TWI391610B - A circulating fluidized bed, an operating system having the circulating fluidized bed, and a driving method of the circulating fluidized bed - Google Patents
A circulating fluidized bed, an operating system having the circulating fluidized bed, and a driving method of the circulating fluidized bed Download PDFInfo
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本發明係關於焚燒處理下水道污泥、城市垃圾、產業廢棄物等的廢棄物之循環型流體化床爐及具備該循環型流體化床爐的系統,特別是關於將脫硫材投入到爐內來進行脫硫反應及脫鹽反應之循環型流體化床爐及具備該循環型流體化床爐的系統。The present invention relates to a circulating fluidized bed furnace for incinerating waste water such as sewage sludge, municipal waste, industrial waste, and the like, and a system including the circulating fluidized bed furnace, in particular, the desulfurization material is put into the furnace. A circulating fluidized bed furnace for performing a desulfurization reaction and a desalination reaction, and a system including the circulating fluidized bed furnace.
以往,在下水道污泥、城市垃圾、產業廢棄物等的廢棄物的燃燒處理,循環型流體化床爐被廣泛地使用。循環型流體化床爐係為藉由從升流管底部導入的一次空氣一邊將廢棄物與流動媒體混合一邊使其燃燒並飛散,將該飛散的流動媒體藉由二次空氣的導入來伴同到乾舷,使排廢氣中的未燃燒成分完全燃燒,藉由旋風器從燃燒排廢氣分離流動媒體,返送至升流管來將流動媒體循環利用。這種的循環型流體化床爐為可瞬間將廢棄物乾燥、焚燒者,藉此,能夠將流動媒體維持於高溫而進行連續燃燒。又,由於流動媒體所保有的熱容量非常大,故,停止時的放熱少,亦適用於間歇運轉,且由於流動媒體的熱傳導率大,故亦可理想地用於下水道污泥這種含水率高的被處理物。Conventionally, circulating fluidized bed furnaces have been widely used in the combustion treatment of wastes such as sewage sludge, municipal waste, and industrial waste. The circulating fluidized bed furnace is characterized in that it is burned and scattered by mixing the waste with the flowing medium by the primary air introduced from the bottom of the riser, and the scattered flow medium is accompanied by the introduction of the secondary air. The freeboard completely burns the unburned components in the exhaust gas, separates the flowing medium from the combustion exhaust gas by the cyclone, and returns it to the riser to recycle the flowing medium. Such a circulating fluidized bed furnace is capable of instantaneously drying and incinerating waste, whereby the flow medium can be maintained at a high temperature for continuous combustion. Moreover, since the heat capacity of the fluid medium is very large, the heat generation at the time of stopping is small, and it is also suitable for intermittent operation, and since the fluid medium has a large thermal conductivity, it is also ideally used for sewage sludge having a high water content. The treated object.
在上述這種的廢棄物中存在著含有硫磺成分者,當以循環型流體化床爐進行燃燒處理之際,會有產生SO2 等的硫磺氧化物(SOx)之情況。含有硫磺氧化物之排廢氣會 成為大氣污染、酸性雨的原因,亦對人體有害,因此為了將其除去而需要進行脫硫處理。In the case where the sulfur-containing component is present in the above-mentioned waste, when the combustion treatment is performed in a circulating fluidized bed furnace, sulfur oxide (SOx) such as SO 2 may be generated. The exhaust gas containing sulfur oxides causes air pollution and acid rain, and is also harmful to the human body. Therefore, in order to remove it, desulfurization treatment is required.
脫硫法中存在有濕式法、半乾式法、乾式法,以往以來被最常採用之方法,有濕式法之一的洗煙塔(洗氣器)。洗氣器係為將添加有鹼性劑的洗淨水散佈於燃燒排廢氣,將以SOx為首的酸性氣體中和進行處理者。但是,洗氣器多數使用苛性鈉(NaOH)作為鹼劑,不僅藥劑成本昂對,且在維修上也花費費用。又,洗氣器被限於可充分地確保水、且不太花用廢水處理費用之場所。且,由於至洗氣器為止,排廢氣中的SOx濃度高,故當煙道中成為露點以下時,則會有容易引起腐蝕之問題產生腐食。Among the desulfurization methods, there are a wet method, a semi-dry method, and a dry method, and the most commonly used method in the past is a smoking tower (air scrubber) which is one of the wet methods. In the scrubber, the washing water to which the alkaline agent is added is dispersed in the combustion exhaust gas, and the acid gas including SOx is neutralized and treated. However, most of the scrubbers use caustic soda (NaOH) as an alkali agent, which is not only costly but also costly to maintain. Further, the scrubber is limited to a place where the water can be sufficiently secured and the waste water treatment cost is not used. Further, since the concentration of SOx in the exhaust gas is high up to the scrubber, when the flue is below the dew point, there is a problem that corrosion is likely to occur and corrosion occurs.
另外,乾式法之一,具有對爐內直接噴入脫硫材之爐內脫硫法。爐內脫硫法,其設備的改造簡單,且不用使用水等的原因,作為簡便的方法被廣泛地採用。作為脫硫材,最多被採用者為Ca系的固體脫硫材之石灰石(CaCO3 )、消石灰(Ca(OH)2 )、白雲石(CaCO3 ‧MgCO3 )等。在一般的爐內脫硫中,使用與流動媒體大致相同粒子徑的脫硫材,藉由使投入到爐內之脫硫材與流動媒體一同循環,來確保滯留時間,並且謀求脫硫效率的提升。Further, one of the dry methods has a desulfurization method in the furnace in which a desulfurization material is directly injected into the furnace. The in-furnace desulfurization method is widely used as a simple method because the equipment is simply modified and does not require the use of water or the like. As the desulfurization material, most of them are limestone (CaCO 3 ), hydrated lime (Ca(OH) 2 ), dolomite (CaCO 3 ‧MgCO 3 ), and the like which are Ca-based solid desulfurization materials. In a general in-furnace desulfurization, a desulfurization material having a particle diameter substantially the same as that of a flow medium is used, and a desulfurization material introduced into the furnace is circulated together with a flow medium to secure a residence time and to obtain a desulfurization efficiency. Upgrade.
進行這種爐內脫硫之循環型流體化床爐為專利文獻1(日本特開2002-130637號公報)等所揭示。A circulating fluidized bed furnace which performs such in-furnace desulfurization is disclosed in Patent Document 1 (JP-A-2002-130637).
又,在專利文獻2(日本特許第3790431號公報)揭示有對爐內以成為2Ca/S當量比以上的方式投入脫硫材,藉以進行爐內脫硫之裝置。In addition, in the patent document 2 (Japanese Patent No. 3,940,431), it is disclosed that a desulfurization material is introduced into the furnace so as to have a 2Ca/S equivalent ratio or more, thereby performing desulfurization in the furnace.
[專利文獻1]日本特開2002-130637號公報[Patent Document 1] Japanese Patent Laid-Open Publication No. 2002-130637
[專利文獻2]日本特許第3790431號公報[Patent Document 2] Japanese Patent No. 3790431
但是,在對含氯的廢棄物使用以往的爐內脫硫之情況,藉由脫硫材,雖可使一部分產生脫鹽反應,但無法充分地除去排廢氣或飛灰中的HCl。因此,為了進行脫鹽而需要對煙道吹入消石灰,但是藥劑需要石灰石與消石灰的2種類,會有造成成本増大,處理繁雜之問題存在。However, in the case where the conventional chlorine in the furnace is used for desulfurization of the chlorine-containing waste, a part of the desulfurization material may cause a desalination reaction, but the exhaust gas or the ash in the fly ash cannot be sufficiently removed. Therefore, in order to carry out desalination, it is necessary to blow slaked lime into the flue, but the chemical requires two types of limestone and slaked lime, which causes a problem of high cost and complicated handling.
又,當將脫硫材與流動媒體予以循環利用時,脫硫材會逐漸,使得爐內的循環粒子增加而造成爐內壓力上升。因此,必須頻繁地抽出流動媒體,又必須增大供給吹起已增加的循環粒子用空氣之鼓風機容量。Further, when the desulfurization material and the flow medium are recycled, the desulfurization material gradually increases, and the circulating particles in the furnace increase to cause the pressure in the furnace to rise. Therefore, it is necessary to frequently extract the flow medium, and it is necessary to increase the blower capacity to supply the air for circulating the increased circulating particles.
因此,本發明是有鑑於上述以往技術的問題點而開發完成的發明,其目的在於提供能夠藉由爐內脫硫來獲得脫硫以及充分的脫鹽效率,且能夠簡便、並低成本進行脫硫與脫鹽之循環型流體化床爐及具備該循環型流體化床爐的處理系統。Therefore, the present invention has been developed in view of the above problems of the prior art, and an object of the invention is to provide desulfurization and sufficient desalination efficiency by desulfurization in a furnace, and to perform desulfurization simply and at low cost. A circulating fluidized bed furnace with desalination and a treatment system equipped with the circulating fluidized bed furnace.
因此,本發明為了解決該課題,一種循環型流體化床爐,係將含有氯成分的廢棄物與流動媒體混合後予以燃燒,藉由旋風器,從燃燒排廢氣分離捕集流動媒體並加以循環利用,並且投入由Ca化合物的粉體所構成的脫硫材,進行爐內脫硫之循環型流體化床爐,其特徵為:前述脫硫材的最大粒子徑為100μm以下,前述旋風器具有捕集前 述流動媒體、一方面使前述脫硫材伴同燃燒排廢氣一同排出之粒子分離性能,藉由伴同前述排廢氣一同排出的脫硫材,在從前述旋風器所延設的煙道上進行脫硫及脫鹽。Therefore, in order to solve the problem, the present invention provides a circulating fluidized bed furnace in which a waste containing a chlorine component is mixed with a flow medium and burned, and a circulating medium is separated and collected from the combustion exhaust gas by a cyclone. A circulating fluidized bed furnace in which a desulfurization material composed of a powder of a Ca compound is introduced and desulfurized in a furnace is characterized in that the maximum particle diameter of the desulfurization material is 100 μm or less, and the cyclone has Before capture The flow medium, on the one hand, the particle separation performance of the desulfurization material discharged together with the combustion exhaust gas, and the desulfurization material discharged from the flue gas is desulfurized by the desulfurization material discharged together with the exhaust gas; Desalting.
若依據本發明,藉由使脫硫材伴同燃燒排廢氣排出至煙道,能夠在煙道上促進脫鹽反應,可使脫鹽效率提升。According to the present invention, by discharging the desulfurization material along with the combustion exhaust gas to the flue, the desalination reaction can be promoted in the flue, and the desalination efficiency can be improved.
又,由於脫硫材的粒子徑為100μm以下之小粒徑,故,反應面積增大,使得脫硫及脫鹽的爐內反應效率提升。又,藉由促進脫鹽,能夠抑制戴奧辛類、氯化銨的產生。Further, since the particle diameter of the desulfurization material is a small particle diameter of 100 μm or less, the reaction area is increased, and the reaction efficiency in the furnace for desulfurization and desalination is improved. Further, by promoting desalination, generation of dioxin and ammonium chloride can be suppressed.
且,由於停留在爐內之脫硫材量減少,故,能夠將爐內壓力保持在低壓力。其結果,能夠減低從爐底排出流動媒體次數,又能夠縮小鼓風機容量。又,由於所循環的粒子徑變小,故能夠減低爐內的耐火材摩耗。又,由於粒子徑小的脫硫材較大的脫硫材廉價,故能夠謀求成本降低。Further, since the amount of the desulfurized material remaining in the furnace is reduced, the pressure in the furnace can be maintained at a low pressure. As a result, the number of times the flow medium is discharged from the bottom of the furnace can be reduced, and the capacity of the blower can be reduced. Moreover, since the particle diameter to be circulated becomes small, the wear of the refractory material in the furnace can be reduced. Moreover, since the desulfurization material having a large particle diameter and a large desulfurization material is inexpensive, it is possible to reduce the cost.
又,本發明的特徵之一,前述旋風器是具有捕集粒子徑150μm以上的粒子之粒子分離性能。Further, in one of the features of the present invention, the cyclone has particle separation performance of particles having a particle diameter of 150 μm or more.
一般,由於流動媒體的粒子徑為200μm左右,故,藉由旋風器可確實地將其捕集,並且能僅使100μm以下的脫硫材伴同燃燒排廢氣排出。In general, since the particle diameter of the fluid medium is about 200 μm, it can be surely collected by the cyclone, and only the desulfurization material of 100 μm or less can be discharged together with the combustion exhaust gas.
且,理想為前述脫硫材的投入量係作為爐的入口之Ca/(S+Cl)當量比成為3.5以上之投入量。Further, it is preferable that the amount of the desulfurization material to be supplied is an input amount of Ca/(S+Cl) equivalent ratio of the inlet of the furnace of 3.5 or more.
如此,藉由將脫硫材的投入量作成為爐的入口之Ca/(S+Cl)當量比成為3.5以上之投入量,能夠使從旋風器所排出的未反應之Ca成分與HCl充分地反應,獲得高度的脫鹽效率。By setting the Ca/(S+Cl) equivalent ratio of the amount of the desulfurization material to the inlet of the furnace to 3.5 or more, the unreacted Ca component and HCl discharged from the cyclone can be sufficiently obtained. The reaction gives a high degree of desalting efficiency.
又,理想為前述脫硫材是與前述廢棄物混合後,再投入到爐內。Further, it is preferable that the desulfurization material is mixed with the waste and then introduced into the furnace.
藉此,即使為小粒徑的脫硫材,也能將該脫硫材確實地供給到爐下部,可獲得充分的滯留時間,進而可提升脫硫效率、脫鹽效率。又,在混合最厲害的爐下部產生反應乙事也有助於脫硫效率提升。Thereby, even if it is a desulfurization material of a small particle size, the desulfurization material can be reliably supplied to the lower part of a furnace, and sufficient retention time can be acquired, and the desulfurization efficiency and the desalination efficiency can be improved. In addition, the reaction of the lower part of the most powerful furnace also contributes to the improvement of desulfurization efficiency.
又,一種處理系統,係具備有前述循環型流體化床爐;和設置於從該循環型流體化床爐的旋風器延設的煙道上之排廢氣處理設備,該排廢氣處理設備至少具有捕集前述燃燒排廢氣中的飛灰的除塵裝置之處理系統,其特徵為:前述除塵裝置為包含袋形過濾器或陶瓷過濾器之過濾器式除塵裝置。Further, a treatment system comprising the above-described circulating fluidized bed furnace; and an exhaust gas treatment device disposed on a flue extending from a cyclone of the circulating fluidized bed furnace, the exhaust gas treatment device having at least A processing system for collecting a dust removing device for burning fly ash in exhaust gas, characterized in that the dust removing device is a filter type dust removing device including a bag filter or a ceramic filter.
藉此,藉由以此過濾器式除塵裝置捕捉小粒徑脫硫材,能夠更有效率地引起脫鹽反應。且更理想為管理過濾器式除塵裝置的差壓,將堆積於過濾器之餅層維持成厚,藉此,藉由被保持於該餅層之脫硫材,能夠更進一步促進脫鹽反應。Thereby, the desalination reaction can be more efficiently caused by capturing the small-sized desulfurization material by the filter type dust removing device. Further, it is more preferable to manage the differential pressure of the filter type dust removing device, and to maintain the thickness of the cake layer deposited on the filter, whereby the desalting reaction can be further promoted by the desulfurized material held in the cake layer.
本發明之循環型流體化床爐的運轉方法係具備將廢棄物與流動媒體混合並燃燒,產生燃燒排廢氣之升流管;及從前述燃燒排廢氣捕集前述流動媒體,將前述燃燒排廢氣排出到煙道,並且讓前述流動媒體返回到前述升流管的旋風器之循環型流體化床爐的運轉方法。此運轉方法具備有對前述升流管內供給第1脫硫材之製程。前述第1脫硫材的粒子徑係為被前述旋風器排出到前述煙道側之粒子徑。The operation method of the circulating fluidized bed furnace of the present invention comprises a riser pipe that mixes and burns waste with a flowing medium to generate exhaust gas for combustion; and collects the flow medium from the exhaust gas of the combustion exhaust gas to exhaust the exhaust gas A method of operating a circulating fluidized bed furnace that is discharged to a flue and returns the aforementioned flow medium to the cyclone of the aforementioned riser. This operation method includes a process of supplying the first desulfurization material into the above-mentioned riser. The particle diameter of the first desulfurization material is a particle diameter that is discharged to the flue side by the cyclone.
若依據此發明,第1脫硫材會與燃燒排廢氣一同被旋風器排出到煙道側。藉此,能夠在煙道側,藉由第1脫硫材將燃燒排廢氣進行脫鹽。According to the invention, the first desulfurizing material is discharged to the flue side by the cyclone together with the exhaust gas. Thereby, the combustion exhaust gas can be desalted by the first desulfurization material on the flue side.
本發明之循環型流體化床爐,係具備有:使廢棄物與流動媒體混合並燃燒,來產生燃燒排廢氣之升流管;從前述燃燒排廢氣捕集前述流動媒體,將前述燃燒排廢氣排出到煙道,並且讓前述流動媒體返回至前述升流管之旋風器;以及對前述升流管內供給第1脫硫材之第1脫硫材供給機構。前述第1脫硫材的粒子徑係為藉由前述旋風器排出到前述煙道側之粒子徑。The circulating fluidized bed furnace of the present invention comprises: a riser pipe that mixes and burns waste with a flow medium to generate exhaust gas; and collects the flow medium from the combustion exhaust gas to exhaust the exhaust gas a cyclone that is discharged to the flue and returns the flow medium to the riser; and a first desulfurization material supply mechanism that supplies the first desulfurization material to the inside of the riser. The particle diameter of the first desulfurization material is a particle diameter that is discharged to the flue side by the cyclone.
如以上所記載,若依據本發明,藉由讓脫硫材伴同燃燒排廢氣排出到煙道,能夠在煙道上促進脫鹽反應,可使脫鹽效率提升。又,由於脫硫材的粒子徑為100μm以下之小粒徑,故,可增大反應面積,進而能使脫硫及脫鹽的爐內反應效率提升。As described above, according to the present invention, by allowing the desulfurization material to be discharged to the flue along with the combustion exhaust gas, the desalination reaction can be promoted in the flue, and the desalination efficiency can be improved. Further, since the particle diameter of the desulfurization material is a small particle diameter of 100 μm or less, the reaction area can be increased, and the reaction efficiency in the furnace for desulfurization and desalination can be improved.
且,由於滯留於爐內之脫硫材量減少,故能夠將爐內壓力保持在低壓,能夠減低從爐底排出流動媒體次數,又能縮小鼓風機容量。又,粒子徑小的脫硫材較大的脫硫材廉價,因此能夠謀求成本降低。Further, since the amount of the desulfurization material remaining in the furnace is reduced, the pressure in the furnace can be kept at a low pressure, and the number of times of discharging the medium from the bottom of the furnace can be reduced, and the capacity of the blower can be reduced. Further, since the desulfurization material having a large particle diameter and a large desulfurization material is inexpensive, it is possible to reduce the cost.
又,藉由旋風器具有捕集粒子徑150μm以上的粒子之粒子分離性能,能確實地捕集流動媒體,並且僅使100μm以下的脫硫材伴同燃燒排廢氣排出。In addition, the cyclone has the particle separation performance of the particles having a particle diameter of 150 μm or more, so that the flow medium can be surely collected, and only the desulfurization material of 100 μm or less is discharged together with the combustion exhaust gas.
且,藉由將脫硫材的投入量作成為Ca/(S+Cl)當量比成為3.5以上之投入量,能夠使從旋風器所排出的未反 應之Ca成分與HCl充分地反應,獲得高度的脫鹽效率。In addition, by setting the amount of the desulfurization material to be an input amount of Ca/(S+Cl) equivalent ratio of 3.5 or more, it is possible to prevent the discharge from the cyclone. The Ca component is sufficiently reacted with HCl to obtain a high degree of desalting efficiency.
又,藉由將脫硫材預先與廢棄物混合後再投入到爐內,即使為小粒徑的脫硫材,也能將該脫硫材確實地供給到爐下部,能獲取充分的滯留時間。Further, by mixing the desulfurization material with the waste and then putting it into the furnace, even if it is a small-sized desulfurization material, the desulfurization material can be reliably supplied to the lower portion of the furnace, and a sufficient residence time can be obtained. .
又,藉由將排廢氣處理設備的除塵裝置作成為過濾器式,使得以過濾器式除塵裝置捕捉小粒徑脫硫材,能夠更有效率地引起脫鹽反應。Further, by using the dust removing device of the exhaust gas treating apparatus as a filter type, the filter type dust removing device can capture the small-sized desulfurized material, and the desalination reaction can be more efficiently caused.
以下,參照圖面,詳細地說明關於本發明的理想實施例。但是在此實施例所記載的構成零件的尺寸、材質、形狀、其相對的配置等,在未有特定記載的情況下,並非將本發明的範圍限定於該記載,僅為單純的說明例。Hereinafter, a preferred embodiment of the present invention will be described in detail with reference to the drawings. However, the dimensions, materials, shapes, relative arrangements, and the like of the components described in the embodiments are not intended to limit the scope of the invention to the description, and are merely illustrative examples.
本實施例的循環型流體化床爐之處理對象為含有氯的廢棄物,例如可舉出下水道污泥、城市垃圾、產業廢棄物等,但是本實施例的循環型流體化床爐特別是可理想地使用於下水道污泥的處理。循環型流體化床爐是將這些廢棄物進行燃燒處理,並且藉由脫硫材的投入來進行爐內脫硫,藉以進行脫硫及脫鹽。The treatment target of the circulating fluidized bed furnace of the present embodiment is chlorine-containing waste, and examples thereof include sewage sludge, municipal waste, industrial waste, and the like, but the circulating fluidized bed furnace of the present embodiment is particularly Ideally used in the treatment of sewage sludge. In the circulating fluidized bed furnace, these wastes are subjected to combustion treatment, and desulfurization in the furnace is carried out by the input of the desulfurization material, thereby performing desulfurization and desalination.
參照圖1,說明關於本實施例的循環型流體化床爐及處理系統。在同圖中,循環型流體化床爐1之主要結構為具備有:由填充於爐底的矽砂等的流動媒體流動化所獲得的流動層2a與位於其上方的乾舷2b所構成之升流管2; 連接於該升流管2的上部,捕集從乾舷2b所吹起的流動媒體,並且將分離了流動媒體之排廢氣排出到煙道21之旋風器3;經由降流管4連接於旋風器3,防止爐內未燃氣體朝旋風器3流通的密封罐5;以及將儲存於密封罐5之流動媒體返送到升流管2之流動媒體返回管6。Referring to Fig. 1, a circulating fluidized bed furnace and a treatment system according to the present embodiment will be described. In the same figure, the main structure of the circulating fluidized bed furnace 1 is constituted by a fluidized bed 2a obtained by fluidizing a flowing medium such as ceramsite filled in a furnace bottom, and a freeboard 2b located above it. Upflow tube 2; Connected to the upper portion of the riser tube 2, traps the flow medium blown from the freeboard 2b, and discharges the exhaust gas from which the flow medium is separated to the cyclone 3 of the flue 21; and connects to the cyclone via the downflow tube 4. The sealed tank 5 for preventing the unburned gas in the furnace from flowing toward the cyclone 3; and the flowing medium returning pipe 6 for returning the flowing medium stored in the sealed can 5 to the riser 2.
在升流管2的底部設有一次空氣導入口11,藉由從該一次空氣導入口11所導入的一次空氣,將流動媒體流動化,形成流動層2a。在該流動層2a上方的升流管爐壁,設有二次空氣導入口(未圖示),藉由從該導入所導入的二次空氣,維持乾舷2b的筒速,並且使燃燒排廢氣中的未燃燒成分燃燒。A primary air introduction port 11 is provided at the bottom of the riser pipe 2, and the flow medium is fluidized by the primary air introduced from the primary air introduction port 11, thereby forming the fluidized bed 2a. A secondary air introduction port (not shown) is provided in the riser wall above the fluidized bed 2a, and the secondary air introduced from the introduction maintains the tube speed of the freeboard 2b and causes the combustion row The unburned components in the exhaust gas are burned.
在前述升流管2的流動層2a上方,設有廢棄物投入手段12。該廢棄物投入手段12是具備有下述結構,即,將從廢棄物投入進料斗所承接的廢棄物,藉由供給進料機,每適宜量地投入到爐內。Above the fluidized bed 2a of the above-mentioned riser pipe 2, a waste input means 12 is provided. The waste injecting means 12 is provided with a structure in which the waste which is taken from the waste into the hopper is supplied to the furnace in an appropriate amount by the supply feeder.
又,循環型流體化床爐1具備有:將脫硫材投入到爐內之脫硫材投入口13、和投入流動媒體之流動媒體投入口(未圖示)。該脫硫材投入口13及流動媒體投入口,若為流動媒體的循環系統,則可設置於任意位置,但是前述脫硫材投入口13,理想為設置於較升流管2的二次空氣導入口更下方側位置。Further, the circulating fluidized bed furnace 1 is provided with a desulfurization material input port 13 for introducing a desulfurization material into the furnace, and a flow medium input port (not shown) for introducing a flow medium. The desulfurization material inlet 13 and the fluid medium inlet may be provided at any position in the circulation system of the fluid medium. However, the desulfurization material inlet 13 is preferably provided in the secondary air of the riser tube 2. The lower side of the inlet is located.
從前述脫硫材投入口13投入到爐內之脫硫材係作成為由Ca化合物的粉體所構成的脫硫材。又,該脫硫材係作成為最大粒子徑為100μm以下的脫硫材。作為脫硫材 ,可舉出例如,石灰石(CaCO3 )、消石灰(Ca(OH)2 )、白雲石(CaCO3 -MgCO3 )。The desulfurization material introduced into the furnace from the desulfurization material inlet 13 is a desulfurization material composed of a powder of a Ca compound. Further, the desulfurized material is used as a desulfurized material having a maximum particle diameter of 100 μm or less. Examples of the desulfurization material include limestone (CaCO 3 ), hydrated lime (Ca(OH) 2 ), and dolomite (CaCO 3 -MgCO 3 ).
前述旋風器3是具有從燃燒排廢氣分離並捕集流動媒體,一方面,使脫硫材伴同排廢氣排出到煙道21之粒子分離性能。理想為旋風器3是具有捕集粒子徑150μm以上的粒子之粒子分離性能。The cyclone 3 has a particle separation performance in which the flow medium is separated from the combustion exhaust gas and the flow medium is collected, and the desulfurization material is discharged to the flue 21 together with the exhaust gas. It is preferable that the cyclone 3 is a particle separation performance of particles having a particle diameter of 150 μm or more.
在從該旋風器3所延設的煙道21上,設有用來處理被旋風器3所分離的燃燒排廢氣之排廢氣處理設備。An exhaust gas treatment device for treating the combustion exhaust gas separated by the cyclone 3 is provided on the flue 21 extending from the cyclone 3.
前述排廢氣處理設備具有下述結構,即,空氣預熱器22、廢熱鍋爐23、氣體冷卻塔24、及袋形過濾器25成串連方式配設著。The exhaust gas treatment apparatus described above has a structure in which an air preheater 22, a waste heat boiler 23, a gas cooling tower 24, and a bag filter 25 are disposed in series.
前述空氣預熱器22是將被壓入用風扇15所導入的空氣與來自於旋風器3之燃燒排廢氣進行熱交換,進行一次空氣或二次空氣的預熱。前述廢熱鍋爐23是藉由燃燒排廢氣,將供給水加熱,來產生蒸氣。前述氣體冷卻塔24是藉由與冷卻水之熱交換,來冷卻燃燒排廢氣。前述袋形過濾器25係為捕集已被冷卻的排廢氣中的飛灰並加以除去之裝置。燃燒排廢氣是藉由設置於袋形過濾器25的後段之誘導用風扇26,通過上述的排廢氣處理設備後,從煙囪27排出到系統外。The air preheater 22 performs heat exchange between the air introduced by the press-in fan 15 and the combustion exhaust gas from the cyclone 3 to perform preheating of primary air or secondary air. The waste heat boiler 23 generates steam by heating exhaust gas and heating the feed water. The gas cooling tower 24 is cooled by heat exchange with cooling water to cool the exhaust gas. The bag-shaped filter 25 is a device that collects and removes fly ash in the exhaust gas that has been cooled. The combustion exhaust gas is discharged from the stack 27 to the outside of the system by the induction fan 26 provided in the rear stage of the bag filter 25 through the above-described exhaust gas treatment device.
再者,排廢氣處理設備不限於上述的結構,可選擇適宜必要的裝置來構成。做為其他的構成例,如圖2所示,具有空氣預熱器22、廢熱鍋爐23、及陶瓷過濾器28以串連方式配設之結構。如此,適用於本實施例之排廢氣處理 設備,若為至少具備有除塵裝置(袋形過濾器25或陶瓷過濾器28等)之結構的話,則可為任意結構。Further, the exhaust gas treatment device is not limited to the above-described structure, and may be configured by a suitable and necessary device. As another configuration example, as shown in FIG. 2, the air preheater 22, the waste heat boiler 23, and the ceramic filter 28 are arranged in series. Thus, the exhaust gas treatment suitable for the present embodiment The apparatus may have any structure if it has at least a structure including a dust removing device (a bag filter 25 or a ceramic filter 28).
在具備上述結構之循環型流體化床爐,藉由廢棄物投入手段12投入到爐內之廢棄物係在流動層2a與流動媒體混合並燃燒,在乾舷2b使未燃燒成分完全燃燒,並且利用從脫硫材投入口13所投入的脫硫材,進行爐內脫硫。在爐內脫硫,主要是藉由下述反應式(1)所示的脫硫反應來除去Sox。In the circulating fluidized bed furnace having the above configuration, the waste introduced into the furnace by the waste charging means 12 is mixed with the fluid medium in the fluidized bed 2a and burned, and the unburned components are completely burned on the freeboard 2b, and Desulfurization in the furnace is performed by using the desulfurization material supplied from the desulfurization material inlet 13 . Desulfurization in the furnace mainly removes Sox by a desulfurization reaction represented by the following reaction formula (1).
SO2 +CaO+1/2O2 →CaSO4 ………(1)SO 2 +CaO+1/2O 2 →CaSO 4 ...(1)
再者,CaO係為石灰石、消石灰等的脫硫材承受爐內的熱所產生者。Further, CaO is a desulfurized material such as limestone or slaked lime which is generated by heat in the furnace.
又,在爐內,以脫硫材,利用下述反應式(2)所示的脫鹽反應,除去一部分的HCl。Further, in the furnace, a part of HCl was removed by a desalting reaction represented by the following reaction formula (2) as a desulfurized material.
2HCl+CaO→CaCl2 +H2 O………(2)2HCl+CaO→CaCl 2 +H 2 O......(2)
但是,由於在爐內之脫鹽效率不大,故HCl會殘存於燃燒排廢氣或飛灰中。However, since the desalination efficiency in the furnace is not large, HCl remains in the combustion exhaust gas or fly ash.
因此,在本實施例,將投入到爐內之脫硫材的最大粒子徑設為100μm以下,並且前述旋風器3具有捕集流動媒體,一方面使脫硫材伴同燃燒排廢氣排出之粒子分離性能,故,在被旋風器3將與流動媒體分離之燃燒排廢氣中 ,伴同未反應之脫硫材,一起排出到煙道21。Therefore, in the present embodiment, the maximum particle diameter of the desulfurization material charged into the furnace is set to 100 μm or less, and the cyclone 3 has a trapping flow medium, and on the other hand, the desulfurization material is separated from the particles discharged from the combustion exhaust gas. Performance, therefore, in the combustion exhaust gas that is separated from the flow medium by the cyclone 3 With the unreacted desulfurized material, it is discharged to the flue 21 together.
然後,藉由所排出之脫硫材,在煙道21進行脫鹽。當然同時亦進行脫硫。脫鹽,特別是溫度變低則反應效率提升,故在通過煙道21之際,幾乎所有的HCl被除去。Then, desalination is carried out in the flue 21 by the discharged desulfurized material. Of course, desulfurization is also carried out. Desalting, especially when the temperature is lowered, increases the reaction efficiency, so almost all of the HCl is removed as it passes through the flue 21.
若依據本實施例,藉由使脫硫材伴同燃燒排廢氣排出到煙道21,能夠在煙道上促進脫鹽反應,進而可使脫鹽效率提升。According to the present embodiment, by discharging the desulfurization material along with the combustion exhaust gas to the flue 21, the desalination reaction can be promoted in the flue, and the desalination efficiency can be improved.
又,由於脫硫材的粒子徑為100μm以下之小粒徑,故使反應面積增大,進而可使脫硫及脫鹽的爐內反應效率提升。又,促進了脫鹽,能夠抑制戴奧辛類、氯化銨的產生。Further, since the particle diameter of the desulfurization material is a small particle diameter of 100 μm or less, the reaction area is increased, and the reaction efficiency in the furnace for desulfurization and desalination can be improved. Further, the desalination is promoted, and the generation of dioxin and ammonium chloride can be suppressed.
且,由於滯留在爐內之脫硫材量減少,故,能夠將爐內壓力保持於低壓。其結果,能夠減低從爐底排出流動媒體之排出次數,又,能夠縮小鼓風機(壓入用風扇15)容量。又,循環的粒子尺寸變小,故,能夠減低爐內的耐火材摩耗。又,粒子徑小的脫硫材較大徑的脫硫材廉價,故可謀求成本降低。Further, since the amount of the desulfurization material remaining in the furnace is reduced, the pressure in the furnace can be maintained at a low pressure. As a result, the number of discharges of the flow medium from the bottom of the furnace can be reduced, and the capacity of the blower (pressing fan 15) can be reduced. Moreover, since the particle size of the circulation becomes small, the wear of the refractory material in the furnace can be reduced. Further, since the desulfurization material having a large particle diameter and a large diameter is inexpensive, it is possible to reduce the cost.
又,前述旋風器3,理想為具有捕集粒子徑150μm以上的粒子之粒子分離性能。一般,由於流動媒體的粒子徑為200μm左右,故能夠藉由旋風器3將其確實地捕集,並且僅使100μm以下的脫硫材伴同燃燒排廢氣一起排出。Further, it is preferable that the cyclone 3 has a particle separation performance of particles having a particle diameter of 150 μm or more. In general, since the particle diameter of the fluid medium is about 200 μm, it can be surely collected by the cyclone 3, and only the desulfurized material of 100 μm or less is discharged together with the combustion exhaust gas.
又,前述脫硫材的投入量,理想為做成爐的入口之Ca/(S+Cl)當量比成為3.5以上之投入量。Moreover, it is preferable that the amount of the desulfurization material to be supplied is an input amount of a Ca/(S+Cl) equivalent ratio of the inlet of the furnace of 3.5 or more.
圖3顯示對脫硫材投入量之脫硫率與脫鹽率。如此圖 表所示,脫硫率,即使Ca/(S+Cl)當量比小,也顯示比較高的值。Figure 3 shows the desulfurization rate and desalination rate of the desulfurization input. Such a picture As shown in the table, the desulfurization rate shows a relatively high value even if the Ca/(S+Cl) equivalent ratio is small.
另外,脫鹽率是以Ca/(S+Cl)當量比呈3.5為境界,急遽地增大。In addition, the salt rejection rate is a sharp increase in the Ca/(S+Cl) equivalent ratio of 3.5.
因此,如此藉由將脫硫材的投入量作成為爐內的Ca/(S+Cl)當量比成為3.5以上之投入量,能夠使從旋風器所排出的未反應之Ca成分與HCl充分地反應,獲得高度的脫鹽效率。Therefore, by setting the amount of the desulfurization material to be an input amount of Ca/(S+Cl) equivalent ratio in the furnace of 3.5 or more, the unreacted Ca component and HCl discharged from the cyclone can be sufficiently obtained. The reaction gives a high degree of desalting efficiency.
又,在本實施例,排廢氣處理設備的除塵裝置,理想為作成包含袋形過濾器或陶瓷過濾器之過濾器式除塵裝置,藉此,藉由以此過濾器式除塵裝置捕捉小粒徑脫硫材,能更有效率地引起脫鹽反應。且理想為管理過濾器式除塵裝置的差壓,將堆積於過濾器之餅層的厚度維持成厚,藉由保持於該餅層之脫硫材,更進一步促進脫鹽反應。Further, in the present embodiment, the dust removing device of the exhaust gas treating apparatus is preferably formed as a filter type dust removing device including a bag filter or a ceramic filter, whereby the small particle diameter is captured by the filter type dust removing device. The desulfurization material can cause the desalination reaction more efficiently. Further, it is desirable to manage the differential pressure of the filter type dust removing device, and to maintain the thickness of the cake layer deposited on the filter to be thick, and to further promote the desalination reaction by the desulfurized material held in the cake layer.
且如圖2所示,預先將脫硫材與廢棄物混合,藉由廢棄物投入手段12投入到爐內為佳。Further, as shown in Fig. 2, it is preferred that the desulfurization material is mixed with the waste in advance and is introduced into the furnace by the waste input means 12.
藉此,即使為小粒徑的脫硫材,也能確實地將該脫硫材供給到爐下部,能夠獲取充分的滯留時間,進而可使脫硫效率、脫鹽效率提升。又,在混合最激烈的爐下部產生反應乙事也有助於脫硫效率提升。Thereby, even if it is a desulfurization material of a small particle diameter, the desulfurization material can be reliably supplied to the lower part of a furnace, and sufficient retention time can be acquired, and the desulfurization efficiency and the desalination efficiency can be improved. In addition, the reaction of the reaction in the lower part of the most intense furnace also contributes to the improvement of desulfurization efficiency.
再者,在本實施例,說明了關於旋風器3具有捕集粒子徑150μm以上的粒子之粒子分離性能,脫硫材的最大粒子徑為100μm以下之情況。但是,如果將脫硫材的平均粒子徑作成為較旋風器3的界限粒子徑小,能夠達到相 同的作用效果。例如,在旋風器3的界限粒子徑為150μm之情況,能夠採用平均粒子徑較150μm小者來作為脫硫材。即使這樣的情況,因大部分的脫硫材被排出到煙道,所以能有效地除去HCl。In the present embodiment, the cyclone 3 has a particle separation performance of particles having a particle diameter of 150 μm or more, and the maximum particle diameter of the desulfurization material is 100 μm or less. However, if the average particle diameter of the desulfurized material is made smaller than the boundary particle diameter of the cyclone 3, the phase can be achieved. The same effect. For example, when the boundary particle diameter of the cyclone 3 is 150 μm, a desulfurization material can be used in which the average particle diameter is smaller than 150 μm. Even in such a case, since most of the desulfurized material is discharged to the flue, HCl can be effectively removed.
再者,在本說明書所指之最大粒子徑係可藉由依據日本工業規格(JIS規格)的「JIS M 8511;天然石墨的工業分析及實驗方法」所獲得的重量累積分佈來求得。In addition, the maximum particle diameter system referred to in the present specification can be obtained by a weight cumulative distribution obtained by "JIS M 8511; Industrial Analysis and Experimental Method of Natural Graphite" according to Japanese Industrial Standards (JIS Standard).
又,在本說明書所指之平均粒子徑係能夠藉由從上述的「JIS M 8511;天然石墨的工業分析及實驗方法」之重量累積分佈,計算累積重量成為50%之中位徑(中號d50 )來求得。In addition, the average particle diameter system referred to in the present specification can be calculated from the weight distribution of the above-mentioned "JIS M 8511; industrial analysis and experimental method of natural graphite", and the cumulative weight is calculated as a medium diameter of 50% (medium number) d 50 ) to find out.
又,在本說明書所指之旋風器3的界限粒子徑,是能以以下的方式來求取。即,將具有充分廣的粒子徑分佈之脫硫材投入到旋風器3。將從旋風器3所排出的脫硫材作為排出脫硫材加以捕集。然後,將排出脫硫材的最小粒子徑作為旋風器3的界限粒子徑予以求取。Further, the boundary particle diameter of the cyclone 3 referred to in the present specification can be obtained in the following manner. That is, the desulfurized material having a sufficiently wide particle diameter distribution is introduced into the cyclone 3. The desulfurization material discharged from the cyclone 3 is collected as a discharge desulfurization material. Then, the minimum particle diameter of the discharged desulfurization material is obtained as the boundary particle diameter of the cyclone 3.
接著,說明關於本發明的第2實施例。Next, a second embodiment of the present invention will be described.
若依據第1實施例,藉由採用平均粒子徑較旋風器3的界限粒子徑小者作為脫硫材,能夠提升脫鹽效果。又,被投入到循環型流體化床爐之廢棄物,會有含有氮化合物之情況。在廢棄物中含有氮化合物之情況,於爐內的排廢氣中亦會含有氮化合物(NH3 、HCN、及N2 O等)之情況 。例如,在投入作為廢棄物之下水道污泥的情況,氮化合物的含有量容易變多。然後,本發明者們發現,在僅使用平均粒子徑較旋風器3的界限粒子徑小的脫硫材(以下稱為第1脫硫材)之情況,含於排廢氣中之氮化合物(NH3 、HCN、N2 O、等)的濃度會增加。According to the first embodiment, the desalination effect can be improved by using the deuterium having a smaller average particle diameter than the boundary particle diameter of the cyclone 3 as the desulfurization material. Further, the waste which is put into the circulating fluidized bed furnace may contain a nitrogen compound. In the case where the waste contains nitrogen compounds, nitrogen compounds (NH 3 , HCN, N 2 O, etc.) may also be contained in the exhaust gas in the furnace. For example, when the sewage sludge is discharged as waste, the content of the nitrogen compound tends to increase. Then, the present inventors have found that the nitrogen compound (NH) contained in the exhaust gas is used only when the desulfurization material having a smaller average particle diameter than the boundary particle diameter of the cyclone 3 (hereinafter referred to as the first desulfurization material) is used. 3. The concentration of HCN, N 2 O, etc. will increase.
圖4是顯示燃燒排廢氣性狀之圖。圖4中顯示僅使用第1脫硫材作為脫硫材的情況時之結果、和僅使用平均粒子徑較旋風器3的界限粒子徑大者(以下稱為第2脫硫材)作為脫硫材的情況時之結果。圖4中,a為顯示CO、為顯示SO2 、c為顯示NOx、d為顯示HCl、e為顯示HCN、f為顯示NH3 。如圖4所示,確認到在僅使用第1脫硫材的情況,較僅使用第2脫硫材的情況,雖能夠減低HCl濃度,但HCN濃度及NH3 的濃度會增加。Fig. 4 is a graph showing the behavior of exhaust gas from combustion. 4 shows the results when only the first desulfurization material is used as the desulfurization material, and the case where only the average particle diameter is larger than the boundary particle diameter of the cyclone 3 (hereinafter referred to as the second desulfurization material) is used as the desulfurization. The result of the material. In Fig. 4, a shows CO, shows SO 2 , c shows NOx, d shows HCl, e shows HCN, and f shows NH 3 . As shown in FIG. 4, it was confirmed that when only the first desulfurization material was used, when the second desulfurization material was used, the HCN concentration and the concentration of NH 3 were increased although the HCl concentration could be reduced.
作為氮化合物增加的理由,可考量為以下這種的結構。As a reason for the increase in the nitrogen compound, the following structure can be considered.
圖5是用來說明具備循環型流體化床爐的系統之脫硫材的作用之概略圖。圖5為顯示使用碳酸鈣(CaCO3 )作為脫硫材之情況的圖。如圖5所示,通常,爐(升流管)內呈高溫(例如大約850℃)。被投入到爐內之CaCO3 ,會在高溫下氧化而產生CaO。所產生的CaO會引起脫硫材本來的作用之脫硫反應,讓Sox變化成CaSO4 。又,在較低溫(例如大約200℃)的煙道側,CaO會與HCl進行脫鹽反應,而產生CaCl2 。Fig. 5 is a schematic view for explaining the action of a desulfurization material in a system including a circulating fluidized bed furnace. Fig. 5 is a view showing a case where calcium carbonate (CaCO 3 ) is used as a desulfurization material. As shown in Fig. 5, generally, the furnace (riser tube) has a high temperature (for example, about 850 ° C). CaCO 3 that is put into the furnace is oxidized at a high temperature to generate CaO. The CaO produced causes the desulfurization reaction of the desulfurized material to cause the change of Sox to CaSO 4 . Also, at the lower temperature (e.g., about 200 ° C) flue side, CaO will be desalted with HCl to produce CaCl 2 .
存在於爐內之CaO,不僅是脫硫反應,在高溫環境下,亦會發揮氮化合物的氧化反應之觸媒作用。即,如圖5 所示,NH3 、HCN、及N2 O等的氮化合物,會因CaO之觸媒作用被氧化,而產生NOx。此反應特別是在產生污泥的熱分解反應之升流管下部引起。此理由如以下所述。被投入到升流管之污泥,由於比重大,故首先會至流於升流管的下部。在被供給到升流管下部之一次空氣中,不含有可將污泥完全地燃燒這種量之氧。因此,在升流管下部,會產生污泥的熱分解反應。其結果,從污泥中的N分(含有氮成分),產生NH3 、HCN、及N2 O等的氮化合物。如此,由於在升流管下部,氮化合物濃度高,故,在升流管下部,容易產生因CaO所引起的氮化合物的氧化反應。另外,在升流管上部,由於二次空氣之氮化合物的氧化行進,故氮化合物濃度低。因此,CaO所引起之氮化合物的氧化反應不易產生。The CaO present in the furnace is not only a desulfurization reaction, but also acts as a catalyst for the oxidation reaction of nitrogen compounds in a high temperature environment. That is, as shown in Fig. 5, nitrogen compounds such as NH 3 , HCN, and N 2 O are oxidized by the catalytic action of CaO to generate NOx. This reaction is caused in particular in the lower part of the riser tube which produces the thermal decomposition reaction of the sludge. This reason is as follows. The sludge that is put into the riser pipe will flow to the lower part of the riser pipe first because of the large specific gravity. In the primary air supplied to the lower portion of the riser, there is no oxygen in an amount sufficient to completely burn the sludge. Therefore, in the lower part of the riser pipe, a thermal decomposition reaction of the sludge occurs. As a result, nitrogen compounds such as NH 3 , HCN, and N 2 O are generated from the N component (containing a nitrogen component) in the sludge. As described above, since the concentration of the nitrogen compound is high in the lower portion of the riser, the oxidation reaction of the nitrogen compound due to CaO is likely to occur in the lower portion of the riser. Further, in the upper portion of the riser pipe, the concentration of the nitrogen compound is low due to the oxidation of the nitrogen compound of the secondary air. Therefore, the oxidation reaction of the nitrogen compound caused by CaO is not easily produced.
在此,如第1實施例般,在僅使用第1脫硫材的情況,被投入到升流管內之第1脫硫材伴同爐內的氣體,朝上方吹起。因此,第1脫硫材不易滯留於升流管下部。且,由於第1脫硫材是從旋風器所排出的,故,也不會有通過降流管供給至升流管下部的情況產生。因此,變得不易充分地發揮氮化合物作為氧化觸媒之作用。其結果,造成排廢氣中之氮化合物濃度上升。Here, as in the first embodiment, when only the first desulfurization material is used, the first desulfurization material that has been introduced into the riser pipe is blown upward with the gas in the furnace. Therefore, the first desulfurization material is less likely to remain in the lower portion of the riser pipe. Further, since the first desulfurization material is discharged from the cyclone, there is no possibility that the first desulfurization material is supplied to the lower portion of the riser pipe through the downflow pipe. Therefore, it becomes difficult to sufficiently exert the function of the nitrogen compound as an oxidation catalyst. As a result, the concentration of nitrogen compounds in the exhaust gas is increased.
因此,在本實施例,實施用來促進爐內之氮化合物的氧化反應的作業。Therefore, in the present embodiment, an operation for promoting the oxidation reaction of the nitrogen compound in the furnace is carried out.
圖6是顯示具備本實施例之循環型流體化床爐的系統之全體構成圖。針對與第1實施例相同的結構,賦予相同 符號,並省略其說明。Fig. 6 is a view showing the overall configuration of a system including the circulating fluidized bed furnace of the present embodiment. The same structure is given to the same as in the first embodiment Symbols and their descriptions are omitted.
如圖6所示,在本實施例的系統中,追加有第1脫硫材供給機構36;第2脫硫材供給機構37;壓力感測器31、壓力感測器32;差壓測定機構33;濃度測定機構34、流動媒體排出機構35;風扇38;及空氣預熱器39。又,設有作為脫硫材投入口13之第1脫硫材投入口13-1與第2脫硫材投入口13-2。As shown in Fig. 6, in the system of the present embodiment, a first desulfurization material supply mechanism 36, a second desulfurization material supply mechanism 37, a pressure sensor 31, a pressure sensor 32, and a differential pressure measuring mechanism are added. 33; concentration measuring mechanism 34, flow medium discharge mechanism 35; fan 38; and air preheater 39. Moreover, the first desulfurization material inlet 13-1 and the second desulfurization material inlet 13-2 as the desulfurization material inlet 13 are provided.
第1脫硫材供給機構36,從第1脫硫材投入口13-1,將第1脫硫材供給到升流管2內。第1脫硫材的粒徑係為在旋風器3能排出到煙道21側這樣的粒徑。The first desulfurization material supply mechanism 36 supplies the first desulfurization material into the riser pipe 2 from the first desulfurization material supply port 13-1. The particle diameter of the first desulfurization material is such a particle diameter that the cyclone 3 can be discharged to the side of the flue 21 .
第2脫硫材供給機構37,從第2脫硫材投入口13-2,將第2脫硫材供給到升流管2內。此第2脫硫材的粒徑是與第1脫硫材不同,為在旋風器3,可與流動媒體一同被捕集這種的粒徑。具體而言,採用平均粒子徑較旋風器3的界限粒子徑大的脫硫材作為第2脫硫材。The second desulfurization material supply mechanism 37 supplies the second desulfurization material into the riser pipe 2 from the second desulfurization material supply port 13-2. The particle size of the second desulfurization material is different from that of the first desulfurization material, and is a particle size that can be trapped together with the flow medium in the cyclone 3. Specifically, a desulfurization material having a larger average particle diameter than the boundary particle diameter of the cyclone 3 is used as the second desulfurization material.
差壓測定機構33是設置用來測定升流管2內的上部與下部的差壓。在升流管上部安裝有壓力感測器31,而在升流管下部安裝有壓力感測器32。差壓測定機構33是依據壓力感測器31與壓力感測器32之壓力測定結果,來測定升流管2內的差壓。The differential pressure measuring mechanism 33 is provided to measure the differential pressure between the upper portion and the lower portion in the riser tube 2. A pressure sensor 31 is mounted on the upper portion of the riser tube, and a pressure sensor 32 is mounted on the lower portion of the riser tube. The differential pressure measuring mechanism 33 measures the differential pressure in the riser tube 2 based on the pressure measurement results of the pressure sensor 31 and the pressure sensor 32.
濃度測定機構34是設置於煙道21。藉由濃度測定機構34,測定燃燒排廢氣中的NOx成分濃度。再者,濃度測定機構34並非一定需要設置於煙道21。若為可測定燃燒排廢氣中的成分濃度之位置,則可設置於其他場所。The concentration measuring mechanism 34 is provided in the flue 21 . The concentration of the NOx component in the exhaust gas of the combustion exhaust gas is measured by the concentration measuring means 34. Furthermore, the concentration measuring mechanism 34 does not necessarily need to be provided in the flue 21 . If it is a position where the concentration of the component in the exhaust gas of combustion can be measured, it can be installed in another place.
流動媒體排出機構35是設置於升流管2的底部。流動媒體排出機構35是設置成用來從流動層2a排出流動媒體。The fluid medium discharge mechanism 35 is provided at the bottom of the riser tube 2. The flow medium discharge mechanism 35 is provided to discharge the flow medium from the fluid layer 2a.
風扇38是經由空氣預熱器39,連接於升流管2內的流動層2a的上方。風扇38係將燃燒用空氣作為二次空氣,供給到流動層2a的上方。The fan 38 is connected to the flow layer 2a in the riser 2 via an air preheater 39. The fan 38 supplies the combustion air as secondary air and supplies it to the upper side of the fluid layer 2a.
風扇38是與供給一次空氣之風扇15一同構成燃燒控制機構。即,藉由控制利用風扇38之二次空氣的供給量、和利用風扇15之一次空氣的供給量,能夠控制升流管2內引起燃燒的容易度。The fan 38 constitutes a combustion control mechanism together with the fan 15 that supplies the primary air. That is, by controlling the supply amount of the secondary air by the fan 38 and the supply amount of the primary air by the fan 15, it is possible to control the easiness of combustion in the riser tube 2.
接著,說明關於本實施例之循環型流體化床爐的運轉方法。Next, a method of operating the circulating fluidized bed furnace of the present embodiment will be described.
被廢棄物投入手段12投入到升流管2內之廢棄物,藉由流動層2a,與流動媒體混合並燃燒,產生燃燒排廢氣。在此,藉由第1脫硫材供給機構36及第2脫硫材供給機構37,對升流管2內供給第1脫硫材及第2脫硫材。利用脫硫材的存在,使得燃燒排廢氣被脫硫。升流管2內的燃燒排廢氣,與第1脫硫材、第2脫硫材、及流動媒體一同被導引到旋風器3。The waste that has been introduced into the riser pipe 2 by the waste input means 12 is mixed with the flow medium by the fluidized bed 2a and burned to generate combustion exhaust gas. Here, the first desulfurization material supply unit 36 and the second desulfurization material supply unit 37 supply the first desulfurization material and the second desulfurization material into the riser tube 2. The presence of the desulfurization material causes the combustion exhaust gas to be desulfurized. The combustion exhaust gas in the riser pipe 2 is guided to the cyclone 3 together with the first desulfurization material, the second desulfurization material, and the flow medium.
在旋風器3,僅捕集第2脫硫材及流動媒體,返回到升流管2。另外,第1脫硫材及燃燒排廢氣從旋風器3排出到煙道21。藉由被排出到煙道之第1脫硫材,與上述的實施例同樣地,進行燃燒排廢氣的脫鹽,能夠除去通過煙道21之燃燒排廢氣中的HCl。In the cyclone 3, only the second desulfurization material and the flow medium are collected and returned to the riser tube 2. Further, the first desulfurization material and the combustion exhaust gas are discharged from the cyclone 3 to the flue 21 . By the first desulfurization material discharged to the flue, as in the above-described embodiment, desalination of the combustion exhaust gas is performed, and HCl in the exhaust gas from the combustion passage passing through the flue 21 can be removed.
在此,在僅供給第1脫硫材的情況,脫硫材變得不會在循環型流體化床爐循環。因此,變得無法充分地保持升流管2內的脫硫材的濃度。Here, when only the first desulfurization material is supplied, the desulfurization material does not circulate in the circulating fluidized bed furnace. Therefore, it becomes impossible to sufficiently maintain the concentration of the desulfurization material in the riser tube 2.
相對於此,在本實施例,由於第2脫硫材返回到升流管2,故,能夠防止升流管2內之脫硫材濃度降低。其結果,既可在煙道21進行脫鹽,亦能促進升流管2內之脫硫作用及未燃成分的氧化作用。On the other hand, in the present embodiment, since the second desulfurization material is returned to the riser pipe 2, the concentration of the desulfurization material in the riser pipe 2 can be prevented from decreasing. As a result, it is possible to perform desalination in the flue 21, and also promote desulfurization in the riser tube 2 and oxidation of unburned components.
說明關於第1脫硫材的粒徑。例如,旋風器3作成為排出150μm以下的粒子,捕集較150μm大的粒子者。即,旋風器3的界限粒子徑作成為150μm。在此情況,理想為採用最大粒子徑較150μm小者作為第1脫硫材。The particle size of the first desulfurization material will be described. For example, the cyclone 3 is configured to discharge particles of 150 μm or less and collect particles larger than 150 μm. That is, the boundary particle diameter of the cyclone 3 was 150 μm. In this case, it is preferable to use a material having a maximum particle diameter smaller than 150 μm as the first desulfurization material.
又,說明關於第2脫硫材的粒徑。旋風器3作成為排出150μm以下的粒子,捕集較150μm大的粒子者。即,旋風器3的界限粒子徑作成為150μm。在此情況,理想為採用平均粒子徑較150μm大者作為第2脫硫材。藉此,能夠充分地保持爐內中特別是升流管下部之脫硫材的濃度,可充分地促進氮化合物的氧化反應。又,第2脫硫材的平均粒子徑,理想為350μm以下。在平均粒子徑超過350μm的情況,會有第2脫硫材堆積於升流管2的下部,變得無法朝上部吹起之情況產生。其結果,變得無法充分地發揮脫硫作用、氧化觸媒作用等。又,也會增加風扇15所需要之動力。Further, the particle size of the second desulfurization material will be described. The cyclone 3 is configured to discharge particles of 150 μm or less and collect particles larger than 150 μm. That is, the boundary particle diameter of the cyclone 3 was 150 μm. In this case, it is preferable to use the second desulfurization material as the average particle diameter of 150 μm. Thereby, the concentration of the desulfurization material in the furnace, in particular, the lower portion of the riser pipe can be sufficiently maintained, and the oxidation reaction of the nitrogen compound can be sufficiently promoted. Further, the average particle diameter of the second desulfurization material is preferably 350 μm or less. When the average particle diameter exceeds 350 μm, the second desulfurization material may be deposited on the lower portion of the riser tube 2 and may not be blown up toward the upper portion. As a result, the desulfurization action, the oxidation catalyst action, and the like are not sufficiently exhibited. Also, the power required by the fan 15 is increased.
在旋風器3的界限粒子徑為150μm的情況,作為第2脫硫材,更理想為採用平均粒子徑較150μm大、且大部 分(在重量基準為50%以上)的粒子之粒子徑為100μm以上350μm以下的範圍者。如果採用具有這樣範圍的粒度分佈之脫硫材,也不會有因長時間運轉造成第2脫硫材蓄積於爐內,且第2脫硫材無法朝上部被吹起之情況產生。When the boundary particle diameter of the cyclone 3 is 150 μm, it is more preferable that the second desulfurization material has an average particle diameter of 150 μm or more. The particle diameter of the particles (50% or more by weight) is in the range of 100 μm or more and 350 μm or less. When a desulfurized material having a particle size distribution in such a range is used, there is no possibility that the second desulfurization material is accumulated in the furnace due to long-term operation, and the second desulfurization material cannot be blown up toward the upper portion.
作為第1脫硫材及第2脫硫材的種類,能夠使用與上述的實施例的脫硫材相同種類(石灰石、消石灰、及白雲石等)。As the type of the first desulfurization material and the second desulfurization material, the same type (limestone, slaked lime, and dolomite) as the desulfurization material of the above-described embodiment can be used.
第1脫硫材及第2脫硫材的投入量,理想為與上述的實施例同樣地,呈爐的入口之Ca/(S+Cl)當量比成為3.5以上之投入量。再者,此投入量,能夠預先測定廢棄物的成分比率來加以決定。The amount of the first desulfurization material and the second desulfurization material to be charged is preferably an input amount of a Ca/(S+Cl) equivalent ratio of the inlet of the furnace of 3.5 or more as in the above-described embodiment. Further, the amount of this input can be determined by measuring the component ratio of the waste in advance.
又,在本實施例,藉由濃度測定機構34,測定燃燒排廢氣中的NOx濃度。然後,依據濃度測定機構34的測定結果,控制燃燒控制機構(風扇15及風扇38)的動作。Further, in the present embodiment, the concentration of the NOx in the exhaust gas is measured by the concentration measuring means 34. Then, the operation of the combustion control means (fan 15 and fan 38) is controlled based on the measurement result of the concentration measuring means 34.
如上述般,在本實施例,藉由第2脫硫材,促進升流管2內的未燃成分的氧化。當未燃成分中之氮化合物(HCN、NH3 等)被氧化時,則會有產生Nox的情況。因此,在燃燒排廢氣中的NOx濃度變得較預定值高的情況,藉由燃燒控制機構(風扇15及風扇38),控制成升流管2內的環境成為不易引起燃燒(氧化)之環境。具體而言,藉由減少一次空氣及二次空氣的供給量,或減少一次空氣對二次空氣的供給比率,來控制成不易引起氧化反應之環境。藉此,能抑制NOx濃度的增加,能夠抑制燃燒排廢氣中的NOx濃度。As described above, in the present embodiment, the oxidation of the unburned components in the riser tube 2 is promoted by the second desulfurization material. When the nitrogen compound (HCN, NH 3 or the like) in the unburned component is oxidized, Nox may be generated. Therefore, when the NOx concentration in the combustion exhaust gas becomes higher than a predetermined value, the environment in the riser pipe 2 is controlled to be less likely to cause combustion (oxidation) by the combustion control mechanism (fan 15 and fan 38). . Specifically, the environment in which the oxidation reaction is less likely to occur is controlled by reducing the supply amount of the primary air and the secondary air or reducing the supply ratio of the primary air to the secondary air. Thereby, the increase in the NOx concentration can be suppressed, and the NOx concentration in the combustion exhaust gas can be suppressed.
又,在僅以燃燒控制機構無法充分地抑制NOx濃度的情況,藉由第2脫硫材供給機構37,減少第2脫硫材的供給量。藉此,能夠確實地抑制升流管2內之氧化反應,可確實地抑制燃燒排廢氣中的NOx濃度。In addition, when the NOx concentration is not sufficiently suppressed by the combustion control means, the second desulfurization material supply means 37 reduces the supply amount of the second desulfurization material. Thereby, the oxidation reaction in the riser pipe 2 can be surely suppressed, and the NOx concentration in the combustion exhaust gas can be reliably suppressed.
又,在本實施例,當進行運轉時,藉由差壓測定機構33,測定升流管2的上部與下部之差壓。如上述般,第2脫硫材循環於循環型流體化床爐。因此,藉由控制第2脫硫材的供給量,能夠控制爐內的差壓。因此,依據此差壓測定機構33之測定結果,第2脫硫材供給機構37控制第2脫硫材的供給量,使升流管2內的差壓成為一定。Further, in the present embodiment, when the operation is performed, the differential pressure between the upper portion and the lower portion of the riser tube 2 is measured by the differential pressure measuring means 33. As described above, the second desulfurization material is circulated in the circulating fluidized bed furnace. Therefore, by controlling the supply amount of the second desulfurization material, it is possible to control the differential pressure in the furnace. Therefore, based on the measurement result of the differential pressure measuring means 33, the second desulfurization material supply means 37 controls the supply amount of the second desulfurization material, and the differential pressure in the riser tube 2 is made constant.
升流管2內的差壓是取決於存在升流管2內之粒子量。即,藉由將存在於升流管2內之差壓控制成一定,則能夠將升流管2內的粒子量控制成一定。藉由將升流管2內的粒子量控制成一定,能夠將升流管2內的溫度均等化。又,藉由差壓呈一定,能夠促進固體成分與氣體成分之接觸,進而可促進脫硫反應及氧化反應等。The differential pressure in the riser 2 is dependent on the amount of particles present in the riser 2. That is, by controlling the differential pressure existing in the riser tube 2 to be constant, the amount of particles in the riser tube 2 can be controlled to be constant. By controlling the amount of particles in the riser tube 2 to be constant, the temperature in the riser tube 2 can be equalized. Further, since the differential pressure is constant, the contact between the solid component and the gas component can be promoted, and the desulfurization reaction, the oxidation reaction, and the like can be promoted.
具體而言,在差壓的測定結果較預定值小的情況,藉由第2脫硫材供給機構37,補充第2脫硫材。另外,在差壓較預定值大的情況,藉由第2脫硫材供給機構37,停止第2脫硫材的供給。又,藉由流動媒體排出機構35,從流動層2a,將第2脫硫材與流動媒體一同排出。Specifically, when the measurement result of the differential pressure is smaller than a predetermined value, the second desulfurization material supply mechanism 37 replenishes the second desulfurization material. In addition, when the differential pressure is larger than the predetermined value, the second desulfurization material supply mechanism 37 stops the supply of the second desulfurization material. Further, the second desulfurization material is discharged together with the flow medium from the fluidized bed 2a by the fluid medium discharge mechanism 35.
如以上說明,若依據本實施例,藉由使用第1脫硫材與第2脫硫材,不僅可可在煙道21促進脫鹽作用,並且可促進升流管2內的氧化作用。As described above, according to the present embodiment, by using the first desulfurization material and the second desulfurization material, not only the demineralization action can be promoted in the flue 21, but also the oxidation in the riser tube 2 can be promoted.
又,在NOx濃度變高之情況,藉由濃度測定機構34及燃燒控制機構(風扇15、風扇38),抑制升流管2內的氧化作用。藉此,能夠抑制NOx濃度。Further, when the NOx concentration is high, the concentration measuring means 34 and the combustion control means (fan 15 and fan 38) suppress the oxidation in the riser tube 2. Thereby, the NOx concentration can be suppressed.
又,藉由差壓測定機構33、第2脫硫材供給機構37、及流動媒體排出機構35,能夠將升流管2內的粒子量保持成一定。藉此,能將升流管2內的溫度均等化。又,藉由促進固氣接觸,可促進脫硫反應。Moreover, the amount of particles in the riser tube 2 can be kept constant by the differential pressure measuring means 33, the second desulfurizing means supply means 37, and the flow medium discharge means 35. Thereby, the temperature in the riser tube 2 can be equalized. Moreover, the desulfurization reaction can be promoted by promoting solid-gas contact.
再者,在本實施例,說明了分別設置第1脫硫材投入口13-1與第2脫硫材投入口13-2之情況。但是這些投入口並非一定需要個別設置,能從共通的投入口投入第1脫硫材與第2脫硫材即可。In the present embodiment, the case where the first desulfurization material inlet 13-1 and the second desulfurization material inlet 13-2 are provided separately has been described. However, these input ports do not necessarily need to be separately provided, and the first desulfurization material and the second desulfurization material can be supplied from a common input port.
又,與上述的實施例同樣地,第1脫硫材供給機構36及第2脫硫材供給機構37,亦可藉由廢棄物投入手段12,使第1脫硫材及第2脫硫材與與廢棄物混合後,再投入到升流管2內。藉此,能夠將脫硫材確實地供給到升流管2的下部,可增長升流管2內之脫硫材的滯留時間。其結果,能夠提高脫硫效率。又,在混合最激烈之升流管2的下部,進行脫硫,從這個觀點來看,則能提高脫硫效率。Further, similarly to the above-described embodiment, the first desulfurization material supply mechanism 36 and the second desulfurization material supply mechanism 37 may be configured to cause the first desulfurization material and the second desulfurization material by the waste input means 12. After being mixed with the waste, it is again put into the riser tube 2. Thereby, the desulfurization material can be surely supplied to the lower portion of the riser pipe 2, and the residence time of the desulfurization material in the riser pipe 2 can be increased. As a result, the desulfurization efficiency can be improved. Further, desulfurization is carried out in the lower portion of the most complicated riser pipe 2, and from this point of view, the desulfurization efficiency can be improved.
若依據本發明,藉由爐內脫硫,能夠獲得脫硫與充分的脫鹽效率,又能夠簡單且低成本地進行脫硫與脫鹽,故,可理想地適用於對含有下水道污泥、城市垃圾、產業廢棄物等的氯之廢棄物進行焚燒處理的循環型流體化床爐、 及具備該床爐的系統全體。According to the present invention, desulfurization and sufficient desalination efficiency can be obtained by desulfurization in a furnace, and desulfurization and desalination can be carried out simply and at low cost, so that it can be suitably applied to sewage sludge and municipal waste. a circulating fluidized bed furnace that incinerates chlorine waste such as industrial waste, And the entire system with the bed furnace.
1‧‧‧循環型流體化床爐1‧‧‧Circulating Fluidized Bed Furnace
2a‧‧‧流動層2a‧‧‧Mobile layer
2b‧‧‧乾舷2b‧‧‧ freeboard
2‧‧‧升流管2‧‧‧Rise tube
3‧‧‧旋風器3‧‧‧Cyclone
4‧‧‧降流管4‧‧‧ downflow tube
5‧‧‧密封罐5‧‧‧Sealed cans
6‧‧‧流動媒體返回管6‧‧‧Mobile media return tube
11‧‧‧一次空氣導入口11‧‧‧One air inlet
12‧‧‧廢棄物投入手段12‧‧‧ Waste input means
13‧‧‧脫硫材投入口13‧‧‧Desulfurization input
13-1‧‧‧第1脫硫材投入口13-1‧‧‧1st desulfurization input
13-2‧‧‧第2脫硫材投入口13-2‧‧‧Second desulfurization input
15‧‧‧壓入用風扇15‧‧‧Filling fan
21‧‧‧煙道21‧‧‧ flue
22‧‧‧空氣預熱器22‧‧‧Air preheater
23‧‧‧廢熱鍋爐23‧‧‧Waste heat boiler
24‧‧‧氣體冷卻塔24‧‧‧ gas cooling tower
25‧‧‧袋形過濾器25‧‧‧Bag filter
26‧‧‧誘導用風扇26‧‧‧Induction fan
27‧‧‧煙囪27‧‧‧ chimney
28‧‧‧陶瓷過濾器28‧‧‧Ceramic filter
31‧‧‧壓力感測器31‧‧‧ Pressure Sensor
32‧‧‧壓力感測器32‧‧‧ Pressure Sensor
33‧‧‧差壓測定機構33‧‧‧Differential pressure measuring mechanism
34‧‧‧濃度測定機構34‧‧‧Concentration measuring agency
35‧‧‧流動媒體排出機構35‧‧‧Mobile media discharge agency
36‧‧‧第1脫硫材供給機36‧‧‧1st desulfurization material feeder
37‧‧‧第2脫硫材供給機37‧‧‧Second desulfurization material feeder
38‧‧‧風扇38‧‧‧fan
39‧‧‧空氣預熱器39‧‧‧Air preheater
圖1是具備本發明的實施例之循環型流體化床爐之系統的全體構成圖。Fig. 1 is a view showing the overall configuration of a system including a circulating fluidized bed furnace according to an embodiment of the present invention.
圖2是具備本發明的實施例的應用例的循環型流體化床爐之系統的全體構成圖。Fig. 2 is a view showing the overall configuration of a system including a circulating fluidized bed furnace according to an application example of the embodiment of the present invention.
圖3是顯示對脫硫材投入量之脫硫率與脫鹽率之圖表。Fig. 3 is a graph showing the desulfurization rate and the desalination rate of the amount of desulfurization input.
圖4是顯示燃燒排廢氣性狀之圖。Fig. 4 is a graph showing the behavior of exhaust gas from combustion.
圖5是用來說明脫硫材的作用之概略圖。Fig. 5 is a schematic view for explaining the action of the desulfurization material.
圖6是顯示具備第2實施例之循環型流體化床爐的系統之全體構成圖。Fig. 6 is a view showing the overall configuration of a system including the circulating fluidized bed furnace of the second embodiment.
1‧‧‧循環型流體化床爐1‧‧‧Circulating Fluidized Bed Furnace
2a‧‧‧流動層2a‧‧‧Mobile layer
2b‧‧‧乾舷2b‧‧‧ freeboard
2‧‧‧升流管2‧‧‧Rise tube
3‧‧‧旋風器3‧‧‧Cyclone
4‧‧‧降流管4‧‧‧ downflow tube
5‧‧‧密封罐5‧‧‧Sealed cans
6‧‧‧流動媒體返回管6‧‧‧Mobile media return tube
11‧‧‧一次空氣導入口11‧‧‧One air inlet
12‧‧‧廢棄物投入手段12‧‧‧ Waste input means
13‧‧‧脫硫材投入口13‧‧‧Desulfurization input
15‧‧‧壓入用風扇15‧‧‧Filling fan
21‧‧‧煙道21‧‧‧ flue
22‧‧‧空氣預熱器22‧‧‧Air preheater
23‧‧‧廢熱鍋爐23‧‧‧Waste heat boiler
24‧‧‧氣體冷卻塔24‧‧‧ gas cooling tower
25‧‧‧袋形過濾器25‧‧‧Bag filter
26‧‧‧誘導用風扇26‧‧‧Induction fan
27‧‧‧煙囪27‧‧‧ chimney
Claims (27)
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EP0574176A1 (en) * | 1992-06-08 | 1993-12-15 | Foster Wheeler Energy Corporation | Fluidized bed reactor system and method having a heat exchanger |
TW421607B (en) * | 1997-10-06 | 2001-02-11 | Hitachi Shipbuilding Eng Co | Process and apparatus for removing acid gases from exhaust gases |
TW425306B (en) * | 1995-04-17 | 2001-03-11 | Ernest Csendes | Method and apparatus for the dry grinding of solids, and process for treating combustion gases for removal of Sox and Nox therein |
EP0889943B1 (en) * | 1996-02-21 | 2002-01-23 | Foster Wheeler Energia Oy | Method of operating a fluidized bed reactor system, and fluidized bed reactor system |
EP1448876A1 (en) * | 2001-11-26 | 2004-08-25 | ALSTOM Technology Ltd | Oxygen fired circulating fluidized bed steam generator |
TWM343524U (en) * | 2008-06-12 | 2008-11-01 | zhuo-ran Lu | Device for manufacturing mixed fuel gas |
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Patent Citations (6)
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EP0574176A1 (en) * | 1992-06-08 | 1993-12-15 | Foster Wheeler Energy Corporation | Fluidized bed reactor system and method having a heat exchanger |
TW425306B (en) * | 1995-04-17 | 2001-03-11 | Ernest Csendes | Method and apparatus for the dry grinding of solids, and process for treating combustion gases for removal of Sox and Nox therein |
EP0889943B1 (en) * | 1996-02-21 | 2002-01-23 | Foster Wheeler Energia Oy | Method of operating a fluidized bed reactor system, and fluidized bed reactor system |
TW421607B (en) * | 1997-10-06 | 2001-02-11 | Hitachi Shipbuilding Eng Co | Process and apparatus for removing acid gases from exhaust gases |
EP1448876A1 (en) * | 2001-11-26 | 2004-08-25 | ALSTOM Technology Ltd | Oxygen fired circulating fluidized bed steam generator |
TWM343524U (en) * | 2008-06-12 | 2008-11-01 | zhuo-ran Lu | Device for manufacturing mixed fuel gas |
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