有機(jī)仍靨EM鍋爐熱力計(jì)算書

序號名稱符號單位計(jì)算公式及數(shù)字來源數(shù)值■設(shè)計(jì)參數(shù)1額定供熱量QMW13.95(10A4kcal/h)12002介質(zhì)額定循環(huán)量Vm3/s0.2191m3/h789—??介質(zhì)進(jìn)出口溫度計(jì)算1介質(zhì)出口溫度t2?c3352介質(zhì)進(jìn)口溫度tl°C假設(shè)后校孩3073介質(zhì)平均溫度tPj°Ctpj=(tl+t2)/2321.054介質(zhì)種類DOWTHERM-A5介質(zhì)平均溫度下比熱Cpj查表2.8096介質(zhì)平均溫度下密度p1kg/m3查表802.897介質(zhì)吸熱量QikwQj=Cpj*m*AtCpj*V*pl*(t2-tl)14051.38設(shè)計(jì)額定供熱量QikwQ1=1OOO*Q13958.7OW(Qj-Ql)/QlWl%成立9計(jì)算介質(zhì)進(jìn)口溫度tij°Ctlj=t2-Ql/(Cpj*V*pl)307.28二.燃料燃燒計(jì)算燃煤種類：山東良莊（II類煙煤）1燃料成分Cy46.55Hy3.06Oy6.11Sy1.94Ny0.86Ay32.48Wy92燃料低位發(fā)熱值QdwkJ/kg176713理論空氣量VONmVkgV0=0.0889(Cy+0?375Sy)+0?265(Hy-0.126Oy)4.8094理論煙氣量Vco20NmVkgVco20=1.866Cy/1000.868Vso20Nm'/kgVso2()=0.7Sy/1000.013VRo20Nm'/kgVRO20=VC020+VS0200.882VN20Nm'/kgVN20=0.79VO+0.008Ny3.806VH2oONm3/kgVH2o0=0?111Hy+0.0124Wy+0.0161V0+1.24Gzq0.528.輻射段煙氣焰溫表計(jì)算5輻射段空氣過剩系數(shù)a輸入1.56實(shí)際空氣址VNmVkgV=a*V07.2147實(shí)際煙氣量Vco2Nm'/kgVCO2=VCO200.868Vso2Nm3/kgVCO2=VSO200.013

序號名稱符號單位計(jì)算公式及數(shù)字來源數(shù)值VRo2Nm'/kgVRo2=Vco2+Vso20.882VN2Nm'/kgVN2=VN20+0.79(a-l)V05.706VH2oNmVkgVH2o=VH2o0+0.0161(a-l)V00.567Vo2Nm'/kgVo2=0.21(a-l)V00.5058煙氣總量VyNm'/kgVy=VCO2+VSO2+VN2+VH2O+VO27.669煙氣體枳白分比CO2%VC02/VyX100%11.338SO2%VS02/VyX100%0.177RO2%VR02/VyX100%11.515N2%N2/VyX100%74.488H2O%VH20/VyX100%7.40302%V02/VyX100%6.592(RO2+N2+H2O+O2)%10010輻射段煙氣熔溫表對流段煙氣焙溫表計(jì)算11對流段漏風(fēng)系數(shù)ad輸入0.112對流段實(shí)際空氣量VNm3/kgV=(a+ad)xV07.69513實(shí)際煙氣量Vco2Nm'/kgVco2=Vco200.868Vso2Nm'/kgVco2=Vso200.013VRo2Nm'/kgVRo2=Vco2+Vso20.882VN2Nm'/kgVN2=VN20+0.79(a1)V06.086VH2oNm'/kgVH2o=VH2o0+0.0161(a-l)V00.574Vo2Nm'/kgVo2=0.21(a-l)V00.60614煙氣總量vyNm'/kgVyd=VCO2+VSO2+VN2+VH2O+VO28.14915煙氣體積白分比CO2%VC02/VydX100%10.658SO2%VS02/VydX100%0.166RO2%VR02/VydX100%10.825N2%N2/VydX100%74.684H2O%VH20/VydX100%7.05302%V02/VydX100%7.436X%(RO2+N2+H2O+O2)%100對流段煙氣焰溫表.熱力平衡計(jì)算冷空氣溫度tck°C20冷空氣平均比熱ClkkJ/(Nm3/C)查表1.32冷空氣焙IlkkJ/kgIlk=a*VO*Clk*tlk177.77熱空氣溫度trk°C輸入120熱空氣平均比熱CrkkJ/(Nm3/C)查表1.3256熱空氣焙IrkkJ/kgIrk=a*VO#Crk*trk1071.15入爐燃料溫度tm°C輸入20

序號名稱符號單位計(jì)算公式及數(shù)字來源數(shù)值煙煤平均比熱CmkJ/(kg-°C)Cm=L091.09燃料帶入的焙值ImkJ/kglm=Cm*tm21.8鍋爐輸入熱量QrkJ/kgQr=Qdw+Im+Qwl17692.8爐體排煙溫度tpy°C假設(shè)后效孩333.09爐體排炬熔ipykJ/kg查焙溫表3785.86爐體排炬熱損q2%q2=apy-Ilk-Ilkd)/Qr*IOO19.21氣體未完全燃燒熱損q3%般情況假設(shè)0.5固體未完全燃燒熱損q4%般情況假設(shè)5散熱損失q5%般情況假設(shè)1爐渣及其它熱損q6%i般情況假設(shè)1鍋爐效率n%100-q2-q3-q4-q5-q673.29實(shí)際燃料消耗量Bkg/sB=Ql/(T]*Qr)1.0763計(jì)算燃料消耗量Bjkg/sBj=(l-q4/IOO)*B0.9902爐子的保溫系數(shù)VV=T)/(r)+q5/(l+Qlky/Ql))0.974Qlky=Qky*BJ入爐熱量QLkJ/kgQL=Qr*(l00-q3-q4-q6)/(10018488.2理論燃燒溫度t°C查弘I表1522.38五.輻射室傳熱計(jì)算結(jié)構(gòu)參數(shù)輻射容積VIm3105.94輻射室水冷壁附加而枳F(im264輻射室水冷壁面積Flm2Fl=fh(7r*2*fr+2*(fll+fl2-2*fr))+fciyx-+-Ffj174.03輻射受熱血當(dāng)量平而面枳DLHm2273.366有效受熱面積Hfyxm2Hfyx=i]s*H'ns=1.0273.36輻射段出口煙溫tpl°C先假設(shè)，后校核（校核值）782.67輻射段出口煙焙1P1kJ/kg查熔溫表8876.29煙氣平均熱容戰(zhàn)VckJ/kg.從tm到tp1區(qū)間內(nèi)Vc=(01-Ipl)/(tm-tpl)12.99煙氣有效輻射層厚度smS=3.6*V1/F11.9131爐膛容積熱負(fù)荷qvkw/m3qv=B*Qdw/Vl179.52三原子氣休輻射減弱系數(shù)*rqKq*rql/(MPa*m)Kq=(l-0.37*Tpl/l000)*((0.78+1?6rH20)/(rq*P*S*10)\5-0.1)*rq*101.55其中Tpl=tp1+273rq=rRO2+rH2OP=0.1MPa飛灰輻射減弱系數(shù)*UfhKfh’UfliI/(MPa*m)Kfh*Ufli=43850*py/(t3A2*dfhA2(l/3)*ufh0.8221碳黑粒子輻射減弱系數(shù)Kthl/(MPa*m)Kth=kj*xl*x20.153火焰發(fā)光部分黑度afgafg=1-A(-(kq+kth+kfhAfh)AA0.3757火焰黑度ahah=afg（燃固體燃料）03757盤管部分水冷壁有效角系數(shù)Xp順排密貼排列1

序號名稱符號單位計(jì)算公式及數(shù)字來源數(shù)值爐頂部分水冷壁有效角系數(shù)Xd順排有隙徘列0.95污染系數(shù)層燃煤0.6水冷壁平均熱有效系數(shù)+0.5237爐膛黑度U1al=(ah+(l-ah)*p)/(l-(1-ah)(l■中)(1-p))0.6051燃燒器火焰經(jīng)驗(yàn)系數(shù)M表64《鍋爐手冊》層燃煤0.52爐膛輻射出口溫度t3°Ct3=Tm/(M*(5.67*10A(-H)*al*T*FZKnA3/(v*BjWc))A0.6+l)-273781.25輻射段出口煙焙13kJ/kg查工I表8858.82對流段傳熱計(jì)算1對流室進(jìn)口煙氣溫度t3°Ct3781.252對流室進(jìn)口煙氣焙13kJ/kg查焙溫表8858.823對流室出口煙氣溫度t4°C查焰溫表得t4333.094對流室出口煙氣焙14kJ/kgI4=(Irk-Ilk)/v+Ipy3785.865對流I室介質(zhì)進(jìn)口溫度tl J °C307」對流II宋介質(zhì)進(jìn)口溫度tr°C307.16對流I室介質(zhì)出口溫度t2°C322.3對流II室介質(zhì)出口溫度t2*°C310.57對流I室逆流大溫差A(yù)tl°CAtl=t31-t2458.94對流I室逆流小溫差A(yù)t2°CAt2=t41-tl109.838對流H室順流大溫差A(yù)tl'°CAtr=t32-tr106.39對流II室順流小溫差A(yù)t2'At2'=t42-t2*25.999對流I室平均溫差A(yù)tcAt=(Atl-At2)/ln(AtM及2)243.66對流II室平均溫差A(yù)t1°CAf=(Atl,-At2')/ln(At17At2')56.93對流段結(jié)構(gòu)參數(shù).第-對流室熱平衡計(jì)算a.對流段蛇管排列形式順列b.煙氣平均流通面積Fym22.56C-管束橫向相對節(jié)距6161=Sl/dl1.57d.管束縱向相對節(jié)距6262=S2/dl2.89e.換熱面積有效對流換熱面積系數(shù)Cyx0.85有效對流換熱面積Hm2DLDH=d*n*Ldl*n*Cyx310.511煙屬有效輻射層厚度SmS=0.9*d*(4/7t*61*62-1)0.164812煙氣平均溫度6pj°C0pj=(t1+t2)/2+At599.0913煙氣平均流速Wym/sNWy=Bj*Vy/Fy*(Gpj+273)/27310.0414煙氣橫向沖刷adkw/(m2*°C)ad=ah*CsieCz*Cw0.0766管束對流放熱系數(shù)15三原子氣體輻射減弱系數(shù)kq1/MPakq=10*((078+1.6rH2o)/sqr(rq*P*S*l0)-O.l)*(l-O.37*Tpy/lOOO)*rq6.7921Tpy=t4+27316煙氣黑度ayay=\-e^(-k^S)0.121617受熱而積灰層表面溫度tb°Ctb=tpj+Ath374.7

序號名稱符號單位計(jì)算公式及數(shù)字來源數(shù)值A(chǔ)th=60°C燃煤18輻射換熱系數(shù)afkw/(m2*°C)a05.1*10A(-ll)*ay*TA3*(l-(Tb/T)A4)/(1-Tb/T)0.0111其中Tb=tb+273,Tpj=9pj+27319綜合傳熱系數(shù)kkw/(m2*°C)k=(ad+af)*\g0.057V=0.557).65燃煙褐煤取0.620第一對流室對流面吸熱量QcrnkJ/kgQcm=k*Ai*h/Bj4361.98第一.二對流室界面煙氣溫度°C416.9?第一對流室熱平衡計(jì)算a.對流段蛇管排列形式順列b.煙氣平均流通面積Fym21.9C-管束橫向相對節(jié)距6161=Sl/dl1.57d.管束縱向相對節(jié)距6262=S2/dl2.89e.換熱面積有-效對流換熱面積系數(shù)Cyx0.85對流室有效對流換熱面積Hm2DLDH=d*H*Ldl*n*Cyx228.3121煙氣有效輻射層厚度SmS=0.9*d*(4/jt*61*62-1)0.1648第二對流室進(jìn)口煙氣溫度°C416.9笫二對流室出口煙氣溫度°C33322煙氣平均溫度Bpj°C0pj=(tl+t2)/2+At375.0123煙氣平均流速Wym/sWWy=Bj*Vy/Fy*(9pj+273)/27310.0424煙氣橫向沖刷adkw/(m2*r)ad=ah*Cs*Cz*Cw0.078管束對流放熱系數(shù)25三原子氣體輻射減弱系數(shù)kq1/MPakq=10*((0.78+1.6rH2o)/sqr(rq*P*S*10).7.2165T^py)=tlf+：273Tpy/1000)*iq26煙氣黑度ayay=l-eA(-kq*P*S)0.130427受熱面積坎層表面溫度tb°Ctb=tpj+Ath368.81△th=60°C燃煤28輻射換熱系數(shù)afkw/(m2*°C)af=5.1*10a(-11)*ay*Ta3?(1-(Tb/T)A4)/(1-Tb/T)0.0071其中Tb=tb+273,Tpj=6pj+27329綜合傳熱系數(shù)kkw/(m2*°C)k=(ad+af)*V0.0553▼=0.557).65燃煙褐煤取0.630第二對流室對流血吸熱QcrwkJ/kgQcrw=k*At*h/Bj726.97631整個(gè)對流室對流血吸熱量QcrkJ/kgQcr=Qcrn+Qcrw5088.96

序號名稱符號單位計(jì)算公式及數(shù)字來源數(shù)值32換熱平衡方程煙氣側(cè)放熱量QphkJ/kgQph=y*(l-q4/l00)*(I3+Ilkd-(l+ad/a)*I4)5085.65校核AQ%AQ=(Qph-Qcr)/Qph*100%W1%因此，出口煙溫tpy是合適的.輻射室吸熱量QfkwQfN/*(QL-I3)*Bj9295.66輻射段熱流密度址kw/m2qf=Qf/Hfyx34對流室吸熱量QpkwQp=Qph*Bj5035.92對流室熱流密度qpkw/m2qp=Qp/Hdyx934爐子總吸熱量QkwQ=Qf+Qp14331.6校核整個(gè)爐子熱力計(jì)算的誤差A(yù)QkJ/kgAQ=Qr/(l-Q4/100)*t]/100(Q仟Qp)/Bj-0.06IAQI/Qr*100%=0相對誤差符合耍求，計(jì)算合理.爐子吸熱量與設(shè)計(jì)熱負(fù)荷接近，因此，本計(jì)算結(jié)果符合要求.?爐內(nèi)介質(zhì)阻力計(jì)算■計(jì)算條件1循環(huán)流童Vm3/s0.2191(m3/h)7892爐管結(jié)構(gòu)形式輻射段爐管(<pn)8根無縫鋼管并聯(lián)輻射段單根爐管長FUDLmFUDL=輻射段單圈長審圈數(shù)十頂盤管單程長140對流段盤管區(qū)段數(shù)：2單區(qū)段對流區(qū)盤管118根無縫鋼管并聯(lián)對流段單根蛇管長DLDLm453輻射段爐管內(nèi)徑面積LGJMm2F=K/4((d-2c)/1000)A20.007694對流段爐管內(nèi)徑而枳SGJMm2F=7t/4((d,-2c,)/1000)A20.00085介質(zhì)出口溫度t2°C3356介質(zhì)進(jìn)口溫度tl°C307.287介質(zhì)平均溫度tpj°Ctpj=(tl+t2)/232L1418介質(zhì)平均密度PPjkg/m3查表802.897二爐管內(nèi)介質(zhì)流速計(jì)算輻射段盤管介質(zhì)流速FUDWm/sFUDW=V/(FUDGU*F)3.558對流段蛇管介質(zhì)流速DLDWm/sDLDW=V/(DLDGU*SGJM)2.309無縫鋼管粗糙度Kmm0.08輻射段流體摩擦阻力系九X=l/(4*(lg3.7*dA)A2)0.018

序號名稱符號單位計(jì)算公式及數(shù)字來源數(shù)值輻射段折算摩擦阻力系數(shù)入0XO=X/d0.188對流段流體摩擦阻力系數(shù)XX=l/(4*(lg3.7*(Vk)A2)0.024對流段折算摩擦阻力系數(shù)入0XO=X/d0.777盤管急劇轉(zhuǎn)彎阻力系數(shù)g1.75盤管入口阻力系數(shù)0.7盤管出口阻力系數(shù)2.618盤管折彎總阻力系數(shù)gpz3」4蛇管折彎總阻力系數(shù)gsz9.34l.l+0.9nA2(dg/dj)A4輻射段盤管阻力△PfPa△P4(入O*FUDL+?NV+?+?pz+gc)*ppj*9.81*FUDWA2/(2g)Mpa0.2051對流段蛇管阻力APsPa△Ps=aO*DLDL+gNw+gr+gsz+gc)*ppj*9.81*DLDWA2/(2g)MPa0.116介質(zhì)管內(nèi)流動(dòng)阻力△PMPa0.321介質(zhì)進(jìn)出口位能損失AHwnMPa0.025介質(zhì)進(jìn)出口總阻力損失APMPa0.346輻射段介質(zhì)流速（國*二\-:————:——:—: 2)FUDWm/s3.558對流段介質(zhì)流速（國標(biāo)>1.5）DLDWm/s2.309.介質(zhì)膜溫度計(jì)算己知條件1介質(zhì)出口溫度t2°C3352介質(zhì)出口運(yùn)動(dòng)粘度Vc2mm/s查表0.2463介質(zhì)出口溫度下的Pr數(shù)Pr查表6.054介質(zhì)出口溫度下密度pckg/m3查表788.255介質(zhì)出口溫度下導(dǎo)熱系數(shù)九m2/s查表7.8E-056輻射受熱面熱流密度qfkw/m2查表34.00447輻射段爐管介質(zhì)流速Wnm/s3.5589—膜溫計(jì)算1介質(zhì)膜溫度tw°C假設(shè)后校核（自動(dòng)迭代）342.82膜溫下運(yùn)動(dòng)粘度Vwm2/s2.4E-073膜溫下介質(zhì)密度pwkg/m3779.894輻射段管內(nèi)徑DnmmDn=(d-2c)/1000995出口溫度介質(zhì)膜溫度下介質(zhì)之粘度比Vc/Vw=(Vc*pc)/(Vw*pw)1.03576管長與管內(nèi)徑比Ln/Dn?601414.147雷諾數(shù)ReRe=Wn*Dn/Vc14264708系數(shù)f78f/8=(l.82*lgRe-1.64)A(-2)/80.0013

序號名稱符號單位計(jì)算公式及數(shù)字來源數(shù)值9努謝爾特?cái)?shù)NuNu=(f78)*Re*Pr/(LO7+12?7(f/8)A0.5*(PrA(2/3)-l))*(Vc/Vw)A0」15485.6910對流換熱系數(shù)akw/(m2*°C)a=Nu*A/Dn4.363611介質(zhì)膜溫度tw*°Ctw'=qAa+t2f342.79tw,與介質(zhì)膜假設(shè)溫度tw相差0.02°C因此，介質(zhì)膜溫度可定為342.81.爐本體內(nèi)煙氣阻力計(jì)算已知參數(shù)1單位燃料煙氣量VyNm3/kg&14962空氣過剩系數(shù)a1.53煙氣重度Vnkg/Nm3Vn=(44Vco2+64Vso2+28VN2++18VH2o+32Vo2)/2241-41.30974計(jì)算燃料消耗戢Bjkg