5000td水泥熟料帶DD型分解爐的NSP窯的設(shè)計

#圖1熱量平衡圖圖2 物料平衡圖物料平衡計算.收入項目：(1)燃料總消耗量：m(kg/kg熟料)r其中：窯頭燃料量：m=Kmyryr分解爐燃料量：m=Km。FrFr(2)生料消耗量、入預(yù)熱器物料量干生料理論消耗量gsl100—mAa100—25.71義1義m r ar100—L100-35.88乎=1.560—0.401m式中a——燃料灰分參入量，100%出袋收塵飛損量及回灰量mFh=mfh(1-n)=0.10x(1-0.996)=0.0001kg/kgm=m,.-m,=0.10-0.0001=0.1kg/kgyhfhFhC.考慮飛損后干料實際消耗量m一m+m100—Lf一1560—0401m+00001x100—35.2—1560—0401mm一m丁m f~一. .m丁U.x . .mgsgslFh100-L r 100-35.88 rkg/kgd.考慮飛損后生料實際消耗量一(1.560-一(1.560-0.401m)x

r100100-0.2-m "100-W一1.563-0.402mkg/kgr已入預(yù)熱器物料量入預(yù)熱器物料量=m+m=1.563-0.402m+0.100

syk r一1.663-0.402mkg/kg

r入窯系統(tǒng)空氣量a.燃料燃燒理論V'〃一0.089C+0.267H+0.033(S-O)

lk ar ar arar-0.089x60.10+0.267x3.96+0.003x(0.35-7.91)一6.157 m3/kg煤(標(biāo)準(zhǔn)狀態(tài))TOC\o"1-5"\h\znr=1.293V'=1.293x6.157-7.961kg/kg煤lk lk入窯實際干空氣量V-aV，Km一1.05x6.157x0.40m=2.586mm3/kg(標(biāo)準(zhǔn)狀態(tài))yhylkFr r rm一1.293V-1.293x2.586m-3.344mkg/kgyk lk r r其中，入窯一次空氣量、二次空氣量及漏風(fēng)量分別為v“=KV”0.10乙yk1 1yk ykV.=KVk=0.85V.yk2 2yk ykV=KV=0.05Vlok1 3yk yk分解爐從冷卻機抽空氣量(a)出分解爐混合室過?？諝饬縑=(a—1)V-m=(1.15—1)*6.157m=0.924mm3/kg(標(biāo)準(zhǔn)狀態(tài))TOC\o"1-5"\h\zL lkr r r(b)分解爐燃料燃燒空氣量V=V'=m=VKm=6.157義0.60m=3.694m/kg(標(biāo)準(zhǔn)狀態(tài))lkFrlk'Fr r r(c)窯尾過?？諝饬縑=(a—1)V?m=(a—1)V?Km=(1.05-1)x6.157x0.40m=0.123mm3/kg(標(biāo)態(tài))ylkyrylkyr r r(d)分解爐及窯尾漏入空氣量V=KV:mF=KV;Km=0.05x6.157x0.60m=0.185m m3/kg6lkFr6lkFr r r(e)分解爐冷卻機抽空氣量V=V+V-V-V=0.924m+3.694m-0.123m-0.185mF2k 1 2 3 4 r r r r=4.310mm3/kg(標(biāo)準(zhǔn)狀態(tài))rm=1.293V=1.293x4.310m=5.573mkg/kgF2k F2k r rd漏入空氣量預(yù)熱器漏入空氣量為:V=KV'm=0.16x6.157m=0.985mm3/kg(標(biāo)準(zhǔn)狀態(tài))5 4lkr r r窯尾系統(tǒng)混入空氣總量為：V=V+Vlok2 4 5=0.185m+0.985m=1.170m m3/kg (標(biāo)準(zhǔn)狀態(tài))rrr全系統(tǒng)漏入空氣量為：V=V+Vloklok1 lok2=0.05x2.586m+1.170m=1.299mm3/kg（標(biāo)準(zhǔn)狀態(tài)）rrr=0.05x2.586m+1.170m=1.299mm3/kg（標(biāo)準(zhǔn)狀態(tài)）rrrm=1.293V=1.293x1.299m=1.680mkg/kglok lok r r2.支出項目(1)熟料：m=1kg。sh(2)出預(yù)熱器廢氣量a.生料中物理水含量mwsW 0.2=m s-=(1.563—0.402m)x—=0.003—0.001mkg/kgs100 r100 rm 0.003—0.001mV=———= ―=0.004一0.001m m3/kg (標(biāo)準(zhǔn)狀態(tài))-s0.804 0.804 rb.生料中化學(xué)水含量m=0.00353mAlOs=0.00353x(1.563-0.401m)x3.03hs gs2 3 r=0.017一0.004mkg/kgrm 0.017一0.004mV=——hs—= _=0.004一0.001mm3/kg(標(biāo)準(zhǔn)狀態(tài))hs0.804 0.804 rc.生料分解放出CO2氣體量M M 44 44CO=COs—CO~+MOs—COr=44.68x +0.29x——=35.422aMgM 56 40.3CO Mgams=m也CO2 gs100L 3542一md=(1.560—0.401m)x 出100 r100一0.0001x35.20100=0.553一0.142mr kg/kgms 0.5520.142mVs= CO2-= r-=0.279—0.072mm3/kg （標(biāo)準(zhǔn)狀態(tài)）TOC\o"1-5"\h\zCO2 1.977 1.977 rd.燃料燃燒生成理論煙氣量22.4C22.4 60.10=1.122mrm3/kg（標(biāo)態(tài)）Vr.== 義=1.122mrm3/kg（標(biāo)態(tài)）CO 12 100r12 100VrN2=VrN2=0.79V'22.4N?m+ x—ar—mlkr28 100r=0.79x6.157mr22.40.97+ x m28 100r=4.872mm3/kg（標(biāo)態(tài)）VrH2VrH2O22.4H22.4W x—arm+ x—ar-m2 100 r18 100r22.41.00）+ x I2 100 18 100）=0.456mm3/kg（標(biāo)態(tài)）rVrSO222.4S x—a^VrSO222.4S x—a^m32 100r22.40.35 x m32 100r=0.002mrm3/kg（標(biāo)態(tài)）Vr=VrCO2+Vr+Vr+Vr

N2 H2OSO2=（1.122+4.872+0.456+0,002）mr=6.452mm3/Kg（標(biāo)態(tài)）rfaA）faA）mr=m'+1——ar~mI1k 100）r7.961+1—I25.71）100）m=8.704mkg/kgrre.煙氣中過?？諝饬縑k=（a—1）V?m=（1.40—1）x6.157m=2.463mm3/kg（標(biāo)態(tài)）f 1kr r rmk=Vkx1.293=2.463x1.293=3.185mkg/kgr其中，有Vk=0.79Vk=0.79x2.463m=1.946mm3/kg（標(biāo)態(tài)）N2 r rTOC\o"1-5"\h\z28 28mk=Vkx =1.946x m=2.433mkg/kgN2 N222.4 22.4r rVkO2=0.21Vk=0.21*2.463m=0.517mm3/kg(VkO232 32mk=Vkx =0.517x m=0.739mkg/kgOO222.4 22.4r rf.總廢氣量=Vco+VN+VH0+VO+匕。=(0.279—0.072m，+1.050m，)+(4.872m，+co2 N2 H2O O2SO2 r r r1.946m)+(0.004—0.001m+0.021—0.005m+0.456m)+0.517m+0.002mr r rr rr=0.304+8.837mrm3/kg(標(biāo)態(tài))①出預(yù)熱器飛灰量m母=0.100kg/kg3.2.3熱量平衡計算如下.⑴收入項目①燃料燃燒生成熱 QRr=mrQ皿ar=23614mrkJ/kg②燃料帶入顯熱 Q=mCt=mx1.154x60=69.240mkJ/kgrrrrr r【0?60℃時熟料平均比熱容Cr=1.154kJ/(kg?℃)】③生料帶入熱量Q=(mC+mC)t=1(1.560—0.401m)x0.878+(0.003—0.001m)x4.182]x50s gsswsws r r=69.111-17.813mkJ/kgr【0?50℃時，水的平均比熱容C=4.182kJ/(kg℃),干生料平均比熱容wC=0.878kJ/(kg℃)】s④入窯回灰?guī)霟崃縌=mCt=0.100義0.836*50=4.180kJ/kgyhyhyhyh【0?50℃時，回灰平均比熱容Cyh=0.836kJ/(kg?℃)】⑤空氣帶入熱量入窯一次空氣帶入熱量TOC\o"1-5"\h\zQ=VCt=0.15VCt=0.15*2.586m義1.298*30=15.105mkJ/kgy1k y1ky1ky1k yky1ky1k r r【0?30℃時，空氣平均比熱容鼠=1.298kJ/(kg?℃)】入窯二次空氣帶入熱量Q=VCt=0.80VCt=0.80*2.586m義1.403義950=2757.4mkJ/kgy2k y2ky2ky2k yky2ky2k r r【0?950℃時，空氣平均比熱容Cy2k=1.403kJ/(kg?℃)】入分解爐二次空氣帶入熱量Q=VCt=4.310m義1.377義740=4391.8mkJ/kgF2k F2kF2kF2k r r【0?740℃時，空氣平均比熱容CF2k=1.377kJ/(kg?℃)】系統(tǒng)漏風(fēng)帶入熱量Q=VCt=1.299m義1.298*30=50.595mkJ/kgloklokloklok r r【0?30℃時，空氣平均比熱容Cl樂=1.298kJ/(kg?℃)】總收入熱量Q=Q+Q+Q+Q+Q+Q+Q+QzsrRrsyh y1k y2k F2k lok=23614m+69.240m+(69.111—17.813m)+4.180+15.105m+2757.4mrr r rr+4391.8m+50.595m=73.291+30880mkJ/kgrr r⑵支出項目熟料形成熱Q=1736.9kJ/kgsh蒸發(fā)生料中水分耗熱量Q=(m+m)q=(0.003—0.001m+0.017—0.004m)x2380ss wshsqh r r=47,600-11.9mkJ/kgr【50℃時，水的汽化熱qqi=2380kJ/kg】廢氣帶走熱量Q=(VC+VC+VC+VC+VC)tf CO2 CO2 N2 N2 H2O H2O O2 O2 SO2 SO2 f=1(0.279+1.050m)x1.921+6.818mx1.319+(0.025+0.450m)x1.550rr r+0.517mx1.370+0.002x1,9651x340r=195.5+4222.8mkJ/kgr【0?340℃時，各氣體平均比熱容(標(biāo)準(zhǔn)狀態(tài)下)：C=1.921CO2kJ/(m3?℃)；C=1.319kJ/加?℃)；C=1.550kJ/(m3?℃)；N2 H2OC=1.370kJ/(m3?℃)；C=1.965kJ/(m3?℃)】O2 SO2出窯熟料帶走熱量Q=1xCt=1x1.078x1360=1466.1KJ/Kgysh shsh【0?1360℃時，熟料平均比熱容Csh=1.078kJ/(kg?℃)】出預(yù)熱器飛灰?guī)ё邿崃縌=mCt=0.100x0.895x300=26.850KJ/Kgfhfhfhfh【0?300℃時，飛灰平均比熱容Cfh=0.895kJ/(kg?℃)】系統(tǒng)表面散熱損失Qb=460kJ/kg支出總熱量為zc=Qsh＋Qss＋Qf＋Qysh＋Qfh＋QB=1736.9＋(47.60－11.9mr)＋(195.5＋4222.8mr)＋1466.1＋26.850＋460=3933.0＋4210.9mrkJ/kg⑶列出收支熱量平衡方程式Qzs=Qzc73.291＋30880mr=3933.0＋4210.9mr求得 mr=0.1447kg/kg即燒成1Kg熟料需要消耗0.1447kg燃料。求得燃料消耗量后，即可列出物料平衡（見表3-1）和熱量平衡表（見表3-2）。表4-1物料平衡表 單位：kg/kg料收入項目數(shù)量%支出項目數(shù)量%燃料消耗量0.1454.45熟料量129.66入預(yù)熱器生料量1.60549.25出預(yù)熱器飛灰量0.1002.97入窯實際干空氣量0.48414.85出預(yù)熱器廢氣量分解爐抽空氣量0.80624.73生料中物理水量0.0030.09窯尾系統(tǒng)漏入空氣量0.2196.72生料分解CO2量0.53215.78生料中化學(xué)水量0.0160.47燃料燃燒理論煙氣量1.25937.35煙氣中過?？諝饬?.46113.68

總計3.259100.0總計3.371100.00表4-2熱量平衡表 單位：kJ/kg熟料收入項目數(shù)量%支出項目數(shù)量%燃料燃燒熱3416.975.31熟料形成熱1736.938.24燃料顯熱10.00.22蒸發(fā)生料水分耗熱45.91.01生料帶入熱66.51.46廢氣帶出熱量806.517.76回灰?guī)霟?.20.09熟料帶出熱量1466.132.28入窯一次空氣帶入熱2.20.05飛灰?guī)С鰺崃?6.850.59入窯二次空氣帶入熱399.08.79系統(tǒng)散熱損失460.010.13入分解爐空氣帶入熱635.514.01系統(tǒng)總漏風(fēng)帶入熱7.30.16合計4537.4100.00合計4542.3100.004、主要熱工技術(shù)參數(shù)的計算⑴熟料單位燒成熱耗為QrR=mrQntr=23614X0.1447=3416.9kJ/kg⑵熟料燒成熱效率n=Qh義100%=1736.9義100%=50.8%SQ 3416.9rR⑶窯的發(fā)熱能力為Q=MQ=KmGQ=0.4x0.1447x211.6666x1000x23614yryrnet,ar yr net,ar=2.893x108kJ/h⑷燃燒帶襯磚斷面熱負(fù)荷為

qAQ "兀C—xD24i2.893x1080.785x4.36qAQ "兀C—xD