100噸翠綠料玻璃瓶課程設(shè)計(jì)解析

蓄熱式馬蹄焰池窯〔燒油〕的熱工計(jì)算(一)原始資料產(chǎn)品：翠綠料機(jī)制玻璃瓶出料量：每天熔化玻璃100噸。(3)1.11.1玻璃成分設(shè)計(jì)玻璃成分%

SiO269.5

AlO234.5

CaO8.5

MgO1.5

NaO214.5

BaO0.5

FeO230.25

CrO230.2料方及原料組成：見(jiàn)表1.2原料名稱(chēng)2 3重晶石原料名稱(chēng)2 3重晶石0.64410.21.257.280.2BaSO:884鉻礦粉0.4686.412.851.449.531.5螢石0.7385.00.13CaF:92.062硝酸鈉1.47536.5氧化銻0.295合計(jì)99.99料方〔濕粉原料化學(xué)組成〔%〕外加料%〕SiO2AlO23CaOMgONaO2BaOFeO23CrO23其他水分硅石粉47.32298.900.080.030.315.0長(zhǎng)石17.68865.6618.382.640.17石灰石7.735550.2白云石4.77330.522.00.2純堿18.85957.2NaCO:97.797.0碎玻璃數(shù)量：占協(xié)作料量的45%。(7)玻璃熔化溫度：1400℃。(8)工作部玻璃液平均溫度：1300℃。1.31.3重油組成、熱值及加熱溫度元素組成低熱值加熱溫度CHONSAWKcal/Kg〔℃〕86.4012.180.530.30.120.020.610000125120℃，0.6Nm3/Kg油噴嘴磚孔吸入的空氣量：0.5Nm3/Kg油：1050℃。(13)1.2.1500℃，1400℃。(15)窯體外外表平均溫度〔℃1.41.4窯體外外表平均溫度〔℃〕窯頂側(cè)胸墻電熔鋯剛玉前后胸墻剛玉磚池墻池底磚池墻熔化部 250180200 160130175熔化池內(nèi)玻璃液溫度〔℃1.51.5熔化池內(nèi)玻璃液溫度〔℃〕液面窯池上部〔平均〔電熔鋯剛玉磚池墻，600mm〕窯池上下部交界層窯池下部〔平均〔粘土磚池墻，600mm〕池底140013401280126512501℃/mm。池墻、池底內(nèi)外表溫度按玻璃液溫度〔1250℃〕取用。處壓力：2mm/水柱。(二) 玻璃形成過(guò)程耗熱量計(jì)算100kg原料形成玻璃液的氧化物量計(jì)算

氧化物數(shù)量〔kg〕名稱(chēng) SiO

AlO

CaO

MgO NaO

BaO

FeO

CrO 總數(shù)2 23 2 23 2343.322/1.15*0.989=37.25737.257石43.322/1.15*0.0008=3.0143.014英37.6716*0.0003=1.1301.130砂37.671*0.003=11.30111.30141.40117.688*0.6566=11.61411.614長(zhǎng)17.688*0.1838=3.2513.251石17.688*0.0264=0.4670.46717.688*0.0017=0.0300.03015.362石7.735*0.55=4.2544.254灰石7.505*0.002=0.0150.01554.269白4.773*0.305=1.4561.456云4.773*0.22=1.0501.050石4.773*0.002=0.0100.0102.516純堿18.859/1.07*0.572=10.08210.08210.0820.644*0.102=0.0660.066重0.644*0.012=0.0080.008晶0.644*0.5778=0.3690.369石0.644*0.002=0.0010.0010.4440.466*0.064=0.0300.03鉻0.466*0.1285=0.0600.06礦0.466*0.0144=0.0070.007粉0.466*0.095=0.0440.0440.466*0.315=0.1470.1470.5580.7376*0.05=0.0290.029螢0.7376*0.0013=0.0010.001石0.7376*0.9206*0.71=0.482①0.5270.7376*0.9206*0.385=-0.261-0.2610.251硝1.4752*0.9812*0.365=0.528①0.528酸1.4752*0.0014*0.435=0.001①0.001鈉1.4752*0.0011*0.585=0.0010.0010.530合計(jì)48.7353.3196.2661.10530.36911.0790.17050.14771.79玻璃成分68.464.668.801.550.5215.560.240.211003%的揮發(fā)量計(jì)算。②2CaF+SiO→2CaO+SiF↑②2 2 4CaF2CaO

SiO2

作用后，其中一份SiO2

SiF4

1〔1kJ/kg〕CaCO3

CaSiO3

的反響耗熱量q11

cao

=367*(0.0000036+0.00122+0.04128+0.01658+0.00007)*4.18=90.64kJ/kgNaCONaSiO的反響耗熱量q3 2 3 22

=227.3*0.10559*4.18=100.32kJ/kgBaSO4

BaSiO3

的反響耗熱量q33

Bao

=540*0.00367*4.18=8.28kJ/kgCaF2

CaSiO3

的反響耗熱量q4q=367G =367*0.00527*4.18=8.08kJ/kg4 cao1kgqq=q+q+q+q硅 1 2 3 4

硅=207.32kJ/kg原料名稱(chēng)硅原料名稱(chēng)硅去氣產(chǎn)物量去氣產(chǎn)物量計(jì)算2COOSOSiF總量22245.146-5.146/1.15=0.6710.003石白云石純堿20.263-20.263/1.07=1.32620.263/1.07*0.572*44/62=7.7010.635*0.88*0.27=0.1510.635*0.88*0.067=0.0371.3267.701重晶石0.0370.151石粉5.065/1.15*0.0008*44/56=0.0035.065/1.15*0.0003*44/40=0.0010.6710.001硅砂61.047-61.047/1.15=7.96361.047/1.15*0.002*44/56=0.0830.0837.96361.047/1.15*0.001*44/40=0.0580.058灰石 7.505*0.55*44/56=3.243 3.2435.435*0.305*44/56=1.3021.3025.435*0.220*44/40=1.3151.315重量〔公斤〕9.9613.6240.0370.1510.4524.22312.3956.9360.0260.0530.09719.507體積〔%〕63.5435.560.130.270.50100.0螢石螢石0.466*0.0144*44/56=0.0050.466*0.095*44/40=0.0490.734*0.9206*104.16/2/78=0.4510.0050.0490.451〔1kgkJ/kg〕CaCO3

CaSiO3

的反響耗熱量q11

cao

=367*0.0745*4.18=114.3kJ/kgNaCONaSiO的反響耗熱量q3 2 3 22

=222.73*0.09305*4.18=88.41kJ/kgNaNO3

NaSiO2

的反響耗熱量q33

=990*0.003744*4.18=15.49kJ/kgBaSO4

BaSiO3

的反響耗熱量q4q=540G =540*0.003744*4.18=8.52kJ/kgBaoCaFCaSiOq2 3 5q=367G =367*0.00462*4.18=7.087kJ/kgcao1kgq硅q=q+q+q+q +q=233.807kJ/kg硅 1 2 3 4 52、協(xié)作料用量計(jì)算5545%1kg45/55=0.8182kg1kg0.8182kg1-0.01*24.223+0.8182=1.576kg熔成1kg玻璃液需粉料和碎玻璃分別為：G =1/1.576=0.63kg粉G =0.8182/1.576=0.52kg碎熔成1kg玻璃液需要的協(xié)作料量為：G料G粉G碎=0.63+0.52=1.15kg3、玻璃形成過(guò)程的熱平衡〔1kg玻璃液計(jì)算，單位是kJ/kg，0℃算起〕支出熱量1400℃耗熱：G*C玻*t1400

=1*0.3145*1400*4.18=1840.45kJ其中C玻1400

=0.1605+1.1*10-4*1400=0.3145kcal/kg℃=1.31461kJ/kg℃加熱去氣產(chǎn)物到1400℃耗熱：C去=0.01*[C

%+SO

%+NO

%〕+C

*HO%+C*o%]1400

CO2 2 2

2 H2O 2

O2 2=0.01*[0.5553*(35.56+0.27)+0.4357*63.54+0.3631*0.13]*4.18=1.991kJ/Nm3℃則耗熱量為0.01V去

G C去粉

t =0.01*19.507*0.63*1.991*1400=342.56kJ溶生成硅酸鹽耗熱q G =48.27*4.18*0.63=127.11kJ硅 粉形成玻璃耗熱83G粉

〔1-0.01V去

〕=83*0.63*〔1-0.01*24.223〕*4.18=165.63kJ蒸發(fā)水分耗熱595G水

G =595**0.0996*0.63*4.18=156.06kJ粉共支出熱量：1840.454+342.56+127.11+165.63+156.06=2631.81kJ/kg收入熱量：由粉料和碎玻璃帶入的熱量〔設(shè)協(xié)作料入窯時(shí)溫度為20℃〕G C t G C碎t粉 粉粉 碎 20 碎=〔0.63*0.23*20+0.52*0.1807*20〕*4.18=19.97kJ熔化1kg玻璃液在玻璃形成過(guò)程中的耗熱量為：q =支出熱量-收入熱量=2631.81-19.97=2611.84kJ玻〔三〕燃料燃燒計(jì)算5、熔化部面積計(jì)算5.1k=1.7t/m2100F=60m2，70%，42m21.59.6m，6.6m1m，1/8，碹股0.8m。熔化帶火焰空間容積與面積計(jì)算f=9.6*6.6=63.36m21火焰空間頂部面積f =9.6*6.6*1.03885=65.82m22f=[1.0+〔2/3〕*0.688]*6.6=9.63m23f=1.0*9.6=9.6m24火焰空間容積V空

=[1.0+(2/3)*0.8]*6.6*9.6=97.15m2

〕的計(jì)算氣氣層有效厚度：l =6.4*V /F有 空 空=6.4*97.15/(ff1 2

f2f)3 4

=6.4*97.15/〔63.36+65.82+9.63+2*9.6〕3.9ml =0.117*3.9=0.46〔atm·m〕有燃燒需氧量燃燒反響燃燒需氧量燃燒反響重油化學(xué)組成〔%〕〔Nm3/kg〕式CO2燃燒產(chǎn)物量〔NmO N2 2C86.421.613C+O=CO2 21.613H12.180.6824H+O=2HO2 21.S0.120.00084S+O=SO2 2N0.30.0024W0.60.02.2958O0.53-0.00372.29214=1.2時(shí)過(guò)剩O20.4580.458共需O2量N2量空氣需要量2.7501410.3310.3313.08燃燒產(chǎn)物量〔Nm3〕燃燒產(chǎn)物成分〔%〕1.6130.45810.331.11.713.3275.009 l =0.0993*3.9=0.39atm·m〕有假定t

=0.109

=0.144 =1.05g = + co2

H2o氣

co2

H2o

=0.109+1.05*0.144=0.26火焰溫度復(fù)算 =Fwm

/F f空 2

2f3

2f4

〕=9.6*6.4/〔65.82+2*9.63+2*9.6〕=0.59已定t熔

=1400℃ggwm4T4w wm(1) g玻1g玻g)wmgmgwm g 玻

=1600℃，t

=1475℃，t

=1350℃T=g=1837.4K=1564.4℃T=1564.4℃ 與假定的火焰溫度接近，故上述各假定的溫度均可用。g〔五〕燃料消耗量及窯熱效率計(jì)算理論燃料消耗量計(jì)算x〔kgkJ/h，0℃圍。熔化部收入的熱量重油的潛熱q1q=10000x*4.18=4.18*104x kJ/h1重油的物理熱q2q=0.5*125x*4.18=261.25xkJ/h2C〔霧化介質(zhì)〕的物理熱q3Ca =0.311*4.18=1.3kJ/Nm3℃120q=0.6*1.3*120x=93.6xkJ/h3d.由噴嘴磚孔吸入空氣的物理熱q440℃Ca=0.31*4.18=1.2958kJ/Nm3℃40q4=0.5*1.2958*40x=26xkJ/he.助燃空氣〔二次空氣〕的物理熱q5二次空氣量Va=13.08-0.6-0.5=11.98Nm3/kg油Ca =0.3382*4.18=1.414kJ/kg℃1050q =11.98*1.414*1050x=17786.7xkJ/h5熔化部支出的熱量消耗于玻璃形成過(guò)程的熱量q11400℃，與玻璃熔化溫度一樣，故加熱去氣產(chǎn)物一項(xiàng)不必另行計(jì)算。kJ/h1加熱回流的玻璃液q2考慮用平底式流液洞，取回流系數(shù)為1.4，回流玻璃液量=〔120*1000〕*〔1.4-1〕/24=2023.6kg/h回流玻璃液的平均溫度=〔1400+1300〕/2=1350℃C 0.16051.1*104(14001300)*0.5*4.18=1.292kJ/〔kg*℃〕cpq=2023.6*1.292*〔1400-1300〕=258606.72kJ/h2窯體散熱5.15.2溢流熱損失由熔化部溢流出的煙氣溫度1400℃.查附表得Cg1400

0.379*4.181.58422 kJ/Nm3℃g1.298kg/Nm30g1400

0.212kg/m3a 1.13kg/m340則溢流熱損失：見(jiàn)表5.3遮蓋。F=0.1/2=0.05m2回火側(cè)兩只噴嘴磚孔有溢流，考慮其一半被噴嘴擋住，實(shí)際的孔口面積為：5.3溢流熱損失通過(guò)部位tg通過(guò)部位tgH〔m〕h1h孔口面積F〔m2〕V加料口14001.6381.5040.4960.620.0510.21測(cè)溫孔14001.1881.0910.9090.620.010.05噴嘴磚孔14001.5381.410.590.820.0042520.02其中：t 溢流煙氣溫度〔℃〕gH 孔口中心距窯頂高〔m〕h 孔口中心到窯頂?shù)膸缀螇侯^h1

H(a40

a1400

)(mm水柱)h 孔口處的壓力，h=h1

=2-h1

〔mm〕---溢流系數(shù)V-----V=F〔2gh/

a1400

〕1/2〔m3/sV-----標(biāo)準(zhǔn)狀況下的溢流量〔Nm3/h〕0q---溢流熱損失q=V*Cg t kJ/h5注釋?zhuān)?/p>

5 0 1400g5.1窯體各局部構(gòu)造散熱散熱部位材質(zhì) 導(dǎo)熱系數(shù)〔kcal/m.h℃〕內(nèi) 外散熱部位材質(zhì) 導(dǎo)熱系數(shù)〔kcal/m.h℃〕內(nèi) 外/窯頂硅磚0.314502500.9+80*10-5〔1450+250〕/2=1.585.2側(cè)胸墻硅磚0.414501800.9+80*10-5〔1450+180〕/2=1.5523.8前胸墻硅磚0.414502000.9+80*10-5〔1450+200〕/2=1.563.上層池墻33#AZS0.313401602.1+19*10-4〔1340+160〕/2=3.42511.下層池墻鐵磚0.312651202+14*10-4〔1265+120〕/2=2.979.池底粘土磚0.312501750.6+55*10-5〔1250+175〕/2=0.9923.3流液洞底33#AZS0.312501752.1+19*10-4〔1250+175〕/2=3.42511.壁流液洞蓋33#AZS板0.312652002.1+19*10-4〔1265+200〕/2=3.511.分隔墻 硅磚0.414501800.9+80*10-5〔1450+180〕/2=1.5523.橋墻蓋磚 硅磚 1.2 1450 180 0.9+80*10-5〔1450+180〕/2=1.552 1.總計(jì)5.2輻射熱損失輻射部位 孔口面積F

輻射處空間溫度t1

被輻射處空間溫度t2

孔口高/孔D/x共計(jì)通過(guò)加料口0.11600500.1/0.4=0共計(jì)通過(guò)加料口0.11600500.1/0.4=0通過(guò)噴嘴磚孔0.0171600600.06/0.14=通過(guò)測(cè)溫孔0.011600500.08/0.4=向小爐口1.81600〔1350+1050/2=12000.73/0.4=1其中：輻射熱損失量q=F*(T

/100)4

/100)4

kJ/h4 1 2加熱燃燒產(chǎn)物由小爐排出的煙氣量為V Vg

V V去氣

=13.78x+120*1000/24*0.63*19.507/100-172.7=13.78x+441.77Nm3/h1400℃Cg0.379*4.181.58kJ/Nm3℃40q=〔13.78x+441.77〕*1.58*1400=30481.36x+977195.24kJ/h6理論燃燒消耗量計(jì)算列熱量收支平衡式41800x+261.25x+93.6x+25.916x+17786.7x=13059200+258606.72+6025917.37*0.8+1423036.09+383033.06+30481.36x+977195.24x=709kg/h近似燃料消耗計(jì)算P=〔120*1000〕/〔60*24〕=83.33kg/m2h查表得K 1.08〔t 1450℃〕2 wW=44000kcal/m2hK取 0.25K1Q=〔Pq玻

KW〕/〔1-K*K 〕2 1 2〔83.33*2611.84/4.18+1.08*44000〕/〔1-0.25*1.08〕=136422kcal/m2h近似耗油量為x=136422*60/1000=819 kg/h實(shí)際燃燒消耗量計(jì)算10％～20％x=(1.1～1.2)*709=779.9～850.8kg/h參考閱歷數(shù)據(jù)，難以估量的熱損失還可以適當(dāng)?shù)托?，故?4.6％x=1.146*709=813kg/h=19.51t/d5.4收入熱量支出熱量5.4收入熱量支出熱量工程kJ/h％工程kJ/h％〔1〕重油潛熱3398340069.7〔1〕玻璃形成耗熱1305920029.79〔2〕重油物理熱2123960.436〔2〕加熱回流玻璃液2586070.53〔3〕壓縮空氣物理熱760970.156〔3〕窯體散熱48207349.89〔4〕吸入空氣物理熱211380.043〔4〕輻射熱損失14230362.92〔5〕助燃空氣物理熱1446059529.61〔5〕溢流熱損失3830330.79〔6〕加熱燃燒產(chǎn)物2575854152.83〔7〕其他熱損失50508.10.10共計(jì)48753659100共計(jì)48753659100熔化部熱負(fù)荷值，單位耗油量及窯熱效率計(jì)算〔按實(shí)際耗油量〕Q=(33983400+212396)/60=569930kJ/m2h單位耗油量=19510/120230=0.163kg/kg玻璃液窯熱效率η=13059200/(33983400+212396)*100％=38.2％據(jù)實(shí)踐，如操作得當(dāng)，單位耗油量可適當(dāng)降低些，窯熱效率可適當(dāng)提高些?！擦承顭崾沂軣嵬獗怼⒖諝饨粨Q器及煙道的計(jì)算蓄熱室計(jì)算格孔尺寸160mm*160mm,150mm取比受熱外表AF /F蓄 熔

35m2/m2則F60*352100m2蓄VF/f格 蓄

2100/14.94140.56m3由于格子體高度一般為7～9m，格子體長(zhǎng)寬尺寸應(yīng)為磚的長(zhǎng)度的整數(shù)倍。故設(shè)格子體尺寸L*B*H為5.25*3.5*7.65實(shí)際V格140.57m3則F 140.57*14.942100m2蓄A(yù)F/F蓄

35m2/m2H/

=7.65/

=1.78LB5.25*3.5格孔流通面積為：F 0.6LB5.25*3.5空格孔空氣流速為：W空

=V / Fa0

=11.98*813/3600/11.03=0.1245m/s廢氣流速為：W =V /F廢 g0 空

=13.78*813/3600/11.03=0.282m/s空氣交換器承受閘板式，設(shè)漏氣量為10％空氣口尺寸設(shè)計(jì)成高*寬*碹升為0.80m*0.95m*0.15m則F 0.76m2口煙道承受地下煙道，漏氣量為15%總煙道口尺寸高*寬*碹上升為1.55m*0.9m*0.15F 1.53m2口〔七〕排煙系統(tǒng)阻力計(jì)算7.17.1局部阻力計(jì)算編號(hào)局部阻力部位與性質(zhì)V tg g

F Wg 0 0

h 漏風(fēng)m1進(jìn)小爐口3.114000.93.441.2980.52.4012在小爐內(nèi)集中3.114001.81.721.2980.10.1203903.113101.81.721.29822.2724進(jìn)蓄熱室擴(kuò)大3.1120018.3750.171.2980.720.0075進(jìn)格子磚3.111002.81.111.2982.61.0676在格子體中3.1626872.81.131.29814.84.4012%7進(jìn)爐條孔擴(kuò)大3.3204003.340.991.2980.10.0165%8出爐條孔擴(kuò)大3.3204003.340.991.2980.050.0089903.3203501.172.841.29821.43810進(jìn)煙道縮小3.32010進(jìn)煙道縮小3.3203301.532.171.2980.20.13811通過(guò)交換器3.3203200.7604.371.2980.51.37412進(jìn)煙道擴(kuò)大3.6523200.7604.811.2970.20.66510%13453.6523001.522.401.2970.50.40014通過(guò)閘板4.2002801.143.681.2961.31.35815%15904.2002801.522.761.2961.51.53016煙囪底部擴(kuò)大4.2002801.522.761.2960.50.51017出煙囪口4.2002201.383.041.2961.01.104h16.001hm

(W2/2g)0

(1t)摩擦阻力計(jì)算7.2蓄熱室?guī)缀螇侯^計(jì)算從蓄熱室頂?shù)?/p>