke combustion region. A switching mechanism for switching the operation of the second furnace and the second furnace is provided. The switching mechanism is provided at a first position that supplies high-temperature water vapor to the first furnace, and supplies combustion air to the second furnace, and supplies combustion air. The second position is switched to the second furnace, and the high temperature water vapor is supplied to the second furnace. In the first position of the switching mechanism, the area inside the furnace of the first furnace functions as a thermal decomposition area, and the area inside the furnace of the second furnace functions as a coke combustion area. In the second position of the switching mechanism, the function of generating the coke combustion area in the furnace area of the first furnace is generated while the function of the thermal decomposition area is generated in the furnace area of the second furnace. According to this structure, 'after the solid fuel undergoes thermal decomposition, coke remaining on the hearth portion' will continue to be introduced into the furnace using combustion air to be burned, and high-temperature combustion gas will be generated. Therefore, it is not necessary to install a coke burner dedicated to coke combustion, and it is also possible to omit the coke supply line for taking out coke from the first furnace and the second furnace and transferring it to the coke combustion furnace. In addition, the first 315906 12 200540372 or the second furnace system may be a batch type in which solid fuel is pre-charged into the furnace before high-temperature water vapor is supplied to the furnace. The first furnace or the second furnace supplies high-temperature water vapor while supplying solid fuel to the continuous supply type in the furnace. Preferably, the combustion gas reheating combustion mechanism has an injecting section for adding a part of the synthetic gas and / or combustion air to the purified combustion gas. The injecting section is composed of, for example, a combustion gas pipe or an air pipe and a synthetic gas. It may be composed of a combustion air pipe or a T-shaped connection portion of an air duct, or may be composed of a burner capable of mixing a combustion gas with a synthesis gas or combustion air. By injecting synthetic gas or combustion air, the combustion gas will be re-burned or re-burned, and the temperature of the combustion gas will rise. The filling of synthetic gas is best to use the situation where the coke combustion area is supplied with sufficient combustion air (that is, when the coke is substantially completely burned in the coke combustion area, and the combustion gas contains a large amount of oxygen), the combustion gas is passed through the synthesis gas. Re-burning. When the supply of combustion air in the coke combustion area is restricted (ie, incomplete combustion of coke in the coke combustion area, the combustion gas contains a large amount of carbon monoxide, etc.), the combustion air is supplied to the filling section, and then added In combustion gases. By injecting combustion air, the combustion gas will be re-combusted, the temperature of the combustion gas will rise, and the complete combustion of the unburned components in the combustion gas will be promoted. Both the synthesis gas and the combustion air may be added to the combustion gas as required. In a preferred embodiment of the present invention, the gasification system is a reforming furnace having thermal decomposition gas and high-temperature water vapor introduced into the above-mentioned thermal decomposition area, and injecting high-temperature air or oxygen of 60 (TC or above (preferably 900eC or above)) In thermal decomposition 13 315906 200540372-gas supply pipeline or reforming furnace. When oxygen is injected into the thermal decomposition gas supply pipeline or reforming furnace, normal temperature (equivalent to the temperature of the atmosphere) .Degree) of oxygen is injected into the pyrolysis gas supply pipeline or reformer. The pyrolysis gas, high temperature water vapor, and high temperature air (or oxygen) are mixed in the reformer, and the carbonization in the thermal decomposition gas Hydrogen (mainly tar) will be reformed using water vapor, and it will be reformed into a reformed gas (synthetic gas) with hydrogen and carbon monoxide as the main components. The best case is that the reformed gas is carried out in the subsequent purification step. Refined and supplied with refined gas to power generation equipment, hydrogen production equipment, etc. * It is best to install a heat recovery device that cools the reformed gas before refining it, and the water supplied to the heat recovery device is convenient to use. The sensible heat of the gas is vaporized into water vapor. This water vapor will be supplied to the water vapor heating device, which will be heated to high temperature water vapor as described above. It is best to supply a part of the refined gas to the air heating device to use room temperature air. The combustion heat of the refined gas is heated to the above-mentioned high-temperature air. According to another embodiment of the present invention, the above-mentioned high-temperature water vapor system has a temperature of φ 900 ° C or more, and the tar content in the thermal decomposition region is suppressed to the minimum limit, and the above modification is omitted. It is best to supply part of the refined gas or thermal decomposition gas as auxiliary fuel to the coke combustion area, and the insufficient coke combustion heat is supplemented by the combustion heat of the refined gas or thermal decomposition gas. This will adjust the coke. The temperature and / or flow rate of the combustion gas in the combustion area is controlled to control the temperature and / or flow rate of the high-temperature water vapor supplied to the thermal decomposition area. The variation may also increase the temperature of the coke combustion area and ash-melt coke ash. BRIEF DESCRIPTION OF THE DRAWINGS The detailed description of the preferred embodiment of the present invention is 14 315906 200540372. Figure 1 Block diagram of the solid fuel gasification system according to the first embodiment of the present invention.-The solid fuel gasification system is provided with a thermal decomposition gasification furnace that thermally decomposes solid fuels such as industrial waste; the temperature is about 100o. ° C high-temperature water vapor is supplied to a water vapor heating device of a thermal decomposition gasification furnace; and a coke combustion furnace that burns coke discharged from the thermal decomposition gasification furnace. The water vapor heating device uses a high temperature water vapor supply pipe It is connected to the thermal separation _ degasifier by way of HS. The thermal decomposition gasifier is connected to the solid fuel supply line L1 that supplies solid fuel to the thermal decomposition gasifier, and is also connected to the coke supply of the thermal decomposition gasifier. The coke supply line L2 to the coke combustion furnace. The air supply line L3 is connected to the coke combustion furnace, and the combustion gas delivery line L4 is connected to the water vapor heating device through a high-temperature dust removal device. The high-temperature dust removal device interposed in the combustion gas delivery line L4 is constituted by, for example, a high-temperature ceramic filter capable of purifying the combustion gas. The branch line L30 of the air supply line L3 is connected between the high-temperature dust removal device and the water vapor heating device, and is connected to the combustion gas delivery line L4. The pyrolysis gasification furnace is connected to the reforming furnace via a pyrolysis gas supply sending line L5, and the reforming furnace is connected to the heat recovery / gas refining device via a reformed gas supply sending line L6. The furnace area of a thermal decomposition gasification furnace blocks air and oxygen except for the air and oxygen existing in the furnace at the initial stage and a small amount of air that flows into the furnace with the solid fuel when the solid fuel is supplied. Supplying substantially only high-temperature water vapor to the furnace interior area of the thermal decomposition gasifier. The thermal decomposition gas system of the thermal decomposition gasification furnace is supplied to the reforming furnace via thermal decomposition 15 315906 200540372, the gas supply sending line L5, and the reformed gas of the reforming furnace is supplied to the reforming gas supply line L6. Heat recovery / gas refining, installation. As required, part of the pyrolysis gas is supplied to the coke burner via branch line L9 (shown by the dotted line). The heat recovery / gas refining device is connected to the water supply line SW and also connected to the upstream end of the water vapor supply line L7. The downstream end of the water vapor supply line L7 is connected to a water vapor heating device. The water vapor generated by the heat recovered from the pyrolysis gas is supplied to the water vapor * heating device through the water vapor supply line L7. The heat recovery / gas refining device is connected to a power generation facility or a hydrogen manufacturing facility via a refined gas delivery line L8. The refined gas system of the heat recovery / gas refining device is supplied as a fuel gas or a raw material gas to a power generation facility or a hydrogen manufacturing facility. The first branch line L11 of the refined gas delivery line L8 is connected to the air heating device, and a part of the refined gas system is supplied to the air heating device as an air heating fuel. The high-temperature air supply line L10 of the air heating device is connected to the thermally decomposed gas supply and supply line L5. High-temperature air of about 1000 φ ° C will be filled into the thermally decomposed gas supply and supply line L5. The second branch line L12 of the purified gas delivery line L8 is connected to a coke burner. As needed, part of the refined gas is supplied to the coke burner as auxiliary fuel. A third branch line L13 is branched from the purified gas sending line L8, and the downstream end of the third branch line L13 is connected between the high-temperature dust removal device and the water vapor heating device, and is connected to the combustion gas sending line L4. Solid fuels such as industrial waste are supplied to the thermal decomposition gasifier and put into the furnace area of the thermal decomposition gasifier. The auxiliary fuel supply equipment (not shown) outside the system is the combustion equipment that supplies the fuel for initial combustion to the coke burner. The supply fan installed in the air supply line L3 will be used for combustion. Air is supplied to the coke burner. According to the needs, the air for combustion and the preheating air preheating device (not shown) are installed in the middle and middle of the air supply pipe L3. Through the combustion operation of the coke burner, the combustion gas having a temperature of about 800 ° C is sent from the coke burner to the combustion gas delivery line L4. The combustion gas is supplied to a water vapor heating device through a high-temperature dust removal device and a combustion mechanism for reheating the combustion gas. The combustion gas reheating combustion mechanism supplies fuel for initial combustion from an auxiliary fuel supply device (not shown) outside the system. The relatively low-temperature water vapor (temperature of about 150 to 30 (about TC)) is initially supplied to the water vapor heating device from a processing steam generator (not shown) outside the system and heats with the combustion gas of a coke burner. It is heated to a high temperature of about 1000 ° C. The high-temperature water vapor is supplied to the thermal decomposition gasification furnace through the high-temperature water vapor supply pipe HS. The furnace area (thermal decomposition area) of the thermal decomposition gasification furnace is cut off. Air supply (thermal decomposition without air supply), only high-temperature water vapor from the water vapor heating device is supplied to the thermal decomposition gasifier. The high-temperature water vapor supply line HS is supplied to the thermal decomposition gasifier. The temperature of the high-temperature water vapor (the outlet temperature of the supply pipe HS) is set to, for example, 1 000 ° C. The pressure in the furnace of the thermal decomposition gasifier is set to atmospheric pressure (normal pressure), or 1 to 2 pressure. Thermal decomposition The regional solid fuel is thermally decomposed by the heat of high-temperature water vapor introduced into the furnace of the thermal decomposition gasifier, and thermal decomposition of the solid fuel generates thermal decomposition gas at a temperature of about 600 ° C. The thermal decomposition gas generated in the thermal decomposition zone is essentially nitrogen-free, and it is mainly composed of hydrogen and carbon monoxide. It has a temperature of 17 315906 200540372. The thermal decomposition gas at a temperature of about 600 ° C is only-it contains a small amount of tar. The thermal decomposition gas is supplied to the thermal decomposition gas supply and delivery pipeline together with the λ. High temperature water vapor in the thermal decomposition gasification furnace. L5. The auxiliary fuel supply equipment (not shown) outside the system supplies the fuel for initial combustion to the air heating device. The air heating device uses the combustion heat of the fuel to heat the air equivalent to the atmospheric temperature to about 1 000 ° C The high temperature air is poured from the high temperature air supply line L10 into the thermal decomposition gas supply and delivery line L5. The addition of the high temperature air is to compensate for the heat required for the modification reaction in the next step (the modification step). The amount of high-temperature air is preferably limited to the minimum amount of air required for heat replenishment. The reforming furnace is composed of a hollow and non-coal reaction vessel. Thermal decomposition gas The thermal decomposition gas, high-temperature water vapor, and high-temperature air that are supplied to the delivery line L5 are poured into the furnace area of the reformer and mixed in the reformer area of the reformer. The hydrocarbons in the thermal decomposition gas are mixed. The steam reforming reaction (endothermic reaction) (mainly tar) is generated during this mixing process. The thermal φ decomposed gas system is reformed to a high content containing a large amount of hydrogen and carbon monoxide through this reforming step. Calorie gas. The reformed area is because of the exothermic reaction of high temperature air and thermal decomposition gas at the same time, so the reformed gas (synthetic gas) with a temperature of about 800 ° C is supplied to the reformed gas supply delivery line L6. In addition to a small amount of water vapor, it also contains a small amount of nitrogen that is supplied to the system with the addition of high-temperature air. The modification of this embodiment is to prevent such nitrogen mixing, and can also replace the air heating device described above. Use an oxygen heating device. In this case, the oxygen preheated by the oxygen heating device is added to the pyrolysis gas from the supply line L10. In the modification, the phase 18 315906 200540372, which is equivalent to atmospheric temperature oxygen (normal temperature oxygen), may be directly added to the pyrolysis gas from the supply line L14 (shown by a dotted line). The reformed gas (synthetic gas) in the reformed gas supply and delivery line L6 is introduced into the heat recovery / gas refining device. The heat recovery / gas refining device includes a heat recovery unit that generates water vapor by using heat exchange between the reformed gas and the supply water, and also includes a purification unit (cleaning gas) that purifies the reformed gas after heat recovery. Device scrubber, etc.). The high-temperature reformed gas, which has a temperature of about 800 ° C, will be cooled by heat exchange with the supply water, and the supply water will be vaporized into water vapor and sent to the water vapor supply line L7. The reformed gas passes through the purification section, which removes water vapor and solids from the reformed gas. The refined gas of the heat recovery / gas refining device is used as fuel gas, and is supplied to the gas turbine engine of the power generation equipment through the refined gas delivery line L8, or is supplied to the hydrogen manufacturing equipment as raw material gas. Part of the purified gas is supplied from the first branch line L11 to the air heating device. The air heating device is, for example, an air heating device having a structure disclosed in Japanese Patent Application Laid-Open No. 2002-158885. The air heating device heats the air at about atmospheric temperature to about 1,000 ° C by using the combustion heat of the refined gas, and supplies it to the high-temperature air supply line L10. Part of the refined gas is used as auxiliary fuel for the coke burner, and is sent to the second branch line L12, and then supplied to the coke burner. Part of the refined gas or part of the combustion air in the air supply line L3 is between the high-temperature dust removal device and the water vapor heating device, and is injected into the combustion gas delivery line L4 from the branch line L13 or the branch line L30. in. 19 315906 200540372. It is also possible to inject both refined gas or fuel air into the combustion gas delivery pipe L4. The filling portion of the purified gas or the combustion air is formed by using a T-shaped connection portion of a pipe or an air pipe or a burner provided in the combustion gas delivery line L4. The temperature of the fuel gas to be supplied to the high-temperature dust removal device is regulated to a temperature of about 600 to 800 ° C by using the combustion control of a coke burner. However, the combustion gas uses refined gas (L13) and / or combustion air (L30). ) Is added for re-combustion or secondary combustion, so the combustion gas temperature * will increase. Therefore, the combustion gas introduced into the water vapor heating device will have a temperature exceeding 1000 ° C, such as a temperature of 1 200 ° C. Figures 2 and 3 are block flow diagrams and schematic structural diagrams showing the heat source structure of the gasification system in this embodiment. When the thermal decomposition gasification reaction of the thermal decomposition gasifier is stable, the supply of auxiliary fuel and water vapor from equipment outside the system is stopped. As shown in Fig. 2, the gasification system uses coke in a thermal decomposition gasification furnace as heat energy for heating water φ steam, and switches to normal operation. As shown in Figure 1, the air (or oxygen) used in the modification of the thermally decomposed gas during normal operation heats the combustion heat of the refined gas, and the supplied water will exchange heat with the modified gas, and Water vapor is generated to be supplied to the water vapor heating device. Therefore, during normal operation, heating of the water supply steam, heating of air (or oxygen), and heat energy for water vapor generation are provided by using coke and decomposition gasification generated in the thermal decomposition gasifier 1. That is, the gasification system is operated using the coke and thermal decomposition gas of the thermal decomposition gasification furnace 1 as energy sources. 0 20 315906 200540372 As shown in FIG. 3, the thermal decomposition gasification furnace i system is provided with a decomposition zone = Furnace body :. . A hearth 12 having a large number of vent holes is formed at the lower end of the furnace body 10. The hearth 12 is preferably a ceramic fixed bed with perforated holes. High temperature water vapor supply pipe anode and coke supply pipe = are connected to the bottom of the furnace. The solid fuel is decomposed from the solid fuel supply line ^ in the decomposition area η, and is accumulated on the hearth 12. Thermal decomposition gasification ^ i ^ A fixed bed furnace that supplies high-temperature water vapor from the bottom of the furnace. The thermal decomposition zone U is the opening of the solid fuel supply line L1 and the tritium decomposed matter supply f delivery line L5 except the upper end of the hearth Outside of the Ministry 'the rest are sloppy. Therefore, 'substantially completely cut off the outside air from entering the thermal decomposition area U. The high-temperature water vapor of the hydrothermal gas heating device 3 is placed in the furnace from the bottom of the furnace to the upper side and contacts the solid fuel 13 through the vent hole of the hearth 12 to heat the solid fuel] 3. In the thermal decomposition region 11 in the state where the line supply is blocked, the solid fuel 13 is subjected to a ... decomposition using only the supply of high-temperature water vapor, and a thermal decomposition gas is generated. In order to accelerate the reaction rate of thermal decomposition, it is best to set the water vapor temperature to 100 ° C or higher. The heat in the thermal decomposition zone u is the decomposition gas and high-temperature water vapor, which is the thermal decomposition that flows out to the upper end of the furnace. The gas supply is sent out from the line L5 and is supplied to the reforming furnace 5. In the thermal decomposition, the thermally decomposed gas and the high-temperature water vapor of the body supply and delivery line L5 are added to the high-temperature air (or oxygen) of the warm air supply line L10 ) ^ As indicated by the dotted line, oxygen at about atmospheric temperature can also be added from the supply line L14 to the pyrolysis gas supply and delivery line. The pyrolysis gas, water vapor and air (or oxygen) will be introduced into the reformer. In the reforming furnace 5 and mixing in the reforming furnace 5, the carbonization in the thermal decomposition gas 315906 200540372 • Hydrogen (mainly tar) is reformed. Therefore, a reformed gas containing a large amount of hydrogen and carbon monoxide (Synthetic gas) is sent to the reformed gas supply and delivery pipe-L6, and it is supplied to the heat recovery / gas refining device (Figure). ^ Quality 燐 5 It is best to use such as Japanese Patent Laid-Open No. 2002_2 丨 〇444 Reveal structural changes The coke produced by the thermal decomposition of the solid fuel combustor 13 flows down from the vent hole of the hearth and is provided through the coke discharge port provided in the bottom area of the furnace. The coke combustion furnace Z is equipped with the same structure as the pyrolysis gasification furnace. That is, the coke combustion furnace and the Lu system are equipped with a furnace body 20 forming a coke combustion region 21, and have a large number of vent holes. Hearth 22. The hearth 22 is preferably a ceramic fixed bed perforated with a large number of vent holes. The air supply pipe is connected to the bottom of the coke combustion furnace 2, and the combustion gas delivery line M is connected to the coke combustion. The upper end of the furnace body of the furnace 2. i. The coke of the coke burning furnace 2 is deposited on the hearth 22, air and air: the combustion air in the pipeline L3 passes through the vent hole of the hearth 22 and faces upward. The person is facing the coke combustion zone 21 0. The furnace temperature of the coke combustion furnace 2 reaches a temperature of more than 80 (rc) by the combustion of charcoal. The temperature is about 600 to 800 t. The right combustion gas will be delivered to the combustion gas. The flow line of the sending line u can be matched with the required '. 2 The refined gas of branch line u2 or the thermal decomposition gas of branch line B9 (not shown by the dotted line) is supplementarily supplied to the thermal decomposition area 11. The combustion gas system passes the high-temperature dust removal device 4 to remove the private gas in the combustion gas. Dust, etc. The combustion gas system is delivered from the high-temperature dedusting device 4 to the circulation line 3] 5906 22 200540372 L42. The inflow portion 40 of refined gas and / or combustion air is connected to the circulation line L42. It is formed by the T-shaped connection part of the branch-line L13, L30 of the circulation line L42, or the burner connected to the branch lines L13, L30 _. The combustion gas will be in the filling part 40, and the refined gas and / or Combustion air is mixed and recombusted or post-combusted. The branch lines L13 and L30 are provided with control lines 45 and 46 for controlling the supply of the purified gas and the combustion air to the filling portion 40, respectively. The control valves 45 and 46 control the flow rates of the purified gas and the combustion air so that the refilling or secondary combustion of the combustion gas is appropriately performed in the filling portion 40. For example, when the coke in the coke combustion zone 21 is completely burned, since the combustion gas contains a relatively large amount of oxygen, the control valves 4 5 and 4 6 mainly supply the refined gas of the branch pipe L13 to the filling section 40. In addition, when the coke in the coke combustion area 21 is incompletely burned, since the combustion gas contains a large amount of carbon monoxide, the control valves 45 and 46 mainly supply the combustion air of the branch line L30 to the filling portion 40. The combustion gas is facilitated by recombustion or post-combustion in the filling portion 40, and the temperature rises to a high temperature of more than 1,000 ° C, and is supplied to the water vapor heating device 3 from the circulation line L43. The combustion gas system, as previously described, will exchange heat with water vapor, heating the water vapor to a high temperature, and cooling itself. The cooled combustion gas system is released from the atmosphere via the exhaust line. The water vapor heating device 3 is composed of, for example, a L jungstrom heat exchanger with high temperature efficiency, and heats the water vapor in the water vapor supply line L7 to a high temperature of about 1 000 ° C and sends it to High-temperature water vapor supply line HS. Water vapor heating device 3 can also be used with ceramic honeycomb structure 23 315906 200540372
Ceepamie honeycomb structure)等蓄熱體的蓄熱器式熱交 換器，或具備熱傳線圈的復熱器（recuperator)s熱交換 器。此情況下，水蒸氣供應管路L7的水蒸氣便利用經由蓄 熱體而成的燃燒氣體與水蒸氣間的熱交換，或者利用流通 過熱傳線圈的水蒸氣與燃燒氣體間的熱交換，而進行加 熱0 另外，當將焦炭當作燃料的焦炭燃燒爐2產生燃燒量 不足的情況時，部分的熱分解氣體或精製氣體將從分支管 路L9、L12’輔助性的供應給焦炭燃燒爐2的燃燒器設備（未 圖示）。 /第4圖至第7圖係概略地顯示本發明第2實施例的氣 化糸統構造概略方塊流程圖及系統構造圖。 ' 上述第1實施例係氣化系統具備有與熱分解氣化 聯連結的焦炭燃燒爐，但是本實施例的氣化系統則如^ 圖與第5圖所示，具備並聯配置的第"盧與第之爐 爐與第2爐分別兼具熱分解氣化爐與焦炭燃燒爐。 第5圖顯示有交替執行的氣化系統之第丨^驟盥 步驟。在第5圖⑷所示第1步财，第1爐麵化運轅2 第2爐則焦炭燃燒運轉。在第5圖（β)所示第2 +， 1爐係焦炭燃燒運轉，第2爐則氣化運轉。篆也，中第 步驟係依數小時或數十小時的時間單位交替執疒 ” ^ Ζ 在第5圖⑴所示第1步驟中，高溫水蒸氣 1爐。經由第1爐的氣化運轉所產生的熱分解氣顺…、、、°第 改質爐。固態燃料係預先投入於第丨焯中 虱w供應給 皿，或與高溫水基 $ w\ 315906 24 200540372 氣的供應同時連續投入於第丨爐中。 一 2 1爐完成氣化運轉（第5圖（A))後，便執行第5圖（B) 八第v k將燃燒用空氣供應給第1爐。在第2步驟 中’弟1爐的氣化運轉中（第5圖⑴）殘留於第1爐爐床部 分的焦炭藉由燃燒用空氣的供應而進行燃燒，第i爐則當 作焦炭燃燒爐並產生動作，將燃燒氣體輸送給除塵裝置: f除塵裝置除塵過的燃燒氣體，便如同上述第i實施例， 糟由燃燒用空氣及/或精製氣體的添加而進行二次燃燒或 再燃燒，經昇溫後形成高溫燃燒氣體並供應給水蒸氣加熱 裝置。，應給水蒸氣加熱裝置的水蒸氣係與高溫燃燒氣體 進行熱交換，而被加熱至約！刪。c。經加熱後的高溫水蒸 氣則供應給第2爐。第2爐便藉由高溫水蒸氣的供應而將 固悲燃料進行熱分解’並將熱分解氣體供應給改質爐。另 外，固態燃料係預先投入於第2爐中，或者與高溫水蒸氣 的供應同時連續投入於第2爐中。 、 第2爐完成氣化運轉之後，便執行第5圖。）所示第1 步驟。在第i步驟中便將第2爐的氣化運轉中（第5圖⑻） 殘留於第2爐之爐床部分的焦炭，將藉由燃燒用空氣的供 應而進行燃燒’第2爐則當作焦炭燃燒爐並產生動作: 南溫燃燒氣體輸送給除塵裝置。經除塵裝置除塵過的料 氣體，便藉由燃燒用空氣及/或精製氣體的添加而進行：： 燃燒或再燃燒，經昇溫後再供應給水蒸氣加熱I置T 氣係藉由與高溫燃燒氣體間進行熱交換，而被㈣=条 剛t，並供應給第W。第】爐便藉由高溫水蒸、氣的供 315906 25 200540372 應而將固態燃料進行埶分 焯。 丁…刀解亚將熱分解氣體供應給改質 第1步驟（第5圖（A))及笫？牛碰/ ^ ΚΗ士十杳，丄…展弟2步驟(第5圖⑻)係依數 J守或數十小日可的時間間隔交替勃 ^ ^ 同乂 I執仃，弟1爐與第2爐便 虽作熱刀解氣化爐、或焦炭燃燒爐而交替 爐與第2爐係交替發捏.吝&拥八& t 日毛揮·產生熱分解氣體的熱分解氣化爐 作用’與利用爐床部分中所条山 甲所奴召焦厌的燃燒而產生高溫燃 丈兀氣肢的焦炭燃燒爐作用。 /第6圖與第7圖係概略地顯示氣化系統的熱源構造之 系統構造圖。* 6圖係顯示有氣化系統的第i步驟，第7 圖係顯示有氣化系統的第2步驟。 第1與第2爐la、lb係具有實質上與上述第！實施例 之熱分解氣化爐相同的構造’在爐體1〇下端配設有穿透多 數通氣孔的爐床12。固態燃料供應管路Lla、Lib、熱分解 氣體供應f路L5a、L5b、及職氣體送出管路L4a、L4b 係連接於爐體上端。固態燃料供應管路Lla、Lib係經由切 換控制閥VI而連接於固態燃料供應管路u ;熱分解氣體 供應管路L5a、L5b係經由切換控制閥V2而連接於熱分解 氣體供應送出管路L5 ;燃燒氣體送出管路Ua、L4b件經 由切換控制閥V3而連接於燃燒氣體送出管路u。. 空氣供應管路L3a、L3b、及高溫水蒸氣供應管路Has、 HSb係連接於第1爐la與第2爐lb的爐底部。空氣供應 管路L3a、L3b係經由切換控制閥V4而連接於空氣供應管 路L3。高溫水蒸氣供應管路Has、HSb係經由切換控制閥 315906 26 200540372 V5而連接於高溫水蒸氣供應管路hs。 切換控制閥VI至V5係在第6圖所示的第i步驟中， 在第1位置的位置處，將固態燃料供應管路L1、熱分解氣 體供應官路L5、及高溫水蒸氣供應管路連接於第}爐 la，並將空氣供應管路L3與燃燒氣體送出管路u連接於 弟2爐lb。第1爐ia係當作熱分解氣化爐的功能，將經 固態燃料13的熱分解而所產生的熱分解氣體，供應給改質 爐5。第2爐1 b係當作焦炭燃燒爐的功能，將利用爐床部 分的焦炭14燃燒而所產生的燃燒氣體，供應給水蒸氣加熱_ 切換控制閥VI至V5係在第7圖所示的第2步驟中， 在第2位置的位置處，將固態燃料供應管路1卜熱分解氣 體供應送出管路L5、及高溫水蒸氣供應送出管路肋連接 於第2爐lb ’並將空氣供應管路u與燃燒氣體送出管路 ^4連接於第1爐la。第2爐lb##作熱分解氣化爐的功 月匕，將經固態燃们3的熱分解而所產生的熱分解氣體，供 應給改質爐5。第1爐#作焦炭燃燒爐的功能， 用爐床部分的焦炭14燃境而所產生的燃 蒸氣加熱裝置3。 應、，，°水 亦可配合所需從f 2分支管路L12辅助性的對隹户 =的第！或第2爐’供應精製氣體送出管路叫二 :衣就體，而且亦可從分支管路L9輔助性的供應埶分 體供應送出管路L5的部分熱分解氣體。 根據此種實施例，利用氣化運轉，在第1爐la與第 315906 27 200540372 2的爐床部所殘㈣焦炭，便不致移送往爐外的隹炭辦 :二是利用第1爐1a或第2爐^的焦炭燃燒運轉而、 可產，水蒸氣加熱用的高溫燃燒氣體。因： 取出置焦厌燃燒專用的焦炭燃燒爐，對於從爐1中 取出焦厌亚移送往焦炭燃燒爐巾的㈣ 圖），亦可省略此裝置的設置。 ^1 /第8圖與第9圖係概略地顯示本發明第3實施例的氣 化系統構造之方塊流程圖及系統構造圖。 ” :上述第i與第2實施例中，氣化系統係具備有焦炭 …几爐、除塵裝置、及燃燒氣體再熱用燃燒機構，但是本 實施例的氣㈣統則具備有㈣精製氣體與空氣的燃燒反 應，而產生高溫燃燒氣體的燃燒器4〇。在燃燒器4〇中導 入，空氣供應管路L3的燃燒用$氣，與分支管路\13的精 製氣體。燃燒用线係配合所需利用线預熱器（虛線所示） =行，熱。超過looot；之燃燒器4〇的燃燒氣體，將經由 抓通官路L43供應給水蒸氣加熱裝置3。燃燒氣體便如前 述，與水蒸氣進行熱交換而冷卻，並經由排氣管路而釋放 出於大氣中。利用與高溫燃燒氣體間的熱交換而被加熱至 約1000 C的水蒸氣，則供應給熱分解氣化爐丨。供應給熱 刀解氣化爐1的南溫水蒸氣便將固態燃料進行熱分解，熱 分解氣化爐1則將熱分解氣體供應給改質爐5。另外，亦 可將熱分解氣體供應送出管路L5的部分熱分解氣體，從分 支官路L9(第9圖）供應給燃燒器4〇。其他構造，因為實質 上如同上述第1與第2實施例，因此便省略其詳細說明。 28 315906 200540372 本貫施例頗適用於採用如生質燃料（bi⑽ass)之類較 難殘留焦炭的固態燃料之氣化系統。燃燒氣體乃因為利用 精製氣體與空氣的燃燒反應而發生，因此便可在未經淨化 裝置進行淨化的情況下（所以，溫度便無限制），供應給水 瘵氣加熱裝置3。所以，可將超過1〇〇〇的高溫燃燒氣體， 馬上導入於水蒸氣加熱裝置3中。另外，亦可將部分的熱 分解氣體（L9)導入於燃燒器40中，並利用熱分解氣體的燃 燒而產生上述高溫燃燒氣體。 本發明之變化例乃如同上述第2實施例，設置第i掉 與第2爐，形成將第丨與第2爐的熱分解氣體或其精製^ 版選擇性供應給燃燒器4 0的構造。此情況下，氣化系統 的熱源例如在第4圖至第8圖所示構造的氣化系統中Y構 成省略流通管路L4a、L4b、L41、L42、切換閥V3及高溫 除塵裝置4的設置，而從第！與第2爐將分解氣體或其精 製氣體交替供應給燃燒器4〇構造。 雖然，前面之敘述係針對本發明的較佳實施例進行說 明，惟本發明並不僅限於上述實施例，可在申請專利範圍 所載的本發明範圍内進行各種變化或改變。 例如藉由將溫度100(rc以上的高溫水蒸氣供應給熱 分解氣化爐’而將焦油的產生抑制為最小限度，藉此便可 省略改質爐的改質步驟。此外’亦可將投入熱分解區域前 的固態燃料’湘微粉碎處理等前處理步驟進行微粉碎。 此外’在上述第1實施例中’焦炭燃燒後的焚化灰爐將從 焦炭燃燒爐排放出，但是亦可藉由將焦炭燃燒爐的爐溫變 315906 29 200540372 為高溫化，而將焚化灰燼進行灰熔融 -實施射’氣化系統係具備有交替發 = 爐與第2爐，但是亦可在氣化系二二 以上此進行切換運轉的爐。 (產業上可利用性） 如上述所說明，本發明通用於 . 、苽棄物等低質固態燃料 的耽化糸統。本發明固態燃料氣化系統係製造以m 化礙為主成分的高散熱量的合成氣體，可 備、氫製造設備等。 如电口又 【圖式簡單說明】. 第1圖係本發明第1實施例之固態燃料氣化系統整體 構造的方塊流程圖。 τ 粗 圖 第2圖係第丨圖所线化系統之熱㈣造的方塊流程 弟3圖係概略顯示第1圖所+名乂么 系統構造圖。圖…化糸統之熱源構造的 第4圖係本發明第2實施例之固態燃料氣化系統整體 構造的方塊流程圖。 第5圖⑴及⑻係第4圖所示氣化系統之熱 的 方塊流程圖。 第6圖係概略顯示第4圖所示氣化系統之_構㈣ 系統構造圖’顯示有第i與第2爐的第i步驟動作形態。 第7圖係概略顯示第4圖所示氣化系統之熱源構:的 概略系統構造圖’顯示有第！與第2爐的第2步驟動作形 3]5906 30 200540372 態0 構造的第二=明第3實施例之固態機科氣化_ 圖所示氣化系統之熱源構造的 第9圖係概略顯示第 系統方塊圖。 第10圖係習知_氣化系統整體構造的方塊~ 氣 圖’乃例示將固態燃料利用氣化熔融爐而氣化之二 化系統。 虱化之方式的 塊圖 第11圖係第1〇圖所不氣化系統之熱源構造的系統方 第12 ®係習知燃料氣化系統整體構造的方塊流程 =㈣示將固態燃料利用熱分解爐進行熱分解，再將執 刀解氣體利用改質爐進行改質之方式的氣化系统。’、、、 塊圖第13圖係第12圖所示氣化系統之熱源構造的系統方 【主 要元件符號說明】 1 熱分解氣化爐 lb 第2爐 3 水蒸氣加熱裝置 5 改質爐 11 熱分解區域 13 固態燃料 20 爐體 22 爐床 la 第1爐 2 焦炭燃燒爐 4 高溫除塵裝置 10 爐體 12 爐床 14 焦炭 21 焦、炭形成區域 40 灌入部Ceepamie honeycomb structure) and other heat storage type heat exchangers, or recuperators with heat transfer coils. In this case, the water vapor in the water vapor supply line L7 facilitates the heat exchange between the combustion gas and the water vapor through the heat storage body, or the heat exchange between the water vapor and the combustion gas flowing through the heat transfer coil. Heating 0 In addition, when the combustion capacity of the coke combustion furnace 2 using coke as a fuel is insufficient, a part of the pyrolysis gas or refined gas is supplementarily supplied to the coke combustion furnace 2 from the branch lines L9 and L12 '. Burner equipment (not shown). / Figures 4 to 7 are schematic block flow diagrams and system configuration diagrams showing the structure of a gasification system according to the second embodiment of the present invention. '' The above-mentioned first embodiment is a gasification system equipped with a coke combustion furnace connected to thermal decomposition gasification, but the gasification system of this embodiment is shown in Figures 5 and 5, and has a " Lu and No.1 furnaces and No.2 furnaces have both a thermal decomposition gasification furnace and a coke combustion furnace. Figure 5 shows the first step of the gasification system with alternate execution. In the first step shown in Fig. 5 (a), the first furnace surface is operated and the second furnace is operated by coke combustion. As shown in Fig. 5 (β), the coke combustion operation of the 1st and 1st furnace systems, and the gasification operation of the 2nd furnace. Also, the first step of the middle step is performed alternately in units of hours or tens of hours. "^ In the first step shown in Fig. 5 (1), high-temperature steam is used in the first furnace. The gasification operation station of the first furnace passes The thermal decomposition gas produced is in the ... ,,, ° modification furnace. The solid fuel is pre-invested in the supply of dishes, or continuously supplied simultaneously with the supply of high-temperature water-based gas. In the first furnace. After the 21st furnace has completed the gasification operation (fig. 5 (A)), the fifth (b) of the fifth furnace is executed to supply the combustion air to the first furnace. In the second step ' During the gasification operation of the first furnace (figure 5), the coke remaining on the hearth of the first furnace is burned by the supply of combustion air, and the i furnace acts as a coke combustion furnace and operates to burn. The gas is sent to the dust removal device: f The combustion gas that has been dusted by the dust removal device is the same as the i-th embodiment described above, and the secondary combustion or recombustion is performed by the addition of combustion air and / or refined gas. The gas is supplied to the water vapor heating device. The water vapor is exchanged with the high-temperature combustion gas, and is heated to about! C. C. The heated high-temperature water vapor is supplied to the second furnace. The second furnace uses the high-temperature water vapor to supply the solid The fuel is thermally decomposed and the thermally decomposed gas is supplied to the reforming furnace. In addition, the solid fuel is previously charged into the second furnace, or continuously supplied into the second furnace simultaneously with the supply of high-temperature water vapor. The second furnace After the gasification operation is completed, the first step shown in FIG. 5 is performed. In the i step, the gasification operation of the second furnace (figure 5) is left in the hearth portion of the second furnace. Coke will be burned by the supply of combustion air. The second furnace will act as a coke burner and generate action: The South temperature combustion gas is sent to the dust removal device. The material gas that has been dusted by the dust removal device is used for combustion. The addition of air and / or refined gas: Combustion or recombustion, which is heated and then supplied to steam for heating. The T gas system is heat exchanged with the high-temperature combustion gas, and ㈣ = 条 Gang t, and Supply to the W. No.] furnace by high Warm water steam and gas supply 315906 25 200540372 The solid fuel should be decanted. Ding Daoya supplies the thermally decomposed gas to the first step of reforming (Figure 5 (A)) and 笫? 牛牛 / ^ ΚΗ 士 十 杳, 丄 ... The 2 steps of the younger brother (figure 5) are alternated by the time interval of dozens of small guards or dozens of small days ^ ^ With the same leader I, the younger one and the second one Although it is used as a hot knife degassing gasifier or a coke burning furnace, the alternating furnace and the second furnace system are alternately pinched. 吝 & 拥 八 & t Nimochi · The role of a thermal decomposition gasifier that generates thermal decomposition gas and its use The coke-burning furnace function of the high-temperature burning of the limbs of the coke burned in the hearth part by the scorching of the mangosteen. / Figures 6 and 7 show the system structure of the heat source structure of the gasification system. Illustration. * Figure 6 shows the i-th step of the gasification system, and Figure 7 shows the second step of the gasification system. The first and second furnaces la, lb have substantially the same as the above! The same structure of the thermal decomposition and gasification furnace according to the embodiment is provided at the lower end of the furnace body 10 with a hearth 12 penetrating through a large number of vent holes. The solid fuel supply lines Lla, Lib, thermal decomposition gas supply lines L5a, L5b, and the work gas delivery lines L4a, L4b are connected to the upper end of the furnace body. The solid fuel supply lines Lla and Lib are connected to the solid fuel supply line u via the switching control valve VI; the pyrolysis gas supply lines L5a and L5b are connected to the pyrolysis gas supply delivery line L5 via the switching control valve V2. The combustion gas sending line Ua, L4b is connected to the combustion gas sending line u via the switching control valve V3. The air supply lines L3a and L3b and the high-temperature water vapor supply lines Has and HSb are connected to the bottom of the first furnace 1a and the second furnace 1b. The air supply lines L3a and L3b are connected to the air supply line L3 via a switching control valve V4. The high-temperature water vapor supply line Has and HSb are connected to the high-temperature water vapor supply line hs via a switching control valve 315906 26 200540372 V5. The switching control valves VI to V5 are in the i-th step shown in FIG. 6, at the position of the first position, the solid fuel supply line L1, the thermal decomposition gas supply line L5, and the high-temperature water vapor supply line It is connected to the first furnace 1a, and the air supply line L3 and the combustion gas sending line u are connected to the second furnace 1b. The first furnace ia functions as a thermal decomposition gasification furnace, and supplies the thermal decomposition gas generated by the thermal decomposition of the solid fuel 13 to the reforming furnace 5. The second furnace 1 b functions as a coke combustion furnace. The combustion gas generated by the combustion of coke 14 in the hearth is supplied to the steam for heating. The switching control valves VI to V5 are shown in Figure 7 In 2 steps, at the position of the second position, connect the solid fuel supply pipe 1 and the pyrolysis gas supply and delivery pipe L5 and the high-temperature water vapor supply and delivery pipe ribs to the second furnace lb 'and connect the air supply pipe The path u and the combustion gas sending line ^ 4 are connected to the first furnace la. The second furnace lb ## is used as a function of the thermal decomposition gasification furnace, and the thermal decomposition gas generated by the thermal decomposition of the solid-state combustion gas 3 is supplied to the reforming furnace 5. The first furnace # functions as a coke combustion furnace, and the steam heating device 3 is generated by burning the coke 14 in the hearth portion. It should also be compatible with the required water from f 2 branch pipe L12. Or, the second furnace 'supply of refined gas delivery pipeline is called second: clothing, and it can also supply part of the pyrolysis gas from the branch pipeline L9 to the auxiliary supply and separate supply pipeline L5. According to this embodiment, coke residues in the hearth section of the first furnace 1a and 315906 27 200540372 2 are not transferred to the charcoal office outside the furnace by gasification operation. The second is to use the first furnace 1a or High-temperature combustion gas for heating and steam production of coke in the second furnace. Because: Take out the coke burner dedicated to coke combustion, for the coke burner taken out of furnace 1 and transferred to the coke burner (picture), the setting of this device can also be omitted. ^ 1 / Figures 8 and 9 are block diagrams and system configuration diagrams schematically showing the structure of a gasification system according to a third embodiment of the present invention. ": In the above i and second embodiments, the gasification system is equipped with coke ... several furnaces, dust removal devices, and combustion mechanism for reheating the combustion gas, but the gas system in this embodiment is equipped with radon refined gas and Combustion reaction of air to generate high-temperature combustion gas burner 40. Introduced into burner 40, the combustion gas for air supply line L3 is used with the refined gas in branch line \ 13. The combustion line is matched The required preheater (shown by the dotted line) = line, heat. Over looot; the combustion gas of the burner 40 will be supplied to the steam heating device 3 through the grabbing official road L43. The combustion gas is as described above, and Water vapor is cooled by heat exchange, and released from the atmosphere through the exhaust pipe. Water vapor heated to about 1000 C by heat exchange with high-temperature combustion gas is supplied to the thermal decomposition gasification furnace 丨The south temperature water vapor supplied to the thermal knife gasification furnace 1 thermally decomposes the solid fuel, and the thermal decomposition gasification furnace 1 supplies the thermal decomposition gas to the reforming furnace 5. In addition, the thermal decomposition gas can also be sent out. Section of pipeline L5 The decomposed gas is supplied to the burner 4 from the branch road L9 (Fig. 9). Since other structures are substantially the same as the first and second embodiments described above, detailed descriptions thereof are omitted. 28 315906 200540372 It is suitable for gasification systems that use solid fuels such as biofuel (bi⑽ass) which are difficult to retain coke. Combustion gas occurs because of the combustion reaction between refined gas and air, so it can be purified without purification equipment In the case (so the temperature is unlimited), it is supplied to the water radon heating device 3. Therefore, high-temperature combustion gas exceeding 10,000 can be immediately introduced into the water vapor heating device 3. In addition, some The thermally decomposed gas (L9) is introduced into the burner 40, and the high-temperature combustion gas is generated by the combustion of the thermally decomposed gas. A modification of the present invention is the same as the second embodiment described above. A structure is formed in which the pyrolysis gas of the first and second furnaces or the refined version thereof is selectively supplied to the burner 40. In this case, the heat source of the gasification system is shown in, for example, FIGS. 4 to 8 In the gasification system of the structure shown in the figure, the arrangement of the flow lines L4a, L4b, L41, L42, the switching valve V3, and the high-temperature dust removal device 4 is omitted, and the decomposed gas or the refined gas is alternately supplied from the first and second furnaces to The structure of the burner 40. Although the foregoing description is directed to the preferred embodiments of the present invention, the present invention is not limited to the above embodiments, and various changes or modifications can be made within the scope of the present invention as contained in the scope of the patent application For example, by supplying high-temperature water vapor at a temperature of 100 ° C. or higher to a thermal decomposition gasification furnace ', the production of tar is suppressed to a minimum, and the reforming step of the reforming furnace can be omitted. In addition, Pre-treatment steps, such as the solid fuel 'Xiang micro-pulverization process' before entering the thermal decomposition zone, perform micro-pulverization. In addition, in the above-mentioned first embodiment, the incineration ash furnace after coke combustion will be discharged from the coke combustion furnace, but the temperature of the coke combustion furnace may be changed by increasing the temperature of the coke combustion furnace by 315906 29 200540372 to increase the incineration ash. The ash melting-injection gasification system is provided with a furnace that alternates with a second furnace and a second furnace, but it is also possible to switch between two or more furnaces in the gasification system. (Industrial Applicability) As described above, the present invention is commonly used in a low-quality solid fuel system such as waste and waste. The solid fuel gasification system of the present invention is a synthetic gas with high heat dissipation capacity, which is mainly composed of hydrogenation inhibitors, and can be used as a hydrogen production facility. Such as the electrical port and the diagram. Brief description. Figure 1 is a block flow diagram of the overall structure of the solid fuel gasification system according to the first embodiment of the present invention. τ Coarse Figure 2 is the block diagram of the thermal fabrication of the linearized system shown in Figure 丨 Figure 3 is a schematic diagram showing the structure of the system shown in Figure 1. Fig. 4 is a block flow diagram of the overall structure of a solid fuel gasification system according to the second embodiment of the present invention. Figures 5 and 5 are block flow diagrams of the heat of the gasification system shown in Figure 4. Fig. 6 is a schematic view showing the structure of the gasification system shown in Fig. 4. Fig. 6 shows the operation pattern of the i-th step and the i-th step of the second furnace. Fig. 7 is a schematic diagram showing the heat source structure of the gasification system shown in Fig. 4: The second step of operation with the second furnace 3] 5906 30 200540372 State 0 structure of the second = solid state machine gasification of the third embodiment _ Figure 9 shows the heat source structure of the gasification system shown in the figure Block diagram of the system. Fig. 10 is a block diagram of the conventional structure of the gasification system ~ gas. The gas diagram 'is an example of a gasification system that uses a gasification melting furnace to solidify solid fuel. Block diagram of lice formation method Figure 11 shows the heat source structure of the non-gasification system shown in Figure 10. The 12th series is the block flow of the overall structure of a conventional fuel gasification system = shows the thermal decomposition of solid fuels The furnace is thermally decomposed, and the gasification system in which the decomposed gas is modified by a reforming furnace is used. ',,, block diagram. Figure 13 is the system side of the heat source structure of the gasification system shown in Figure 12. [Description of the main component symbols] 1 Thermal decomposition gasifier lb Second furnace 3 Water vapor heating device 5 Modification furnace 11 Thermal decomposition zone 13 Solid fuel 20 Furnace body 22 Furnace la 1st furnace 2 Coke burning furnace 4 High-temperature dust removal device 10 Furnace body 12 Furnace 14 Coke 21 Coke and char formation area 40 Filling section
3]5906 31 200540372 40 燃燒器 45 控制閥 46 控制閥 HS、 Has、HSb高溫水蒸氣供應管路 LI、 Lla、Lib固態燃料供應管路 L2 焦炭供應管路 L3、L3a、L3b空氣供應管路 L4、 L4a、L4b燃燒氣體送出管路 L5、 L5a、L5b熱分解氣體供應送 出管路 L6 改質氣體供應送出 管路 L7 水蒸氣供應管路 L8 精製氣體送出管路 L9 分支管路 L10 高溫空氣供應管路 Lll 第1分支管路 L12 第2分支管路 L13 第3分支管路 L14 供應管路 L30 分支管路 L4卜 L42、L43流通管路 SW 供水管路 VI、V2、V3、V4、V5切換控制閥3] 5906 31 200540372 40 Burner 45 Control valve 46 Control valve HS, Has, HSb High temperature water vapor supply line LI, Lla, Lib Solid fuel supply line L2 Coke supply line L3, L3a, L3b Air supply line L4 , L4a, L4b Combustion gas delivery line L5, L5a, L5b Thermal decomposition gas supply delivery line L6 Modified gas supply delivery line L7 Water vapor supply line L8 Refined gas delivery line L9 Branch line L10 High temperature air supply line Line Lll 1st branch line L12 2nd branch line L13 3rd branch line L14 Supply line L30 Branch line L4, L42, L43 Circulation line SW Water supply line VI, V2, V3, V4, V5 switching control valve
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