200944493 六、發明說明： 【明屬 發明領域 气技術領域】 【0001】 L月係有關於〜種水泥製造方法，特別是有關於一 種自水泥尾至最下段旋風器之㈣氣流路，從將燃 燒氣體之氣之氣體所含之灰塵將錯等重金屬類分 離之方法。200944493 VI. Description of the invention: [The field of gas technology in the field of invention] [0001] The L-month system has a method for manufacturing cement, especially for a (four) airflow path from the cement tail to the lowermost cyclone, which will burn The dust contained in the gas of the gas gas will be separated from the heavy metals.
10 發明背景 [0002] 習知，由於水泥中之鉛(Pb)固定化，而認為沒有溶析至 土壤。然而，隨著近年之水泥製造裝置之再利用資源之活 用里之增加，水泥中之鉛之量亦增加，正逐漸大幅超過目 15則之含有量。由於隨著濃度增加，亦有溶析至土壞之可能 性，故需將水泥中之鉛濃度減低至目前之含有量程度。 【0003】 又，近年來，推動廢棄物之水泥原料化或燃料化之再 利用，隨著廢棄物之處理量增加，帶入至水泥窯之氣、硫 20黃、鹼等揮發成份之量亦增加，氣旁路灰塵之產生量亦增 加。由於預料其產生量之増加或含有鉛之重金屬類之水泥 容許濃度之超過，故要求剩餘氣旁路灰塵之利用方法的開 發。 3 【0004】 200944493 鑑於上述點，於專利文獻1為將供給至水泥製造步驟之 廢棄物中之氣成份及鉛成份有效地分離去除，而揭示一種 廢棄物之處理方法，其具有廢棄物之水洗步驟、已過濾之 固態成份之鹼溶析步驟、從此濾液使鉛沉澱而分離之脫鉛 5 步驟、從已脫鉛之濾液使鈣沉澱而分離之脫鈣步驟、將此 濾液加熱，將氣化物析出而分離回收之氣回收步驟。 【0005】 又，專利文獻2記載一種廢棄物之處理方法，其具有從 飛灰等廢棄物將鉛及辞分類而去除時，將含有鈣離子之溶 1〇 液混合而獲得泥漿後，固液分離，而獲得含有鋅之固態成 份及含有鉛之水溶液之步驟、將硫化劑添加於含有鉛之水 溶液後，固液分離，獲得硫化鉛及含有鈣離子之溶液之步 程。 【0006】 15 再者，專利文獻3記載一種方法，其係為從在水泥製造 步驟產生之氣旁路灰塵等回收重金屬類，從水泥製造步驟 分離為含重金屬類灰塵’從該含重金屬類灰塵將水泥窯燃 燒氣體之一部份抽氣’將所抽氣之燃燒氣體所含之灰塵集 塵’而去除或回收從鉈、鉛、硒選擇之1個以上。 20 【0007】 【專利文獻1】日本專利公開公報2003-1218號 【專利文獻2】日本專利公開公報2003-201524號 【專利文獻3】日本專利公開公報2006-347794號 t發明内容3 200944493 發明揭示 發明欲解決之課題 【0008】 然而，在上述專利文獻記載之習知技術中，去除氯旁 5 路灰塵等所含之鉛等重金屬類，而經由氯旁路灰塵去除至 系統外之重金屬類之比例僅為全體之30%左右，舉例言 之，即使將氯旁路灰塵中之重金屬類去除1〇〇%，剩餘之70% 左右仍然進入至從水泥窯排出之熟料，故使水泥之重金屬 類含有率降低並不容易。是故，促進水泥窯内之重金屬類 10 之揮發，提高在氣旁路灰塵等之重金屬類之濃縮率為重要。 【0009】 舉例言之，重金屬類之揮發技術已知有氯揮發法及還 原揮發法。然而，當將一般進行之氯化揮發法應用於水泥 燒結步驟時，在水泥製造上，需投入遠超過一般之量之氯。 15 另一方面，由於應用還原揮發法，水泥之顏色呈黃色，故 在水泥之品質面造成問題。 【0010】 又，為提高重金屬類之揮發率，故亦有抑制水泥窯之 窯尾部之氧濃度，形成產生CO氣體之氣體環境，當因CO 20 氣體之產生，產生用於水泥窯之燃燒排氣之集塵用之電集 塵機***之危險，且有因CO氣體排出至系統外引起之環境 負擔之增加之虞。 【0011】 是故，本發明即是鑑於上述習知技術之問題點而發明 200944493 者，其目的係在不對水泥之品質造成影響下，確保水泥製 造裝置之安全性，且亦避免環境負擔之增加，而可以良好 效率從水泥製造步驟將重金屬類分離。 用以欲解決課題之手段 5 【0012】 本發明人等為達成上述目的，反覆致力研究之結果， 發現藉將碳成份含有率在預定值以上之可燃物投入至水泥 窯内，可在包含該水泥窯之燒結步驟内提高重金屬類的揮 發率。 10 【0013】 本發明即是根據此見解而發明者，其係將含有20質量 %以上之碳成份之可燃物供給至水泥窯之900°C以上、1300 °C以下之區域，從自該水泥窯之窯尾至最下段旋風器之窯 排氣路徑將燃燒氣體之一部份抽氣，將該燃燒氣體所含之 15 灰塵集塵，從所集塵之灰塵將重金屬類分離。此外，碳成 份係有助於燃燒之成份，可分離之重金屬類係鉛、辞、鎘、 録、砸、神、飽。 【0014】 當將上述可燃物投入至水泥窯之不到900°C之部份 20 時，在到達重金屬類以良好效率揮發之區域前，大部份便 燃燒，而難以充分提高重金屬類的揮發率，另一方面，當 投入至1300°C以上之部份時，水泥之顏色呈黃色，故在水 泥之品質面造成問題。藉於上述温度區域投入可燃物，可 有效地提高在水泥窯内之窯尾部之重金屬類的揮發率，而 200944493 藉利用氣旁路系統，提高在氯旁路灰塵之重金屬類的濃縮 率’可使水泥製造步驟之重金屬類去除率上升。 【0015】 5 Ο 10 15 在上述水泥製造方法中，在水泥窯之前述區域，可以 80%以上之揮發率使前述重金屬類揮發。 【0016】 又，在上述水泥製造方法中，令前述可燃物之碳成份 含有率為α質量％，令投入至前述水泥窯之含有前述碳成 份之可燃物量為熟料生產量每時，令召之積 為30以上、5000以下。當α及召之積不到30時，不易充分 提高重金屬類之揮發率，另一方面，當^:及点之積超過5〇〇〇 時’即使投入超過之碳成份’重金屬類之揮發率仍達至丨最 高’當以有價購入時，亦導致該可燃物之使用所需之成本 之增大，故並不實際。 【0017】 再者，在上述水泥製造方法中，從前述所扯氣之燃_ 氣體將灰塵集塵時，可使用乾式集塵機或濕式集& 【0018】 在上述水泥製造方法中’當將前述可燃物供給至水尸 窯之90(TC以上、130(TC以下之區域時，可使用蔣分 ^'琢可燃物 投入至水泥窯之窯尾、或在被以溫度分解之物皙治潘 貝包覆的狀 態下，投入至附設於前述水泥窯之預熱器，以丨用時門差 分解含碳物質，或者將前述可燃物從設置於水泥窝本體部 之入口直接投入至窯内之任一方法。 20 【0019】 200944493 又，在上述水泥製造方法中’令前述可燃物為從由焦 炭、煤焦油遞青、輪胎、煤、無煙煤、煙煤、褐炭、褐煤、 石墨、難燃性塑膠、酚醛樹脂、呋喃樹脂、熱硬化性樹脂、 5纖維素、木炭、廢調色劑、混合焦炭、細焦炭、電極碎片、 活性焦厌、碳化物及飛灰所含有之未燃碳構成之群選擇之1 個或2個以上。 【0020】 再者，可將前述可燃物以造粒或/及分粒進行粒度調整 10後，投入至前述水泥窯内。由於當可燃物為小徑時，因通 過窯之氣體而飛散至低溫側，故重金屬類在揮發溫度區域 之供給量減少，而無法確保有效率之揮發率。標準宜為當 令可燃物粒徑為dp，投入部之氣體風速為、時，從斯托克BACKGROUND OF THE INVENTION [0002] It is known that lead (Pb) in cement is immobilized and is not considered to be dissolved to soil. However, with the increase in the utilization of resources for reuse of cement manufacturing equipment in recent years, the amount of lead in cement has also increased, and it is gradually exceeding the content of the target. As the concentration increases, there is also the possibility of dissolution to the soil, so the concentration of lead in the cement needs to be reduced to the current level. [0003] In addition, in recent years, the recycling of cement raw materials or fuels has been promoted. As the amount of waste treatment increases, the amount of volatile components such as sulfur, sulfur, and alkali that are brought into the cement kiln is also Increased, the amount of gas bypass dust generated also increased. The development of a method for utilizing residual gas bypass dust is required because it is expected to exceed the allowable concentration of the cement added or the heavy metal containing lead. [0004] In the above-mentioned point, in Patent Document 1, the gas component and the lead component in the waste supplied to the cement manufacturing step are effectively separated and removed, and a waste disposal method is disclosed, which has a waste water washing. a step of separating the solid component of the filtered solid component, a step of deleaving separated from the filtrate by precipitation of the lead, a decalcification step of separating the precipitated calcium from the deleashed filtrate, heating the filtrate, and vaporizing the filtrate The gas recovery step of separating and recovering is carried out. Further, Patent Document 2 discloses a method for treating waste, which comprises removing a lead and a word from a waste such as fly ash, and mixing the solution containing calcium ions to obtain a slurry, and then solid-liquid. Separating, obtaining a solid component containing zinc and an aqueous solution containing lead, adding a vulcanizing agent to an aqueous solution containing lead, and separating the solid and liquid to obtain a step of obtaining lead sulfide and a solution containing calcium ions. Further, Patent Document 3 describes a method of recovering heavy metals from gas bypass dust generated in a cement manufacturing step, and separating from a cement manufacturing step into heavy metal-containing dust from the heavy metal-containing dust. One part of the combustion gas of the cement kiln is evacuated and the dust contained in the exhausted combustion gas is collected to remove or recover one or more selected from bismuth, lead and selenium. [Patent Document 1] Japanese Patent Laid-Open Publication No. 2003-1218 [Patent Document 2] Japanese Patent Laid-Open Publication No. 2003-201524 [Patent Document 3] Japanese Patent Laid-Open Publication No. 2006-347794 No. OBJECTS TO BE SOLVED BY THE INVENTION [0008] However, in the prior art described in the above-mentioned patent documents, heavy metals such as lead contained in five-way dust such as chlorine are removed, and heavy metals such as lead are removed to the outside of the system via chlorine bypass dust. The ratio is only about 30% of the total. For example, even if the heavy metals in the chlorine bypass dust are removed by 1%, the remaining 70% will still enter the clinker discharged from the cement kiln, so the heavy metal of the cement It is not easy to reduce the class content. Therefore, it is important to promote the volatilization of heavy metals in the cement kiln and to increase the concentration of heavy metals such as gas bypassing dust. [0009] For example, the volatilization technique of heavy metals is known as a chlorine volatilization method and a reduction volatilization method. However, when the generally used chlorination volatilization method is applied to the cement sintering step, it is necessary to invest a chlorine in a much larger amount than the usual amount in the manufacture of cement. 15 On the other hand, due to the application of the reduction volatilization method, the color of the cement is yellow, which causes problems in the quality of the cement. [0010] Moreover, in order to increase the volatilization rate of heavy metals, it is also possible to suppress the oxygen concentration in the tail portion of the kiln of the cement kiln to form a gas environment for generating CO gas, and when the CO 20 gas is generated, a combustion row for the cement kiln is generated. The dust collector used for dust collection is in danger of explosion, and there is an increase in the environmental burden caused by the discharge of CO gas to the outside of the system. [0011] Therefore, the present invention is invented in view of the above-mentioned problems of the prior art, and the object of the invention is to ensure the safety of the cement manufacturing apparatus and the environmental burden without affecting the quality of the cement. And the heavy metals can be separated from the cement manufacturing step with good efficiency. Means for Solving the Problem [0012] In order to achieve the above object, the present inventors have repeatedly made efforts to study the results, and found that the combustibles having a carbon content of a predetermined value or more are put into the cement kiln, and The volatilization rate of heavy metals is increased in the sintering step of the cement kiln. [0013] The present invention has been invented by the present invention, which is to supply a combustible material containing 20% by mass or more of carbon component to a region of a cement kiln of 900 ° C or more and 1300 ° C or less, from the cement. The kiln exhaust path from the kiln's kiln to the lowermost cyclone evacuates one part of the combustion gas, and collects 15 dust from the combustion gas to separate heavy metals from the collected dust. In addition, the carbon component is a component of combustion, and the heavy metals that can be separated are lead, cadmium, cadmium, recorded, sputum, god, and satiety. [0014] When the combustibles are put into the cement kiln at a fraction of less than 900 ° C, most of the combustibles are burned before reaching the region where the heavy metals are volatilized with good efficiency, and it is difficult to sufficiently increase the volatilization of heavy metals. Rate, on the other hand, when the temperature is above 1300 ° C, the color of the cement is yellow, which causes problems in the quality of the cement. By investing in combustible materials in the above temperature zone, the volatilization rate of heavy metals in the kiln tail in the cement kiln can be effectively improved, and the use of the gas bypass system to increase the concentration of heavy metals in the chlorine bypass dust can be used. The heavy metal removal rate of the cement manufacturing step is increased. [0015] 5 Ο 10 15 In the above cement production method, the heavy metal may be volatilized at a volatilization rate of 80% or more in the aforementioned region of the cement kiln. Further, in the cement manufacturing method, the carbon component content of the combustible material is α% by mass, and the amount of combustibles contained in the cement kiln containing the carbon component is clinker production amount per hour, and the call is made. The product is 30 or more and 5000 or less. When the product of α and ZH is less than 30, it is difficult to sufficiently increase the volatilization rate of heavy metals. On the other hand, when the product of ^: and the point exceeds 5 ', even if the carbon content of the input exceeds the volatility of heavy metals It is still unrealistic when it comes to the highest price when it is purchased at a price, which also leads to an increase in the cost of the use of the combustible material. [0017] Further, in the above cement manufacturing method, when dust is collected from the above-mentioned gas-burning gas, a dry dust collector or a wet set may be used. [0018] In the above cement manufacturing method, The above combustibles are supplied to the water kiln at 90 (above TC, 130 (in the area below TC, the fuel can be used to put the combustibles into the kiln tail of the cement kiln, or to be treated by temperature decomposition) In the state of shell coating, the preheater attached to the cement kiln is decomposed to decompose the carbonaceous material by the door difference, or the combustible material is directly input into the kiln from the inlet provided at the main part of the concrete pit. Any method. 20 [0019] 200944493 In addition, in the above cement manufacturing method, 'the aforementioned combustibles are from coke, coal tar, green tires, coal, anthracite, bituminous coal, brown carbon, lignite, graphite, flame retardant plastic a group of phenolic resin, furan resin, thermosetting resin, 5 cellulose, charcoal, waste toner, mixed coke, fine coke, electrode chips, activated pyrolysis, carbides and unburned carbon contained in fly ash select One or two or more. [0020] Further, the combustible material may be subjected to particle size adjustment by granulation or/and classification, and then put into the cement kiln. Since the combustible material is a small diameter, it is passed. The gas in the kiln flies to the low temperature side, so the supply amount of heavy metals in the volatilization temperature region is reduced, and the effective volatilization rate cannot be ensured. The standard should be such that when the particle size of the combustible material is dp and the gas velocity of the input portion is From Stoke
15 dx時，以造粒或分粒調整粒度為dx以上之粒徑。在此，μ為 氣體黏度，ρρ為可燃物密度，pg為氣體密度，§為重力加速 度。關於最大粒徑，過大時，至混入水泥或形成水泥礦物 之燒結帶為止燃燒未結束， 泥之品質面造成問題之虞， 【0021】 在上述水泥製造方法中， 水泥之顏色呈黃色，故有在水 而宜為不對該等影響之大小。 前述可燃物之粒徑可為1mm 以上、50mm以下。當可燃物$ 揮發溫度區域之供給量減少， 一方面，當可燃物之粒徑超過 當可燃物之粒徑不到1mm時，重金屬在 無法確保有效之揮發率，另 50mm時，有重金屬類混入至 200944493 水泥或水泥之顏色呈黃色，而在水泥之品質面造成問題之 虞。 發明效果 【0022】 5 ❹ 10 15 ❹ 如以上，根據本發明，對水泥之品質不造成影響，確 保水泥製造裝置之安全性，亦玎避免環境負擔之增加，且 可以良好效率從水泥製造步驟將重金屬類分離。 用以實施發明之最佳形態 【0023】 接著，就本發明之實施形態，一面參照圖式，一面說 明。此外，在以下之說明中，以以本發明實施形態將重金 屬類之一之鉛分離之情形為例來說明。 【0024】 第1圖係顯示適用本發明水泥製造方法之水泥製造裝 置，此水泥製造裝置1具有用以將可燃物c投入至水泥窯（以 下簡稱為「窯」）2之窯尾2a(煅燒爐3及最下段旋風器4具有 之端部）之投入裝置5。 【0025】 另一方面，如第2圖所示，於窯2具有氯旁路裝置1〇， 從窯2之窯尾2a至最下段旋風器4(參照第1圖）之窯排氣流路 之抽氣氣體在探針11以冷卻風扇12之冷風冷卻後，導入至 分粒機13，分離成粗粉塵、微粉及氣體。粗粉塵返回至熏 系統，含有氣化鉀(kci)等之微粉(氣旁路灰塵）以集塵機14 20 200944493 回收。從集塵機14排出之排氣經由風扇15，返回至附設於 窯2之預熱器或預熱器之出口等排氣流路。 【0026】 接著，就使用上述水泥製造裝置1之本發明之水泥製造 5方法作說明。 【0027】 在第1圖中，於窯2之水泥燒結中，以投入裝置5將可燃 物C投入至窯2之窯尾2a。此可燃物C係含有碳成份20質量％ 以上者，可使用焦炭、煤焦油瀝青、輪胎、煤、無煙煤' 10 煙煤 '褐炭、褐煤、石墨、難燃性塑膠、酚醛樹脂、呋喃 樹脂、熱硬化性樹脂、纖維素、木炭、廢調色劑、混合焦 炭、細焦炭、電極碎片、活性焦炭、碳化物及飛灰所含有 之未燃碳等。將具有此種碳成份含有率之可燃物C投入之理 由如下述。 15 【0028】 第3圖係顯示使用電爐之鉛之揮發率之試驗結果之圖 表’比較在電爐内，對從水泥製造步驟採取之進入黧2前之 原料（從最下段旋風器4排出之原料）1〇〇〇將焦碳（固定碳87 %=α)添加5〇(50kg/t-cli相當=/3，αχ冷=435〇)而燒結的情 20形及僅放入從最下段旋風器4排出之原料而燒結之情形。從 此圖亦可明瞭，當放入焦炭時，在燒結溫度9〇〇。〇〜13⑻。c 之區域，鉛之揮發率大幅上升。此溫度範圍相當於從窯2之 窯尾2a至中央部左右。 10 【0029】 200944493 在窯2揮發之鉛在第2圖中，包含在以探針11所括氣之 氣體，抽氣氣體在探針11冷卻後，導入至分粒機13，分離 為粗粉塵、微粉及氣體，微粉以集塵機14回收。在此微粉， 鉛揮發較多，鉛較習知濃縮計多，故藉將此鉛分離，而可 5 從水泥製造步驟以良好效率去除鉛，而可使在窯2製造之水 泥熟料之鉛含有率降低。 【實施例】 【0030】At 15 dx, the particle size was adjusted to a particle size of dx or more by granulation or classification. Here, μ is the gas viscosity, ρρ is the combustible density, pg is the gas density, and § is the gravity acceleration. Regarding the maximum particle size, when it is too large, the combustion is not completed until the cement or the sintered mineral band is formed, and the quality of the mud causes problems. [0021] In the above cement manufacturing method, the color of the cement is yellow, so In water, it is not the size of the impact. The particle size of the combustible material may be 1 mm or more and 50 mm or less. When the supply of the combustible material in the volatilization temperature region is reduced, on the one hand, when the particle size of the combustible material exceeds the particle diameter of the combustible material by less than 1 mm, the heavy metal cannot ensure an effective volatilization rate, and when another 50 mm, there is heavy metal incorporation. Until 200944493 The color of cement or cement is yellow, which causes problems in the quality of cement. Effect of the Invention [0022] 5 ❹ 10 15 ❹ As described above, according to the present invention, the quality of the cement is not affected, the safety of the cement manufacturing apparatus is ensured, the environmental burden is also avoided, and the cement manufacturing step can be performed with good efficiency. Heavy metal separation. BEST MODE FOR CARRYING OUT THE INVENTION [0023] Next, an embodiment of the present invention will be described with reference to the drawings. Further, in the following description, a case where the lead of one of the heavy metals is separated in the embodiment of the present invention will be described as an example. [0024] Fig. 1 is a view showing a cement manufacturing apparatus to which the cement manufacturing method of the present invention is applied, the cement manufacturing apparatus 1 having a kiln tail 2a for charging a combustible material c to a cement kiln (hereinafter referred to as "kiln" 2 (calcining) The input device 5 of the furnace 3 and the lowermost cyclone 4 has an end portion). [0025] On the other hand, as shown in Fig. 2, the kiln 2 has a chlorine bypass device 1〇, and the kiln exhaust flow path from the kiln tail 2a of the kiln 2 to the lowermost cyclone 4 (refer to Fig. 1) The exhaust gas is cooled by the cold air of the cooling fan 12 after the probe 11 is cooled, and then introduced into the classifier 13 to be separated into coarse dust, fine powder, and gas. The coarse dust is returned to the smoking system, and the fine powder (gas bypass dust) containing potassium carbonate (kci) or the like is recovered by the dust collector 14 20 200944493. The exhaust gas discharged from the dust collector 14 is returned to an exhaust flow path such as an outlet of a preheater or a preheater attached to the kiln 2 via the fan 15. Next, a method of manufacturing the cement 5 of the present invention using the cement manufacturing apparatus 1 described above will be described. In Fig. 1, in the cement sintering of the kiln 2, the combustibles C are introduced into the kiln tail 2a of the kiln 2 by the input device 5. This combustible material C contains 20% by mass or more of carbon components, and can be used for coke, coal tar pitch, tires, coal, anthracite '10 bituminous coal' brown carbon, lignite, graphite, flame retardant plastic, phenolic resin, furan resin, and heat hardening. Resin, cellulose, charcoal, waste toner, mixed coke, fine coke, electrode fragments, activated coke, carbide and unburned carbon contained in fly ash. The reason for putting the combustible material C having such a carbon component content into the following is as follows. 15 [0028] Figure 3 is a graph showing the results of the test for the volatilization rate of lead in an electric furnace. 'Compared with the raw material before the enthalpy 2 taken from the cement manufacturing step in the electric furnace (the raw material discharged from the lowermost cyclone 4) 1〇〇〇 Add coke (fixed carbon 87% = α) to 5 〇 (50kg / t-cli equivalent = / 3, α χ cold = 435 〇) and sinter the shape 20 and only put in the whirlwind from the bottom The case where the material discharged from the device 4 is sintered. It can also be seen from this figure that when coke is placed, it is at a sintering temperature of 9 Torr. 〇~13(8). In the area of c, the volatilization rate of lead increased significantly. This temperature range is equivalent to from the kiln tail 2a of the kiln 2 to the center portion. 10 [0029] 200944493 The lead volatilized in the kiln 2 is contained in the gas contained in the probe 11 in FIG. 2, and the exhaust gas is cooled by the probe 11, and then introduced into the classifier 13 to be separated into coarse dust. , fine powder and gas, the fine powder is recovered by the dust collector 14. In this fine powder, lead volatilizes more, and lead is more abundant than conventional concentrators. Therefore, by separating the lead, it is possible to remove lead from the cement manufacturing step with good efficiency, and lead the cement clinker produced in the kiln 2 The content rate is reduced. [Examples] [0030]
如表1所示，實施例使用可燃物A(固定碳成份30質量 10 %)，比較例使用可燃物B(固定碳成份17質量％)，使用投入 裝置5，將兩者投入至窯2之窯尾2a，而比較鉛揮發率。 【0031】 【表1】 實施例 比較例 可燃物 A B 發熱量 30MJ/kg(約 7,000kcal/kg) 16MJ/kg(約4,000kcal/kg) 揮發成份 67% 70% 固定碳 30% 17% 【0032】 15 如表2所示’實施例係使可燃物A之投入量在3個等級變 化，對各等級進行3天試驗，採取進入窯2前之原料(a)及通 過窯2後之熟料（製品）(b)，以下式算出鉛揮發率。 (l-b/a)xl00%。此外，在此式中，3表示原料之鉛含有率，b 表示熟料之鉛含有率。另一方面，比較例係使可燃物B之投 20入量在3個等級變化，對各等級進行3天試驗，與實施例同 11 200944493 樣地測量錯揮發率。此外’在本比較例中，將可燃物A之投 入量維持一定。 【0033】 【表2】 實施例 比較例 水準 1 2 3 1 2 3 曰數 123 456 789 123 456 789 可燃物A(t/h) 2 1 0 2 2 2 可燃物B(t/h) 0 0 0 4 2 0 合計(t/h) 2 1 0 6 4 0 5 【0034】 由於表2之實施例及比較例，試驗時之寞2之熟料生產量 為285t/h ’故可燃物A之投入量為等級1之2t/h時，2000kg/h+ 285t/h=7kg/t-cli.。因而，在實施例之等級卜 7kg/t-cli. = a， ' 可燃物Α之固定碳30%二召時，α χ /3 = 210。同樣地計算 10 時，在實施例之等級2 ’ 3.5kg/t-cli.== α，可燃物A之固定碳 30%= /3 時，α xy3 = 1〇5。 【0035】 ❹ 於第4圖顯示上述試驗結果，從同圖可知，在比較例 中’等級1至3 ’鉛揮發率無法看出變化，在實施例，隨著 15從等級1至等級3，亦即’隨著降低可燃物A之投入量，鉛揮 發率逐漸降低。藉此’可知，固定碳成份3〇質量％之可燃 物之投入有助於錯揮發率之上升。 【0036】 接著，如表3所示’實施例係在熟料生產量85t/h之窯2， 12 200944493 使可燃物C(固定碳87%= α)之投入量在4個等級變化，比較 例係不於窯2投入可燃物C’採取進入窯2前之原料(a)及通過 窯2後之熟料（製品)(b)，使用上述計算式，測量錯揮發率。 從此表可明暸，在比較例，鉛揮發率未達80。/。，相對於此， 5在實施例，隨著可燃物C之投入量之增加，鉛揮發率提高。 【0037】 【表3】 — ~· 實施例 比較例 水準 1 2 3 4 可燃物C投入量(t/h) 0.3 0.6 1.2 2.4 0 可燃物C投入量(kg/t-cil.)=冷 3.5 7.1 14 28 0 αχβ 304.5 617.7 1218 2436 0 揮發率(％) 88.8 94.0 98.8 99.9 77.9 【0038】 此外，在上述實施形態中，以投入裝置5將可燃物C投 10 入至窯2之窯尾2a，亦可在被以溫度分解之物質包覆之狀態 下，投入至附設於窯2之預熱器，以利用時間差分解含碳物 質，在投入至預熱器之含碳物質達窯2之900°C以上，1300 °C以下之區域時，含有20質量％以上之碳成份，可發揮與 上述相同之效果。又，亦可直接將可燃物C從設置於窯2之 15 本體部之入口直接投入至窯2内。 【0039】 又，在上述實施形態中，例示了從氯旁路將鉛分離之 情形，關於錯、鋅、録、録、叾西、石申、銘亦可與以上述相 同之要領分離。 13 200944493 t圖式簡單說明3 第1圖係顯示用以實施本發明之水泥製造方法之裝置 之一例的概略圖。 第2圖係顯示附設於水泥燒結爐之氣旁路裝置全體結 5 構之流程圖。 第3圖係顯示使用電爐之鉛之揮發率之試驗結果之圖 表。 第4圖係顯示本發明之水泥製造方法之試驗結果之圖 表。 10 【主要元件符號說明】 1...水泥製造裝置 12...冷卻風扇 2...水泥窯 13...分粒機 2a...窯尾 14...集塵機 3...锻燒爐 15...風扇 4...最下段旋風器 A...可燃物 5...投入裝置 B...可燃物 10...氯旁路裝置 C...可燃物 11·..探針As shown in Table 1, the examples used combustibles A (fixed carbon component 30 mass 10%), and comparative examples used combustibles B (fixed carbon components 17 mass%), using the input device 5, and putting both into the kiln 2 The kiln tail 2a, while comparing the lead volatilization rate. [0031] [Table 1] Example Comparative Example Combustibles AB Calorific value 30 MJ/kg (about 7,000 kcal/kg) 16 MJ/kg (about 4,000 kcal/kg) Volatile component 67% 70% Fixed carbon 30% 17% [0032] 】 15 As shown in Table 2 'Examples, the input amount of combustible A is changed in three grades, three grades are tested for each grade, and the raw materials before entering the kiln 2 (a) and the clinker after passing the kiln 2 are taken. (Product) (b) The lead volatility was calculated by the following formula. (l-b/a) xl00%. Further, in the formula, 3 represents the lead content of the raw material, and b represents the lead content of the clinker. On the other hand, in the comparative example, the amount of the combustibles B was changed in three levels, and the respective grades were tested for 3 days, and the false volatility was measured in the same manner as in the example 11 200944493. Further, in the present comparative example, the amount of the combustible material A was kept constant. [0033] [Table 2] Example Comparative Example Level 1 2 3 1 2 3 Number of turns 123 456 789 123 456 789 Combustible material A(t/h) 2 1 0 2 2 2 Combustible material B(t/h) 0 0 0 4 2 0 Total (t/h) 2 1 0 6 4 0 5 [0034] Due to the examples and comparative examples in Table 2, the clinker production amount of 寞2 during the test was 285t/h, so the combustible material A When the input amount is 2t/h of level 1, 2000kg/h+285t/h=7kg/t-cli. Thus, at the level of the embodiment, 7 kg/t-cli. = a, 'the fixed carbon of the combustibles is 30%, α χ /3 = 210. Similarly, when 10 is calculated, α xy3 = 1〇5 when the grade 2 ′ 3.5 kg/t-cli.== α of the embodiment and the fixed carbon of the combustible A 30%=/3. [0035] The results of the above test are shown in Fig. 4. As can be seen from the same figure, in the comparative example, the 'level 1 to 3' lead volatilization rate cannot be seen to change, in the embodiment, with 15 from level 1 to level 3, That is, with the reduction of the input of combustible A, the lead volatilization rate gradually decreases. From this, it can be seen that the input of the combustibles having a fixed carbon content of 3% by mass contributes to an increase in the volatility. [0036] Next, as shown in Table 3, the embodiment is based on the kiln 2, 12 200944493, which has a clinker production capacity of 85 t/h, and the input amount of combustible C (fixed carbon 87% = α) is changed in four levels, For example, the raw material (a) before entering the kiln 2 and the clinker (product) (b) after passing through the kiln 2 are not taken into the kiln 2, and the wrong volatility is measured using the above formula. It can be seen from this table that in the comparative example, the lead volatilization rate is less than 80. /. On the other hand, in the embodiment, as the amount of input of the combustible material C increases, the lead volatilization rate increases. [0037] [Table 3] — ~· Example Comparative Example Level 1 2 3 4 Combustible C Input (t/h) 0.3 0.6 1.2 2.4 0 Combustible C Input (kg/t-cil.) = Cold 3.5 7.1 14 28 0 αχβ 304.5 617.7 1218 2436 0 Volatilization rate (%) 88.8 94.0 98.8 99.9 77.9 [0038] Further, in the above embodiment, the combustible material C is fed into the kiln tail 2a of the kiln 2 by the input device 5, It may be put into a preheater attached to the kiln 2 in a state of being coated with a substance which is decomposed by temperature to decompose the carbonaceous substance by time difference, and the carbonaceous substance which is put into the preheater reaches 900° of the kiln 2 In the case of C or more and 1300 ° C or less, 20% by mass or more of the carbon component is contained, and the same effects as described above can be exhibited. Further, the combustibles C can be directly introduced into the kiln 2 from the inlet of the main body portion of the kiln 2 15 . Further, in the above embodiment, the case where the lead is separated from the chlorine bypass is exemplified, and the same as the above-mentioned method can be separated from the case of the wrong, zinc, recording, recording, western, and stone. 13 200944493 t BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a schematic view showing an example of an apparatus for carrying out the cement manufacturing method of the present invention. Fig. 2 is a flow chart showing the overall structure of the gas bypass device attached to the cement sintering furnace. Fig. 3 is a graph showing the test results of the volatilization rate of lead using an electric furnace. Fig. 4 is a graph showing the test results of the cement manufacturing method of the present invention. 10 [Description of main component symbols] 1... Cement manufacturing equipment 12... Cooling fan 2... Cement kiln 13... Parting machine 2a... Kiln tail 14... Dust collector 3... Calcination Furnace 15...fan 4...lowermost cyclone A...combustible 5...input device B...combustible 10...chlorine bypass device C...combustible 11·.. Probe