201022182 六、發明說明： 【發明所屬之技術領域】 本發明涉及用於對諸如水泥生料（cemenmwmeai)、石 灰石或其他含碌物質原料之類的原料（rawmaterial)進行熱處 理的方法’通過該方法，原料在預熱器系統中被預熱並且可能 ^锻燒㈤dne).，並且原料可能在窠中被燃燒，且其中，在 軋化反應器（gasification reaetor)中存在蒸汽時，使固體和/ ，液體燃料與經賴_料相翻，使得簡部分地分德為含 氯的可燃氣體、且部分地分顧為含碳固體燃料殘潰，該含氮的 Φ可燃氣體經由氣體出口從氣化反應器中排出，該含碳固體燃料 殘潰經由固體出口從氣化反應器中排出。本發明還涉及用於實 施該方法的設備。 【先前技術】 水泥廠和礦物加工廠是能源密集型的工廠，其使用大量的 化石燃料（fossil fuel)，是全球人為二氧化碳排放的重要原因 之一。由於這一原因，人們做出巨大努力來減小這些工廠的二 氧化碳排放。下面總結的是當前可用的各種可選方案，但是這 ❹些可選方案中沒有一個涉及基於對廢氣的二氧化碳進行後續 分離的所謂“後清潔，’技術（“post_cleaning” techn〇1〇gy)。 一種常用的方法是用不同程度二氧化碳中性的燃料 (carbon dioxide neutral fuel)(所謂的替代燃料（alternative fuel))代替化石燃料。在進行了包括研磨、切割或類似加工、 還可能包括乾燥的預處理之後，替代燃料可能適合於在滿足適 度溫度條件的預熱器或鍛燒爐中懸浮燃燒。然而，水泥熟料 (cement clinker)的煅燒要求更高的溫度水準，由此排除了用 替代燃料完全代替化石燃料的可能性。替代燃料和化石燃料的 共燃在現代回轉窯燃燒器（r〇tary kiln burners)中是可行的， 3 201022182 但是這同樣必須通過研磨、切割或類似加工來減小粗粒燃料的 顆粒。 第二種技術是所謂的濃化氧燃燒（oxygen_enriched combustion，OEC)，其中通過供應純氧，使回轉窯燃燒器的 燃燒空氣的氧含量增加到百分之二十三至百分之二十五。這導 致火焰溫度較高並且特定的廢氣體積減小；這兩個因素都有助 於減小每生產單位數量的水泥熟料所消耗的能量，並有助於提 咼工廠的設備能力，這意味著與購買氧氣或安裝及操作氧氣設 備有關的成本在某些情況下可被接受。在〇EC的最終形式 © 中，完全用純氧代替燃燒空氣，由此大體上實現了廢氣基本上 由二氧化碳和蒸汽組成的條件。蒸汽可以通過冷凝去除，二氧 化石厌隨後被壓縮並被封存到地下中。正在發電廠部門中開發部 分廢氣被再循環且與純氧混合的這種類型的c〇2捕獲設備，並 且已經有人建議在水泥廠中也採用這種技術，例如在國際能源 機構提出的概念研究（IEA溫室氣體研究計畫“c〇2 Capture in the Cement Industry，” Technical Study，Report No. 2008/3 )中提 出過這種建議。然而，數量相對較大的漏氣（false air)的滲 參透是水泥廠的特有問題，這可能複雜化使提取的廢氣中的二氧 化碳達到可接受的濃度的處理。根據IEA提出的概念研究，看 起來採用另一 OEC處理配置具有更好的經濟效益，在該配置 中，在被供應給燃料和純氧的單獨預熱器中實施緞燒。可以從 該單獨預熱器提取更濃縮的二氧化碳流（stream 〇f carb〇n dioxide ) ’由此使工廠的總二氧化碳排放減少約百分之五十（該 數字包括在常規發電廠處為水泥廠提供電力而排放的相關的 二氧化碳）。 用於從水泥和礦物製造加工減少二氧化碳排放的第三種 201022182 方法，涉及將廢氣和預熱器中的餘熱用於蘭金循環處理 (Rankine cycle process )(使用蒸汽或有機介質）形式的能量 產生過程’由此減少工廠的淨功率耗損（net power consumption)。這種所謂的聯合生產尤其在中國的一些工廠 中實施。然而’可用的能量數量相對有限且僅產生低級熱量， 這意味著產生功率的效率將非常低。因為這些因素，利用餘熱 的蘭金循環聯合生產廠的投資通常並不能獲得利潤。 電力和礦物/水泥的聯合生產可以使用氣化技術 (gasification technology)來建立，氣體隨後在氣體發動機或 β 用於產生電力的其他裝置中燃燒。因此，可以產生的電力數量 將不依賴於來自加工的餘熱’這可能是與用於製造氧氣和麗縮 二氧化碳的能源密集型輔助系統的操作相關的巨大優點。例 如，如德國Rudersdorf的水泥廠所實踐，氣化可以發生在單獨 的單元中’或者’如文獻（S. Weil等“Hydrogen Energy from Coupled Waste Gasification and Cement Production — a Thermochemical Concept Study" , International Journal of Hydrogen Energy31，2006)所提議，氣化發生在部分集成的單 φ 元（partially integrated unit)中’其中燃料通過與經預熱的水 泥生料和蒸汽接觸而被間接加熱。使用後一種方法，依據氣體 中二氧化碳的數量而定，可以產生具有約1〇_15 MJ/Nm3的相 對高的熱值的氣體。在被冷卻、被引導通過管道系統、且在氣 體發動機或產生電力的其他裝置中使用之前，必須從氣體中去 除焦油物質，而該焦油物質是現有技術的典型問題。 如上所述’人們正在付諸巨大努力來開發用於減少水泥廠 和礦物加工廠的二氧化碳排放的技術。根據上述的介紹，可以 總結出與現有技術有關的很多問題和缺點。 5 201022182 •不能夠用替代燃料完全替代化石燃料’並且 僅是部分的c〇2中性的（c〇2_neutral)。 •為了懸浮燃燒而對替代燃料進行的預處理通常複雜而 費用高。 •漏氣滲透導致與利用OEC技術的C〇2捕獲相關 的顯著增加。 ♦使用OEC技術的單獨煅燒不能獲得大於約百分之五 的C02捕獲。 Ο201022182 VI. Description of the Invention: [Technical Field of the Invention] The present invention relates to a method for heat-treating a raw material such as a cement raw material, a limestone or other raw material, by which the method The feedstock is preheated in the preheater system and may be calcined (f), and the feedstock may be burned in the crucible, and wherein, in the presence of steam in the gasification reaetor, the solids and/or The liquid fuel is turned over with the slag, so that the singular portion is a flammable gas containing chlorine, and is partially disintegrated as a carbon-containing solid fuel, and the nitrogen-containing Φ combustible gas is vaporized from the gas through the gas outlet. Discharged from the vessel, the carbonaceous solid fuel is withdrawn from the gasification reactor via a solids outlet. The invention also relates to an apparatus for carrying out the method. [Prior Art] Cement plants and mineral processing plants are energy-intensive plants that use large amounts of fossil fuels and are one of the major causes of anthropogenic carbon dioxide emissions worldwide. For this reason, great efforts have been made to reduce carbon dioxide emissions from these plants. The following summarizes the various options currently available, but none of these alternatives involve a so-called "post-cleaning" technique based on the subsequent separation of carbon dioxide from the exhaust gases ("post_cleaning" techn〇1〇gy). A common method is to replace fossil fuels with different degrees of carbon dioxide neutral fuel (so-called alternative fuels). Pre-treatments including grinding, cutting or similar processing, and possibly drying, are also carried out. After treatment, the alternative fuel may be suitable for suspension combustion in a preheater or calciner that meets moderate temperature conditions. However, the calcination of cement clinker requires a higher temperature level, thereby eliminating the use of alternative fuels. The possibility of completely replacing fossil fuels. Co-firing of alternative fuels and fossil fuels is feasible in modern rotary kiln burners, 3 201022182 but this must also be reduced by grinding, cutting or similar processing. Particles of coarse grain fuel. The second technique is the so-called concentrated oxygen combustion (oxygen_enriched co Mbustion, OEC), in which the oxygen content of the combustion air of the rotary kiln burner is increased to 23% to 25% by supplying pure oxygen. This results in a higher flame temperature and a specific volume of exhaust gas. Small; both of these factors help to reduce the amount of energy consumed per unit of production of cement clinker and help to improve the plant's equipment capacity, which means that it is related to the purchase of oxygen or the installation and operation of oxygen equipment. The cost is acceptable in some cases. In the final form of the 〇EC, the combustion air is completely replaced by pure oxygen, thereby substantially realizing the condition that the exhaust gas consists essentially of carbon dioxide and steam. The steam can be removed by condensation. The anaerobic anaesthetic is then compressed and sealed underground. In the power plant sector, this type of c〇2 capture equipment, in which some of the exhaust gas is recycled and mixed with pure oxygen, has been developed and has been suggested in cement plants. Using this technology, for example, the concept study presented by the International Energy Agency (IEA Greenhouse Gas Research Project “c〇2 Capture in the Cement Industry,” Technical This proposal was made in Study, Report No. 2008/3. However, the relatively large amount of false air leakage is a unique problem in cement plants, which may complicate the carbon dioxide in the extracted exhaust gas. Processing to an acceptable concentration. According to a conceptual study presented by the IEA, it appears that the use of another OEC treatment configuration is more economical, in which it is implemented in a separate preheater that is supplied to the fuel and pure oxygen. Satin burning. Streams of 〇f carb〇n dioxide can be extracted from the separate preheater' thus reducing the total CO2 emissions of the plant by approximately 50% (this figure is included at conventional power plants) Related carbon dioxide emissions from the power supply to the cement plant). A third 201022182 method for reducing carbon dioxide emissions from cement and mineral manufacturing processes, involving the use of waste heat in the exhaust gas and preheater for energy generation in the form of a Rankine cycle process (using steam or organic media) The process 'by this reduces the net power consumption of the plant. This so-called co-production is carried out especially in some factories in China. However, the amount of energy available is relatively limited and only produces low levels of heat, which means that the efficiency of generating power will be very low. Because of these factors, the investment in the combined production plant of the Rankine cycle using waste heat is usually not profitable. The combined production of electricity and minerals/cement can be established using gasification technology, which is then burned in a gas engine or other device used to generate electricity. Therefore, the amount of power that can be generated will not depend on the waste heat from processing' which may be a huge advantage associated with the operation of energy intensive auxiliary systems for the manufacture of oxygen and condensed carbon dioxide. For example, as practiced in a cement plant in Rudersdorf, Germany, gasification can occur in a single unit 'or' as in the literature (S. Weil et al., "Hydrogen Energy from Coupled Waste Gasification and Cement Production — a Thermochemical Concept Study", International Journal of Hydrogen Energy 31, 2006) proposes that gasification takes place in a partially integrated unitary integrated unit where the fuel is indirectly heated by contact with preheated cement raw meal and steam. The latter method is used, Depending on the amount of carbon dioxide in the gas, a gas having a relatively high calorific value of about 1 〇 15 MJ/Nm 3 can be produced. It is cooled, guided through the piping system, and used in gas engines or other devices that generate electricity. Previously, tar substances had to be removed from the gas, which is a typical problem in the prior art. As mentioned above, 'people are making great efforts to develop technologies for reducing carbon dioxide emissions from cement plants and mineral processing plants. Introduction, can summarize the relevant technology Many problems and shortcomings. 5 201022182 • It is not possible to completely replace fossil fuels with alternative fuels' and is only partially c〇2 neutral (c〇2_neutral). • Pretreatment of alternative fuels for suspension combustion is often complicated. High cost • Leakage infiltration results in a significant increase associated with C〇2 capture using OEC technology. ♦ Separate calcination using OEC technology does not achieve greater than about five percent C02 capture.
♦用於產生電力的可用餘熱數量不足且轉換效率低。 _在熱氣化氣體被氣體發動機或用於產生電力的其他裝 置使用之前，必須從熱氣化氣體中去除焦油物質。 氣化氣體典型地包含使氣體的熱值減小的二氧化碳。 【發明内容】 本發明的目的是提供一種用於消除或顯著減少上述問題 和缺點的方法和設備。 根據本發明，通過上述介紹中提及的那種方法實現該目 的’其特徵在於’含氫的可燃氣體的至少一部分被用來對原料 進行熱處理。 通過使用氣化技術和OEC技術的組合，由於含氫可燃氣 體例如在供應空氣的條件下可用作燃料、以用於預熱原料和/ 或用於燃燒熏中的水泥熟料這一事實，可以使水泥廠和礦物加 ，，的一氧化碳排放減小百分之五十以上。在通過現有技術方 ^ π潔之後基本上包含氮氣和蒸汽的燃燒氣體可被排放到空 氣中。來自氣化反應器的的固體燃料殘渣基本上由碳構成，該 固體燃料殘渣例如在供應純氧的條件下可用作煅燒爐 (calciner)中的燃料，由此提供濃縮的熱二氧化碳流，該熱 6 201022182 二氧化碳流可用於預熱原料或用於抬升蒸汽，隨後該熱二氧化 石厌流被壓縮並被從工廠提取出，以便被封存到地下或者被進一 步處理。同時，燃料的分餾使得用替代燃料完全取代化石燃料 成為可能’並且燃料的分餾消除和降低了對替代燃料進行預處 理的需求。 曰3氫的可燃氣體可能包含了原始燃料中所含有的大部分 月bl。假定如上所述，固體燃料殘渣可用於滿足煅燒的能量需 求而锻燒的旎量需求構成總能量需求的重要部分，則可能導 致含氫可燃氣體的過剩。該氣體可用於在氣體發動機、燃料電 看池或其他裝置中生成電力，由此，與專Η基於餘熱的利用相 ，，顯，增大了電廠產生電力的潛能。根據本發明，過剩的含 ^可燃氣體可以被從氣化反應器中提取出，且在單獨的熱交換 器中通過與較冷原料直接進行熱交換來冷卻該含氫可燃氣 體，從而導致所有焦油物質都被冷凝在原料的表面上。如此加 熱的，料隨後可以被進一步加熱，且在供應純氧的條件下利用 來自氣化反應器的固體殘渣在單獨的預熱器系統中煅燒該原 料。因此，冷凝在原料上的焦油物質也被燃燒。本發明的本實 #施例的一個顯著特徵是，在熱交換過程中原料與可燃氣體，即 還原空氣，相接觸。因而’在常規預熱時可能構成排放問題的 原料十的揮發性有機物質將增加燃燒氣體的數量。這使得處理 所謂的備選原料（alternativerawmaterial)成為可能，該 材料的特徵為有機結合成分（organicallyb〇undele_t)的含 量高。然後，可以使用現有技術方法來處理所得到的無焦油且 經冷卻的可燃氣體，以便去除顆粒以及諸如硫化氣和氣化 類的不希望的成分。 在從氣化反應器提取的含氫可燃氣體被用於對原料進行 7 201022182 熱處理之前’該含氫可燃氣體可以首先在能夠發生焦油裂解的 溫度下與完全或部分锻燒過的原料接觸，且隨後在能夠發生再 碳化（recarbonisation)的溫度下與完全或部分煅燒過的原料 接觸。現有技術已知，某些材料，尤其是諸如氧化舰樣的經 煅燒的材料，對焦油裂解（tar cracking )有催化作用（catalytkal effect)。焦油裂解反應典型地在高於75〇〇c的溫度以合理速度 發生，而經烺燒的水泥生料的再碳化反應在約55〇〇c至約65〇 °C的溫度範圍内發生，在該溫度範圍，包含在可燃氣體中的二 氧化碳可以與原料中的氧化飼反應。因此二氧化碳可以從燃燒 ® 氣體中去除，同時氣體的熱值會增加。用於吸收二氧化碳的經 烺燒的原料可由包含從氣化反應器中提取的燃料殘渣的固體 材料所構成，該經煅燒的原料隨後被再循環到煅燒爐。 氣化反應器中的燃料的分顧、且因而導致含氫可燃氣體的 數量和組成，取決於經預熱的原料的溫度，該溫度至少應為 500°C，且較佳至少為800〇C。在根據本發明的用於對水泥生 料進行熱處理的工廠的較佳實施例中，例如在“移動機床”反 應器（’’movingbed” reactor)中，或者，在轉動圓筒（rotating ❹ drum)、旋風器（CyCl〇ne)或其他氣體-固體接觸器（gas_s〇lid contactor)中，在存在蒸汽時，固體燃料和/或液體燃料將與溫 度約為850°C的完全或部分烺燒過的水泥生料接觸。經由氣體 出口從氣化反應器提取出這樣產生的可燃氣體，而在約600。(： 的溫度下經由固體出口從氣化反應器提取出固體材料，即煅燒 過的水泥生料、燃料灰（fuel ash)、燒焦物（char)和最終的 金屬顆粒。假定可以在接近600°C的溫度範圍通過經煅燒的水 泥生料以碳酸鈣的形式提取二氧化碳，則可燃氣體將在二氧化 碳吸收器中與從氣化反應器提取的固體材料相接觸，該二氧化 201022182 碳吸收器例如也可以是“移動機床，’反應器，或者，是 或其他氣體-固體接觸器。 <器 來自二氧化碳吸收器的一些無二氧化碳的可燃氣體 被引導到迴紅窯燃燒器（rotary kiln burner )，以用於燃掉水、' 熟料，且產生的熱窯氣（hot kiln gas)可被傳遞到預熱器尼 用於將原料預熱到約75(TC的溫度水準。原料可以從^熱器= 送到煅燒爐，在煅燒爐裏，在供應純氧的條件下，來自&化子 應器的固體材料可以用作燃料。在來自氣化反應器的固體材^ 被用作燃料之前，該固體材料可以經過碾碎和篩選，使得最= ® 的金屬顆粒被分離出且大顆粒燒焦顆粒尺寸被減小。來自煅^ 爐=包含二氧化碳的氣體可以被引導到單獨的預熱器，在預^ 器裏，可以以類似的方式將原料加熱到約75〇乞的水準 $ 將原料傳遞到烺燒爐。或者，來自煅燒爐的氣體可以在單獨^ 預熱器中被冷卻到約60(TC，在此溫度水準，形成沉積物的風 險大大減小，且氣體被送到用於產生電力的蒸汽鍋爐。無二 化碳的可燃氣體的第二部分可以被引導到單獨的熱交換器在 熱交換器裏，通過與原料直接進行熱交換，氣體從約6〇°〇t>c的 φ水準冷卻到南於氣體的水露點溫度。單獨的熱交換器中的原料 可以由如前所述的以有機物質含量高為特徵的備選原料組 ，。氣體可以從單獨的熱交換器被送到用於去除硫化氫和硫化 氣的特定過濾器和氣體洗滌器（scrubber)，且氣體隨後被用 在氣體發動機、燃料電池或其他裝置中產生電力。或者，可燃 氣體可用作用於製造液體燃料的所謂的合成氣（syngas) 成氣體（synthesis gas))。來自單獨的熱交換器的原料可二 與分別來自預熱器和來自單獨預熱器的原料一起被送到煅燒 爐。 201022182 為讓本發明之實施例的上述特徵和優點能更明顯易懂，下 文特舉實施例，並配合所附圖式，作詳細說明如下。 【實施方式】 圖1和圖2示出根據本發明的用於原料的熱處理的設備的 兩個實施例。 在圖1中示出了用於煅燒原料的設備，其中原料經由入口 γ被引入到預熱器1，且隨後經由管道丨〗被送到第二預熱器5, 遠第二預熱器5經由入σ 27接收原料且經由入口 25接收氧 氣。原料在預熱器5中被锻燒，且一些經煅燒的原料經由管道 3」被送去作進-步的處理，而經锻燒的原料的剩餘部分經由 β道12被送到氣化反應器3，該氣化反應器3還經由入口 15 被供給燃料且經由入口 16被最終供給蒸汽。來自氣化反應器 3的含有焦油的可燃氣體經由管道1?被引導到預熱_】，在預 =器1裏’在經由人口 32供應空氣的條件下，可燃氣體被燃 燒，且來自預熱器1的冷卻氣體經由出口 10被傳遞去作進一 步處理。-些冷部的含有二氧化碳的氣體從預熱器$經由管道 29被引導走，以便進行進_步處理。來自氣化反應器3的經 參锻燒的原料和固體燃料殘渣經由管道13被傳遞，再經由管道 =以懸絲來自賴H 5的被再彳純的含有二氧化碳的氣體 中的方式，被傳遞回預熱器5。 圖2中不出了用於製造水泥熟料的設備，其中水泥生料經 $ = 口 9被引入到預熱器！，且隨後經由管道u被傳遞到煅 、’祕燒爐2經由人p 25被饋人氧氣。—些水泥生料 ,$管?31、被從锻繞爐2送到迴旋窯（rotary kiln) 8，在迴 =、、、8裏匕被燃燒為熟料，該熟料經由出口 33提取出。經煅 的水泥生料的嶋部分經由管道^被制氣化反應器3， 201022182 該氣化反應器3經由入口 15接收燃料且最終經由入口 16接收 蒸汽。來自氣化反應器3的含有焦油的可燃氣體經由管道17、 且來自氣化反應器3的經烺燒的水泥生料和固態燃料殘渣經 由管道13，共同被引導到二氧化碳吸收器4。包含在可燃氣體 中的二氧化碳與水泥生料中的氧化鈣產生反應而形成碳酸 鈣，該碳酸鈣與來自氣化反應器3的其他固態材料一起經由出♦ The amount of available waste heat used to generate electricity is insufficient and the conversion efficiency is low. _Before the hot gasification gas is used by a gas engine or other device for generating electricity, the tar substance must be removed from the hot gasification gas. The gasification gas typically contains carbon dioxide that reduces the calorific value of the gas. SUMMARY OF THE INVENTION It is an object of the present invention to provide a method and apparatus for eliminating or significantly reducing the above problems and disadvantages. According to the present invention, the object of the present invention is characterized by the method mentioned in the above description, characterized in that at least a part of the hydrogen-containing combustible gas is used for heat-treating the raw material. By using a combination of gasification technology and OEC technology, due to the fact that hydrogen-containing combustible gases can be used as fuel for supplying air, for preheating raw materials and/or for burning cement clinker in smoked, It can reduce carbon monoxide emissions from cement plants and minerals by more than 50%. The combustion gas substantially containing nitrogen and steam after being cleaned by the prior art can be discharged into the air. The solid fuel residue from the gasification reactor consists essentially of carbon which can be used as a fuel in a calciner, for example under conditions of supply of pure oxygen, thereby providing a concentrated stream of hot carbon dioxide, Heat 6 201022182 The carbon dioxide stream can be used to preheat the feedstock or to lift the steam, which is then compressed and extracted from the plant for storage in the ground or further processed. At the same time, fractional distillation of fuel makes it possible to completely replace fossil fuels with alternative fuels' and the fractionation of fuels eliminates and reduces the need for pre-treatment of alternative fuels. The flammable gas of 曰3 hydrogen may contain most of the monthly bl contained in the original fuel. It is assumed that as described above, the solid fuel residue can be used to meet the energy requirements of calcination and the calcination demand for calcination constitutes an important part of the total energy demand, which may result in excess of the hydrogen-containing combustible gas. This gas can be used to generate electricity in a gas engine, fuel cell or other device, thereby increasing the potential of the plant to generate electricity, in conjunction with the utilization of waste heat based utilization. According to the present invention, excess flammable gas can be extracted from the gasification reactor, and the hydrogen-containing flammable gas is cooled by direct heat exchange with the colder raw material in a separate heat exchanger, thereby causing all tar The substance is condensed on the surface of the raw material. The material thus heated can then be further heated and the raw material is calcined in a separate preheater system using solid residue from the gasification reactor under supply of pure oxygen. Therefore, the tar substance condensed on the raw material is also burned. A notable feature of the present embodiment of the present invention is that the raw material is in contact with the combustible gas, i.e., reducing air, during the heat exchange process. Thus, volatile organic matter, which may constitute a discharge problem during conventional preheating, will increase the amount of combustion gases. This makes it possible to deal with so-called alternative raw materials which are characterized by a high content of organically bound components (organicallyb〇undele_t). The resulting tar-free and cooled combustible gas can then be treated using prior art methods to remove particulates and undesirable components such as sulfurized gas and gasification. The hydrogen-containing combustible gas extracted from the gasification reactor is used to heat the raw material before the heat treatment of 7 201022182 'the hydrogen-containing combustible gas may first be contacted with the fully or partially calcined raw material at a temperature at which tar cracking can occur, and It is then contacted with the fully or partially calcined starting material at a temperature at which recarbonisation can occur. It is known in the art that certain materials, especially calcined materials such as oxidized ships, have a catalytkal effect on tar cracking. The tar cracking reaction typically occurs at a reasonable temperature above 75 〇〇c, while the recarburization reaction of the calcined cement raw meal occurs at a temperature ranging from about 55 〇〇c to about 65 ° C. This temperature range, the carbon dioxide contained in the combustible gas, can react with the oxidized feed in the feedstock. Therefore, carbon dioxide can be removed from the combustion ® gas while the heat value of the gas increases. The calcined feedstock for absorbing carbon dioxide may be comprised of a solid material comprising a fuel residue extracted from the gasification reactor, which is then recycled to the calciner. The dilution of the fuel in the gasification reactor, and thus the amount and composition of the hydrogen-containing combustible gas, depends on the temperature of the preheated feedstock, which temperature should be at least 500 ° C, and preferably at least 800 ° C . In a preferred embodiment of the plant for heat treating cement raw meal according to the present invention, for example, in a "moving bed" reactor, or in a rotating drum In a cyclone (CyCl〇ne) or other gas-slid contactor, the solid fuel and/or liquid fuel will be completely or partially burned at a temperature of approximately 850 ° C in the presence of steam. The cement raw material is contacted. The combustible gas thus produced is extracted from the gasification reactor via the gas outlet, and the solid material, that is, the calcined cement, is extracted from the gasification reactor via the solid outlet at a temperature of about 600 ° Raw material, fuel ash, char and final metal particles. It is assumed that carbon dioxide can be extracted from calcined cement raw meal in the form of calcium carbonate at a temperature close to 600 ° C. Will be contacted in the carbon dioxide absorber with the solid material extracted from the gasification reactor, which may for example also be a "mobile machine, a 'reactor,' or Yes or other gas-solid contactors. < Some carbon dioxide-free combustible gases from the carbon dioxide absorber are directed to the rotary kiln burner for burning off water, clinker, and The hot kiln gas can be transferred to the preheater for preheating the feedstock to a temperature level of about 75. The feedstock can be sent from the heater to the calciner in the calciner. Under the condition of supplying pure oxygen, the solid material from the & actor can be used as a fuel. Before the solid material from the gasification reactor is used as a fuel, the solid material can be crushed and screened, so that the most = ® metal particles are separated and large particle charred particles are reduced in size. From the calciner = gas containing carbon dioxide can be directed to a separate preheater, in a similar manner, in a pre-processor The material is heated to a level of about 75 $ to transfer the material to the crucible furnace. Alternatively, the gas from the calciner can be cooled in a separate preheater to about 60 (TC, at this temperature level, forming a deposit. The risk is greatly reduced, The gas is sent to a steam boiler for generating electricity. The second portion of the carbon-free combustible gas can be directed to a separate heat exchanger in a heat exchanger for direct heat exchange with the feedstock, from about 6 The φ level of 〇°〇t>c is cooled to the water dew point temperature of the gas. The raw material in the separate heat exchanger can be selected from the group of alternative raw materials characterized by high organic matter content as described above. From a separate heat exchanger is sent to a specific filter and gas scrubber for removing hydrogen sulfide and sulfur gas, and the gas is then used to generate electricity in a gas engine, fuel cell or other device. Alternatively, the combustible gas can be used as a so-called syngas gas for producing a liquid fuel. The feedstock from the separate heat exchanger can be sent to the calciner together with the feed from the preheater and from the separate preheater, respectively. The above features and advantages of the embodiments of the present invention will become more apparent and understood. [Embodiment] Figs. 1 and 2 show two embodiments of an apparatus for heat treatment of a raw material according to the present invention. An apparatus for calcining a raw material is shown in Fig. 1, in which a raw material is introduced into a preheater 1 via an inlet γ, and then sent to a second preheater 5 via a pipe, a far second preheater 5 The feedstock is received via sigma 27 and oxygen is received via inlet 25. The raw material is calcined in the preheater 5, and some of the calcined raw material is sent through a pipe 3" for further processing, and the remaining portion of the calcined raw material is sent to the gasification reaction via the β-channel 12. The gasification reactor 3 is also supplied with fuel via an inlet 15 and is finally supplied with steam via an inlet 16. The tar-containing combustible gas from the gasification reactor 3 is guided to the preheating via the pipe 1?, in the pre-charger 1, under the condition that the air is supplied via the population 32, the combustible gas is burned and comes from the preheating The cooling gas of the device 1 is passed through the outlet 10 for further processing. - Some of the cold part of the carbon dioxide containing gas is directed from the preheater $ via line 29 for further processing. The ginseng-fired feedstock and solid fuel residue from the gasification reactor 3 are transferred via line 13 and passed through a conduit = a re-purified carbon dioxide-containing gas from H5. Return to the preheater 5. Figure 2 shows the equipment used to make cement clinker, where the cement raw meal is introduced into the preheater via $ = port 9! And then transferred to the calcination via the pipe u, the secret furnace 2 is fed with oxygen via the person p25. Some cement raw materials, $tube 31, are sent from the forging furnace 2 to the rotary kiln 8, which is burned to clinker in the back =, ,, and 8, and the clinker is extracted through the outlet 33. . The helium portion of the calcined cement raw meal is passed through a conduit to a gasification reactor 3, 201022182. The gasification reactor 3 receives fuel via inlet 15 and ultimately receives steam via inlet 16. The tar-containing combustible gas from the gasification reactor 3 is collectively guided to the carbon dioxide absorber 4 via the pipe 17, via the pipe 17, and the calcined cement raw meal and solid fuel residue from the gasification reactor 3. The carbon dioxide contained in the combustible gas reacts with the calcium oxide in the cement raw meal to form calcium carbonate which is passed through together with other solid materials from the gasification reactor 3.
口 14，再經由管道24以懸浮於來自預熱器5的被再循環的包 含二氧化碳的氣體中的方式，被傳回煅燒爐2。一些無二氧化 碳的可燃氣體經由管道18從二氧化碳吸收器4被引導到迴旋 窯8 ’在迴旋窯8裏’在經由入口 32供給空氣的條件下，該 可燃氣體被燃燒。窯氣（kiln gas)經由管道30被從迴旋熏§ 引導到預熱器1 ’冷卻氣體經由出口 10從該預熱器1提取出。 無二氧化碳的可燃氣體的剩餘部分經由管道被引導到預熱 參 器6,該預熱器6經由入口 20被饋入冷水泥生料。被這樣預 熱的水泥生料經由管道21被送到煅燒爐2，而來自預熱器6 的冷卻的無焦油且無二氧化碳的可燃氣體經由管道22被引導 到用於去除顆粒、硫化氫、硫化氣和汞的氣體清潔單元7,且 隨後經由出π 23傳劇儲存處或被被用於在氣體發動機（娜 engine)、燃料電池（fuelcell)或其他裝置中產生電力。包含 二氧化碳的氣體從煅燒爐2經由管道26被引導到預熱器1 3 該預熱器5經由人σ 27接收水泥生料。來自預熱器]、、的預敎 原料經由管道28被送到煅燒爐2。包含二氧化碳的部分^ 經由管道29被從預熱器5送到蒸汽鍋爐34或用於 類似裝置’且隨後經由出口 35提取出以用於進力的 含二部分經由管道24再循環到锻燒爐2且 雖然本發月已以實施例揭露如上，然其並非用以限定本發 11 201022182 明’任何㈣此技藝者’在*麟本發明之精神和範圍内，a 可作些許之更動與潤飾，因此本發明之保護範圍當 : 請專利範圍所界定者為準。 无附之申 【圖式簡單說明】 圖1為根據本發明的用於原料的熱處理的設備所示出的 實施例的示意圖。 圖2為根據本發明的用於原料的熱處理的設備所示出的另一 個實施例的示意圖。 【主要元件符號說明】 ❹ 1、5、6:預熱器 2 :煅燒爐 3:氣化反應器 4:二氧化碳吸收器 7:氣體清潔單元 8 :迴旋窯 9、 15、16、20、27、25、32 :入口 10、 14、23、33、35 :出口 φ n、12、13、17、18、19、2卜 22、24、26、28、29、30、 31 :管道 34 :蒸汽鍋爐 12The port 14 is then passed back to the calciner 2 via a conduit 24 in a manner suspended in a recycled carbon dioxide-containing gas from the preheater 5. Some of the carbon dioxide-free combustible gas is directed from the carbon dioxide absorber 4 via line 18 to the rotary kiln 8' in the rotary kiln 8 where the combustible gas is combusted under the condition that air is supplied via the inlet 32. The kil gas is guided from the swirling smoke to the preheater 1 via the pipe 30. The cooling gas is extracted from the preheater 1 via the outlet 10. The remainder of the carbon dioxide free combustible gas is directed via conduit to the preheating ginseng 6, which is fed into the cold cement raw meal via inlet 20. The cement raw material thus preheated is sent to the calcining furnace 2 via the pipe 21, and the cooled tar-free and carbon dioxide-free combustible gas from the preheater 6 is guided via the pipe 22 to remove particles, hydrogen sulfide, vulcanization. The gas and mercury gas cleaning unit 7 is then used to generate electricity in a gas engine, fuel cell or other device via a π 23 transfer store. The gas containing carbon dioxide is directed from the calciner 2 via line 26 to the preheater 1 3. The preheater 5 receives the cement raw meal via the human σ 27 . The raw material from the preheater is sent to the calciner 2 via the line 28. The portion containing carbon dioxide is transferred via line 29 from the preheater 5 to the steam boiler 34 or for a similar device 'and then extracted via the outlet 35 for the two parts of the feed for recirculation to the calciner via line 24 2 and although the present disclosure has been disclosed above by way of example, it is not intended to limit the scope of the present invention to any of the present inventions. Therefore, the scope of protection of the present invention is as follows: The scope defined by the patent scope shall prevail. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 is a schematic view showing an embodiment of an apparatus for heat treatment of a raw material according to the present invention. Figure 2 is a schematic illustration of another embodiment of an apparatus for heat treatment of a feedstock in accordance with the present invention. [Description of main components] ❹ 1, 5, 6: Preheater 2: Calciner 3: Gasification reactor 4: Carbon dioxide absorber 7: Gas cleaning unit 8: Rotary kiln 9, 15, 16, 20, 27, 25, 32: inlets 10, 14, 23, 33, 35: outlets φ n, 12, 13, 17, 18, 19, 2, 22, 24, 26, 28, 29, 30, 31: pipe 34: steam boiler 12