1、(1)理论烟气量和燃烧产物计算序号名称符号单位计算公式结果1理论空气量V0m3/kg0.0889(Car+0.375Sar)+0.265Har - 0.0333Oar6.4302082理论氮气容积V0N20.79 V0+0.8Nar/1005.0830643理论水蒸汽容积V0H2 O0.111Har+0.0124Mar+0.0161 V00.3542264RO2容积VRO21.866Car/100+0.7Sar/1001.268414漏风系数燃烧产物过量空气系数空气的过量空气系数入口出口进口出口制粉系统0.1炉膛0.071.131.20凝渣管1.2低温过热器0.031.23高温过热器1.26I
2、I级省煤器0.021.28II级空气预热器1.311.061.03I级省煤器1.33I级空气预热器1.361.09(2)制粉系统和各受热面漏风系数以及各进出口过量空气系数注:空气预热器区域的漏风只考虑由带正压的受热面空气侧漏入具体选取过程:根据2和3上相关内容,设计所对应煤种Vdaf约为9%,再根据其发热量为23000kJ/kg,可以推断出煤种是劣质无烟煤。固态排渣室燃炉,燃料是无烟煤,炉膛出口过量空气系数范围是1.201.25,取1.20。根据2 表5-4、5-5、5-6可以查出所有的值。然后可以依次计算出制粉系统和各受热面的、,以及两级空气预热器的、。(3)烟气容积及有关特性计算炉膛*和凝
3、渣管低温过热器高温级省煤器空气预热器级平均过量空气系数pj1/2(+”)1.2151.2451.271.2951.3201.345实际水气容 积VH2ONm3/kgV0H2O+0.0161(pj-1) V00.374930.376480.379590.382180.384770.387350.38994烟气容积VyV0N2+ V0H2O+ VRO2+(pj-1) V07.99178.08828.28118.44198.60268.76348.9241份 额rRO2 VRO2/Vy0.158720.156820.153170.150250.147450.144740.142135H2O容积份额r
4、H2OVH2O/Vy0.046910.046550.045840.045270.044730.044200.043706三原子气体容积份额rqrRO2+rH200.205630.203370.199010.195520.192170.188940.185837烟气质量Gykg/kg1-Aar/100+1.306pj V010.848410.974411.226311.436311.646211.856212.06618烟气灰粒浓 度h0.9Aar/100Gy0.019000.018780.018360.018020.017700.017380.01708炉膛的一些辐射特性,如辐射减弱系数的肯定
5、是以炉膛出口状态(如”l)为准基,故采用出口过量空气系数,而对各对流受热面的传热计算,是以平均特性为基础的,故采用平均过量空气系数。 烟气温度VRO2=V0N2=V0H2O=I0yV0=(CT)IRO2I0N2I0H2OI0k100170215.63130660.8015153.49929.92132848.79200358454.092601321.60305108.041883.732661710.44300559709.043921992.56463164.012865.614032591.37400772979.225272678.77626221.753879.745423485.1
6、75009941260.806643375.15795281.614917.576844398.2660012251553.818044086.78969343.255983.848305337.0770014621854.429484818.741149407.017080.179786288.7480017052162.6510945560.871334472.548196.0611297259.7090019522475.9412426313.171526540.559329.6612828243.53100022042795.5813927075.621723610.3310481.5
7、414379240.21110024583117.7615447848.251925681.8911647.90159510256.18120027173446.2816978625.962132755.2112827.45175311272.15190045745801.73280414252.9136901307.1021361.73289918641.17200048446144.20296515071.2839261390.6922606.17306619715.02210051156487.94312815899.8241631474.6423862.41323420795.2922
8、0053876832.95328916718.2044021559.3025110.45340221875.57(4)烟气和空气温焓表续上表l=nz=1.2grI=1.23grII=1.26smI=1.28smII=1.31kyI=1.33kyI=1.36II1235.482413.9632448.1712499.481264.003591.203668.9371254.9743720.7651272.5934855.581264.394960.1391291.205029.8431309.0786061.1166149.081293.506281.0291320.897371.4751310
9、.367478.221329.138526.588715.2451343.778841.021362.809865.791339.2010083.581368.3310978.3611225.671359.8811472.981389.4012329.581351.2212606.791381.1213699.131369.5515081.881382.7525089.9726549.181459.21128021.461472.28629485.561464.097由于1000afhAar/ Qar,net=1000*0.9*22.9/23000=0.901.43,烟气焓值不考虑所含灰粒的焓
10、值。(根据7表5-2,固态排渣煤粉炉的afh取0.900.95,在这里取0.90)所用到的计算公式:I0k=V0Cktk;Iy=(VRO2CTRO2+V0N2CTN2+V0H2OCTH2O) ;I=I0y+(-1)I0k 。(5) 锅炉整体热平衡计算公式及数据来源计算炉膛出口过量空气系数l选取,按照步骤(2)中所得数据一公斤燃料输入锅炉热量QrkJ/kgQr=Qnet,ar+ir+Qwr+QzqMar=5(%)小于 Qar,net/628=23000/628=36.62,不计燃料显热ir;不考虑外来热源加热空气以及燃油雾化蒸汽带来热量,以 Qwr、Qzq都记为0,所以Qr=Qnet,ar230
11、00排烟温度py选取。见2表5-2折算硫分Sar,zs=Sar/ Qar,net4182= 0.036%0.2%,硫分低,酸露点不会很高。再加上Mar=5%位于420之间,根据2表5-2,应该取120130,取130排烟热焓Ipy查步骤(4)中温焓表根据py=1.36,通过插值法计算而得1614.68冷空气温度t0lk选取再无特殊外来热源时,一般取定30 oC30冷空气焓Iolk根据(4)中温焓表根据插值法计算得到:(848.79-0)/10030+0 254.64排烟热损失q2%(1614.68-1.36254.64)(100-4)/230005.294机械不完全燃烧损失q4选取,见4P10
12、3根据锅炉原理,进行锅炉设计时,对于固态排渣炉,燃用无烟煤时,选取 q4=4%9化学不完全燃烧损失q3根据4,进行锅炉设计时,煤粉炉q3=0 10灰渣热损失q6Aar=22.9%, Qar,net/418=23000/418=55.02%,不计灰渣热损失11散热损失q5按4图4-2选取0.6412各项热损失之和qiq2+q3+q4+q5+q65.29+0+4+0.64+09.9313锅炉热效率100-9.9390.0714保温系数90.07/(90.07+0.64)0.99315锅炉额定蒸发量Dkg/s给定130*103/360036.1116额定气温过热蒸汽焓igr查水蒸气性质表按P=3.8
13、2+0.1=3.92Mpa,tgs=4503331.817给水焓igs按P=3.821.11.08+0.1=4.64Mpa634.918排污水量Dpy0.03*36.111.08319排污水焓ipy1.1+0.1=4.3Mpa的饱和水焓1107.620锅炉有效利用热Qyx36.11(3331.8-634.9)+1.083(1107.6-634.9)97907.621燃料消耗量B97907.6100/(90.0723000)4.72622计算燃料消耗量Bj4.726*(100-4)/1004.537若排污率2%,排污水热量可不计入有效利用热,然而这里取得=3%,所以需要考虑排污水带走热量。(6)
14、炉膛计算A 炉膛结构计算侧墙面积Fcqm20.5(4.6972.676)+0.5(4.697+5.121)2.404+0.5(5.121+6.225)1.104+6.22510.75+0.5(6.225+3.564) 1.9100.567前墙面积Fqq(2.6762+2.404+1.104+10.750+2.319+0.53.564) 6.99165.740后墙面积Fhq(10.750+2.319+0.5103.808烟窗面积Fyc(1.561+4.395+0.8) 47.224炉膛包复面积F12 Fcq+ Fqq + Fhq + Fyc2111.46+177.97+116.04+47.225
15、17.91炉膛容积V1m3Fcqa111.4609702.964水冷壁管尺寸选用60水冷壁节距Smm75水冷壁管中心到炉膛距离e60水冷壁角系数x1据s/d=75/60=1.25;e/d=60/60=1.0 0.96烟窗角系数xyc透过烟窗热量全部被下游受热面吸收1.0燃烧器面积Fr每个燃烧器占炉墙面积不超1m2,不计水冷壁有效辐射受热面积H1x1(F1-Fyc-Fr) 0.96(517.91-47.224-0)451.855烟窗有效辐射受热面积H2xycFyc1.0炉膛总有效辐射受热面积HlH1+H2451.855+47.224499.080炉膛有效辐射层厚度sm3.6*V1/V23.670
16、2.96/517.974.886炉膛高度h1自冷炉斗中心到出口烟窗中心1.9+10.750+0.5(1.104+2.404+2.676)15.742燃烧器中心到冷炉斗中心高度hr3.60续上表 注:对于容量不大的锅炉,炉膛尺寸主要是根据qv(本设计qv150kW/m3)、灰熔融特性和燃烧器布置而确定。B 炉膛热力计算选取,根据(2)中的表炉膛漏风系数1制粉系统漏风系数zf0.10热空气温度trk选取,见4表8-2根据4表8-2,无烟煤固态排渣炉推荐热风温度为360400,选取360。360热空气焓IorkKJ/Kg查(4)中-I表3127.65tlk30.0254.636每公斤燃料送入炉内空气
17、热量Q k(1-1-zf)Iork+(1+zf)Iolk(1.20-0.07-0.10) 3127.65+(0.07+0.10)3264.771每公斤燃料送入炉内热量Q l23000 1-0/(100-4)+ 3264.77126264.771理论燃烧温度ll通过在1900和2000之间差值得到结果1980.51火焰最高温度处相对高度xmaxhr/hl+x(3.6/15.742)+00.2287系数M0.56-0.5xmax0.56-0.50.4457假定炉膛出口烟温oC先假定,后复核需要迭代1062.0炉膛出口烟焓I13178.705烟气平均热容量(VC)pjKJ/(KgoC)(Q1-I”1)/( 11-”1)(26264.771-13178.705)/( 1980.51-1062)14.247三原子气分压力PqMpaP0.10. 20560.02056