220t鍋爐課程設(shè)計(jì)220th煤粉鍋爐熱力設(shè)計(jì)

1、鍋爐課程設(shè)計(jì)課題名稱：220t/h煤粉鍋爐熱力設(shè)計(jì)專業(yè)、班級(jí)：熱能與動(dòng)力工程、熱動(dòng)111、設(shè)計(jì)題目：220t/h煤粉鍋爐熱力設(shè)計(jì)二、原始資料：鍋爐額定蒸發(fā)量：D=220t/h=220X103kg/he給水溫度：t=215Cgs過熱蒸汽溫度：t=540Cgr過熱蒸汽壓力：p=9.8MPagr制粉系統(tǒng)：中間倉(cāng)儲(chǔ)式（熱空氣作干燥劑、鋼球筒式磨煤機(jī)）燃燒方式：四角切圓燃燒排渣方式：固態(tài)環(huán)境溫度:20C高溫對(duì)流過熱煙氣流程：爐膛f高溫對(duì)流過熱器f低溫對(duì)流過熱器f高溫省煤器f高溫空氣預(yù)熱器f低溫省煤器f低溫空氣預(yù)熱器鍋爐受熱面的布置結(jié)構(gòu)如右圖：本組選用的燃料為新汶煤，首先要對(duì)燃料的應(yīng)用基成分進(jìn)行校核，本燃

2、料校核是100%,一上顋空預(yù)窣-下辭悝睪表1-7新汶煙煤煤質(zhì)分析數(shù)據(jù)元素成分()收到基低位量(kJ/kg)干燥無灰基揮發(fā)分Vdaf(%)空氣干燥基水Mad(%)BTH法可磨性系數(shù)Kkm灰熔點(diǎn)水分灰分碳?xì)溲醯蜃冃螠囟菵T(C)軟化溫度ST(C)熔化溫度FT(C)MarAarCarHarOarNarSar618.8604.16.81.42.9251404021.412001500表2-8燃燒計(jì)算表序號(hào)項(xiàng)目名稱符號(hào)單位計(jì)算公式及數(shù)據(jù)結(jié)果1理論空氣量V0Nm3/kg0.0889(C+0.375S)+0.265H-0.03330arararar5.2258778752理論氮容積V0N22Nm3kgNV

3、0.8+0.79V01004.1516435213RO容2積VRO2Nm3/kgCS1.866碩+0.7碩1.13994理論干煙氣容積V0GYNm3/kgV0+VN2RO225.2915435215理論水蒸汽容積V0H2ONm3/kgHMdVd11.1a+1.24ar+1.61dV0(d=0.01kg/k100100kk總g)0.6136366346飛灰份額afh查表2-40.8三、空氣平衡量及焓溫表表2-9煙氣特征表序號(hào)項(xiàng)目名稱符號(hào)單位爐膛，屏凝渣管高過低過高溫省煤器高溫空預(yù)器低溫省煤器低溫空預(yù)器1漏風(fēng)系數(shù)a0.050.0250.0250.020.050.020.052受熱面出口過量空氣系數(shù)

4、a_1.21.2251.251.271.321.341.393煙道平均過量空氣系數(shù)aPJ_1.21.21251.23751.261.2951.331.365干煙氣容Vm3/kg6.33676.402046.532686.650276.833177.016087.198984積GY190962579517176974943228946水蒸氣容Vm/kg0.63040.631510.633610.635510.638450.641400.644345H2O積63961566890842159694117236505煙氣總?cè)軻m3/kg6.96717.033557.166307.285787.471

5、637.657487.843336積Y830578238860139274435494354517R02容積rROc6.33676.402046.532686.650276.833177.016087.19898份額21909625795171769749432289468水蒸氣容rH2O0.63040.631510.633610.635510.638450.641400.64434積份額63961566890842159694117236505三原子氣r9體和水蒸6.96717.033557.166307.285787.471637.657487.84333汽溶劑總8305782388601

6、3927443549435451份額容積飛灰g/m321.58621.383220.987020.642920.129419.640919.175510濃度v91666024995083994644813581544續(xù)表11煙氣質(zhì)量kg/kg9.00199.08739.25799.41149.65039.889210.128my9580608262331759559670474453511202312質(zhì)量飛灰卩ykg/kg1.35391.36671.39231.41541.45141.48731.5232濃度001693116393149889381571942501692822）煙氣焓、空氣

7、焓、蒸汽焓的計(jì)算：爐膛、屏式過熱器、高溫過熱器、低溫過熱器、高溫省煤器、高溫空氣預(yù)熱器、低溫省煤器、低溫空氣預(yù)熱器等所在煙氣區(qū)域的煙氣在不同溫度下的焓，并列成表格作為溫焓表。具體見下表。表2-10煙氣焓溫表（用于爐膛、屏式過熱器、高溫過熱器計(jì)算）煙氣或空氣溫理論煙氣焓h0y（kj/kg）理論空氣焓h0k（kj/kg）理論煙氣焓增（每100C）h0y爐膛、屏、凝渣管高溫過熱器a=1.2a=1.225hyhyhyhy度0(C)4003450.0240732831.1715984376.2583934141.181683927.04553941174.3680891109.2853085004377

8、.0696133575.2843485550.6264825250.4669911132.443911385.9110221318.867436005509.5135224336.1199086936.5375046569.334422795.61906931054.311256985.87413967006305.1325925112.5808437990.848767555.208561997.33419931258.9466761190.2898368007302.4667915900.6432269249.7954368745.4983971012.616971279.43786812

9、08.8006619008315.0837616701.24771710529.23339954.2990571031.7627341303.8440441230.55074810009346.8464957511.1542711833.0773511184.849811045.8484561322.5576751247.991127110010392.694958334.70036413155.6350212432.840931058.3602331334.0728211261.330894120011451.055189163.26330114489.7078413694.17183107

10、2.2731531394.3478371284.518773130012523.3283410003.6367215884.0556814978.69061078.7616061459.0277911300.920464140013602.0899410849.9676417343.0834716279.611061088.8805011445.9305671308.311625150014690.9704411700.2179718789.0140417587.922691097.486911340.8748011301.127087160015788.4573512557.15743201

11、29.8888418889.049781108.5046331516.3942081337.374805170016896.9619913416.605321646.2830520226.424581107.663571397.6158561318.857091180018004.6255614276.3667323043.898921545.281671116.5874851465.1004511339.084172190019121.2130415148.9315624508.9993622884.365841119.2055471447.5094781338.45906920002024

12、0.4185916020.4512125956.5088324222.824911129.7268491433.5149281346.739638210021370.1454416899.3916127390.0237625569.564551126.7882061422.2209261342.198016220022496.9336417776.5552128812.2446926911.76257表2-11煙氣焓溫表(用于低溫過熱器、高溫省煤氣的計(jì)算)煙氣或空氣溫理論煙氣焓h0y(kJ/kg)理論空氣焓h0k(kJ/kg)理論煙氣焓增(每100C)h0y低溫過熱器高溫省煤器度0(C)a=1

13、.25a=1.27hyhyhyhy3002548.4152392104.4087613114.1779093156.266085901.60883451097.7830631112.318324003450.0240732831.1715984211.9609734268.584405927.04553941127.8881271142.7703825004377.0696133575.2843485339.84915411.3547871132.443911337.8883191353.1050316005509.5135224336.1199086677.7374196764.459817

14、795.61906931005.2856631020.8148827006305.1325925112.5808437683.0230827785.274699997.33419931209.9913951225.7526438007302.4667915900.6432268893.0144789011.027342表2-12煙氣溫焓表(用于高溫空預(yù)器、低溫省煤氣的計(jì)算)煙氣或空氣溫度0(C)理論煙氣焓h0y(kJ/kg)理論空氣焓h0k(kJ/kg)理論煙氣焓增(每100C)h0y高溫空預(yù)器低溫省煤器a=1.32a=1.34hyhyhyhy100824.1517506692.0630071

15、057.7642331071.605493849.2398971086.4888011100.4868372001673.3916481391.9648312144.2530332172.09233875.02359141117.2334891131.4823683002548.4152392104.4087613261.4865233303.574698901.60883451148.6564621163.1917194003450.0240732831.1715984410.1429854466.766417927.04553941179.976021194.8582755004377.0

16、696133575.2843485590.1190045661.6246911132.443911391.1468091406.36356005509.5135224336.1199086981.2658137067.988211表2-13煙氣焓溫表(用于低溫空預(yù)器計(jì)算)煙氣或空氣溫度0(C)理論煙氣恰h0y(kJ/kg)理論空氣恰h0k(kJ/kg)理論煙氣恰增(每100C)h0y低溫空預(yù)器a=1.39hyhy100824.1517506692.0630071106.208643849.2398971135.4819282001673.3916481391.9648312241.690572

17、875.02359141167.1045643002548.4152392104.4087613408.795136901.60883451199.5298614003450.0240732831.1715984608.324996927.04553941232.0639125004377.0696133575.2843485840.3889091132.443911444.4052986005509.5135224336.1199087284.7942062.4鍋爐熱平衡及燃料消耗量計(jì)算計(jì)算鍋爐輸入熱量，包括燃料的收到基低位發(fā)熱量，燃料物理顯熱、外來熱源加熱空氣時(shí)帶入的熱量。各項(xiàng)熱損失，包括

18、化學(xué)不完全燃燒熱損失q3和機(jī)械不完全燃燒熱損失q4,鍋爐散熱損失q5,灰渣熱物理?yè)p失q6，排煙熱損失q2。具體數(shù)據(jù)見鍋爐熱平衡及燃料消耗量計(jì)算表2-14.表2-14鍋爐熱平衡及燃燒消耗量計(jì)算序號(hào)名稱符號(hào)單位公式結(jié)果1鍋爐輸入熱量QkJ/kg式(2-8)QrQ25140.0002排煙溫度C先估后算125.0003排煙焓hkJ/kg查焓溫表用插值法求1036.4624冷空氣溫度tlkC取用20.0005理論冷空氣焓holkkJ/kgho=(ct)Vlkk138.4136化學(xué)未完全燃燒損失q%取用0.5007機(jī)械未完全燃燒損失q4%取用1.5008排煙處過量空氣系數(shù)apy查表2-9即低溫空預(yù)器出口過

19、量空氣過量系數(shù)1.3909排煙損失q2%(100-q)(h-aho)/Q4pypylkr3.30710散熱損失q5%取用0.50011灰渣損失%式(2-13)0.00012鍋爐總損失E%2+43+5+45+465.80713鍋爐熱效率n%100-Eq94.19314保熱系數(shù)1-q5/(n+q5)0.99515過熱蒸汽焓hggkJ/kg查附錄B-6、B-7，高溫過熱器出口參數(shù)p=9.9Mpa（查表1-6）,t=540C3475.40016給水溫度tC給定215.00017給水焓hgskJ/kg查附錄B-6、B-7,低溫省煤器入口參數(shù)p=10.78Mpa（查表1-6）,t=215C924.1501

20、8鍋爐實(shí)際負(fù)荷Dkg/h220000.00019鍋爐有效利用熱QkJ/hD(h-h)grgggs561275000.00020實(shí)際燃料消耗量Bkg/h100*Q/(nQr)23702.47821計(jì)算燃料消耗量B.kg/hB(1-q/100)423346.940第三章爐膛熱力計(jì)算表3-1爐膛的結(jié)構(gòu)數(shù)據(jù)序號(hào)名稱符號(hào)單位公式結(jié)果1前墻總面積Aqm27.68(1.395+0.905)+3.995/2+22.176x(5.888+2x1.276)219.622側(cè)墻總面積2Acm2A=(6.912+3.995)x1.762x0.5clA=5.126x12.976C2A=5.126+(6.912-0.896

21、T.76)x1.106x0.5C3A=(6.912-0.896-1.76)x0.334C4A=(6.912-0.896-1.76)+3.39x0.86x0.5C5AC6=6.974x3.39AA=A+A+A+A+A+C6CclC2C3C4C5C6218.483后墻總面積Ahm27.68(1.395+0.905)+3.995/2+12.976x(5.888+2x1.276)+7.68x2.032157.744噴燃器及門孔面積Aycm265爐頂面積Aldm27.68(3.39+0.869)-2x0.5x0.896x0.89632.116爐膛與屏的交界面積A2m2(6.974+0.225+0.334

22、)x7.6865.617爐墻總面積Alm2A+2A+A+A+Ahchld2693.568爐膛截面面積AAm26.912x7.680.8962x251.4799水冷壁管外徑dmm6010水冷壁管節(jié)距smm6411管子至墻中心距emm012水冷壁角系數(shù)XSL0.9813爐頂角系數(shù)XLD0.9814出口煙窗角系數(shù)XYC115爐膛容積VLm3Ax7.68+(7.68+5.888)x0.896x0.5x(22.176+12.976)c1052.616冷灰斗二等分平面到出口煙窗中心距離HLm19.84617冷灰斗二等分平面到爐頂?shù)木嚯xH0m23.93818冷灰斗二等分平面到燃燒器中心距離Hrm4.9621

23、9爐膛總有效輻射受熱面積Alzm20.98x(AA-A)+Al2yc2675.1220爐膛水冷程度XS/ALZ】0.9721爐膛有效輻射層厚度Sm3.6xV/AL】5.466表3-9爐膛校核熱力計(jì)算序號(hào)名稱符號(hào)單位公式結(jié)果1爐膛出口過量空氣系數(shù)ffai查表1-5漏風(fēng)系數(shù)和過量空氣系數(shù)1.2002爐膛漏風(fēng)系數(shù)Aai查表1-5漏風(fēng)系數(shù)和過量空氣系數(shù)0.0503制粉系統(tǒng)漏風(fēng)系數(shù)AaZF查表1-5漏風(fēng)系數(shù)和過量空氣系數(shù)0.1004熱風(fēng)溫度trkC先估后校核270.0005理論熱風(fēng)焓h0rkkj/kg查溫焓表1890.6766理論冷風(fēng)焓h0lkkj/kg查表2-14鍋爐熱平衡及燃料消耗量計(jì)算138.41

24、37空氣帶入爐膛熱量QKkj/kg(aAaAa)h0+llZFrk(Aa+Aa)h0ZFllk2005.9718對(duì)應(yīng)每公斤燃料送入爐膛的熱量QLkj/kgQq+qQQ(1-)+Qr100-qK427018.2779理論燃燒溫度00C查焓溫表2074.06710燃燒絕對(duì)溫度T0K0+27302347.06711火焰中心相對(duì)高度系數(shù)XhAXl0.25012系數(shù)MMA-BX注：A,B取值杳表3-5，表3-60.43513爐膛出口煙氣溫度0lC先估后校1125.00014爐膛出口煙氣焓h”glkj/kg查焓溫表13489.15315煙氣平均熱容量VCkj/(kgC)(Q-h”)/(0-0)Lgl0l1

25、4.25516水冷壁污染系數(shù)匚SL查表3-4水冷壁灰污系數(shù)0.20017水冷壁角系數(shù)x查表3-1爐膛結(jié)構(gòu)數(shù)據(jù)0.98018水冷壁熱有效系數(shù)si屮SL:xSLsl0.19619屏、爐交界面的污染系數(shù)gYC0乙SL0.19620屏、爐交界面的角系數(shù)XYC取用1.00021屏、爐交界面的熱有效系數(shù)屮YCgXYCYC0.19622燃燒孔及門孔的熱有效系數(shù)屮R未敷設(shè)水冷壁0.00023平均熱有效系數(shù)屮PJ(屮A+屮A+屮A)/ASLYC2Ryc10.19424爐膛有效輻射層厚度Sm查表3-1爐膛結(jié)構(gòu)數(shù)據(jù)5.46625爐膛內(nèi)壓力PMPa0.10026水蒸汽容積份額rH2O查表2-9煙氣特征表0.09027

26、三原子氣體容積份額r查表2-9煙氣特征表0.25428三原子氣體輻射減弱系數(shù)kQ1/(m.MP0.78+16r1021.6H2O0.039丄itja)IJ10.2-r-P-s丿rt)10.37L1I1000丿29煙氣質(zhì)量飛灰濃度ykg/m3查表2-9煙氣特征表1.35430灰粒平均直徑dh卩m查附錄B-1筒式鋼球磨球機(jī)（通常取13卩m）13.00031灰粒輻射減弱系數(shù)kH1/(m.MPa)55900毛T2.d2plh0.23232燃料種類修正系數(shù)x1取x=0.510.50033燃燒方法修正系數(shù)x2取x=0.120.10034煤粉火焰輻射減弱系數(shù)k1/(m.MPa)kr+k卩+10 xxQHy1

27、20.82535火焰黑度aH1_e-kps0.76036爐膛黑度alaHa+(1-a)屮HHSL0.94237爐膛出口煙氣溫度ylCT”3600CaAlT327M(爲(wèi)B(tài)T10)+1jC31152.60038計(jì)算誤差A(yù)9收0-D（估）（允許誤差100C）ll27.60039爐膛出口煙氣焓h“yikj/kg查焓溫表13857.35740爐膛有效熱輻射熱量QfLkj/kg申(Q-h”)l只13091.42741輻射受熱面平均熱負(fù)荷qsw/m2BxQf/(3.6xA)jLlz125757.38042爐膛截面熱強(qiáng)度qFw/m2BxQ/(36Ad)A.jr3167106.35043爐膛容積熱強(qiáng)度qVw/m

28、3Bxq/(3.6V)jrL154892.141表3-10爐膛頂棚輻射受熱面吸熱量及工質(zhì)焓增計(jì)算序號(hào)名稱符號(hào)單位公式結(jié)果1頂棚管徑dmm382節(jié)距smm47.53排數(shù)n1584頂棚管角系數(shù)x查標(biāo)準(zhǔn)線算圖1（即附錄A-1）0.985頂棚面積Aid32.116蒸汽流通面積Ait158x(3.14x0.032)/40.1127爐膛頂棚熱負(fù)荷分配不均系數(shù)nH查標(biāo)準(zhǔn)線算圖11（即附錄A-6）（對(duì)本爐型：x=h/H=H/H=23938/23938）0000.6808爐膛頂棚總輻射吸熱量QLDKj/h3.6n人qHAlds423.4049減溫水總量DJWKg/h先估后校8800.00010爐膛頂棚蒸汽流量D

29、LDKg/hDDJW211200.00011爐膛頂棚蒸汽焓增hldKj/kgQ/DLDLD0.00212爐膛頂棚進(jìn)口蒸汽焓h，ldKj/kg查附錄B-6、B-7注：蒸汽參數(shù)汽包壓力對(duì)應(yīng)的干飽和蒸汽2746.95013爐膛頂棚出口蒸汽焓h”ldKj/kgh，+hldld2746.95214爐膛頂棚出口蒸汽溫度t“LDC查附錄B中水和水蒸氣性質(zhì)表按計(jì)算負(fù)荷下汽包壓力p=10.98MPa（查表1-6）317.805第四章對(duì)流受熱面校核熱力計(jì)算一、對(duì)流受熱面計(jì)算步驟：1、假設(shè)受熱面出口煙氣溫度，查取相應(yīng)焓值。2、根據(jù)出口煙焓，通過Q=（I-I+AaIo）計(jì)算對(duì)流傳熱量。dLF3、依據(jù)煙氣側(cè)放熱量等于工

30、質(zhì)側(cè)吸熱量原理，求取工質(zhì)出口焓和相應(yīng)溫度。4、計(jì)算平均對(duì)流傳熱溫差。5、計(jì)算煙氣側(cè)對(duì)流放熱系數(shù)及管壁污染系數(shù)。6、計(jì)算工質(zhì)側(cè)對(duì)流放熱系數(shù)。7、計(jì)算管壁污染層溫度。8、計(jì)算煙氣黑度，及確定煙氣側(cè)輻射放熱系數(shù)。9、計(jì)算對(duì)流放熱系數(shù)K。10、計(jì)算對(duì)流傳熱量。與計(jì)算結(jié)果相比較，其差值應(yīng)在允許范圍之內(nèi)。否則重新假設(shè)受熱面出口煙溫，重復(fù)上述計(jì)算。二、對(duì)流傳熱系數(shù)的處理1）對(duì)流放熱系數(shù)與氣流沖刷方式、速度及介質(zhì)的溫度和物性等有關(guān)。計(jì)算中，可按氣流沖刷方式，直接從線算圖中查取。（2）對(duì)流面結(jié)構(gòu)不同時(shí)，對(duì)流放熱系數(shù)按以下原則處理：一部分管子錯(cuò)列、一部分管子順列布置時(shí)，放熱系數(shù)按管束平均煙氣溫度，分別求出順列和錯(cuò)

31、列的對(duì)流放熱系數(shù)，然后按對(duì)流換熱面積計(jì)算平均對(duì)流放熱系數(shù)。斜向沖刷受熱面時(shí)，對(duì)流放熱系數(shù)按橫向沖刷計(jì)算，在進(jìn)行修正。順列管束，修正系數(shù)為1.07，錯(cuò)列管束不進(jìn)行修正。（3）污層對(duì)于對(duì)流受熱面?zhèn)鳠徇^程的影響，用污染系數(shù)來表示。燃用固體燃料順列布置的受熱面以及凝渣管、對(duì)流管束等，灰污層對(duì)傳熱的影響常用熱有效系數(shù)來表示。（4）利用系數(shù)是考慮煙氣對(duì)受熱面沖刷的不均勻、不完全時(shí)對(duì)傳熱過程的影響修正系數(shù)，各種對(duì)流受熱面的熱力計(jì)算應(yīng)考慮利用系數(shù)。（5）再計(jì)算高溫區(qū)受熱面的對(duì)流換熱量時(shí)，常用煙氣輻射放熱系數(shù)來考慮高溫?zé)煔獾妮椛錈崃浚渲蹬c煙氣黑度、溫度等有關(guān)。（6）出屏式受熱面以外，其他各受熱面加熱介質(zhì)對(duì)管壁

32、的放熱系數(shù)，都包括對(duì)流放熱系數(shù)輻射放熱系數(shù)兩部分。4.1屏、凝渣管的熱力計(jì)算：A,屏式過熱器在熱力計(jì)算方面具有以下特點(diǎn)：在換熱方式上，既受煙氣沖刷，又吸收爐膛及屏間高溫?zé)煔獾臒彷椛洌黄潦竭^熱器屬于中間過熱器，其進(jìn)出口處的工質(zhì)參數(shù)在進(jìn)行屏的計(jì)算時(shí)往往是未知數(shù)；屏與屏之間橫向節(jié)距大，煙氣流速低，且沖刷不完善。所以某些交換參數(shù)不同于一般對(duì)流受熱面。B,凝渣管的熱力計(jì)算主要特點(diǎn)：1，和后屏過熱器類似，也直接吸收爐膛輻射熱。當(dāng)管少于5排時(shí)，將有部分爐膛輻射熱落在其后受熱面上。2，凝渣管區(qū)域都布置其它附加受熱面。3，凝渣管內(nèi)為汽水混合物，在沸騰狀態(tài)下進(jìn)行換熱，工質(zhì)溫度始終為飽和溫度。4，凝渣管總吸熱量包含對(duì)流吸熱量和輻射吸熱量。具體見表4-3。表4-5屏的結(jié)構(gòu)數(shù)據(jù)計(jì)算表序號(hào)名稱符號(hào)單位公式結(jié)果1管子外徑dmm42x52屏的片數(shù)Z123每片屏的管子排數(shù)n4x10404屏的深度Lm2.7065屏的平均高度hm7.46一片屏的平面面積Apm213.57屏的橫向節(jié)距s1mm屏的節(jié)距5918比值c1S/d14.19屏的縱向節(jié)距s2mm4610比值c2S/d1.0911屏的角系數(shù)xP指導(dǎo)書附錄圖1,曲線50.9812屏的計(jì)算受熱面積Apj