201105909 六、發明說明： 【發明所屬之技術領域】 本發明係關於一種用於處理灰分、尤其適用於自粉塵 相鋼爐内（例如在能量生產廠及其類似者中）化石燃料之 燃燒或其與CDR或生質共同燃燒所獲得之輕灰分的設備及 方法〇 【先前技術】 控制輕灰分在水泥及混凝土生產令之使用的現行法律 對其粒度分析及其未燃燒物質之含量百分比加以限制。確 定及施加極限值以便不會改變所獲得之最終產物之特徵。 為生產水泥，有必要利用大量自然資源，尤其是石灰 石及火山灰，其由特定礦坑獲得。使混入其他礦物組分中 之石灰石及火山灰在水泥廠之爐中燃燒，獲得水泥熟料， 其經適當研磨變成真正的水泥。 生產一噸熟料產生約一噸c〇2。可添加未燃燒物質百分 比低於5重量％且品質優良之輕灰分至水泥熟料中直至百 分比為30%»藉由進行此替代，每年可減少數百萬噸 在鍋爐内由固體燃料產生之輕灰分中存在的未燃燒2物 質百分比會視所用燃料之骟剞、盘斗租/1201105909 VI. INSTRUCTIONS OF THE INVENTION: TECHNICAL FIELD OF THE INVENTION The present invention relates to a process for treating ash, particularly for combustion of fossil fuels in a dust-phase steel furnace (for example, in an energy production plant and the like) Apparatus and method for light ash obtained by co-combustion with CDR or biomass [Prior Art] The current law governing the use of light ash in cement and concrete production orders limits its particle size analysis and the percentage of unburned material. The limit values are determined and applied so as not to change the characteristics of the final product obtained. In order to produce cement, it is necessary to use a large amount of natural resources, especially limestone and volcanic ash, which are obtained from specific pits. The limestone and volcanic ash mixed into other mineral components are burned in a furnace of a cement plant to obtain cement clinker which is appropriately ground to become a real cement. The production of one ton of clinker produces about one ton of c〇2. Adding less than 5% by weight of unburned material and good quality light ash to cement clinker up to a percentage of 30%» By replacing this, millions of tons of light produced by solid fuel in the boiler can be reduced annually The percentage of unburned 2 substances present in the ash will depend on the fuel used, and the rent of the bucket / 1
燃現東略時突出。在該等狀況下， 』丹在採用所謂「低Ν〇χ 發生殘碳之熱失活過裎 6 201105909 此由“曝露所決定。實際上，在輕微氧化性條件（不铁 甚至為還原性條件）下該高溫曝露表示〜 化過程及後續熱失活的條件。 促進殘… 解決輕灰分中未燃燒物質之問題的可能答案係以藉助 於輕灰分在燃燒室中之直接再循環來再燃燒—部分輕灰分 的方法為代表 '然@，關於再燃燒輕灰分及重灰分中特： 百分比之未燃燒物質的研究表明簡單的再燃燒過程顯二 有輕微成效，因為殘碳之熱失活使得在再燃燒階段之剩餘 反應性有同樣的極大降低。 【發明内容】 因此，本發明所提出且解決之技術問題為提供一種用 於處理輕灰分之設備及方法，其允許避免以上關於已知技 術所提及之缺陷，且詳言之允許以有效但低成本之方式實 質上降低輕灰分中存在之未燃燒物質的含量，從而允許該 輕灰分本身在工業用途中且尤其在水泥及混凝土生產中之 後續重要的再利用。 該問題係藉由如申請專利範圍第1項之設備及如申請 專利範圍第22項之方法來解決。 本發明之較佳特徵存在於隨附申請專利範圍中。 本發明提供一些重要的優點。主要優點在於以下事 實·其成功克服了上述已知技術方法之缺陷，因為其允許 幸至灰分發生重要的再活化且因此使其中含有之碳在後續再 進入之鍋爐中發生廣泛轉化。 詳言之，本發明達成： 201105909 -大幅降低輕灰分中未燃燒物質&含量，從而藉由提高 其品質且使其由廢料轉化成再售產品而為原始工廠（例如 發電廠）之處置公司即使就未處理廢料堆而言亦獲得巨大 收益； 由疋為排出物之廢料轉化成可用於水泥及混凝土 行業t之原料且因此減少在水泥自身之生產過程中釋放到 環境中之c〇2獲得的環境優勢。 若與W〇2G06/GG5574 (其以引用方式併人本文中）中 所說明之再循環系統相聯繫，則本發明藉由在此情況下成 功實現僅有高品質之輕灰分作為燃燒之唯—產物而尤其有 利。 【實施方式】 藉由概述下文所示之較佳具體實例之實施方式來提供 一種使輕灰分中存在之未燃燒物質再活化及使該物質在燃 燒至中再循環直至結束氧化如此活化之碳之過程的系統。 建議使用之系統主要由以下構成： _ 一系統，其用於收集自用於處理排至煙道中之前的燃 燒煙霧之設備輸出之輕灰分（在用於處理燃燒煙霧之靜電 集塵器存在下）’該回收系統僅連接至具有未燃燒物質含量 較高之灰分的分離器區域； -一可能之濃縮設備，其用於濃縮該具有較高含量未燃 燒物質之灰分，若存在用於處理燃燒煙霧之機械過濾系統 則尤其有利； -一裝置/設備’其用於該灰分之再活化，視再活化過 8 201105909 程疋連續或間斷進行而定，該設備可由以下組成： -一封裝於一金屬密封容器中之金屬輸送機，在其 輸送帶上形成流體床或固定床，或 -一具有相同功能之儲存槽； -用於將熱空氣饋送至該再活化裝置/設備之構件及用 於自該再活化裝置/設備進行抽吸且處理所抽吸之空氣的 件； _ 一可能之管路，其連接於該再活化裝置/設備與用於 處置該再活化過程下游之空氣的煙霧管路之間； _ 一系統，其用於將經處理之灰分輸送至燃燒室； _ 一調節控制系統，其能確保該等操作自動進行，其將 於下文中在操作描述部分中描述。 才據X舉例方式但無限制意圖而展示的一些具體實例 之以下實施方式，本發明之其他優點、特徵及應用模式將 變得顯而易知。下文將參考附隨圖式之各圖。 首先參考圖丨，用於再活化輕灰分，旨在使輕灰分在產 ’、…燒至中再循環以便降低該輕灰分中未燃燒物質之 總含量的設備整體以1表示。 厂、s X備1且其將被描述為整合於基於化石燃料之 燃燒及/或其與CDR或生質之共同燃燒的生產能量之工廠 100 (例如發電礙）中。 工廠⑽以已知方式包含上述燃燒室（以1〇1表示） 且例如由粉塵相型鍋爐構成。 鋼爐101還以p左七4、土 ^已知方式連接至具有獨立環境之空氣/煙 霧交換器102，复&户、人欠„ /、在冷部该1辰境且詳言之帶有煙霧側104It is prominent when it burns out. Under these conditions, "Dan is using the so-called "low-lying heat-depleting heat" 6 201105909 This is determined by "exposure." In fact, this high temperature exposure under mild oxidative conditions (no iron or even reducing conditions) indicates conditions for the deuteration process and subsequent thermal deactivation. Promote the disability... The possible answer to the problem of solving unburned substances in light ash is to re-burn by direct recycling of light ash in the combustion chamber - part of the light ash is represented by 'Ran @, about reburning light ash and Heavy ash: A study of the percentage of unburned materials indicates that the simple reburning process is slightly effective because the residual heat of the residual combustion has the same significant reduction in residual reburning. SUMMARY OF THE INVENTION Accordingly, the technical problem proposed and solved by the present invention is to provide an apparatus and method for processing light ash that allows to avoid the above-mentioned drawbacks mentioned with respect to the known art, and in detail allows for effective but The low cost approach substantially reduces the amount of unburned material present in the light ash, thereby allowing the light ash itself to be subsequently reused in industrial applications and especially in cement and concrete production. This problem is solved by the apparatus of claim 1 and the method of claim 22 of the patent application. Preferred features of the invention are found in the scope of the accompanying claims. The present invention provides some important advantages. The main advantage lies in the fact that it succeeded in overcoming the drawbacks of the above-mentioned known technical methods, since it allows for the re-activation of the ash to be important and thus the conversion of the carbon contained therein in the subsequent re-entry of the boiler. In particular, the present invention achieves: 201105909 - A disposal company that initially reduces the amount of unburned matter & in light ash, thereby improving the quality and converting it from scrap to resale product to the original factory (eg, power plant) Even if it does not deal with waste piles, it also gains huge benefits; because the waste material for the discharge is converted into raw materials that can be used in the cement and concrete industry, and thus reduced in the production of cement itself, Environmental advantage. In connection with the recycling system described in W〇2G06/GG5574 (which is incorporated herein by reference), the present invention is successful in achieving only the high-quality light ash in this case as the only combustion- The product is especially advantageous. [Embodiment] An embodiment of a preferred embodiment shown below is provided to provide a method for reactivation of an unburned material present in a light ash and recycling of the substance to the end of combustion until the end of oxidation of the thus activated carbon The system of the process. The recommended system consists essentially of the following: _ A system for collecting light ash from the output of equipment used to treat combustion fumes before discharge to the flue (in the presence of an electrostatic precipitator for treating combustion fumes) The recovery system is only connected to a separator zone having a higher ash content of unburned matter; - a possible concentrating device for concentrating the ash having a higher content of unburned matter, if present for treating combustion fumes A mechanical filtration system is particularly advantageous; - a device/equipment' for the reactivation of the ash, depending on whether the reactivation has been carried out continuously or intermittently, the device may consist of the following: - a package sealed in a metal a metal conveyor in a container forming a fluid bed or a fixed bed on its conveyor belt, or a storage tank having the same function; - means for feeding hot air to the reactivation device/equipment and for Reactivation device/device for pumping and processing the aspirated air; _ a possible conduit connected to the reactivation device/equipment and for disposal Between the smoke lines of the air downstream of the reactivation process; a system for delivering the treated ash to the combustion chamber; _ an adjustment control system that ensures that the operations are automated, as will be described below Described in the operation description section. Other advantages, features, and modes of application of the present invention will become apparent from the following detailed description of the <RTIgt; Reference will now be made to the accompanying drawings. Referring first to the drawings, the apparatus for reactivation of light ash, which is intended to recirculate light ash in production, to reduce the total content of unburned substances in the light ash, is indicated by 1. The plant, s X, 1 and which will be described as being integrated into a plant 100 (e.g., power generation) based on the combustion of fossil fuels and/or its co-combustion with CDRs or biomass. The plant (10) comprises the above described combustion chamber (indicated by 1〇1) in a known manner and consists, for example, of a dust phase type boiler. The steel furnace 101 is also connected to the air/smoke exchanger 102 with independent environment in the manner of p left VII, soil, and the households and people owe „ /, in the cold part of the 1st and the detailed belt Smoke side 104
[S 201105909 及相應的冷卻空氣側l〇3。 交換器H)2還以已知方式在煙霧侧1〇4上連接 系統1〇5,其旨在自流動物中排出其令所夹帶之揮發性灰I 之煙霧。在本發明實施射，該過㈣統為靜電 : 其具有7個出口區段，纟中之—例如以1〇6表示。 自裝置1G5之過爐區段輸出之_部分輕灰分，且詳山 之落於頭三個區段上之一部分輕灰分係藉助於亦為吾人： 知的工廠UK)之灰分輸送管、線1〇8饋送至用於儲存 之裝置107。 為簡單性起見，未圖示工廠1〇〇之其他（已知）單元 (例如煙霧輸出煙道）且將不對其另作描述。 仍參考圖1且跟隨收集、再活化及再循環輕灰分之流 程，本發明具體實例之設備丨首先包含用於收集已沈積： 靜電集塵器105之後四個區段中之輕灰分的構件。在本發 明實施例中，該收集構件因而提供四個專用收集管線，每 一者對應於每一區段且分別以參考數字2丨〇至24〇表示。 因而，本發明具體實例之系統被組態為與主要管線 有偏離（deviation)，以輸送靜電集塵器之該區段處自燃燒 室輸出之輕灰分，該輕灰分典型地具有高含量未燃燒物 質。眾所周知，實際上’集塵器之後面區段具有此特徵之 灰分。無論如何，一般而言，對設計過程中各段灰分之收 集及分析允許以簡單且確定之方式根據具體情況測定靜電 集塵器之哪些區段或區域必須連接至上述收集管線。 返回至對本發明具體實例之描述，上述專用收集管線 210至240彙集至一條共同管線2，後者與用於饋送輸送空 201105909 氣之構件（通常以3表示）連通。基於一個較佳具體實例， 有可能在正壓力下或在藉助於專用排氣機之抽吸下，藉由 使用該構件之推力將管線2連接至工廠1〇〇之上述主要回 故管線108，如圖1中示意性顯示。 共同管線2又彙集至用於輸送灰分之另一管線4,其相 對於自集塵器105中抽取之灰分之主要流動方向在管線2 中之流動的上游及下游，具有用於調節及/或截止流量之第 一及第二構件，分別以41及42表示》詳言之，輸送管線4 在與第一調節及/或截止構件41鄰接之第一端處連接至工 廠1〇〇的流入儲存裝置107中之輕灰分之主要輸送管線 1〇8。相反，位於管線2中之流動及第二調節及/或截止構件 42下游的官線4之另一端連接至用於分離灰分之裝置5(例 如旋風型裝置）之人口，該裝置易於使輸送空氣流與灰分 汾離且藉助於出口管線6將該空氣饋送至工廠1〇〇之主要 輸送s線108 ’其中該出口官線6較佳亦裝備有調節及/或 截止構件61。 田然，裝置5還具有另一出口，其藉助於另一管線7 且在特疋情況下藉助於插入用於投料/饋料至流體床或固定 士型再活化裝f (整體以8表示）中之系統η (例如旋轉 早7L (r〇t〇Cell))饋送剩餘灰分。有利的S，饋送灰分至裝 置8中可連續進行。 在本發明具體實例中’再活化裝置8包含輸送帶Η， 個貫構該流體床或固定床且該輸送帶較佳具有複數 / (此。__)。輸送帶W封裝於外殼83中， 该外U3具有連接至用於饋送再活化熱^之構㈠[S 201105909 and the corresponding cooling air side l〇3. The exchanger H) 2 is also connected to the system 1〇5 on the smoke side 1〇4 in a known manner, which is intended to vent the fumes of the volatile ash I entrained from the flow. In the practice of the invention, the over (four) system is static: it has seven outlet sections, for example in the range of 〇6. Part of the light ash from the output of the furnace section of the 1G5, and the light gray ash of one part of the first three sections of the unit is also used by the ash unit of the factory: The crucible 8 is fed to the device 107 for storage. For the sake of simplicity, other (known) units of the factory 1 (e.g., smoke output flue) are not shown and will not be described otherwise. Still referring to Figure 1 and following the process of collecting, re-activating, and recycling the light ash, the apparatus of the present invention first includes means for collecting the light ash in the four sections after the electrostatic precipitator 105 has been deposited. In an embodiment of the invention, the collection member thus provides four dedicated collection lines, each corresponding to each segment and represented by reference numerals 2丨〇 to 24〇, respectively. Thus, the system of the specific embodiment of the present invention is configured to deviate from the main line to deliver light ash from the combustion chamber at the section of the electrostatic precipitator, which typically has a high content of unburned substance. It is well known that in fact the rear section of the dust collector has the ash of this characteristic. In any event, in general, the collection and analysis of the ash segments of the design process allows for the determination of which sections or areas of the electrostatic precipitator must be connected to the collection line in a simple and deterministic manner. Returning to the description of a specific example of the present invention, the above-described dedicated collection lines 210 to 240 are combined into a common line 2 which is in communication with a member (generally indicated at 3) for feeding the transport air 201105909 gas. Based on a preferred embodiment, it is possible to connect the line 2 to the above-mentioned main return line 108 of the factory 1 by using the thrust of the member under positive pressure or under suction by means of a dedicated exhaust. This is shown schematically in Figure 1. The common line 2 is again collected into another line 4 for transporting ash, which has upstream and downstream flow in the line 2 relative to the main flow direction of the ash extracted from the dust collector 105, for adjustment and/or The first and second members of the cut-off flow are indicated by 41 and 42 respectively. In detail, the transfer line 4 is connected to the inflow storage of the factory at the first end adjacent to the first regulating and/or closing member 41. The main conveying line 1 〇 8 of the light ash in the device 107. Conversely, the other end of the line 4 downstream of the flow in the line 2 and downstream of the second conditioning and/or shutoff member 42 is connected to a population of means 5 for separating ash, such as a cyclone type device, which facilitates the delivery of air The flow is separated from the ash and the air is fed to the main transport s line 108' of the factory by means of an outlet line 6 which is preferably also equipped with an adjustment and/or shut-off member 61. Tian Ran, the device 5 also has another outlet, which is by means of another line 7 and, in the special case, by means of insertion for feeding/feeding to the fluid bed or to a fixed-type reactivation device f (indicated by 8 in its entirety) The system η (for example, 7L (r〇t〇Cell)) feeds the remaining ash. Advantageously S, the feeding of ash into the apparatus 8 can be carried out continuously. In a particular embodiment of the invention, the 'reactivation device 8 comprises a conveyor belt, which is configured to have a fluid bed or a fixed bed and which preferably has a plurality / (here. __). The conveyor belt W is encapsulated in a casing 83, and the outer U3 has a structure for feeding reactivation heat (1)
Γ N J 11 201105909 於其不久將談到）的複數個側向開口 82，及—或多個位於 /連接至用於抽取再活化空氣之構件i“關於其不久 將談到）的開口 84。 輪送帶81可根據EP 〇 252⑹或Ep。93ΐ 98ι之教示 建構’其中該等文獻亦以引用方式併入本文中。 使裝置8與上述用於饋送再活化熱空氣之構件相聯 接’㈣件整體以9表示且具有複數個管線用於饋送該熱 二氣該複數個管線配置於輸送帶81之下且每一者對應於 相關外殼83之侧向開口 82。在本發明實施例中，該等管線 為六個，其分別以參考數字丨丨至16表示，且其每一者較佳 具有用於截止及/或調節流量之各別構件（其中之一例如以 121表示）。 由構件9饋送之空氣之溫度較佳包含在約3〇〇。〇至 500°C之範圍内。 該空氣可自外部環境收集且以希望之溫度引入特定交 換器（在本發明實施例中未示出）中，隨後在藉助於以i 〇 表示之風扇之情況下送至裝置8。較佳地，在可能時，裝置 8之入口處所必需之熱空氣係由離開空氣/煙霧交換器1 〇2 之預熱燃燒空氣之管線收集。 整個配置使由管線11至16饋送之熱空氣橫穿過位於輸 送帶81上之灰分層，從而穿過輸送帶81之專用狹槽且因 此根據灰分層之穿過速度建構固定床或流體床。 設備1及/或裝置8較佳併有用於控制輸送帶81上之灰 分之滯留時間的系統。或者，該滯留時間預先藉由該部分 之特定預配置來確定。 12 201105909 就再活化裝置8之一般操作原理而言，將如丁說明。 本發明之基本技術為藉助於一系列基本階段進行燃燒 開發。在碳燃燒之半詳細動力學機制的較簡單公式中，必 須考慮與以下反應有關之基本過程： (i) Cf + 〇2 _> C(O) (藉由對大氣氧之化學吸附作用來使碳形成氧化表面 複合物之反應） (ii) C(〇) + 〇2 C0、C〇2 + c⑼ (氧化表面複合物之交換反應），及 (!ϋ) C(O) CO ' C02 + Cf (伴Ik形成CO及C〇2之表面氧化物之解吸附反應）。 反應（111 )之氧化表面複合物之解吸附過程在中等溫度 下緩慢，在高溫下變得極快，此為碳燃燒系統所特有。 根據反應（i)，裝置8中進行之再活化處理促進未燃燒 之碳對氣流中可利用之氧的化學吸附。該化學吸附一旦達 成後，即保持穩定。根據反應（ii)及（⑴），在該方式下， 右未燃燒之碳應處於燃燒室之典型溫度條件下，則其將會 以相同的初始反應性燃燒，以便完成如此活化之碳之氧化 過程0 •因此，本發明之基本概念為使具有較高含量未燃燒物 質之揮發性灰分部分發生預氧化，隨後再進入燃燒室中， 目的在於使含有已廣彡氧化之碳的灰分再進入該燃燒室 中該預氧化可在約30(TC至500。〇之溫度下於實際上如裝 置^般之專用設備中以相對較快之動力學有效進行。當自 經較廣泛預氧化之木炭起始時，經如此預調節之灰分再進Γ NJ 11 201105909 will soon be referred to) a plurality of lateral openings 82, and/or a plurality of openings 84 located/connected to a member i for extracting reactivated air "as will be discussed shortly." The feed belt 81 can be constructed in accordance with the teachings of EP 〇 252 (6) or Ep. 93 ΐ 98 ι, wherein such documents are also incorporated herein by reference. The device 8 is coupled to the above-described member for feeding reactivated hot air. Represented by 9 and having a plurality of lines for feeding the hot digas, the plurality of lines are disposed below the conveyor belt 81 and each corresponding to a lateral opening 82 of the associated outer casing 83. In an embodiment of the invention, such The pipeline is six, which are denoted by reference numerals 丨丨 to 16, respectively, and each of which preferably has individual components for shutting off and/or regulating the flow (one of which is for example indicated at 121). The temperature of the air is preferably comprised in the range of about 3 Torr to 500 ° C. The air can be collected from the external environment and introduced into a specific exchanger (not shown in the embodiment of the invention) at a desired temperature. And then by means of The fan, i 〇 denoted, is sent to the device 8. Preferably, when necessary, the hot air necessary at the inlet of the device 8 is collected by a line of preheated combustion air exiting the air/mist exchanger 1 〇2. The entire configuration stratifies the hot air fed by lines 11 through 16 across the ash located on the conveyor belt 81 to pass through the dedicated slots of the conveyor belt 81 and thus construct a fixed bed or fluid bed depending on the traversing speed of the ash layer. Apparatus 1 and/or apparatus 8 preferably have a system for controlling the residence time of the ash on conveyor belt 81. Alternatively, the residence time is determined in advance by a particular pre-configuration of the section. 12 201105909 Reactivation device 8 The general operating principle will be described as follows. The basic technique of the present invention is to carry out combustion development by means of a series of basic stages. In the simpler formula of the semi-detailed dynamic mechanism of carbon combustion, the basics related to the following reactions must be considered. Process: (i) Cf + 〇2 _> C(O) (Reaction of carbon to form an oxidized surface complex by chemical adsorption of atmospheric oxygen) (ii) C(〇) + 〇2 C0, C〇 2 + c (Exchange reaction of oxidized surface complex), and (!ϋ) C(O) CO ' C02 + Cf (desorption reaction of surface oxides with Ik forming CO and C〇2). Oxidized surface of reaction (111) The desorption process of the complex is slow at moderate temperatures and extremely fast at elevated temperatures, which is unique to carbon combustion systems. According to reaction (i), the reactivation treatment in unit 8 promotes unburned carbon in the gas stream. Chemical adsorption of available oxygen. Once the chemical adsorption is achieved, it remains stable. According to reactions (ii) and ((1)), in this mode, the right unburned carbon should be at the typical temperature of the combustion chamber. It will burn with the same initial reactivity in order to complete the oxidation process of the carbon thus activated. 0. Therefore, the basic concept of the invention is to pre-oxidize the volatile ash portion with a higher content of unburned material and then enter In the combustion chamber, the purpose is to re-enter the ash containing the extensively oxidized carbon into the combustion chamber at a pre-oxidation of about 30 (TC to 500). The temperature at that temperature is effectively carried out with relatively fast kinetics in a dedicated device such as a device. When pre-adjusted ash is initiated from the more pre-oxidized charcoal
i S J 13 201105909 入鍋爐中可使將碳轉化成灰分之動力學更加迅速。 藉由以此方式進行，可克服使自碳形成氧化表面複合 物之過程在鍋爐中發生所存在的困難，該困難與穿過火焰 區域之灰分可利用之滯留時間極其有限的事實相關。 回顧對本文所研究之特定具體實例的描述，應瞭解， 外忒83上之熱空氣入口之位置及相對於輸送帶Μ介於下 部與上部區域之間所建立的壓力》允許空氣穿過輸送帶自 身及灰分層運送，從而改良空氣/灰分接觸且提高氧氣化學 吸附效率。 严亦將用於抽取已穿過輸送帶81上之灰分層之再活化空 氣的系統與裝置8相聯接。該整體以18表示之抽取裝置又 可聯接至提供於空氣抽吸管線2〇上之抽吸構件2〇1 :在連 接至引進裝置8中之上述管線7的情況下，除塵裝置”可 插入構件18與管線20之間以處置由$氣流分離之灰分。 *甚至在本文中最後介紹之管線之各者上，且詳言之在 管線2〇上以及在插入裳置18與除塵器19《間的管道及插 入除塵器19與管線7之間的f道上，可提供用於截止及/ 或調節流量之相應構件。 所抽取之空氣可自抽吸管線2〇饋送至工 管路以經由煙道排出，或直接饋送至大氣中或甚至 廠100之空氣箱中以用於燃燒室1〇1之入口。 再活化裝置 且配置於輸送帶 灰分流下游。 8具有主要排出位置85，其較佳具有料斗 81之末端，位於彙集於出口管線21上之 管線21可具有用於截止及/或調節流量之構件（例如在 201105909 水冷卻情況下之旋轉單元23)以提高其效能。最後，出口 :線彙集於最終輸送管線24上’後者較佳在中間燃燒 器平面之層面上且典型地藉助於氣動輸送下將再活化灰分 饋达至燃燒室1〇1。當然，該後一管線24亦可具有用於截 止及/或調節相關流量之各別構件。 上述關於將再活化灰分引進燃燒室中之位置的選擇係 由以下吊要所支配：允許在燃燒室十有足夠的滯留時間， 從而允許完成預處理之未燃燒物質的氧化，然後由燃燒煙 霧夾帶較輕粒子且彼等自燃燒煙霧夾帶中逸出之粒子藉由 重力作用降落於鋼爐底部。 圖3之具體實例因再活化裝置之不同構造而與適才描 述者不同，此處以80表示。該裝置80包含一儲存槽，其 藉助於再活化空氣流建構上述灰分流體床或固定床。裂置 80在典型情況下間斷工作。用於饋送再活化熱空氣之構件 9及在特定情況下用於建構必需推力以引進該空氣之構件 (例如壓力風扇10 )(完全類似於彼等已說明者）被聯接至 裝置80。 根據實質上類似於彼等已參考第一具體實例所描述之 模式的模式’裝置80提供與可能之除塵裝置19連通之上 部空氣出口。 裝置80進一步在類似於已描述之管線21的出口管線 211上提供下部灰分出口。 圖2之具體實例改為在以下方面不同於圖1:在已介紹 之裝置5與再活化裝置8之入口之間插入分級/分離裝置25 且在其下游彙集已介紹之除塵裝置19之粉末出口。i S J 13 201105909 Entering the boiler makes the kinetics of converting carbon into ash more rapid. By doing so, the difficulty in causing the process of forming an oxidized surface complex from carbon to occur in the boiler can be overcome, which is related to the fact that the residence time of the ash available through the flame region is extremely limited. Recalling the description of the specific examples studied herein, it should be understood that the location of the hot air inlet on the outer sill 83 and the pressure established between the lower and upper regions relative to the conveyor belt 》 allows air to pass through the conveyor belt. Self and ash layered transport to improve air/ash contact and increase oxygen chemisorption efficiency. The system for extracting the reactivated air that has passed through the ash layer on the conveyor belt 81 is also coupled to the apparatus 8. The extraction device, indicated generally at 18, can in turn be coupled to a suction member 2〇1 provided on the air suction line 2〇: in the case of the above-described line 7 connected to the introduction device 8, the dust removal device” insertable member Between 18 and line 20 to dispose of the ash separated by the $ gas stream. * Even on each of the pipelines described at the end of this article, and in detail on line 2〇 and between the insertion of the skirt 18 and the precipitator 19 The pipe and the channel between the plug-in precipitator 19 and the line 7 provide corresponding means for shutting off and/or regulating the flow. The extracted air can be fed from the suction line 2 to the line for passage through the flue. Discharged, or fed directly into the atmosphere or even to the air tank of the plant 100 for the inlet of the combustion chamber 101. The reactivation device is disposed downstream of the conveyor belt ash stream. 8 has a primary discharge location 85, which preferably has At the end of the hopper 81, the line 21 located on the outlet line 21 may have means for shutting off and/or regulating the flow (e.g., the rotating unit 23 in the case of water cooling in 201105909) to improve its efficiency. Finally, the outlet: line collection On the final transfer line 24, the latter preferably feeds the reactivated ash to the combustion chamber 1〇 on the level of the intermediate burner plane and typically by pneumatic transport. Of course, the latter line 24 can also be used. The individual components for the cut-off and/or adjustment of the relevant flow. The above selection of the location for introducing the reactivated ash into the combustion chamber is governed by the following cranes: allowing sufficient residence time in the combustion chamber to allow for the completion of the pre-fill The oxidation of the treated unburned material is then entrained by the combustion fumes with lighter particles and the particles escaping from the entrainment of the combustion smoke fall by gravity to the bottom of the steel furnace. The specific example of Figure 3 is due to the different construction of the reactivation device. Unlike the appropriate descriptor, here is indicated at 80. The apparatus 80 includes a storage tank that constructs the ash fluid bed or fixed bed by means of a reactivated air stream. The rupture 80 typically operates intermittently. a member 9 for activating hot air and a member for constructing the necessary thrust to introduce the air in a specific case (for example, a pressure fan 10) (completely similar to them) Illustrator) is coupled to device 80. The device 80 is provided in communication with a possible dust removal device 19 in accordance with a mode substantially similar to the mode that has been described with reference to the first embodiment. Device 80 is further similar The lower ash outlet is provided on the outlet line 211 of the line 21 which has been described. The specific example of Fig. 2 is instead different from Fig. 1 in the following aspects: insertion of a grading/separating device between the introduced device 5 and the inlet of the reactivation device 8 25 and downstream of the powder outlet of the dust removal device 19 already described.
E S 15 201105909 在配備用於調節/截止相關流量之構件且較佳連接至工 廠100之主要輸送管線108的情況下’分離裝置25被聯接 至具有低含量未燃燒物質之灰分出口管線26。 即使當主要工廠100具有機械型過濾系統（例如袋濾 式過濾器而非靜電集塵器）時，分離裝置25之存在亦尤其 重要。 實際上，如上文已提醒，已知在靜電集塵器中對相對 於煙霧行進方向在最後區域發現的具有高含量未燃燒物質 之灰分的選擇已可確定的是灰分電阻率與所含有之未燃燒 物質之百分比成正比。在改為進行機械捕集之過濾器中， 未發現此分離且未燃燒物質將基於所捕集之灰分的總流量 而被稀釋。在機械過濾系統之情況下，其因而導致可合理 提供未燃燒物質含量較高之灰分部分的濃縮相。因此，欲 再活化的未燃燒物質百分比較高之灰分之流量可允許最優 化鍋爐中再活化及再循環系統之尺寸。 圖4展示該不同的工廠組態，其中該袋濾式過滤器係 以109表示。在此情況下，自袋濾式過濾器丨〇9自身之每 一出口區段提供灰分饋料，在所圖示之實施例中為四段饋 料且分別以參考數字110至113表示。又，在所圖示之實施 例中’接著提供四個專用收集管線，分別以參考數字3〇至 33表示。 裝置25對具有較高含量未燃燒物質之灰分進行適當分 級，從而避免處理流量極大之輕灰分。該裝置25可為摩擦 電型、通風型（aeraulic )或等效型，其允許藉由將欲再活 化之灰分流與欲送至儲料倉107者分離而選出欲再活化之 16 201105909 灰分流。 如先前已提及，在太立去( 你不文考慮之所有具體實例中可提供 調節及控制系統，其能確保操作自動進行。 此時，應更好地瞭解到，根據上文說明之具體實例， 本發明提供-種用於回收、活化及在燃燒室中再循環由處 理煙霧之系統捕集之輕灰分的設備。 '應瞭解，若再活化空氣流量可與欲處理之灰分之流量 相當且無論如何降低，則如何處置欲處理之灰分下游的再 活化空氣及其自何處收集之選擇僅僅視工廢容易性要求而 定。此外，由於未燃燒物質之再活化必需之氧數量較少， 因此再活化空氣流甚至會被污染且具有由該過程產生之廢 熱，此使所提出之應用在投資及額外操作成本方面代價略 顯較高。 甚至應瞭解，灰分再活化未必藉助於其自用於過據燃 燒煙霧之系統的抽取，但原則上在其自燃燒環境抽取之後 的任何階段且在可能再進入該燃燒環境中完成燃燒之前發 生，例如在用於收集輕灰分之料倉下游。 此外，灰分輸送甚至可為機械型而非氣動型的，例如 可機械輸送灰分，其可自用於處理煙霧之系統輸出及部分 地輸送遠至燃燒室。 最後’應瞭解，本發明標的亦為一種較佳對應於上文 所述及以下申請專利範圍中所定義之設備及工廠之操作模 式而建構的再活化方法。 至此已藉由參考較佳具體實例來描述了本發明。應瞭 解可存在其他具體實例，其屬於如由隨附申請專利範圍 17 201105909 之保護範疇所界定的本發明之核心内容。 明 說 單 簡 式 圖 圖1展示併有本發明之再活化設備之第一較佳具體實 例的工廠（詳言之係指配備有電過濾器之工廠）之組態的 不意圖， 圖2展示相對於圖1組態之具體實例變型，其中提供 用於濃縮具有高含量未燃燒物質之灰分的預防性處理； 圖3展示併有本發明之再活化設備之第二較佳具體實 例的工廠（在此情況下亦係指配備有電過濾器之工廠）之 組態的示意圖；且 圖4展示併有圖2之再活化設備之具體實例變型的工 廠（詳言之係指配備有袋濾式過濾器之工廠）之組態的另 一示意圖。 【主要元件符號說明】 1 再活化設備或工廠 2 共同管線或空氣輔助輸送系統 3 用於饋送輸送空氣之構件 4 輸送管線或空氣輔助輸送系統 5 用於分離灰分之裝置 6 出口管線 7 管線 8 再活化裝置 9 用於饋送再活化熱空氣之構件 18 201105909 ίο 風扇 11 用於饋送再活化熱空氣之管線 12 用於饋送再活化熱空氣之管線 13 用於饋送再活化熱空氣之管線 14 用於饋送再活化熱空氣之管線 15 用於饋送再活化熱空氣之管線 16 用於饋送再活化熱空氣之管線 18 用於抽取再活化空氣之構件或抽取裝置 19 除塵裝置或除塵器 20 空氣抽吸管線 21 出口管線 23 旋轉單元 24 最終輸送管線 25 分級/分離裝置 26 具有低含量未燃燒物質之灰分出口管線 30 收集管線 31 收集管線 32 收集管線 33 收集管線 41 第一調節及/或截止構件 42 第二調節及/或截止構件 61 調節及/或截止構件 71 用於投料/饋料之系統 80 再活化裝置 輸送帶 19 81 201105909 8 2 側向開口 83 外殼 84 開口 85 主要排出位置 100 能量生產廠 101 鍋爐或燃燒室 102 空氣/煙霧交換器 103 冷卻空氣側 104 煙霧側 105 過濾系統或靜電集塵器 106 出口區段 107 儲存裝置或儲料倉 108 灰分輸送管線或主要回收管線或主要輸送管線 或輸送系統 109 袋濾式過濾器或過濾系統 110 灰分饋料 111 灰分饋料 112 灰分饋料 113 灰分饋料 121 用於截止及/或調節流量之構件 201 抽吸構件 210 收集管線 211 出口管線 220 收集管線 230 收集管線 240 收集管線 20E S 15 201105909 In the case of a main delivery line 108 equipped with means for regulating/cutting the relevant flow and preferably connected to the plant 100, the separation device 25 is coupled to an ash outlet line 26 having a low content of unburned material. The presence of the separation device 25 is especially important even when the main plant 100 has a mechanical filtration system (e.g., a bag filter instead of an electrostatic precipitator). In fact, as already reminded above, it has been known that the choice of ash having a high content of unburned material found in the last region relative to the direction of travel of the smoke in the electrostatic precipitator has been determined by the ash resistivity and the contained The percentage of burning matter is proportional. In a filter that was mechanically trapped instead, this separated and unburned material was not found to be diluted based on the total flow of the captured ash. In the case of a mechanical filtration system, it thus results in a condensed phase which can reasonably provide a higher ash content of unburned material. Therefore, the higher ash flow rate of the unburned material to be reactivated may allow for optimization of the size of the reactivation and recirculation system in the boiler. Figure 4 shows the different plant configuration, wherein the bag filter is indicated at 109. In this case, ash feeds are provided from each of the outlet sections of the bag filter cartridge 9 itself, in the illustrated embodiment, four segments of feed and are indicated by reference numerals 110 through 113, respectively. Again, in the illustrated embodiment, four dedicated collection lines are then provided, indicated by reference numerals 3A through 33, respectively. The apparatus 25 appropriately grades the ash having a higher content of unburned matter, thereby avoiding the treatment of a very light ash. The device 25 can be of the triboelectric, aeraulic or equivalent type, which allows for the selection of the ash shunt to be reactivated by separating the ash shunt to be reactivated from the one to be transferred to the silo 107. . As mentioned earlier, in Taili (you can provide adjustment and control systems in all specific examples, which ensure that the operation is carried out automatically. At this point, it should be better understood, according to the specifics described above By way of example, the present invention provides an apparatus for recovering, activating, and recycling light ash trapped by a system for treating smoke in a combustion chamber. 'It should be understood that if the reactivated air flow rate is comparable to the flow rate of the ash to be treated In any case, the choice of how to dispose of the reactivated air downstream of the ash to be treated and where it is collected depends only on the ease of work and waste. In addition, the amount of oxygen required for reactivation of unburned substances is less. Therefore, the reactivated air stream may even be contaminated and have waste heat generated by the process, which makes the proposed application slightly more expensive in terms of investment and additional operating costs. It should be understood that ash reactivation may not be self-contained by itself. Extraction from a system that burns smoke, but in principle at any stage after its extraction from the combustion environment and possibly re-entry into the combustion environment Occurs before combustion, for example downstream of a silo for collecting light ash. Furthermore, the ash delivery can even be mechanical rather than pneumatic, for example mechanically transporting ash, which can be used for system output for processing fumes and partly The delivery is as far as the combustion chamber. Finally, it should be understood that the subject matter of the invention is also a reactivation method preferably constructed corresponding to the mode of operation of the apparatus and plant as defined above and in the scope of the following claims. The invention has been described with reference to the preferred embodiments. It is understood that there may be other specific examples which are the subject matter of the invention as defined by the scope of protection of the accompanying application. A configuration of a factory showing a first preferred embodiment of the reactivation apparatus of the present invention (in detail, a factory equipped with an electric filter) is not intended, and FIG. 2 shows a specific configuration relative to FIG. An example variant in which a prophylactic treatment for concentrating ash having a high content of unburned material is provided; Figure 3 shows a reactivation of the invention A schematic diagram of a configuration of a second preferred embodiment of the plant (in this case also a factory equipped with an electric filter); and Figure 4 shows a factory with a specific example variant of the reactivation device of Figure 2 (In other words, a schematic diagram of the configuration of a plant equipped with a bag filter.) [Key component symbol description] 1 Reactivation equipment or plant 2 Common pipeline or air-assisted conveyor system 3 for feeding air Component 4 Transfer line or air-assisted delivery system 5 Device for separating ash 6 Outlet line 7 Line 8 Reactivation device 9 Member for feeding reactivated hot air 18 201105909 ίο Fan 11 for feeding reactivated hot air 12 for feeding reactivated hot air 13 for feeding reactivated hot air 14 for feeding reactivated hot air 15 for feeding reactivated hot air 16 for feeding reactivated hot air 18 Member or extraction device for extracting reactivated air 19 Dust removal device or dust collector 20 Air suction line 21 Outlet line 23 Rotating unit 24 Final Transfer Line 25 Fractionation/Separation Device 26 Ash Output Line 30 with Low Content Unburned Material Collection Line 31 Collection Line 32 Collection Line 33 Collection Line 41 First Adjustment and/or Cutoff Member 42 Second Adjustment and/or Cutoff Member 61 Adjustment and / or cut-off member 71 System for feeding / feeding 80 Reactivation device conveyor belt 19 81 201105909 8 2 Lateral opening 83 Housing 84 Opening 85 Main discharge position 100 Energy production plant 101 Boiler or combustion chamber 102 Air / Smoke exchanger 103 Cooling air side 104 Smoke side 105 Filtration system or electrostatic precipitator 106 Outlet section 107 Storage or storage silo 108 Ash transfer line or main recovery line or main transfer line or conveyor system 109 Bag filter Or filtration system 110 ash feed 111 ash feed 112 ash feed 113 ash feed 121 member 201 for shutting off and/or regulating flow rate suction member 210 collection line 211 outlet line 220 collection line 230 collection line 240 collection line 20