200923065 九、發明說明 【發明所屬之技術領域】 本發明有關一用於生產及冷卻諸如由固 氣化所獲得之氣體的方法及裝置，藉此以帶 氣之氣化劑的輔助在壓力之下加熱該等氣體 【先前技術】 當固態、像粉塵或微粒燃料材料係以帶 氣的氣化劑或反應氣體之輔助被加熱時，視 得一氣態之氣化產品，該產品本質上具有合 包含液體成份、諸如灰燼或熔渣。此固體氣 行爲一火燄反應。煤係頻繁地使用之進料， 生物燃料材料作爲進料係亦合適的。所使用 部份被轉換，且所伴隨獲得之固態物質、諸 灰僅只包含一微小部份之無氣化碳。所產生 被純化，且如此變得適於各種應用。該產品 於合成之產品。 該氣化反應本身發生在超過該灰燼之固 該等製程之典型反應控制使用由攝氏1200 3 度範圍及由〇 · 3至7.0百萬帕的壓力。熔渣 面分開及往這些壁面下方流動。該微粒灰燼 該產品氣體離開該反應器。 於大部份案例中，該反應室被設計爲一 且配備有用於餵入該燃料材料及該反應氣體 態燃料材料的 有氧氣及水蒸 有氧氣或水蒸 該進料而定獲 成氣體特色及 化作用主要進 但石油煤焦或 之燃料進料大 如熔渣或煙道 之產品氣體能 氣體係特別適 化點的溫度。 i 2500度之溫 在該反應器壁 的一部份隨同 圓柱形房間’ 之裝置。該圓 -4 - 200923065 柱形燃燒室通常被安裝在一壓力密封的殻容器中，使用特 定零組件供懸掛或支撐該室。該殼容器亦容納配置毗連該 氣化反應器之所謂混合或淬冷管，並可設有加熱或冷卻裝 置。 此型式之幾乎每一氣化製程的共通特色爲：該氣態的 氣化產品在該氣化之後被送至一混合或淬冷管，藉此與一 導入的氣體或液體混合，以致該產品能夠充分地消耗其高 內能，亦被稱爲“淬冷”之製程。在此製程之發展中，該氣 態之氣化產品被冷卻至一較低溫度，以致被該細微地分佈 熔體所夾帶之成份的一部份沉澱，並可由該產品氣體分開 。該氣化產品自該反應器經由該淬冷管之抽出能於一向上 或往下流束中被施行。 不論何時選擇該向上流束之選擇方案，其係相當易於 由該反應氣體分開該等夾帶之液體成份。僅只包含細顆粒 熔渣微粒之排出氣體係在離開該反應器之後與淬冷氣體混 合，以致該熔渣微粒固化及能在下游設備中由該氣體分開 〇 文件DE91 1313敘述一用於固態燃料材料之氣化的裝 置，該氣化反應本身在一特別之反應器中發生，該反應器 之形狀像一置於耐火磚結構的系統中之球形或梨子形反應 器。該氣化劑係經由橫側地配置之噴嘴注射，且該燃料材 料係藉著螺旋輸送器餵入至該反應器。所產生之產品氣體 係在一向上流束中經由一設有冷卻夾套及用於該冷卻或淬 冷氣體之餵入裝置的管子排出。該熔渣的一部份係經過一 -5- 200923065 位在該反應器的下側面上之開口排出。 文件EP400740 A1敘述一氣化反應器，其設計有長度 與直徑之特別比率，並以燃燒器在一切線角度燃燒。此配 置允許所獲得之煙道灰數量的減少。該反應器之上側面係 設有一用於該產品氣體之直立向上排出流束的管子。該反 應器之下側面具有一用於特別是呈溶融熔渣形式的液態氣 化產品之出口。 文件US 544 1 5 47詳細指明一用於固態燃料材料之氣化 的裝置，該氣化反應本身在一圓柱形反應器中發生。該反 應器使用特定之附接件被安裝在一專業殼容器中。此殼型 容器之設計通常亦在該外部側面限定本發明中所界定之裝 置。該產品氣體係經由一出口排出，且於一直立向上之流 束中送經一配備有用於淬冷或冷卻氣體而直接在該出口上 方的餵入裝置之管子。 設有用於該產品氣體的一向上排出流束之裝置的任何 反應器具有該缺點，即需要設有一相當大的高度之設備的 零件，因爲與該淬冷劑之良好混合需要一長氣道，且這涉 及一相當大危險之熔渣固化。該反轉總是發生在該淬冷製 程之後，以便預防由於黏黏的灰燼微粒而形成沈積物。如 此獲得之原料氣體藉著適當之熱交換器、過濾器或洗滌器 遭受進一步處理。 於一用於由該反應器移去該產品氣體的往下流束之案 例中，該氣態之氣化產品係由該氣化器經過一配置在該反 應器之下部的淬冷管直立地排出。此設計確保藉由淬冷所 -6 - 200923065 獲得之熔渣藉由重力往下掉落進入該熔渣池。該已冷卻的 氣體可藉由適當之導件或反轉機構在該熔渣池之上游反轉 ，以便允許使用適當的熱交換或淨氣裝置進一步處理所產 生之原料氣體。 文件DE400 1 739 A1敘述一用於固態燃料材料之氣化 的裝置，該氣化產品於一直立往下之流束中離開該反應器 。在該氣體離開該反應器之後，同心地配置之噴嘴被用於 以一徑向方式噴灑具有水之熱的及裝滿粉塵之氣體流束， 使得該固態之氣化產品被限制，且該氣體流束被同時冷卻 。該氣體隨後於一寬廣的圓柱形攪拌器中釋放粗粒的固態 成份，且經由導引板被送出供進一步處理。該粗粒的固體 係自該系統經由一鎖閘單元移去。 文件US4494963詳細指明一用於固態燃料材料之氣化 的裝置，該氣化產品於一直立往下之流束中離開該反應器 ，且以此一可使所夾帶之粗粒的固體被同時地移去之方式 ，在該連續之接觸區中藉由與一冷卻劑之熱交換被淬冷。 用於運送該淬冷氣體及產品氣體之管子經由一密封圓錐體 排出進入一含有冷卻劑之容器，其中該淬冷氣體釋放固體 及被進一步冷卻。 設有用於在往下氣體流束中排出該產品氣體之內部零 件的任何反應器具有該缺點，即以此型式之反應控制，該 熔渣輕易地造成由該反應器至該下游設備的管線中之浮渣 或阻塞，因爲該熔渣亦包含粗粒的熔渣微粒’其僅只慢慢 地固化，且其黏黏之表面係藉由亂流與反轉移向該等壁面 200923065 。其通常係需要對於寬廣之混合室及管線或設備提供相當 大之高度，以便預防不想要之沈積物的形成。該習知之具 有往下氣體排放的氣化廠需要一與那些具有向上排出流束 者類似之高起部份，因爲氣化、淬冷、及熔渣移除之區域 具有一類似之高度，且因爲僅只堆疊它們之順序係不同的 【發明內容】 因此，本發明之目的係提供一適合以淬冷氣體之輔助 將氣化製程之氣態產品冷卻至較低溫度的簡單裝置。該分 開之固態反應產品必需可被由該製程輕易地移除及處理， 使得該反應控制線由於沈積物或浮渣之阻塞被避免。一不 複雜的設計型式被指定，但其仍必需確保該產品氣體之純 化及冷卻被最佳化。再者，其被指定該裝置必需具有一低 於該傳統設備之高度。 本發明之目的被一用於煤氣化之裝置所達成，以一本 質上往下流束之輔助，該裝置允許該氣態之裝滿粉塵氣化 產品與淬冷氣體於一直立管子降流管中之混合。該熔渣的 一主要部份業已由於一特別之反應器設計在該反應器側壁 上被分開。按照本發明之反應器裝置係設有用於熔渣排出 之分開的橫側出口，該出口同時被用於移去業已在該反應 器中分開的固體，以便確保於一以水充塡的裝置中之冷卻 ，且隨後由該容器移除。爲了保護該壓力容器頂抗該熔渣 之高溫，位在此出口下邊之氣室被一保護屏蔽板所完全地 -8- 200923065 包圍，該屏蔽板可爲多層型式及設計成一被冷卻的薄膜壁 面。該產品氣體係經由第二出口開口分開地排出及運送於 一排出管中，用於使其與淬冷氣體混合。 根據一在本發明指定之裝置，用於產品氣體之出口開 口係在該反應器之內部側面上配備有一軸環形或漏斗形凹 部，以便避免該液態熔渣之排入該氣體排出管。爲了避免 熔渣層之形成於該凹部中，該凹部之下部可設有一陶瓷覆 層或藉由陶瓷塡塞劑化合物所覆蓋之栓銷。一用於餵入該 淬冷劑之裝置係位在該產品氣體進入該混合管子之入口後 方。藉由分開地排出該等液態氣化產品及該產品氣體，離 開該反應器的氣體流束中所包含之熔渣微粒數量係實質上 減少。此方法有利於該氣體之冷卻及由該氣體移除粉塵， 且大幅地減少該混合管子之積垢趨勢。 根據本發明的一具體實施例，用於排出該液態熔渣之 出口開口排入一以水充塡及用於冷卻該熔渣之裝置。該熔 渣可經由一適當之鎖閘被減壓及由以水充塡之裝置、因此 由該製程本身回收。當作一選擇，一額外之燃燒器能被設 在該熔渣排出裝置上方，以便再次液化已經開始固化的熔 渣。 該申請專利之目的係特別一用於固態、粉狀或微粒燃 料材料在壓力之下氣化的方法，並以下列技術之細節爲其 特色： •所使用之燃料材料係在攝氏12〇0度至攝氏2500度 之溫度及〇_3至7.0百萬帕（Mpa)的壓力氣化，並於已 200923065 冷卻的氣化反應器中以一帶有氧氣或水蒸氣之介皙輔助， 及 •所獲得之氣態的氣化產品係自該氣化器經由一分開 之收集裝置及開口排出’且所獲得之液態及固態的氣化產 品經由一分開之收集裝置及開口排出，及 •所獲得之液態的氣化產品係傳送至一以水充遁之裝 置，且隨後經由減壓裝置移去，及 ♦所獲得之氣態的氣化產品係以一本質上直立之往下 流束的輔助由該反應器移去，及 •該氣態的反應產品被由該反應器送至一混合或淬冷 管’在其中該等反應產品係與一導入的介質混合，以消耗 其高內能及如此遭受一冷卻。 按照本發明的一具體實施例，所使用之燃料材料係微 粒或像粉塵般一致性之煤。該燃料材料微粒之粒徑較佳地 係< 0 · 5毫米。 於本發明的另一具體實施例中，所使用之燃料進料係 微粒或像粉塵般一致性之生物材料。該燃料材料之粒徑較 佳地係< 0.5毫米。 於本發明之另一具體實施例中，所使用之燃料進料係 有機材料、諸如微粒或顆粒型式之塑膠或石油煤焦。該燃 料材料之粒徑較佳地係< 0 · 5毫米。 再者，該申請專利之目的係一適用於本發明中所指定 之方法的性能之裝置，且以下列之特色爲其特徵： •該裝置包括一圓柱形或橢圓形之反應器容器，及 -10- 200923065 •該反應器容器係設有一分開之收集裝置及開口，用 於液態與固態的氣化產品之排出，及 •一空間係位於毗連該開口，且適用於排出操作，而 允許液態與固態的氣化產品之移除； •一裝置係位在用於排出液態與固態的氣化產品之空 間的底部下方，該空間能被以水充塡或用作對於另一具有 水存量之裝置的調節附件，使得該液態與固態之氣化產品 能被送進此水槽，及 •一用於移去該等產品之裝置係位在具有水存量而用 於液態與固態的氣化產品的裝置之下方，及 •該氣化燃料材料及該反應氣體係藉著橫側地附接至 該反應器之至少二燃燒器、或一安裝於該頂板中之燃燒器 的其中之一餵入，及 •該等橫側燃燒器之開口水平地指向進入該燃燒器室 、或在〇度至45度之角度往上或在0度至10度之角度正 割地進入該燃燒器室，及 •該反應容器具有一分開之開口及收集裝置，用於排 出該氣態的氣化產品，一淬冷房係於一直立及本質地往下 方向中坐落毗連該反應容器，及 •用於導入的介質之餵入裝置係附接至該淬冷房，該 淬冷房係亦配備有特別之器械，以由該外側提供冷卻，及 •該反應器容器被一壓力密封的殼體所封閉，該殼體 因此形成該整個結構之分界。 根據本發明中所指定之裝置的反應容器本身較佳地係 -11 - 200923065 呈圓柱形設計，但亦能以橢圓形之方式設計其形狀，以改 善結構之型式。一被採用於按照本發明的方法之反應器通 常係配備有至少二燃燒器，雖然其亦能以單一燃燒器操作 。該等燃燒器藉由餵入反應氣體及經硏磨之燃料材料加熱 該反應器，該等燃燒器被橫側地安裝或於該反應器之頂板 中。於橫側地安裝燃燒器之案例中，其有利的是藉由附接 至該容器殼體之特定緊固件支撐它們。再者，該等橫側地 安裝之燃燒器允許一朝向該燃燒室之水平方位、或一在0 度至45度之角度的向上方位、或以正割方式在0度至10 度之角度。 爲了改善該氣化反應及燃燒器控制，其係可能以一渦 漩提供該等反應配搭物，特別是該燃燒氣體。於頂板安裝 式燃燒器之案例中，小導引板能被安裝在該燃燒器出口或 、用於此目的安裝特別設計之燃燒器。 視設計之型式而定，該燃料材料能被不同方法餵入至 該反應器。如此，譬如，該像粉塵之燃料材料可經由一分 開之餵入管子及該燃燒器輸送進入該反應器。然而，其係 亦可能經過該容器頂板中之分開的開口將該燃料材料餵入 至該反應器。在該開口提供一適當之輸送帶係特別有益的 ，以致此輸送帶能將該進料推經該開口進入該反應器。譬 如一螺旋輸送帶係很好地適用於此目的。此韻入方法係特 別適用於未能以粉塵形式方便地餵入至該反應器的進料， 塑膠材料或有機污染物典型用於此標準。 按照本發明的一具體實施例，提供該反應器內部壁面 -12- 200923065 之冷卻。通常，該反應器容器之內部壁面具有覆蓋著陶瓷 化合物之金屬栓銷。其係亦可能以沸水噴灑該反應器內部 壁面。該等燃料材料較佳地係以微粒或像粉塵般一致性之 形式餵入。帶有氧氣或水蒸氣之反應氣體係經由橫側地安 裝或於該反應容器的頂板中之燃燒器餵入。純氧亦可被用 作反應氣體。該氣化反應通常在大量之粉塵中發生。 按照本發明之另一具體實施例，該產品氣體中所包含 之熔渣係在離開該氣化器之後藉由該淬冷方法被冷卻，且 如此固化。各種氣體係適合當作淬冷氣體，該較佳之淬冷 氣體係被冷卻的產品氣體、水蒸氣、氮氣或惰性氣體、或 這些氣體之混合物。一液態淬冷劑、諸如由該製程返回之 水係同樣適合的。該淬冷管之長度通常視該反應器尺寸而 定。該隨後之大約値應用於：該管子中之最上方淬冷氣體 餵入點與該反應器底部間之距離應爲比該反應器直徑小 1 0 X ° 不論何時該熱產品氣體會合該淬冷劑，該氣體藉由消 耗能量傳送之方法遭受一主要冷卻。此製程被連結至一夾 帶液態氣化產品之固化。爲了改善精確的混合，該淬冷管 能設有一或數個漏斗形頸縮部，該等頸縮部造成該混合管 子之較小直徑。另一選擇係使該淬冷管設有用於此目的之 內部裝置，以致該氣體流束遭受一漏斗型集束。該等內部 裝置可爲譬如一環狀之金屬裙部或一環型陶瓷孔口板。此 方法有利於與該淬冷劑混合及該夾帶液態氣化產品之固化 作用。爲了保護該淬冷房之壁面頂抗液態微粒，其方便的 -13- 200923065 是提供用於沿著該淬冷房注射該淬冷劑之數個位準。 用於該產品氣體之進一步冷卻，一液態冷卻劑能被注 射進入該氣體流束。其被推薦該冷卻劑係在該漏斗形頸縮 部之上方注射，而呈一平行於該漏斗表面之平坦噴流。在 該漏斗形頸縮部下方待餵入之液態冷卻劑應如平行於該產 品氣體流束之噴灑流束般被注射。於此案例中，沿著該淬 冷房之冷卻劑注射可同樣地發生在數個位準。 按照本發明的一具體實施例，一裝置係配置在該混合 管子之下方，且包含水或係適合用於容納一具有水存量之 裝置，該裝置被設計成可收集在該產品氣體中之淬冷處理 期間所固化之固態成份的一部份，藉由該重力或慣性效應 發生該傳送。在有需要時，在具有水存量的裝置中所獲得 之固態成份或帶有水之固體能藉著幫浦由該製程回收。 於本發明之另一具體實施例中，在具有水存量的裝置 上方之空間被用於安裝一出口管子，用於排出該被淨化之 產品氣體及用於該氣體反轉及進一步運送。於此階段中， 該氣體僅只包含微小粒徑之固態顆粒。該氣體流束之反轉 及進一步運送由該淬冷房開始，使用較佳地配置在>90度 之角度的一或數個管子。選擇性地，應用於該產品氣體反 轉管之角度可被設計爲較小的，但於此案例中，如此運送 之產品氣體的固體濃度將稍微增加。一分類器可被安裝在 該淬冷房中，以移去較粗的固體，特別是在排放進入具有 水存量之裝置的端部之上游。此一裝置之安裝，於此案例 中，一用於射流之反轉的分類器譬如允許由該淬冷房移除 -14- 200923065 較粗的熔渣或灰燼微粒。 本發明之另一具體實施例 管在該反轉區段之下游運送該 冷卻及純化。爲了由該產品氣 區段能在該反轉點或於其附近 如除霧器或柵板塔盤。 於離開該系統時，較佳地 氣體之進一步冷卻及純化。該 成水之局部蒸發，這增加該已 量。此程序時常包括洗滌器之 滌器以噴灑或噴澆於該氣體上 卻。此方法減少該氣體溫度， 雜質及可溶解於水中之液態或 在純化及冷卻之後，離開 氧化、毒性氣體（C 0 S、C ◦、 或酸或鹼性、腐触氣體（HC1 爲了改善該製程之能量產出， 器出口之下游分出爲該氣化流 。該部分流束能在該氣化器出 交換器。此製程較佳地係在該 免該熱交換器操作由於夾帶熔 當作一選擇，其係可能於 水蒸氣或C〇2至該製程。視該 想要的產品氣體中之產量改良 提供用於一排出管，該排出 產品氣體至一系統供進一步 體移去雜質，該管子之反轉 配備有一微滴分離單元、例 是藉由與水混合施行該產品 氣體與水之直接冷卻同時造 冷卻的氣化產品之水蒸氣含 使用，於逆流流動中，該洗 之水的輔助提供用於氣體冷 且該氣體係同時地釋放固體 氣態物質。 該系統之氣體流束能遭受可 HCN )的一催化轉換，及/ ' NH3、H2S )之吸附作用。 至少一部分流束可在該氣化 束，且被餵入至一熱交換器 口下游之任何點被送經該熱 淬冷製程之後進行，以便避 渣之任何干擾。 起動期間餵入一氣體、諸如 製程控制而定，此方法允許 、或有利於該氣化反應控制 -15- 200923065 爲了允許規則之檢查及有利於該反應器系統之維護， 該反應器容器及該氣密殼體結構間之環狀空間係特別的， 而可經由人孔進出該空間。用於此目的’該上托盤及在該 氣化器底部下邊的壓力容器之橫側壁面係設有人孔。該反 應容器可同樣地配備有人孔，以允許接近至該空間。 諸如本發明中所主張之設計型式具有該優點：即其可 能以一簡單之方式由該氣態之反應產品分開該固體。因此 ，本發明中所指定之設計與最新式技術的比較顯示其製成 該結構係較便宜，且所產生之產品氣體的淨化係更有效率 。與最新式技術一致所製成之設備比較，在本發明中所指 定之裝置清楚地允許較小高度之設備項目。 此用於氣化固態燃料材料的裝置之本發明具體實施例 係基於所附三圖面更詳細地敘述，在本發明中所指定之方 法不限於下面所槪述之結構型式。 【實施方式】 圖1顯示如在本發明中所指定之氣化反應器的一典型 設計。該氣化本身在由攝氏1200度至攝氏2500度之溫度 範圍及〇_3至7·0百萬帕的壓力發生於該反應室1中。該 反應室或反應器本身被該氣化器內部壁面2所封閉。該整 個反應器裝置被整合進入該壓力容器3，其同時用作緊固 件及附接件與維持該高壓。該反應氣體係經由該等燃燒器 4餵入。該氣化製程產生液態之氣化產品，該等氣化產品 -16- 200923065 沈澱在該反應器之橫側壁面2上，且經由出口開口 5離開 該容器。此開口 5排放進入具有水存量9之裝置，該已冷 卻的固態氣化產品被傳送至一鎖閘裝置1 〇，且然後被排出 。該氣態之氣化產品或該產品氣體係自該反應器經由出口 開口 6移除。此開口的一有利具體實施例提供用於一安裝 在該反應器內部壁面2上之軸環形凹部6a，以致該熔渣不 能流入該出口開口 6。一淬冷氣體進料器7係附接至反應 器2之外部壁面，且位在該出口開口 6。該淬冷氣體係與 該產品氣體混合，且被送至淬冷管8。於此區段中，該產 品氣體被冷卻，使得該任何被夾帶之熔體或蒸氣變成該固 態，且其一部份藉由重力及慣性落入具有水存量1 4之裝 置。一反轉管12被安裝在具有水存量之裝置上游，且確 保該產品氣體之進一步運送至另一處理單元。該被淬冷與 純化之產品氣體係經由該排出管1 3排出。如果被污染物 所污染之燃料材料將在該氣化器中被消除，其係亦可能經 由一餵入裝置1 1餵入此材料。 圖2顯示按照本發明之氣化反應器的一典型設計。該 氣化本身在由攝氏1 200度至攝氏25 00度之溫度範圍及 0.3至7.0百萬帕的壓力發生於該反應室1中。該反應室 或反應器本身被該氣化器內部壁面2所封閉。該整個反應 器裝置被整合進入該壓力容器3，其同時用作緊固件及附 接件與維持該高壓。該反應氣體係經由該等燃燒器4餵入 。該氣化製程產生液態之氣化產品，該等氣化產品沈澱在 該反應器之橫側壁面2上，且經由出口開口 5離開該容器 -17- 200923065 。此開口 5排放進入具有水存量9之裝置，該已冷卻的固 態氣化產品被傳送至一鎖閘裝置1 〇，且然後被排出。該氣 態之氣化產品或該產品氣體係自該反應器經由該出口開口 6移除。本發明的一有利具體實施例提供用於一安裝在該 反應器內部壁面2上之軸環形凹部6a，以致該熔渣不能流 入該出口開口。一淬冷氣體進料器7係附接至反應器2之 外部壁面，且位在該出口開口 6。該淬冷氣體係本質上平 行於該混合管子8注入，在其中該淬冷氣體係與經由該排 出管13送至該另一處理單元之產品氣體混合。如果被污 染物所污染之燃料材料將在該氣化器中被消除，其係亦可 能經由該餵入裝置1 1餵入此材料。 圖3顯示如在本發明中所指定之氣化反應器的一典型 設計。該氣化本身在由攝氏1200度至攝氏2500度之溫度 範圍及0.3至7.0百萬帕的壓力發生於該反應室1中。該 反應室或反應器本身被該氣化器內部壁面2所封閉。該整 個反應器裝置被整合進入該壓力容器3，其同時用作緊固 件及附接件與維持該高壓。該反應氣體係經由該等燃燒器 4餵入。該氣化製程產生液態之氣化產品，該等氣化產品 沈澱在該反應器之橫側壁面2上，且經由出口開口 5離開 該容器。此開口 5排放進入具有水存量9之裝置，該已冷 卻的固態氣化產品被傳送至一鎖閘裝置1 0，且然後被排出 。爲了保護該壓力容器3免於太高溫度，在該開口 5下方 之氣體房間能被單一或多層之屏蔽板1 6所封閉。該氣態 之氣化產品或該產品氣體係自該反應器經由出口開口 6移 -18- 200923065 除。本發明的一有利具體實施例提供用於一具有軸環形凹 部6a之開口，以致該熔渣不能流入該出口開口 6。淬冷氣 體進料器7係附接至反應器2之外部壁面，且位在該出口 開口 6。直接在該洋冷處理之後，該產品氣體能以一藉由 橫側地配置的噴嘴7 a所注入之水蒸氣噴霧的輔助被額外 地冷卻。該噴灑水係本質上平行於該混合管子8注入，在 其中該水係與該產品氣體混合。該等被固化之成份被傳送 進入具有水存量1 4之裝置。爲了分開該混合的液滴及乾 燥該產品氣體，該產品氣體通過一蒸氣或微滴分離單元：! 5 。該純化及已冷卻的產品氣體最後係經由排出管1 3。如果 被污染物所污染之燃料材料將在該氣化器中被消除，其係 亦可能經由一餵入裝置1 1餵入此材料。 【圖式簡單說明】 圖1顯示根據本發明之氣化反應器的第一較佳具體實 施例。 圖2顯示根據本發明之氣化反應器的第二較佳具體實 施例。 圖3顯不根據本發明之氣化反應器的第三較佳具體實 施例。 【主要元件符號說明】 1:氣化反應用之反應室 2 :反應器容器 -19- 200923065 3 :壓力密封的殻容器 4 :燃燒器 5 :液態氣化產品用之出口開口 6 :氣態氣化產品用之出口開口 6 a :該反應器內部壁面上之混合管子的軸環形凹部 7 =淬冷氣體進料器 7a :灑水噴嘴 8 :混合或淬冷管 9 :用於該氣化反應之固體產品（熔渣）而具有水存 量之裝置 1 〇 :用於固態氣化產品（熔渣）之鎖閘裝置 1 1 :用於燃料材料之餵入裝置 1 2 :反轉管 1 3 :用於氣態氣化產品（產品氣體）之排出管 14:具有水存量之裝置 1 5 :微滴分離單元 16:單一或多層之屏蔽板 -20-200923065 IX. INSTRUCTIONS OF THE INVENTION [Technical Field] The present invention relates to a method and apparatus for producing and cooling a gas obtained by solidification, whereby a gasification agent is used under pressure Heating the gases [Prior Art] When a solid, dust-like or particulate fuel material is heated with the aid of a gasified gasifying agent or a reactive gas, a gasified product is considered to be substantially contained in the gas. Liquid ingredients such as ash or slag. This solid gas acts as a flame reaction. Coal feedstocks are frequently used as feedstocks, and biofuel materials are also suitable as feed systems. The portion used is converted, and the solid matter and ash that are obtained together contain only a small portion of the gas-free carbon. The resulting is purified and thus becomes suitable for a variety of applications. This product is a synthetic product. The gasification reaction itself occurs in excess of the ash solids. The typical reaction control of these processes uses a pressure range of 1200 ° C and a pressure of 〇 · 3 to 7.0 MPa. The slag faces separate and flow below these walls. The particulate ash product gas exits the reactor. In most cases, the reaction chamber is designed to be equipped with a gas for feeding the fuel material and the gaseous fuel material, and oxygen and water are steamed with oxygen or water to vaporize the feed to obtain a gas characteristic. The hydration is mainly the temperature at which the petroleum coal coke or fuel feed is as large as the slag or flue gas gas system. i 2500 degrees of temperature in a portion of the reactor wall along with the cylindrical chamber' device. The circle -4 - 200923065 cylindrical combustion chamber is usually installed in a pressure-sealed shell container with special components for hanging or supporting the chamber. The shell container also houses a so-called mixing or quenching tube disposed adjacent to the gasification reactor and may be provided with a heating or cooling device. A common feature of almost every gasification process of this type is that the gaseous gasification product is sent to a mixing or quenching tube after the gasification, thereby mixing with an introduced gas or liquid, so that the product can be fully The ground consumes its high internal energy, also known as the "quenching" process. In the development of this process, the gaseous vaporized product is cooled to a lower temperature so that a portion of the component entrained by the finely distributed melt precipitates and can be separated by the product gas. The gasification product can be pumped from the reactor via the quenching tube in an upward or downward stream. Whenever the upflow bundle option is selected, it is relatively easy to separate the entrained liquid components from the reactive gas. An vent gas system comprising only fine particle slag particles is mixed with the quenching gas after leaving the reactor so that the slag particles solidify and can be separated by the gas in downstream equipment. Document DE 91 1313 describes a solid fuel material. In the gasification unit, the gasification reaction itself takes place in a special reactor which is shaped like a spherical or pear-shaped reactor placed in a system of refractory brick structures. The gasifying agent is injected through a nozzle disposed laterally, and the fuel material is fed to the reactor by a screw conveyor. The product gas produced is discharged in an upward stream through a tube provided with a cooling jacket and a feed device for the cooling or quenching gas. A portion of the slag is discharged through an opening in the lower side of the reactor from -5 to 200923065. Document EP400740 A1 describes a gasification reactor which is designed with a specific ratio of length to diameter and which is combusted at all line angles by the burner. This configuration allows for a reduction in the amount of flue ash obtained. The upper side of the reactor is provided with a tube for the upright discharge stream of the product gas. The underside of the reactor has an outlet for a liquid gasification product, in particular in the form of molten slag. Document US 544 1 5 47 specifies a device for gasification of a solid fuel material which itself occurs in a cylindrical reactor. The reactor is mounted in a specialized housing container using a specific attachment. The design of the shell-shaped container also typically defines the device as defined in the present invention on the outer side. The product gas system is discharged through an outlet and is passed through a stream in an upright direction through a tube equipped with a feed device for quenching or cooling the gas directly above the outlet. Any reactor provided with means for an upward discharge stream of gas of the product has the disadvantage that a part of the apparatus of a considerable height is required, since a good air mixing with the quenching agent requires a long air passage, and This involves a rather dangerous slag solidification. This reversal always occurs after the quenching process in order to prevent deposits from forming due to sticky ash particles. The raw material gas thus obtained is subjected to further processing by means of a suitable heat exchanger, filter or scrubber. In the case of a downward flow for removing the product gas from the reactor, the gaseous gasification product is discharged from the gasifier through a quenching tube disposed at a lower portion of the reactor. This design ensures that the slag obtained by quenching -6 - 200923065 falls down by gravity into the slag pool. The cooled gas can be reversed upstream of the slag bath by a suitable guide or reversing mechanism to allow further processing of the produced feed gas using a suitable heat exchange or scrubber unit. Document DE 400 1 739 A1 describes a device for the gasification of a solid fuel material which leaves the reactor in a stream which is always standing down. After the gas exits the reactor, the concentrically arranged nozzles are used to spray a hot water and dust-laden gas stream in a radial manner such that the solid gasification product is confined and the gas is The stream is cooled simultaneously. The gas then releases the coarse solid component in a wide cylindrical agitator and is sent via a guide plate for further processing. The coarse solids are removed from the system via a lock unit. Document US 4 449 963 specifies a device for the gasification of a solid fuel material which leaves the reactor in a stream that is always standing down, and thereby allows the entrained coarse solids to be simultaneously The removal is quenched by heat exchange with a coolant in the continuous contact zone. The tube for transporting the quenching gas and product gas is discharged via a sealed cone into a vessel containing a coolant, wherein the quenching gas releases solids and is further cooled. Any reactor provided with internal parts for discharging the product gas in the downward gas stream has the disadvantage that this type of reaction control is easily caused by the reactor to the downstream equipment line. The scum or blockage, because the slag also contains coarse slag particles 'which only slowly solidify, and the sticky surface is turbulent and reverse-transferred to the walls 200923065. It is often desirable to provide a considerable height for a wide mixing chamber and pipeline or equipment to prevent the formation of unwanted deposits. The conventional gasification plant having a downward gas discharge needs to have a similar height as those having an upward discharge stream because the gasification, quenching, and slag removal regions have a similar height, and Since the order in which only they are stacked is different, it is therefore an object of the present invention to provide a simple apparatus suitable for cooling a gaseous product of a gasification process to a lower temperature with the aid of a quenching gas. The separate solid reaction product must be easily removed and treated by the process such that the reaction control line is avoided due to blockage of deposits or scum. An uncomplicated design pattern is specified, but it must still be ensured that the product gas is purified and cooled. Furthermore, it is specified that the device must have a height lower than that of the conventional device. The object of the present invention is achieved by a device for coal gasification, assisted by an essentially downward flow, which allows the gaseous state to be filled with dust gasification products and quenching gas in the upright pipe downcomer mixing. A major portion of the slag has been separated on the side walls of the reactor by a particular reactor design. The reactor apparatus according to the present invention is provided with separate lateral outlets for slag discharge which are simultaneously used to remove solids which have been separated in the reactor in order to be secured in a water-filled apparatus. It is cooled and then removed by the container. In order to protect the pressure vessel against the high temperature of the slag, the gas chamber located below the outlet is surrounded by a protective shield plate completely -8-200923065, the shield plate can be multi-layer type and designed as a cooled film wall surface . The product gas system is separately discharged and transported through a second outlet opening in a discharge pipe for mixing with the quenching gas. According to a device designated by the present invention, the outlet opening for the product gas is provided with an annular or funnel-shaped recess on the inner side of the reactor to prevent the liquid slag from being discharged into the gas discharge pipe. In order to prevent the formation of the slag layer in the recess, a lower portion of the recess may be provided with a ceramic coating or a pin covered by a ceramic plug compound. A means for feeding the quenching agent is located after the product gas enters the inlet of the mixing tube. By separately discharging the liquid vaporized product and the product gas, the amount of slag particles contained in the gas stream leaving the reactor is substantially reduced. This method facilitates the cooling of the gas and the removal of dust from the gas, and substantially reduces the tendency of the mixed tube to foul. According to an embodiment of the invention, the outlet opening for discharging the liquid slag is discharged into a device for charging water and for cooling the slag. The slag can be depressurized via a suitable lock and replenished by means of water, and thus recovered by the process itself. Alternatively, an additional burner can be placed above the slag discharge to re-liquefy the slag that has begun to solidify. The purpose of this patent application is in particular a method for gasifying a solid, powder or particulate fuel material under pressure and featuring the following technical details: • The fuel material used is at 12 ° C. At a temperature of 2500 ° C and a pressure of 〇 3 to 7.0 MPa (Mpa), and in a gasification reactor cooled in 200923065 with a medium with oxygen or water vapor, and The gaseous gasification product is discharged from the gasifier through a separate collection device and opening and the liquid and solid gasification products obtained are discharged through a separate collection device and opening, and the liquid state obtained The gasification product is transferred to a water-filled device and subsequently removed via a pressure-reducing device, and the gaseous gasification product obtained is removed from the reactor by an auxiliary up-down stream. The gaseous reaction product is sent from the reactor to a mixing or quenching tube where the reaction product is mixed with an incoming medium to consume its high internal energy and thus undergo a cooling. According to one embodiment of the invention, the fuel material used is microparticles or coal that is as dusty consistency. The particle diameter of the fuel material particles is preferably < 0 · 5 mm. In another embodiment of the invention, the fuel feed used is particulate or biomaterial like dust consistency. The particle size of the fuel material is preferably < 0.5 mm. In another embodiment of the invention, the fuel feed used is an organic material, such as a particulate or particulate type of plastic or petroleum coal. The particle size of the fuel material is preferably < 0 · 5 mm. Furthermore, the object of the patent application is a device suitable for the performance of the method specified in the present invention and characterized by the following features: • The device comprises a cylindrical or elliptical reactor vessel, and - 10- 200923065 • The reactor vessel is provided with a separate collection device and opening for the discharge of liquid and solid gasification products, and • a space system adjacent to the opening and suitable for discharge operations, allowing liquid and Removal of solid gasification products; • A device is positioned below the bottom of the space for discharging liquid and solid gasification products, which space can be filled with water or used as a device with another water inventory Adjusting accessories such that the liquid and solid gasification products can be fed into the water tank, and • a device for removing such products in a device having a water inventory for liquid and solid gasification products Below, and/or the gasification fuel material and the reaction gas system are fed by at least two burners laterally attached to the reactor, or one of the burners mounted in the top plate And/or the openings of the lateral burners are directed horizontally into the burner chamber, or tangentially into the burner chamber at an angle of from 45 degrees to 10 degrees or from 0 degrees to 10 degrees, and The reaction vessel has a separate opening and a collecting device for discharging the gaseous gasification product, and a quenching room is adjacent to the reaction vessel in an upright and intrinsic downward direction, and a medium for introduction A feeding device is attached to the quenching room, the quenching house is also equipped with special equipment to provide cooling from the outside, and the reactor vessel is closed by a pressure-tight housing, the housing thus forming The boundary of the entire structure. The reaction vessel itself according to the apparatus specified in the present invention preferably has a cylindrical design of -11 - 200923065, but can also be shaped in an elliptical shape to improve the shape of the structure. A reactor employed in the process according to the invention is typically equipped with at least two burners, although it can also be operated as a single burner. The burners heat the reactor by feeding a reaction gas and a honed fuel material which are laterally mounted or in the top plate of the reactor. In the case where the burners are mounted laterally, it is advantageous to support them by means of specific fasteners attached to the container housing. Further, the laterally mounted burners allow for a horizontal orientation toward the combustion chamber, or an upward orientation at an angle of 0 to 45 degrees, or an angle of 0 to 10 degrees in a secant manner. In order to improve the gasification reaction and burner control, it is possible to provide the reaction partners, in particular the combustion gases, with a vortex. In the case of a top mounted burner, a small guide can be installed at the burner outlet or a specially designed burner for this purpose. Depending on the type of design, the fuel material can be fed to the reactor in different ways. Thus, for example, the dust-like fuel material can be delivered to the reactor via a separate feed tube and the burner. However, it is also possible to feed the fuel material to the reactor through separate openings in the top plate of the vessel. It is particularly advantageous to provide a suitable conveyor belt at the opening such that the conveyor belt can push the feed through the opening into the reactor.譬 A spiral conveyor belt is well suited for this purpose. This method is particularly suitable for feeds that are not easily fed to the reactor in the form of dust. Plastic materials or organic contaminants are typically used for this standard. According to a particular embodiment of the invention, cooling of the inner wall of the reactor -12-200923065 is provided. Typically, the inner wall of the reactor vessel has a metal pin that is covered with a ceramic compound. It is also possible to spray the inner wall of the reactor with boiling water. The fuel materials are preferably fed in the form of particles or dust-like consistency. A reaction gas system with oxygen or water vapor is fed via a burner mounted laterally or in the top plate of the reaction vessel. Pure oxygen can also be used as a reaction gas. This gasification reaction usually takes place in a large amount of dust. According to another embodiment of the invention, the slag contained in the product gas is cooled by the quenching process after leaving the gasifier and is thus solidified. Various gas systems are suitable as quenching gases, the preferred quenching gas system being cooled product gas, water vapor, nitrogen or an inert gas, or a mixture of such gases. A liquid quenching agent, such as the water system returned by the process, is also suitable. The length of the quench tube is generally dependent on the size of the reactor. The subsequent approximation is applied to: the distance between the uppermost quenching gas feed point in the tube and the bottom of the reactor should be 10 0 X ° smaller than the diameter of the reactor whenever the hot product gas meets the quenching The agent, which is subjected to a major cooling by the method of consuming energy transfer. This process is linked to the curing of a liquid gasification product. To improve precise mixing, the quench tube can be provided with one or more funnel-shaped necks that result in a smaller diameter of the mixing tube. Another option is to have the quench tube provided with internal means for this purpose such that the gas stream is subjected to a funnel-type bundling. The internal devices may be, for example, a ring-shaped metal skirt or a ring-shaped ceramic orifice plate. This method facilitates mixing with the quenching agent and curing of the entrained liquid gasification product. In order to protect the wall top of the quenching chamber against liquid particles, the convenient -13-200923065 is provided for several levels for injecting the quenching agent along the quenching chamber. For further cooling of the product gas, a liquid coolant can be injected into the gas stream. It is recommended that the coolant be injected over the funnel-shaped neck portion to present a flat jet parallel to the surface of the funnel. The liquid coolant to be fed below the funnel-shaped neck portion should be injected as a spray stream parallel to the product gas stream. In this case, the coolant injection along the quenching chamber can likewise occur at several levels. According to an embodiment of the invention, a device is disposed below the mixing tube and comprises water or a system adapted to receive a device having a water inventory, the device being designed to collect quenching in the product gas The transfer occurs as part of the solid component solidified during the cold treatment by the gravity or inertia effect. Solid components or solids with water obtained in a device having a water inventory can be recovered by the process by a pump, if necessary. In another embodiment of the invention, a space above the apparatus having a water inventory is used to mount an outlet tube for discharging the purified product gas and for reversing and further transporting the gas. At this stage, the gas contains only solid particles of a small particle size. The reversal and further transport of the gas stream begins with the quenching chamber using one or more tubes preferably disposed at an angle of >90 degrees. Alternatively, the angle of the gas counters applied to the product can be designed to be small, but in this case, the solids concentration of the product gas thus transported will increase slightly. A classifier can be installed in the quenching chamber to remove coarser solids, particularly upstream of the end that is discharged into the device having the water inventory. The installation of such a device, in this case, a classifier for the reversal of the jet, for example, allows the coarser slag or ash particles to be removed from the quenching room -14-200923065. Another embodiment of the invention carries the cooling and purification downstream of the reversal section. In order for the gas section to be from the product to be at or near the reversal point, such as a demister or grid tray. Upon exiting the system, it is preferred to further cool and purify the gas. This partial evaporation of water forms this amount. This procedure often includes a scrubber scrubber for spraying or spraying onto the gas. This method reduces the temperature of the gas, impurities and liquids that can be dissolved in water or after purification and cooling, leaving oxidizing, toxic gases (C 0 S, C ◦, or acid or alkaline, corrosive gases (HC1 in order to improve the process) The energy output is separated from the downstream of the outlet into the gasification stream. The partial stream can exit the exchanger at the gasifier. The process is preferably performed in the heat exchanger operation due to entrainment melting. Alternatively, it may be in the form of water vapor or C〇2 to the process. The yield improvement in the desired product gas is provided for a discharge pipe that discharges the product gas to a system for further removal of impurities. The reversal of the tube is provided with a droplet separation unit, for example, by mixing water with water to directly cool the product gas and water while cooling the vaporized product of the vaporized product, in the countercurrent flow, the washing water Auxiliary is provided for gas cooling and the gas system simultaneously releases solid gaseous substances. The gas stream of the system can be subjected to a catalytic conversion of HCN) and /[NH3, H2S) adsorption. At least a portion of the stream may be conducted after the gasification beam is fed to the hot quenching process at any point downstream of a heat exchanger port to avoid any interference with the slag. Feeding a gas during start-up, such as process control, this method allows, or facilitates, the gasification reaction control -15-200923065 to allow for inspection of the rules and to facilitate maintenance of the reactor system, the reactor vessel and The annular space between the hermetic housing structures is special and can be accessed through the manhole. For this purpose, the upper tray and the lateral wall surface of the pressure vessel below the bottom of the gasifier are provided with manholes. The reaction vessel can likewise be equipped with a manhole to allow access to the space. A design such as that claimed in the present invention has the advantage that it may separate the solid from the gaseous reaction product in a simple manner. Thus, a comparison of the design specified in the present invention with the state of the art technology shows that it is less expensive to make the structure and that the resulting product gas purification system is more efficient. The device specified in the present invention clearly allows for equipment items of a lower height as compared to devices made in accordance with the latest technology. DETAILED DESCRIPTION OF THE INVENTION The present invention is described in more detail on the basis of the accompanying three drawings, and the method specified in the present invention is not limited to the structural forms described below. [Embodiment] Fig. 1 shows a typical design of a gasification reactor as specified in the present invention. The gasification itself occurs in the reaction chamber 1 at a temperature ranging from 1200 °C to 2500 °C and a pressure of 〇_3 to 7.0 MPa. The reaction chamber or reactor itself is closed by the inner wall 2 of the gasifier. The entire reactor unit is integrated into the pressure vessel 3, which serves as both a fastener and an attachment and maintains the high pressure. The reaction gas system is fed via the burners 4. The gasification process produces a liquid gasification product which is deposited on the transverse side wall face 2 of the reactor and exits the vessel via the outlet opening 5. This opening 5 is discharged into a device having a water inventory 9, which is delivered to a lock device 1 and then discharged. The gaseous gasification product or product gas system is removed from the reactor via the outlet opening 6. An advantageous embodiment of this opening provides for a cylindrical annular recess 6a mounted on the inner wall 2 of the reactor so that the slag cannot flow into the outlet opening 6. A quenching gas feeder 7 is attached to the outer wall of the reactor 2 and is located at the outlet opening 6. The quench gas system is mixed with the product gas and sent to the quenching tube 8. In this section, the product gas is cooled such that any entrained melt or vapor becomes the solid state, and a portion thereof falls into the apparatus having the water inventory 14 by gravity and inertia. A reversing tube 12 is installed upstream of the device having the water inventory and ensures further transport of the product gas to another processing unit. The quenched and purified product gas system is discharged through the discharge pipe 13. If the fuel material contaminated by the contaminants will be eliminated in the gasifier, it may also be fed through a feed device 1 1 . Figure 2 shows a typical design of a gasification reactor in accordance with the present invention. The gasification itself occurs in the reaction chamber 1 at a temperature ranging from 1 200 ° C to 2500 ° C and a pressure of 0.3 to 7.0 MPa. The reaction chamber or reactor itself is closed by the inner wall 2 of the gasifier. The entire reactor unit is integrated into the pressure vessel 3, which serves as both a fastener and an attachment and maintains the high pressure. The reaction gas system is fed via the burners 4. The gasification process produces a liquid gasification product which is deposited on the transverse side wall face 2 of the reactor and exits the vessel via the outlet opening 5 -17-200923065. This opening 5 is discharged into a device having a water inventory 9, which is delivered to a lock device 1 and then discharged. The gaseous gasification product or product gas system is removed from the reactor via the outlet opening 6. An advantageous embodiment of the invention provides a cylindrical annular recess 6a for mounting on the inner wall 2 of the reactor such that the slag cannot flow into the outlet opening. A quenching gas feeder 7 is attached to the outer wall of the reactor 2 and is located at the outlet opening 6. The quench gas system is essentially flushed into the mixing tube 8 where the quench gas system is mixed with product gas sent to the other processing unit via the discharge tube 13. If the fuel material contaminated by the contaminants is to be eliminated in the gasifier, it is also possible to feed the material via the feeding device 11. Figure 3 shows a typical design of a gasification reactor as specified in the present invention. The gasification itself occurs in the reaction chamber 1 at a temperature ranging from 1200 ° C to 2500 ° C and a pressure of 0.3 to 7.0 MPa. The reaction chamber or reactor itself is closed by the inner wall 2 of the gasifier. The entire reactor unit is integrated into the pressure vessel 3, which serves as both a fastener and an attachment and maintains the high pressure. The reaction gas system is fed via the burners 4. The gasification process produces a liquid gasification product which is deposited on the lateral side wall 2 of the reactor and exits the vessel via the outlet opening 5. This opening 5 is discharged into a device having a water inventory 9, which is delivered to a lock device 10 and then discharged. In order to protect the pressure vessel 3 from too high a temperature, the gas chamber below the opening 5 can be closed by a single or multi-layer shielding plate 16. The gaseous gasification product or product gas system is removed from the reactor via outlet opening 6 by -18-200923065. An advantageous embodiment of the invention provides for an opening having a cylindrical annular recess 6a such that the slag cannot flow into the outlet opening 6. A quenched gas feeder 7 is attached to the outer wall of the reactor 2 and is located at the outlet opening 6. Immediately after the ocean cooling treatment, the product gas can be additionally cooled by the aid of a water vapor spray injected by the nozzles 7 a disposed laterally. The spray water system is injected substantially parallel to the mixing tube 8 where the water system is mixed with the product gas. The solidified components are transferred to a device having a water inventory of 14. In order to separate the mixed droplets and dry the product gas, the product gas is passed through a vapor or droplet separation unit: ! The purified and cooled product gas is finally passed through the discharge line 13. If the fuel material contaminated by the contaminants is to be eliminated in the gasifier, it is also possible to feed the material via a feed device 11. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 shows a first preferred embodiment of a gasification reactor according to the present invention. Figure 2 shows a second preferred embodiment of a gasification reactor in accordance with the present invention. Figure 3 shows a third preferred embodiment of a gasification reactor in accordance with the present invention. [Explanation of main component symbols] 1: Reaction chamber for gasification reaction 2: Reactor vessel -19- 200923065 3 : Pressure-sealed shell container 4: Burner 5: Outlet opening 6 for liquid gasification products: gasification Product outlet opening 6 a : shaft annular recess 7 of the mixing tube on the inner wall of the reactor = quenching gas feeder 7a: sprinkling nozzle 8: mixing or quenching tube 9: for the gasification reaction Device for solid product (slag) with water storage 1 〇: Locking device for solid gasification product (slag) 1 1 : Feeding device for fuel material 1 2 : Reverse tube 1 3 : Used Discharge tube 14 for gaseous gasification product (product gas): device with water inventory 1 5 : droplet separation unit 16: single or multi-layer shield plate-20-