30t转炉计算书.docx
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30t转炉计算书
30t转炉计算书
一.工艺参数:
1.炉子公称容量:
30t
2.最大铁水装入量:
41t
3.最大脱碳速度:
VC=0.5%/min
4.冶炼周期:
36min
5.炉气温度:
1500℃
6.炉气量;23940Nm3/h
7.炉气含尘浓度:
120g/Nm3
8.炉气成份:
CO
CO2
O2
N2
其它
86%
10%
0.5%
3.3%
0.2%
二.工艺流程:
转炉-活动烟罩-汽化冷却烟道-溢流文氏管(一文)-重力挡板脱水器-RD矩形文氏管(二文)-90°弯头脱水器-湿旋脱水器-煤气鼓风机-三通切换阀-放散烟囱
水封逆止阀-煤气柜
三.炉气量计算:
V0=G*VC*22.4/12*[1/(CO+CO2)]*60
=41000*0.005*(22.4/12)*[1/(0.86+0.1)]*60
=23917Nm3/h
四.烟气量计算:
α=10%
V=(1+1.88*0.1*0.86)*V0
=(1+1.88*0.1*0.86)*23917
=1.1617*23917
=27785Nm3/h
五.燃烧10%后烟气成份:
CO’=(1-0.1)*CO*V0/V
=(1-0.1)*0.86*23917/27785
=0.774*0.861
=66.64%
CO2=(0.1*CO+CO2)*V0/V
=(0.1*0.84+0.1)*23917/27785
=15.9%
O2=0.005*V0/V
=0.005*23917/27785
=0.43%
N2=(1.88*α*CO+N2)*V0/V
=(1.88*0.1*0.86+0.033)*23917/27785
=0.19468*0.861
=16.8%
六.烟气浓度修正:
C=C0/(V/V0)
=120/(27785/23917)=120/1.162=103.27g/Nm3≈103g/Nm3
七.溢流文氏管(一文)计算:
1.进口烟气量:
进口烟气温度:
900℃当地大气压P=760mmHg
进口处烟气要求负压:
P1=30mmH2O
V1=V*[(273+900)/273]*760/(760-30/13.6)
=27785*[(273+900)/273]*760/757.8
=27785*4.2967*1.003
=119742m3/h
2.水气比:
当t1=900℃时
水气比i=(0.55~0.815)手册P185页
取i=0.8
3.供水量:
W1=0.8*V1
=0.8*119742=95794kg/h取W1=96m3/h
4.一文入口热量:
烟气定压容积比热(900℃)C1=0.364千卡/Nm3手册P20页
供水温度t’1=35℃水的比热CS=1
Q1=V*C1*t1+W1*CS*t’1
=27785*0.364*900+96000*1*35
=9102366+3360000
=12462366kCal/h取Q1=12.462x106kCal/h
5.一文出口热量:
1)假定:
一文出口烟气温度:
t2=70℃
烟气定压容积比热C2=0.324千卡/Nm3
饱合水蒸汽分压力(70℃时)PH=233.7mmHg手册P567页
2)含湿量:
f1
一文出口负压值:
30+300=330mmH2O
f1=0.804*PH/[(P-330/13.6)-PH]
=0.804*233.7/[(760-330/13.6)-233.7]
=187.895/[735.74-233.7]
=187.895/502.04=0.3743kg/Nm3
3)蒸发水量:
W蒸1=V*f1=27785*0.3743=10400kg/h
4)一文排水量:
W’1=W1-W蒸1
=96000-10400=85600kg/h
5)水蒸汽热焓:
i1=595+0.46*t2
=595+0.46*70=595+32.2
=627.2kCal/kg(也可查冶金设计手册表23-14
得627.2kCal/kg)
6)排水温度:
tpw=70-5=65℃
7)一文出口热量:
Q2
Q2=V*C2*t2+W’1*C水*tpw+W蒸1*i1
=27785*0.324*70+85600*1*65+10400*627.2
=630164+5564000+6522880
=1271044kCal/h=12.71x106kCal/h
Q2≈Q1前面假定值可行
6.一文出口烟气量:
V2=[760/(760-330/13.6)]*[(273+70)/273]*(1+f1/0.804)*V
=1.033*1.25641*(1+0.3743/0.804)*27785
=1.29787*1.46554*27785
=52850m3/h
7.饱和烟气的密度:
(干烟气在标准状态下的密度:
r0=1.365kg/Nm3)
r1=(r0+f1)/(V2/V)
=(1.365+0.3743)/(52850/27785)
=1.7393/1.9021=0.914kg/m3
8.一文几何尺寸计算:
1)一文进口直径:
U=20m/s
F1=V1/(3600*U)
=119742/(3600*20)=119742/72000=1.663m2
D1=(1.663*4/3.140)1/2=1.455m取D1=1.45m
2)喉口直径:
DTUT=60m/s
DT=[(V2*4)/(3.14*3600*U)]1/2
=[(52850*4)/(3.14*3600*60)]1/2
=[211400/678585.6]1/2
=0.5582m取DT=560mm
3)收缩管长度:
L1
α收=23°(α收/2)=11.5°
L1=(D1-DT)/[2(tg11.5°)]
=(1450-560)/[2(tg11.5°)]
=890/[2*0.2035]
=890/0.407=2187mm取L1=2180mm
4)一文出口直径:
D2U2=20m/s
F2=V2/(3600*U)
=52850/(3600*20)
=0.734m2
D2=(0.734*4/3.1416)1/2
=0.93461/2
=0.967m取D2=1020mm
5)扩散管长度:
L2
α扩=7°(α收/2)=3.5°
L2=(D2-DT)/[2(tg3.5°)]
=(1020-560)/(2*tg3.5)
=460/(2*0.061163)
=460/0.12233=3760mm
6)喉口长度:
LT=DT=560mm
9.一文溢流水量:
WT
qT=5500kg/喉口园周米长.时手册P185页
WT=3.1416*DT*5500
=3.1416*0.56*5500
=9676kg/h取WT=9.7m3/h
10.一文阻损:
计算公式见手册P191页
△P=(ξk+ξwiYw/Yg)Vr2Yg/2gξwi=(0.89-0.34i)i
=[0.4+(0.89-0.34i)i*1/0.945]602*0.945/(2*9.8)
=[0.4+(0.89-0.34*0.80)*0.80*1.0582]*3600*0.0482
=[0.4+0.618*0.80*1.0582]173.52
=[0.4+0.5232]*173.52
=0.9232*173.52=160.2mmH2O取△P=300mmH2O
八.重力脱水器计算:
1.脱水器有效断面积:
烟气通过脱水器流速:
取5m/s
F=V2/(3600*5)
=52850/(3600*5)=2.9361m2(F=1500x1960)
D=(2.9361*4/3.1416)1/2=1.933m取D=1920mm
2.脱水器进口管管径:
流速:
取15m/s
D=[(52850*4)/(3600*15*3.14)]1/2
=[211400/169646]1/2=1.116m取D=1120mm
2.脱水器阻损:
△P=ξVj2*Yg/2g=2.85*152*Yg/19.6
=2.85*152*0.945/19.6
=30.92mmH2o取△P=31mmH2o
九.调径文氏管(二文)计算:
1.二文入口热量:
Q3
二文供水量气水比按1.2考虑
W3=1.2*V2=1.2*52850/1000=63.42m3/h
取W3=64m3/ht3=35℃
Q3=V*C2*t2+W3*C水*t3+W蒸1*i1
=27785*0.324*70+64000*1*35+10400*627.2
=630164+2240000+6522880
=9393044kCal/h=9.393x106kCal/h
2.二文出口热量:
Q4(烟气在二文管内降温为7℃左右)
二文出口烟气温度为t4=70-7=63℃
烟气63℃时的水蒸汽分压力PH=171.39mmHg
排水温度t5=63-3=60℃
二文阻损(煤气回收时800~900mmH2o)(放散时1000~1200mmH2o)计算取ΔP=1100mmH2o
1)二文出口负压值:
P’
P’=760-(30+300+31+1100)/13.6
=760-1461/13.6
=760-107.4=652.6mmHg
2)含湿量:
f2
f2=0.804*[PH/(P’-PH)]
=0.804*[171.39/(652.6-171.39)]
=0.804*[171.39/481.21]
=0.804*0.3562=0.2864kg/m3
3)排水量:
W4
W4=W3+V*(f1-f2)
=64000+27785*(0.3743-0.2864)
=64000+27785*0.0879
=64000+2442=66442kg/h取W4=66.44m3/h
4)水蒸汽热焓:
I’2
I’2=595+0.46*63=624kCal/kg
5)蒸发水量:
W’2
W蒸2=Vf2=27785*0.2864=7958kg/h
6)二文出口热量:
Q4
Q4=V*C2*t4+W4*C水*t5+W蒸2*I’2
=27785*0.324*63+66442*1*60+7958*624
=567147+3986520+4965792
=9519459
=9.52x106kCal/h
Q4≈Q3
3.二文出口烟气量:
V3=V*(1+f2/0.804)*[(273+63)/273]*(760/P’)
=27785*(1+0.2864/0.804)*[336/273]*760/652.6)
=27785*1.3562*1.2308*1.1646
=54013m3/h
4.二文几何尺寸确定:
1)二文进口尺寸:
V=15m/s
F1=V2/(3600*15)
=52850/(3600*15)=52850/54000=0.979m2
取F1=1240x790=0..98m2
2)二文喉口尺寸:
V=100m/s
FT=V3/(3600*100)
=54013/360000=0.15m2(按订货喉口进行核算)
喉口厂家资料:
喉口断面0.475m2矩形为950mmx500mm
DT=(0.475*4/3.1416)1/2=0.6041/2=0.78m
3)二文出口尺寸:
V=15m/s
F2=V3/(3600*15)
=54013/54000=1.00m2取F2=1250x800=1.00m2
4)收缩管长度:
L1
a)收缩角α收=23°
b)收缩管长:
L1=(1240-950)/2tg11.5°
=290/(2*0.203)
=714mm
5)扩散管长度:
L2
a)扩散角α收=7°
b)L1==(1250-950)/2tg31.5°
=300/(2*0.0611626)
=2452mm
6)喉口长度:
LT=0.75DT=0.75*0.78=0.585m取LT=0.6m
十.弯头脱水器计算:
1.进口面积:
V=12m/s
0.8-考虑隔板占去的面积系数
F入=V3/(3600*12*0.8)
=54013/34560=1.566m2(取F入=1420×1150)
2.出口面积:
V=10m/s
F出=V3/(3600*10*0.8)
=54013/28800=1.88m2(取F出=1420×1370)
3.弯头脱水器截面积:
V=8m/s
F0=V3/(3600*8*0.8)
=54013/23040=2.3443m2(取F出=1420×1690)
4.阻损:
(计算从简)一般取30mmH20
十一.复式挡板脱水器:
1.塔内烟气速度:
VC=3m/s
2.进口流速:
VP=20m/s
3.出口流速:
VZ=15m/s
4.烟气容重:
rt=(r0+f2)/(V3/V)
=(1.365+0.2864)/(54013/27785)
=1.6514/1.944=0.85kg/Nm3
5.烟气温度:
t4=63℃含湿量f2=0.2864kg/Nm3
供水温度:
tj=35℃
6.进风管断面及直径:
F入DP
F入=V3/(3600*20)=54013/(3600*20)=0.75m2
DP=(0.75/0.785)1/2
=0.95541/2=0.98m取DP=980mm
7.筒体内径:
DC
DC=(V3/3600*3*0.785)1/2
=(54013/8478)1/2=2.52m取DC=2520mm
8.出风管断面及直径:
F出DZ
F出=V3/(3600*15)=54013/(3600*15)=1.00m2
DZ=(1.0/0.785)1/2
=1128m取DZ=1120mm
9.筒体高度:
HC
HC=π*DC*tgθ+DP+h0h0=100~200
=3.1416*2520*tg15+980+200θ=13~17取θ=15°
=7917*0.268+1180
=2122+1180=3302mm取HC=3300mm
10.芯管外径:
DI
DC/DI≈3则DI=DC/3=2520/3=840mm
取DI=820mm
11.排尘浆口内径:
De
De=(1/8)*DC=0.125*2520=315mm取De=320mm
12.阻力:
C=31.4/UP1.1=31.4/201.1=31.4/27=1.163
ΔP=C*U2P*ρa/2g
=1.163*202*0.85/2g=20.2mmH2O
取ΔP=50mmH2O
十二.风机前管道计算:
V=20m/s
1.管径:
D=[V3/(3600*20*0.785)]1/2
=[54013/56520]1/2
=0.956m取D=1020mm
2.烟气容重:
烟气压力:
P=760-[(30+300+31+1100+30+50)/13.6]
=760-113.3=646.7mmHg
含湿量:
f3=0.804*[PH/(P-PH)]
=0.804*171.39/(646.7-171.39)
=131.7/475.31=0.277kg/Nm3
烟气容重:
rx=(r0+f3)/(V3/V)
=(1.365+0.277)/(54013/27785)
=1.642/1.944
=0.845kg/m3
十三.风机的选用:
1.从二文至风机管道温降按3℃计,则进入风机烟气温度为tj=60℃,PH=149.39mmHg。
2.风机前负压:
Pj
一文前30mmH2O一文300mmH2O
重力脱水31mmH2O二文1100mmH2O
弯头脱水30mmH2O复式挡板脱水50mmH2O
管道300mmH2O风机前阀门50mmH2O
合计:
1891mmH2O
3.60℃时烟气含湿量:
f4=0.804*149.39/(760-1891/13.6-149.39)
=0.804*149.39/(760-139.04-149.39)
=120.11/471.57=0.255kg/m3
4.风机实际操作烟气量;
VJ=V*(1+f4/0.804)*[(273+tj)/273]*760/[754-(Pj/13.6)]
=27785*(1+0.255/0.804)*[(273+60)/273]*760/[760-(1891/13.6)]
=27785*1.317*1.22*760/620.96
=54640m3/h(910m3/min)取VJ=1000m3/min
5.风机前烟气重度:
rj=(r0+f4)/(VJ/V)
=(1.365+0.253)/(54640/27785)
=1.618/1.966=0.823kg/m3
6.水封逆止阀:
水封逆止阀筒体直径:
筒体气流上升速度u=1.2m/s
1)D=[54640/(3600*1.2*0.785)]1/2=4.01m取D=4000mm
2)进气管D1:
取管内流速20m/s
D1=[54640/(3600*20*0.785)]1/2=0.983m取D1=1020mm
3)出气管D2:
取管内流速15m/s
D2=[54640/(3600*15*0.785)]1/2=1.135m取D2=1120mm
7.风机后正压;
三通阀+30mmH2O逆止阀+120mmH2O
管道+200mmH2O煤气柜+450mmH2O
合计:
+800mmH2O
8.系统全压:
1891+800=2691mmH2O=26388Pa
9.选用风机;
煤气鼓风机(防爆型)D1000-11型
性能参数:
进口流量1000m3/min
升压27000Pa
主轴最高转速2900r/min
重量19.3t(不含电机)
轴功率700kW
进口气体重度0.823kg/m3
风机配用电机功率为850kW
配用电机:
防爆型电机
电压6000V
转速2900r/min
配用液力偶合器:
YOTcs500型(要求防爆型)
输入转速:
3000r/min
传递功率:
670~1640kW
转差率:
1.5~3
鄂钢二炼钢增建4#转炉工程
30t转炉一次烟气(煤气)净化系统
计算书
室审:
审核:
设计:
2003.12.31