280噸循環(huán)流化床設(shè)計(jì)說明

1、 . 280t/h燃煤循環(huán)流化床鍋爐設(shè)計(jì)- 59 - / 65目 錄摘 要············································

2、;·····················ABSTRACT···························

3、83;································1 緒 論················

4、3;················································1 1.1國外CFB

5、鍋爐發(fā)展與現(xiàn)狀·············································1 1.1.1 國CFB鍋爐發(fā)展·&

6、#183;···············································11.1.2國外CFB鍋爐

7、發(fā)展·················································

8、3;1 1.2 循環(huán)流化床鍋爐優(yōu)缺點(diǎn)···············································

9、·12 鍋爐結(jié)構(gòu)和設(shè)計(jì)簡介···············································

10、···3 2.1 原始資料·············································&#

11、183;··············32.2 煤的元素分析數(shù)據(jù)校核和煤種判別································

12、······3 2.2.1 煤的元素分析數(shù)據(jù)校核·········································

13、····3 2.2.2 煤種判別············································

14、·············42.3 鍋爐的整體布置···································

15、···················43 220t/hCFB鍋爐熱力計(jì)算····························

16、··················63.1 鍋爐燃燒產(chǎn)物和鍋爐熱平衡計(jì)算·····························

17、;···········6 3.1.1 燃燒產(chǎn)物計(jì)算····································

18、83;················6 3.1.2 無脫硫工況計(jì)算·······························

19、····················6 3.1.3 有脫硫工況計(jì)算···························

20、83;·······················8 3.1.4 煙氣特性計(jì)算表························

21、··························11 3.1.5煙氣焓溫計(jì)算表·····················

22、83;·····························123.2 鍋爐熱平衡與燃燒和石灰石消耗量計(jì)算················

23、3;················123.3爐膛與汽冷屏設(shè)計(jì)與熱力計(jì)算······························

24、3;···········15 3.3.1 爐膛結(jié)構(gòu)設(shè)計(jì)與計(jì)算···································

25、3;··········15 3.3.2 爐膛水冷壁傳熱計(jì)算····································

26、3;·········18 3.3.3 汽冷屏結(jié)構(gòu)設(shè)計(jì)與計(jì)算·····································

27、83;······21 3.3.4 汽冷屏傳熱計(jì)算·········································

28、;·········22 3.3.5 鍋爐爐膛整體熱力計(jì)算·····································

29、3;······253.4 汽冷旋風(fēng)分離器設(shè)計(jì)與熱力計(jì)算·······································293.4.1

30、旋風(fēng)分離器結(jié)構(gòu)計(jì)算··············································293.4.2 旋風(fēng)分離器熱力

31、計(jì)算··············································30 3.5 高溫過熱器設(shè)計(jì)與熱力計(jì)算

32、83;··········································333.5.1 高溫過熱器結(jié)構(gòu)計(jì)算····

33、3;·········································333.5.2 高溫過熱器熱力計(jì)算······

34、;········································353.6低溫過熱器設(shè)計(jì)與熱力計(jì)算·······

35、····································383.6.1 低溫過熱器結(jié)構(gòu)計(jì)算···········&

36、#183;··································383.6.2 低溫過熱器熱力計(jì)算············&#

37、183;·································403.7省煤器設(shè)計(jì)與熱力計(jì)算··············

38、;··································433.7.1 省煤器結(jié)構(gòu)計(jì)算·············&#

39、183;····································433.7.2 省煤器熱力計(jì)算···········

40、;·······································453.8管式空氣預(yù)熱器設(shè)計(jì)與熱力計(jì)算·······

41、3;································473.8.1 管式空氣預(yù)熱器結(jié)構(gòu)計(jì)算··············

42、83;···························473.8.2 管式空氣預(yù)熱器熱力計(jì)算···················&#

43、183;······················50 3.9熱力計(jì)算數(shù)據(jù)的修正·························

44、;·························52 3.10 熱力計(jì)算數(shù)據(jù)匯總表······················

45、··························544 結(jié) 論·······················

46、;·········································56 辭········&

47、#183;·················································&

48、#183;·······57參考文獻(xiàn)·········································&

49、#183;·····················58附 錄···························&#

50、183;······································59摘 要循環(huán)流化床鍋爐是近幾十年發(fā)展起來的一種新型燃燒設(shè)備，其具有燃料適應(yīng)性廣、有利于環(huán)保、負(fù)荷調(diào)節(jié)性好、燃燒熱強(qiáng)度大、爐傳熱能力強(qiáng)等

51、優(yōu)點(diǎn)。所以，其一經(jīng)推出就在世界圍得到了廣泛的應(yīng)用。特別是在中國，循環(huán)流化床鍋爐技術(shù)在近幾十年取得了長足的進(jìn)步。循環(huán)流化床鍋爐包括本體設(shè)備和輔助系統(tǒng)兩部分。CFB鍋爐本體由爐膛與布風(fēng)裝置、循環(huán)灰分離器、回料閥、尾部受熱面豎井煙道與可以加置的外置式循環(huán)灰換熱器組成。循環(huán)流化床鍋爐主要輔助系統(tǒng)包括風(fēng)煙系統(tǒng)、煤制備系統(tǒng)、石灰石制備系統(tǒng)、灰渣處理系統(tǒng)、燃油點(diǎn)火啟動(dòng)系統(tǒng)、熱控系統(tǒng)1。在整個(gè)設(shè)計(jì)過程中進(jìn)行了鍋爐整體的熱力計(jì)算。熱力計(jì)算包括爐膛、高溫過熱器、低溫過熱器、省煤器以與空氣預(yù)熱器的計(jì)算。在此基礎(chǔ)上，利用CAD繪制鍋爐結(jié)構(gòu)圖、主要部件三視圖。關(guān)鍵詞：循環(huán)流化床鍋爐；熱力計(jì)算；汽冷屏；旋風(fēng)分離器；過熱器

52、The Design of 280t/h CFB BoilerABSTRACTThe CFB is the new combustion equipment which is developed in the recent years, it has the advantages of be widely adapt to fuels,be good for environment,load adjustment well,burning intensity is big,heat transfer is strong in the firebox and so on.So,it is wid

53、ely applied in the world.Especially in China,the technolog of CFB is made great progress in the recent years.CFB boiler including body systems and auxiliary equipment two parts. CFB body are compose of boiler furnace and air distribution device, loop ash separator, return valve, silo flue of heating

54、 surface and external circulating ask heat exchanger.The main auxiliary systems of circulating fluidized bed boiler system including Wind and Smoke, coal preparation system, limestone preparation system, ash handling system, fuel ignition system, thermal control systems.Throughout the design process

55、, we make the thermodynamic calculation. Thermodynamiccalculation of the furnace, high temperature superheater, low temperature superheater, economizer and air preheater of calculation.On this basis, the use of CAD drawing the boiler chart and three view of the main parts.Key Words:CFB; thermodynami

56、c calculations; Gas cooled screen; The Cyclone Separator; superheater unit1 緒 論1.1 國外CFB鍋爐發(fā)展與現(xiàn)狀鍋爐作為一種能源轉(zhuǎn)換設(shè)備，在工業(yè)生產(chǎn)和生活中得到廣泛的應(yīng)用。鍋爐是利用燃料燃燒釋放的熱能或其它熱能將工質(zhì)加熱到一定參數(shù)的設(shè)備。隨著科學(xué)技術(shù)的發(fā)展，鍋爐無論在受熱面的結(jié)構(gòu)還是在燃燒方式上都有了很大的改進(jìn)，以至于鍋爐效率得到了提高，這對能源利用，保護(hù)環(huán)境都有重要的意義。燃煤鍋爐燃燒排放出大量的灰渣、二氧化硫等氣固污染物，嚴(yán)重影響生態(tài)環(huán)境。再由于煤等化石燃料的燃燒而日益枯竭，高效率、低污染的燃燒方式就顯得格外重要

57、。循環(huán)流化床鍋爐是從上世紀(jì)七十年代發(fā)展的清潔燃燒技術(shù)，對環(huán)境問題的解決與其重要2。1.1.1 國CFB鍋爐發(fā)展自1979年熱功率為15MW的首臺商業(yè)化循環(huán)流化床鍋爐在芬蘭Pihlava投運(yùn)以來，循環(huán)流化床鍋爐得到較快發(fā)展。為了吸收和借鑒國外CFB鍋爐的先進(jìn)技術(shù)和成功經(jīng)驗(yàn)，1987年，引進(jìn)國外先進(jìn)設(shè)備，建立了我國100MW CFB鍋爐示電站。引進(jìn)示工程建在我國重點(diǎn)高硫煤地區(qū)之一的省，100MWCFB鍋爐發(fā)電機(jī)組安裝在江發(fā)電總廠高壩發(fā)電廠3。經(jīng)過10多年的研究和實(shí)踐，國一批技術(shù)實(shí)力雄厚、多年從事CFB鍋爐技術(shù)開發(fā)研究的科研院所和高校，已擁有一定的試驗(yàn)設(shè)施和試驗(yàn)研究手段，已具備較強(qiáng)的CFB鍋爐技術(shù)開

58、發(fā)能力。已生產(chǎn)出了具有自主知識產(chǎn)權(quán)的50MW等級CFB鍋爐，并已具備設(shè)計(jì)100MW等級CFB電站鍋爐的能力，目前正在研制具有自主知識產(chǎn)權(quán)的100MW等級和125MW級CFB電站鍋爐，并擬在消化吸收國外先進(jìn)技術(shù)的基礎(chǔ)上，與國研究、制造單位合作，有所創(chuàng)新地自行研制300MW等級的CFB電站鍋爐4。1.1.2 國外CFB鍋爐發(fā)展國外的先進(jìn)性表現(xiàn)在：基礎(chǔ)工作扎實(shí)、鍋爐的再用效率較高、燃燒效率高、負(fù)荷調(diào)節(jié)性好, 自動(dòng)控制水平高。 目前國外CFBB設(shè)計(jì)結(jié)構(gòu)特點(diǎn)上主要分為三大流派：德國魯奇公司為代表的魯奇型CFBB、芬蘭奧斯龍公司的百寶爐型CFBB 、 美國福斯特·惠勒公司的CFBB、德國Circ

59、ofluid型和循環(huán)型5。1.2 循環(huán)流化床鍋爐優(yōu)缺點(diǎn)（1）CFB優(yōu)點(diǎn)，具體如下：煤種適應(yīng)性廣。它除了燃用一般種類的煤外，還可以燃燒低熱值的煤矸石、煤泥、造氣爐渣、生活垃圾等，從而對處理城市垃圾、能源的綜合利用和減少環(huán)境污染有著非常顯著的經(jīng)濟(jì)效益和社會效益6。高效脫硫。由于循環(huán)流化床鍋爐燃燒溫度在850-950之間，對脫硫非常有利，且分離器效率高，脫硫劑很細(xì)，再加上物料循環(huán)使脫硫劑得以循環(huán)利用，石灰石的利用率高，因此脫硫效率高。燃燒效率高。CFBB燃燒效率高是因?yàn)?:空氣和燃料混合充分；燃燒速率高：對粗燃料分離效率高，未燃盡的燃料會被循環(huán)裝置再循環(huán)至爐膛再次燃燒7。氮氧化物排放低。循環(huán)流化床鍋

60、爐 的爐膛溫度一般較低，再通過合理配風(fēng)、組織分段燃燒，可以有 效地減少 的生成。也可易于實(shí)現(xiàn)灰渣 的綜合利用。（2）CFB缺點(diǎn)，具體如下：支持燃料沸騰的一次風(fēng)由鼓風(fēng)機(jī)從爐膛底部噴入，但受風(fēng)機(jī)功率的限制，影響了鍋爐的出力8。CFBB的運(yùn)行維護(hù)比較煩繁瑣。循環(huán)流化床更容易結(jié)焦。爐膛密相區(qū)磨損嚴(yán)重，密封性差。2 鍋爐結(jié)構(gòu)和設(shè)計(jì)簡介2.1 原始數(shù)據(jù)（1）額定蒸發(fā)量 ： 280t/h ；（2）過熱蒸汽壓力 ： 9.8MP ；（3）過熱蒸汽溫度 ： 540 ；（4）設(shè)計(jì)熱效率 ： >=85% ；（5）排污率 ： 2% ；（6）給水溫度 ： 215 ；（7）冷空氣溫度 ： 20 ；（8）燃料特性 ：

61、原料名稱：元寶山褐煤 ； 煤的收到基成分：Car=39.3%、Oar=11.2%、Sar=0.9%、Har=2.7%、Nar=0.6%、Mar=24.0%、Aar=21.3%9； 煤的干燥無灰基揮發(fā)分與低位發(fā)熱量：Vdaf=44.0%、Q=14580kj/kg； 灰熔點(diǎn)：DT=1150、ST=130010；2.2 煤的元素分析數(shù)據(jù)校核和煤種判別2.2.1 煤的元素分析數(shù)據(jù)校核（1）煤的元素各種成分之和為100%的校核 ：Oar + Sar + Har + Nar + Mar +Aar +Car =11.2+0.9+2.7+0.6+24.0+21.3+39.3=100%（2）煤的元素分析數(shù)據(jù)校核

62、 ： 干燥無灰基成分份額 ： Kdaf=100/(100- Mar - Aar)=1.828Cdaf= Kdaf * Car =1.828*39.3=71.84% 、Hdaf=1.828*2.7=4.94%、Odaf=1.828*11.2=20.47%、Ndaf=1.828*0.6=1.10%、Sdaf=1.828*0.9=1.65% 干燥基灰分計(jì)算 ： Ad=100 Aar/(100- Mar)=100*21.3/(100-24.0-21.3)=28.03% 干燥無灰基低位發(fā)熱量的計(jì)算 ： Q=( Q+25* Mar)*100/(100- Mar - Aar) =(14580+25*24)*

63、100/(100-24.0-21.3) =27751kj/kg2.2.2 煤種判別（1）因干燥無灰基Vdaf=44.0% ，屬于圍Vdaf>40%；且Q=14580kj/kg>11500 kj/kg,所以此煤為高揮發(fā)分的煙褐煤。（2）折算成分計(jì)算 ： Aar.zs=4187* Aar/ Q=4187*21.3/14580=6.12% Mar.zs=4187* Mar / Q=4187*24.0/14580=6.89% Sar.zs=4187* Sar / Q=4187*0.9/14580=0.26%Aar=21.3%<24%,為常灰分的煤；Vdaf=44.0%、Mar=24.

64、0%，為高水分高揮發(fā)分煤；Sar=0.9%，為低硫煤。2.3 鍋爐的整體布置（1）爐膛溫度，是CFBB設(shè)計(jì)時(shí)的關(guān)鍵數(shù)據(jù)之一。根據(jù)煤種與爐膛放熱份額為1，選擇較高的爐膛燃燒溫度為950，因?yàn)樗鼤绊戝仩t的燃燒效率和水冷壁的吸熱量以與吸收劑的利用情況，從而滿足和的排放要求。（2）布風(fēng)板作為重要的布風(fēng)裝置，其在流化床鍋爐中作用有三個(gè)：一是支承靜止的燃料層：二是使布風(fēng)板上具有均勻的氣流速度分布：三是維持流化床層的穩(wěn)定。本鍋爐采用風(fēng)帽式布風(fēng)板。風(fēng)帽上小孔的面積之和遠(yuǎn)小于布風(fēng)板的面積，通過風(fēng)帽上的小孔的氣流速度很大，高速氣流進(jìn)入床層的底部，對床層顆粒產(chǎn)生強(qiáng)烈的擾動(dòng)，氣固質(zhì)量交換強(qiáng)烈，這對于均勻床層和提高流

65、化質(zhì)量都是非常重要的11。（3）循環(huán)流化床鍋爐的爐膛由膜式水冷壁構(gòu)成，保證了良好的氣密性。底部為一次風(fēng)區(qū)。一次風(fēng)經(jīng)布風(fēng)板上的風(fēng)帽均勻進(jìn)入爐膛底部，確保底部流化狀態(tài)，使燃燒粒子充分混合。二次風(fēng)離底部約5m高處射入爐膛燃燒。回料口與給煤口均位于爐膛的下部1.5到兩米處。此機(jī)組燃燒器為風(fēng)道型燃燒器，實(shí)施床下點(diǎn)火，是高溫?zé)煔馀c一次風(fēng)一起，經(jīng)布風(fēng)板送入爐膛，加熱床料12。（4）爐膛尺寸主要為爐膛深度、寬度、高度和爐膛下部界面收縮部分的尺寸。燃燒室的截面寬度與深度的確定應(yīng)考慮如下主要因素：燃燒室受熱面、局部受熱面、分離器的布置等相協(xié)調(diào)；二次風(fēng)在燃燒室的穿透深度；燃料、石灰石與回灰的供給與擴(kuò)散13。本次設(shè)計(jì)

66、選取爐膛寬深比為1:1，截面為8804mm*8804mm,截面熱負(fù)荷為2.53MW/m2。（5）燃燒室的高度,是循環(huán)床鍋爐設(shè)計(jì)的一個(gè)重要參數(shù)。高度的確定應(yīng)綜合考慮幾個(gè)方面的要求：保證燃料流化完全燃燒；有足夠的空間布置受熱面保證吸熱量；保證脫硫所需的氣體最短停留時(shí)間；保證足夠的循環(huán)物料正常回送；與尾部受熱面布置所需的高度相協(xié)調(diào)14。此次280t/h燃煤循環(huán)流化床鍋爐設(shè)計(jì)的爐膛高度為自布風(fēng)板至爐頂最低處為33米。 （6） 過熱器由屏式過熱器、旋風(fēng)分離器、高溫過熱器、低溫過熱器、爐頂包覆管。蒸汽流程為：鍋筒-屏式過熱器-旋風(fēng)分離器-一級噴水減溫器-低溫過熱器-二級噴水減溫器-爐頂包覆管-高溫過熱器-

67、由集箱進(jìn)入汽輪機(jī)。（7） 本設(shè)計(jì)鍋爐爐膛四壁由膜式水冷壁組成,膜式水冷壁采用的無縫鋼管，管節(jié)距為80mm。前墻水冷壁管屏下部與集箱連接，上部過爐頂后與上集箱連接，最后蒸汽由管子引入鍋筒。后墻水冷壁管屏與前墻相似，但不過爐頂。兩側(cè)水冷壁管屏下部分別與下級箱連接，上部與上集箱連接，再由管子引入鍋筒。（8） 該分離器直徑D0為6458mm，筒體高h(yuǎn)為9000mm，總高度H為20000mm，排灰口直徑D0為1242mm，分離器入口高度a為8000mm，分離器入口寬度b為1600mm，排氣管直徑De為2990mm，排氣管插入深度hc 為1355mm。分離器從到外分別是耐火層、保溫層、鋼外殼?？偙诤?00

68、mm。（9） 尾部對流受熱面的設(shè)計(jì)。高溫分離器接著連接尾部對流煙道，布置有過熱器、省煤器和空氣預(yù)熱器。在高溫與低溫過熱器之間，布置有噴水減溫器，使過熱蒸汽溫度在設(shè)計(jì)允許的圍波動(dòng)。過熱器之后，布置有省煤器，省煤器出口煙溫比給水溫度高為適宜，本次設(shè)計(jì)控制在40左右，使省煤器和空氣預(yù)熱器之間達(dá)到最佳吸熱比15。Mar.zs=6.89%(3%20%)、tgs=215(215280),故所選排煙溫度暫定為135?？諝忸A(yù)熱器，本次設(shè)計(jì)為豎管式，管流體為煙氣管外為空氣，以減少漏風(fēng)，煙氣速度一般取16，本次設(shè)計(jì)為10.64m/s。具體設(shè)計(jì)尺寸見第三章詳解。3 220t/hCFB鍋爐熱力計(jì)算3.1 鍋爐燃燒產(chǎn)物

69、和鍋爐熱平衡計(jì)3.1.1 燃燒產(chǎn)物計(jì)算計(jì)算理論空氣量和理論煙氣容積：Oar + Sar + Har + Nar + Mar + Aar +Car（1）、理論空氣量：V0=0.0889*（Car +0.375* Sar）+0.265*（Har - Oar /8） =0.0889*（39.3 +0.375* 0.9）+0.265*（2.7 11.2/8） =3.87m3/kg（2）、理論氮?dú)馊莘e：VN20=0.8* Nar /100+0.79 V0 =0.8*0.6/100+0.79*3.87 =3.54 m3/kg（3）、三原子氣體容積：VRO2=1.866* Car /100+0.7* Sar

70、 /100 =1.866*39.3/100+0.7*0.9/100 =0.74 m3/kg（4）、理論水蒸氣容積：VH2O0=11.1* Har /100+1.24* Mar /100+0.0161* V0 =11.1*2.7/100+1.24*24.0/100+0.0161*3.87 =0.60 m3/kg（5）、理論煙氣容積：Vy0= VH2O0+ VRO2+ VN20 =3.54+0.74+0.60 =4.88 m3/kg3.1.2 無脫硫工況計(jì)算 根據(jù)該鍋爐的燃料屬性為劣質(zhì)褐煤，查循環(huán)流化床燃燒鍋爐選擇爐膛出口過量空氣系數(shù)為=1.20，具體見表3.2（1）、無脫硫工況的燃料計(jì)算：表3-

71、1 無脫硫工況時(shí)燃料計(jì)算 序號 名稱符號公式與來源數(shù)值單位1理論空氣量0.0889(+0.375)+0.265-0.03333.87m3/kg續(xù)表3-12三原子氣體體積0.74m3/kg3理論氮?dú)怏w積3.54m3/kg4理論水蒸氣體積0.60m3/kg5飛灰份額測量值0.7（2）、無脫硫工況的煙氣體積計(jì)算：表3-2 無脫硫工況時(shí)煙氣體積計(jì)算名稱公式符號爐膛旋風(fēng)筒高溫過熱器低溫過熱器省煤器空氣預(yù)熱器單位出口過量空氣系數(shù)1.201.221.241.271.281.38平均過量空氣系數(shù)1.1951.211.231.2651.281.335過量空氣量0.75470.81270.89011.02561.

72、08361.2965m3/kg水蒸氣體積0.61220.61310.61430.61650.61740.6209m3/kg煙氣總體積5.64695.70585.78445.92215.98106.1974m3/kg3.1.3 有脫硫工況計(jì)算有脫硫工況的燃燒計(jì)算：表3-3 脫硫計(jì)算序號名稱符號公式與來源數(shù)值單位1SO2原始排放濃度（1.998×104）/2887.0mg/m32SO2允許排放濃度“GB13271鍋爐大氣污染物排放標(biāo)準(zhǔn)”表2900mg/m33計(jì)算脫硫效率（1-/）×100%68.53mg/m34燃煤子脫硫能力系數(shù)A測量值80.85石灰石脫硫能力系數(shù)K測量值0.8

73、0556鈣硫摩爾比M)/A/K1.1717石灰石中CaCO3含量見表2-397.32%8入爐石灰石量3.122m/0.0338kg/kg 9CaCO3未利用率測量值15.0%10煅燒成CaO時(shí)吸熱量（1-）×5561.8m/10049.82kj/kg11脫硫時(shí)放熱量15597.7(/100)× (/100)96.20kj/kg12可支配熱量 (+A ×)/(1+)16085.37kj/kg續(xù)表 3-313燃燒所需理論空氣量 見表3-23.87m3/kg14脫硫所需理論空氣量1.667(/100)× (/100)0.0103m3/kg15燃燒和脫硫當(dāng)量理論

74、空氣量(+)/(1+)3.75m3/kg16燃燒產(chǎn)生理論氮?dú)怏w積見表3-23.54m3/kg17脫硫所需空氣中氮?dú)怏w積0.790.00814m3/kg18當(dāng)量理論氮?dú)怏w積(0.8/100)/(1+)+0.792.9671m3/kg19燃燒產(chǎn)生RO2體積見表3-20.74m3/kg20煅燒石灰石生成CO2體積0.699m(/100)0.00737m3/kg21脫硫使SO2減少量0.699(/100)× (/100)0.00431m3/kg22燃燒和脫硫時(shí)產(chǎn)生RO2當(dāng)量體積(+-)/(1+)0.7188m3/kg23燃燒產(chǎn)生理論水蒸氣體積見表3-20.60m3/kg24當(dāng)量理論水蒸氣體積

75、0.0124(+Md)+0.111/(1+)+0.01610.6422m3/kg25入爐燃料灰量/1000.213kg/kg26入爐石灰石直接生成飛灰量3.122(/100)m(/)0.00507kg/kg27入爐石灰石灰分含量(100-)/100* (1-/100- Md/100)7.4kg/kg續(xù)表 3-328未反應(yīng)CaO的量1.749(100-)/100m(/100)-(/100)(/100)4.88kg/kg29脫硫產(chǎn)物CaSO4的量 4.26(/100)(/100)0.0263kg/kg30當(dāng)量灰分(+)/(1+)24.18%31未脫硫時(shí)底灰份額 取定0.332脫硫工況時(shí)底灰份額(/

76、100)+/(1+)(/100)0.383333未脫硫時(shí)飛灰份額1-0.734脫硫時(shí)飛灰份額(/100)+/1+)(/100)0.616735分離效率設(shè)計(jì)值99%36灰循環(huán)倍率/（1-）69.337分離器前飛灰份額+69.9238脫硫后的SO2排放濃度（1.998×104）×1-(/100)913.11mg/m339脫硫效率（1-/）×10068.37%40誤差（-）/=0.00230.15%合格3.1.4 煙氣特性計(jì)算表不同過量空氣系數(shù)下燃燒產(chǎn)物的容積與成分見表3-4。 表3-4 煙氣特性表名稱符號公式分離器前分離器后單位a=54.33a=0.5433爐膛分離器

77、高溫過熱器低溫過熱器省煤器空氣預(yù)熱器平均過量空氣系數(shù)(+)/21.1951.211.231.2651.281.335水蒸氣容積0.65390.65480.65610.65820.65910.6624m3/kg煙氣總?cè)莘e5.07115.5.12825.20455.33795.39505.6046m3/kgRO2容積份額0.14170.14020.13810.13470.13320.1282H2O容積份額0.12890.12770.12610.12330.12220.1182三原子氣體容積份額0.27060.26790.26420.25800.25540.2464飛灰濃度3333.923296.8

78、03248.473167.293133.763016.57g/m3煙氣重量6.68876.76326.86247.03667.11117.3840kg/kg煙氣密度1.31901.31881.31861.31821.13811.1375kg/m33.1.5煙氣焓溫計(jì)算表不同過量空氣系數(shù)下燃燒產(chǎn)物的焓溫表見表3-5。表3-5 煙氣焓溫表Iy= I0y +( -1) I0k空預(yù)器=1.3816804.691628.682474.473345.294211.105151.156089.367050.28026.879008.22省煤器=1.2915760.041538.802338.533162.5

79、23980.224871.095758.726668.697594.478523.84低溫過熱器后=1.2714750.121518.832308.323121.903928.914808.855685.246583.917498.388415.83高溫過熱器后=1.2413735.231488.872263.003060.983851.954715.505575.026456.747354.248254.27V0D=3.75m3/kg(C)k× V0D12496.13998.631510.502030.752565.383111.753673.884239.004804.50538

80、5.38(C)k11132.3266.3402.8541.8684.1829.8979.71130.41281.21436.11595.2I0ykj/(kg)3+5+7+910616.161249.201900.482573.603236.263968.684693.295439.386201.166961.78ADar=24.18% 0f=0.6167(C)A×Aa 0f/100912.0525.2239.3453.7068.3783.5498.78114.37130.48146.72(C)A880.8169.1263.8360.1458.5560.2662.4767.0875.0

81、983.91096.9VDH20=0.6422m3/kg(C)H2O× VDH20796.78195.48296.95402.21481.46621.13736.73857.72978.711107.80(C)H2O6150.7304.4462.6626.3794.7967.21147.21335.61524.01725.01925.9V0DN2=2.9671m3/kg(C)CN2× V0DN25385.13771.461162.811562.771970.152385.252807.473242.453689.594124.27(C) N24129.8260.0391.9

82、526.7664.0803.9946.21092.81243.51390.01544.9VDRO2=0.7188m3/kg(C)CO2 ×VDRO23122.20257.04401.74554.92716.28878.731050.311224.841402.381583.02(C)CO22170.0357.6558.9772.0996.51222.51461.21704.01951.02202.32457.7溫度1100200300400500600700800900100011003.2 鍋爐熱平衡與燃燒和石灰石消耗量計(jì)算表3-6 鍋爐熱平衡與燃料和石灰石的計(jì)算續(xù)表 3-6序號名

83、稱符號計(jì)算公式來源數(shù)值單位1可支配熱量見表3-3 16085.37kj/kg2排煙溫度設(shè)定1353排煙焓查焓溫表3-61093.08kj/kg4冷空氣溫度給定205冷空氣焓616.查焓溫表3-690.23kj/kg6脫硫工況時(shí)底灰含炭量試驗(yàn)數(shù)據(jù)1.5%7脫硫工況時(shí)底灰份額見表3-30.38338脫硫工況時(shí)飛灰含炭量試驗(yàn)數(shù)據(jù)6.0%9脫硫工況時(shí)飛灰份額見表3-30.616710固體不完全燃燒損失1.71%11底灰溫度85012灰焓查循環(huán)流化床鍋爐設(shè)計(jì)與計(jì)算表8-2821kj/kg13灰渣物理熱損失0.35%14氣體不完全燃燒損失查循環(huán)流化床鍋爐設(shè)計(jì)與計(jì)算表8-10.04%續(xù)表 3-615排煙損失6.75%16散熱損失查循環(huán)流化床鍋爐設(shè)計(jì)與計(jì)算表8-10.5%17鍋爐熱效率90.65%18保溫系數(shù)0.994519過熱蒸汽出口焓MPa，3477.16kj/kg20飽和蒸汽焓MPa，2709.36kj/kg21飽和水焓 MPa，1443.10kj/kg22給水溫度給定21523給水焓 M