CFB脱硫塔设计计算复习课程.xls

SCRUBBER DESIGN(PACKED COLUMN)Prepared by:Column Tag No.:HCL ScrubberChecked by:Job No.:4506ADate:Client:JOLProject:SR-Plant-4,5Input DataStream:HCL Vap.Packing type=Intallox SaddlesPacking size=25 mmPacking MOC=PPGas pr.Drop/m bed=15 mmWC/m packing height=147.1(N/m2)/mTotal packing height=3.2 m(including all packed beds)Gas/Vapour PropertiesGas/Air flow rate=1000 kg/hOR0 m3/h=0.2778 kg/s=0 m3/sGas pressure at entry=1.0000 atmGas temperature at entry=30.00oC=303.00oKGas/Air mol weight=29Component to be scrubbedComponent Name=HCL VapComponent flow rate=70 Kg/h%comp.in air/gas=6%(v/v)(presumed)/(given by client)/(by process cal.)Molecular weight of comp.=36.5Liquid/Scrubbing media PropertiesScrubbing media=20%NaOHLiquid flow rate,L=77 kg/h=0.0214 kg/sLiquid Density,L=1100 kg/m3Conversion:Liquid Viscosity,L=0.0035000 Ns/m23.5 Cp =0.00350000Ns/m2Packing factor,Fp=21 m-1Charac.Packing Factor,Cf=33 Ref.Table 6.3,Characterstics of Random packingsConversion factor,J=1.0 factor for adequate liquid distribution&irrigation across the bedSheet 1 of 42 CalculationsTO CALCULATE COLUMN DIAMETERSince larger flow quantities are at the bottom for an absorber,the diameter will be chosen to accommodate the bottom conditions.To calculate Gas densityAvg.molecular weight=29.45 Kg/KmolIf gas flow rate is given in kg/hIf gas flow rate is given in m3/hGas in =0.009432183 Kmol/sGas in =(m3/s)x 273x pr.in atm x 1kmol=mass/mol wt T in kelvin1.0 atm22.4=(kmol/s)x T in kelvin x 1.0 atm x 22.4 273 pr.In atm 1=0 Kmol/s=0.234499 m3/s=0 Kg/smass=mol wt x kmolSelect vol.flow rate and mass flow rate from above,Selected mass flow rate=0.277778 Kg/sSelected vol.Flow rate=0.234499 m3/sSelected molar flow rate=0.009432 Kmol/sTherefore,gas density=1.1846 Kg/m3(mass flow rate/vol.Flow rate)To find L,G and Tower c/s areaAssuming essentially complete absorbtion,Component removed=0.0207 Kg/s(molar flow rate x%comp.x mol.Wt.)Liquid leaving=0.0420 Kg/s(Inlet liquid flow rate+comp.Removed)L G0.5=0.00497G LUsing 0.00497as ordinate,Refer fig.6.34 using a gas pressure drop of147.1(N/m2)/m G 2 Cf L0.1 J=0.04 (from graph)G(L-G)gcTherefore,G=0.04 G(L-G)gc0.5 Cf L0.1 J=1.6665 Kg/m2.sTower c/s area=0.1667 m2(c/s area=mass flow rate/G)Tower diameter=0.4607 m=460.7 mm=500 mmCorresponding c/s area=0.1963 m2Sheet 2 of 42 TO ESTIMATE POWER REQUIREMENTEfficiency of fan/blower=60%assumed/givenTo calculate pressure dropPressure drop for irrigated=470.72 N/m2(pressure drop per m packing x total ht.of packing)packingFor dry packing,O/L Gas flow rate,G=1.3095 Kg/m2.s(Gas inlet flow rate-Component removed)/c/s areaO/L Gas pressure=100854.3 N/m2(subtracting pressure drop across packing)Gas density,G=gas mol wt.x 273 xgas o/l pr.22.41m3/Kmol T in kelvin101330=1.1605 Kg/m3CD=96.7 Ref.Table 6.3,Characterstics of Random packingsDelta P=CD G 2 ZG =142.89 N/m2Pressure drop for packing=613.61 N/m2(irrigated packing+dry packing)Pressure drop for internals=25 mmWC(packing supports and liquid distributors)=245.17 N/m2Gas velocity=7.5 m/sInlet expansion&outlet=1.5 x Velocity heads=1.5 x(V2/2g)contraction losses=42.19 N m/Kg=49.97 N/m2(divide by density)Total pressure drop=908.75 N/m2(packing+internals+losses)Fan power output=pressure drop,N/m2 x(gas in-component removed)Kg/sO/L gas density,Kg/m3=201.35 N.m/s=0.20 kWPower for fan motor=0.34 kW(fan power output/motor efficiency)=0.45 hpSheet 3 of 42 COLUMN DIAMETER/HYDRAULIC CHECKLiq.-Vap.Flow factor,FLV=(L/V)x (V/L)=0.0025Design for an initial pressure drop of 15mm H2O/m packingFrom K4 v/s FLV,K4=0.85K4 at flooding=6.50Trial%flooding=(K4/K4 at flooding)x 100=36.1620Gas mass flow rate,Vm=K4.V(L-V)13.1 Fp(L/L)0.1=3.7763 kg/m2.sTrial column c/s area=V/Vm(Trial As)=0.0736 m2Trial column dia.,D=0.3060 mD=(4/pi)x Trial AsRound off D to nearest standard sizeTherefore,D=0.500 mColumn C/S area,As=0.1963 m2As=(pi/4)x D2%flooding=13.5472%flooding=Trial%flooding x(Trial As/As)ConclusionGenerally packed towers are designed for 50%-85%flooding.If flooding is to be reduced,(i)Select larger packing size and repeat the above steps.OR(ii)Increase the column diameter and repeat the above steps.(1/2)Sheet 4 of 42 HETP PREDICTIONNortons Correlation:ln HETP =n-0.187 ln +0.213 ln Applicable when,liquid phase surface tension 4 dyne/cm&0.08 cP&0.83 cPConversion:Input Data0.018 N/m =18dyne/cmLiquid-phase Surface Tension,=20 dyne/cmNortons Correlation ApplicableLiquid Viscosity=3.5 cPNortons Correlation NOT applicablen=1.13080Calculationln HETP=0.837437HETP=2.310437 ft=0.704221 mFor separations,less than 15 theoritical stages,a 20%design safety factor can be applied.Considering 20%safety factor,HETP=0.845065 mFor separations,requiring 15 to 25 theoritical stages,a 15%design safety factor can be applied.Considering 15%safety factor,HETP=0.809854 mSheet 5 of 42 Table 6.2Constant for HETP CorrelationRef.:Random Packings and Packed Towers -StrigleRef.:Chemical Engineering,Volume-6,COULSON&RICHARDSONSRef.:Mass Transfer Operation:Treybal工况烟气量计算烟气温度（）标况烟气量（Nm3/h）工况烟气量（m3/h）150.0060000.0092967.03标况烟气量计算烟气温度（）工况烟气量（m3/h）标况烟气量（Nm3/h）150.00180000.00116170.21耗水量计算系统进口烟气温度（）标况烟气量（Nm3/h）系统出口烟气温度（）150.00180000.0065.00脱硫塔蒸发水量（Kg/h）除雾器冲洗水量（Kg/h）钠碱含水量（Kg/h）4500.003391.205.76二氧化硫含量计算耗煤量（t/h）标况烟气量（Nm3/h）燃煤含硫率（%）5.0050000.001.00二氧化硫浓度（mg/Nm3）二氧化硫总量（Kg/h）二氧化硫脱除量（Kg/h）1700.0085.0079.05物料计算(小时耗量)排放浓度（mg/Nm3）脱硫效率（%）纯生石灰的量（Kg/h）400.0076.4772.63需要烧碱的量（Kg）石膏产生量（Kg/h）氧化空气用量（m3/h）98.81212.6479.05石膏结晶水（Kg/h）脱硫渣含水（Kg/h）烧碱耗量（Kg/h）44.5121.262.47反应池中的钠、钙、硫平衡进反应池的Na2SO3进反应池的Ca(OH)2出反应池的CaSO3155.6391.40148.22出反应池的Na(OH)98.81输入值计算值锅炉数量1.00脱硫塔计算公式设计参数单位数值塔高m18.00塔径m4.0085%生石灰价格元/吨300.00烧碱价格元/吨3000.00脱硫效率%93.00年运行时间h8000.00脱硫塔截面积m212.56烟气流速m/s3.98年脱出SO2总量t632.40纯生石灰的量t/年581.02烧碱的量t/年19.8685%生石灰的量t/年683.55生石灰费用万元20.51烧碱费用万元5.96按分支1计算类型泵泵的计算流量m3/h1200.00泵的计算扬程mH2O4.47流量系数1.00压力系数1.00泵泵的的扬扬程程m3/h4.474.47泵泵的的流流量量mH2O1200.001200.00介质的密度kg/m31150.00泵电机功率安全系数1.15泵效率0.85泵传动效率0.98循环浆液泵电动机功率KW23.20循环浆液泵动机轴功率KW20.17电机功率KW75.00入口液柱顶高m12.10入口液柱底高m1.00喷嘴高度（出口）m2.70喷嘴压损m6.90入口管道总长度m5.00出口母管管道总长度m20.00出口分支1管道总长度m50.00固定压力差m(8.40)入口管阻力(沿程+局部)*1.1m1.15出口母管阻力(沿程+局部)*1.1m1.02出口分支1阻力(沿程+局部)*1.1m4.57附加阻力m0.50入口管道计算流量Dgsm3/h1200.00入口管道内径Dimm458.00流速m/s2.02入口管道等值粗糙度Kdmm0.20入口管道摩擦系数0.016入口直管段阻力系数10.17容器至管道0.50个1管道至容器1.00个090弯头0.35个045-弯头0.20个130-弯头0.15个0异径(渐缩)0.10个1泵入口管出口母管分支1分支2异径(渐扩)0.40个0三通分流1.50个0三通合流0.40个0蝶阀0.24个1球心阀或截止阀6.40个0旋塞阀0.05个0调节阀1.10个0膨胀节0.30个1滤网3.50个1特殊段或附加1.00个0入口局部阻力系数之和4.84出口母管管道计算流量Dgsm3/h1200.00出口母管管道内径Dimm458.00流速m/s2.02出口管道等值粗糙度Kdmm0.20出口管道摩擦系数0.016出口直管段阻力系数10.694容器至管道0.50个0管道至容器1.00个090弯头0.35个345-弯头0.20个030-弯头0.15个0异径(渐缩)0.10个0异径(渐扩)0.40个1三通分流1.50个1三通合流0.40个0蝶阀0.24个2球心阀或截止阀6.40个0旋塞阀0.05个0调节阀1.10个0膨胀节0.30个1滤网3.50个0特殊段或附加1.00个0出口局部阻力系数之和3.73出口分支1管道计算流量Dgsm3/h150.00出口分支1管道内径Dimm142.00流速m/s2.63出口管道等值粗糙度Kdmm0.20出口管道摩擦系数0.021出口直管段阻力系数17.503容器至管道0.50个0管道至容器1.00个090弯头0.35个845-弯头0.20个030-弯头0.15个0异径(渐缩)0.10个1异径(渐扩)0.40个1三通分流1.50个0三通合流0.40个0蝶阀0.24个4球心阀或截止阀6.40个0旋塞阀0.05个0调节阀1.10个0膨胀节0.30个0滤网3.50个0特殊段或附加1.00个0出口局部阻力系数之和4.26按分支2计算类型泵泵的计算流量m3/h300.00泵的计算扬程mH2O48.07流量系数1.00压力系数1.00泵泵的的扬扬程程m3/h48.0748.07泵泵的的流流量量mH2O300.00300.00介质的密度kg/m31150.00泵电机功率安全系数1.15泵效率0.85泵传动效率0.98循环浆液泵电动机功率KW62.35循环浆液泵动机轴功率KW54.22电机功率KW75.00入口液柱顶高m12.50入口液柱底高m1.00喷嘴高度（出口）m25.50喷嘴压损m20.00入口管道总长度m9.50出口母管管道总长度m50.00出口分支2管道总长度m80.00固定压力差m14.00入口管阻力(沿程+局部)*1.1m0.85出口母管阻力(沿程+局部)*1.1m3.76出口分支2阻力(沿程+局部)*1.1m6.86附加阻力m0.50入口管道计算流量Dgsm3/h300.00入口管道内径Dimm253.00流速m/s1.66入口管道等值粗糙度Kdmm0.20入口管道摩擦系数0.018入口直管段阻力系数10.69容器至管道0.50个1管道至容器1.00个090弯头0.35个045-弯头0.20个130-弯头0.15个0异径(渐缩)0.10个1分支1应与分支2的管道损失应相同，应在分支1管路上加节流孔板，若不加节流孔板，管道会根据各管路压损自行分配流量，已达到自平衡异径(渐扩)0.40个0三通分流1.50个0三通合流0.40个0蝶阀0.24个1球心阀或截止阀6.40个0旋塞阀0.05个0调节阀1.10个0膨胀节0.30个1滤网3.50个1特殊段或附加1.00个0入口局部阻力系数之和4.84出口母管管道计算流量Dgsm3/h300.00出口母管管道内径Dimm199.00流速m/s2.68出口管道等值粗糙度Kdmm0.20出口管道摩擦系数0.020出口直管段阻力系数14.921容器至管道0.50个0管道至容器1.00个090弯头0.35个545-弯头0.20个030-弯头0.15个0异径(渐缩)0.10个0异径(渐扩)0.40个1三通分流1.50个1三通合流0.40个0蝶阀0.24个2球心阀或截止阀6.40个0旋塞阀0.05个0调节阀1.10个0膨胀节0.30个1滤网3.50个0特殊段或附加1.00个0出口局部阻力系数之和4.43出口分支2管道计算流量Dgsm3/h150.00出口分支2管道内径Dimm142.00流速m/s2.63出口管道等值粗糙度Kdmm0.20出口管道摩擦系数0.021出口直管段阻力系数112.005容器至管道0.50个0管道至容器1.00个090弯头0.35个1245-弯头0.20个030-弯头0.15个0异径(渐缩)0.10个1异径(渐扩)0.40个1三通分流1.50个0三通合流0.40个0蝶阀0.24个4球心阀或截止阀6.40个0旋塞阀0.05个0调节阀1.10个0膨胀节0.30个0滤网3.50个0特殊段或附加1.00个0出口局部阻力系数之和5.66类型事故浆液泵排出泵地坑泵泵的计算流量m3/h180.00160.0050.00泵的计算扬程mH2O22.9638.7524.73流量系数1.001.001.00压力系数1.201.201.20泵的扬程m3/h27.5646.5029.68泵的流量mH2O180.00160.0050.00介质的密度kg/m31150.001150.001150.00泵电机功率安全系数1.151.151.15泵效率0.850.850.85泵传动效率0.980.980.98循环浆液泵电动机功率KW21.4532.176.42循环浆液泵动机轴功率KW18.6527.975.58电机功率KW630.0020.0015.00入口液柱顶高m1.0011.22(1.00)喷嘴高度（出口）m15.0025.0015.00喷嘴压损m0.0017.000.00入口管道总长度m5.005.005.00出口管道总长度m150.00150.0050.00固定压力差m14.0013.7816.00入口管阻力(沿程+局部)*1.1m1.570.640.64出口管阻力(沿程+局部)*1.1m4.804.775.19附加阻力m0.500.500.50入口管道计算流量Dgsm3/h180.00160.0050.00入口管道内径Dimm176.00176.0092.00流速m/s2.061.832.09入口管道等值粗糙度Kdmm0.200.200.20入口管道摩擦系数0.0200.0200.024入口直管段阻力系数10.570.571.29容器至管道0.50个111管道至容器1.00个00090弯头0.35个00045-弯头0.20个11130-弯头0.15个000异径(渐缩)0.10个111异径(渐扩)0.40个000三通分流1.50个110三通合流0.40个000蝶阀0.24个111球心阀或截止阀6.40个000旋塞阀0.05个000调节阀1.10个000膨胀节0.30个011滤网3.50个100特殊段或附加1.00个000入口局部阻力系数之和6.042.841.34出口管道计算流量Dgsm3/h180.00160.0050.00出口管道内径Dimm176.00176.0092.00流速m/s2.061.832.09出口管道等值粗糙度Kdmm0.200.200.20出口管道摩擦系数0.0200.0200.024出口直管段阻力系数117.21317.21312.909容器至管道0.50个000管道至容器1.00个11190弯头0.35个3101045-弯头0.20个02230-弯头0.15个000异径(reducer)0.10个000异径(Extension)0.40个111三通分流1.50个000三通合流0.40个022蝶阀0.24个022球心阀或截止阀6.40个000旋塞阀0.05个000调节阀1.10个011膨胀节0.30个222滤网3.50个000特殊段或附加1.00个000出口局部阻力系数之和3.058.288.28事故浆液泵排出泵地坑泵2010.01.1325m40m25m102050920508950108.00502195052950273504785057.00501945015950277501335032501850油保000000000000000000000000000000000岩棉保温环境温度(ta)保温结构外表面温度(ts)设备和管道外表面温度(t)(tm)保温平均温度烟道3047.5170108.75钢灰库3047.5170108.75吸收塔3047.5180113.75输灰管3047.5170108.75蒸汽道管3047.5170108.75说明：本方法中，烟道，灰库，吸收塔保温按平面计算，介质温度认为不超过350度，用岩棉来保温的情况下设计。表表1.计计算算出出的的散散热热密密度度应应符符合合下下表表规规定定，否否则则重重新新选选择择保保温温层层厚厚度度计计算算保保温温结结构构外外表表面面允允许许最最大大散散热热密密度度介介质质常常年年运运行行季季节节运运行行介介质质常常年年运运行行温温度度温温度度 W/m2W/m2 W/m2W/m2 W/m2W/m2 505811640022710093163450244150116203500262200140244550279250163273600296300186296650314350209308 表表2.对对于于防防烫烫伤伤保保温温，一一般般可可直直接接选选取取，计计算算结结果果同同下下表表比比较较可可以以作作为为参参照照防防烫烫伤伤保保温温层层厚厚度度介质温度 150250350450管道外径mm 岩棉、矿渣棉制品硅酸钙制品57 2030506089133 20305070159219 20406080273426 30406090480920 304070100表3.保温材料损耗附加量及施工余量保温材料损耗附加量及施工余量硅酸钙制品10%硅酸铝复合制品5%岩棉、矿渣棉、玻璃棉制品5%憎水膨胀珍珠岩制品12%复合硅酸盐保温涂料5%镀锌铁皮25%铝合金板25%玻璃丝布25%抹面10%表4.管道计算过程辅助表保温层厚度()传热系数()导热系数()散热密度(q)外表面温度修正(ts)最大散热密度(q)47.12792258.140.047953126.6222245.5555555614047.12792258.140.047953126.6222245.5555555614051.20407148.140.048627127.5671645.67164179140按下表选8.140.048379#VALUE!#VALUE!95.62132749140按下表选8.140.048379#VALUE!#VALUE!95.62132749140计算时需输入数据季季节节运运行行 烟道，塔，库计算结果温温度度 计算结果代入表4得出保温厚度W/m2W/m2 从表4中得出厚度代入可得校正数据314 计算过程数据 校正数据 550450550硅酸铝复合保温(内层厚+外层厚)8020+40 30+40 9030+40 40+50 10030+50 50+50 11040+50 50+50 12040+50 60+50 说明：本方法中，烟道，灰库，吸收塔保温按平面计算，介质温度认为不超过350度，用岩棉来保温的情况下设计。表表2.对对于于防防烫烫伤伤保保温温，一一般般可可直直接接选选取取，计计算算结结果果同同下下表表比比较较可可以以作作为为参参照照硅酸钙制品 管管 道道 保保 温温 层层 厚厚 度度 的的 计计 算算 方方 法法(三三种种方方法法)(一).通过控制保温层外表面温度的方法计算管道内介质的温度 t=290输入主保温层外表面温度 tw1=40.12保温层平均温度 tp=165.06保温材料在tp温度下的导热系数 W/m1=0.048输入管道外径 mdw=0.121输入管道周围空气温度tk=37.9输入管道外的风速 m/s=3输入保温层表面到周围空气的放热系数 W/(m2k)h=23.66775311设管道主保温层外径为d1:d1/dwln(d1/dw)=3.7732令d1/dwln(d1/dw)=xlnx查表得：xlnx=3.7732输入x=3.94输入则保温层厚度为:m=0.1779(二).通过控制最大热损失的方法计算管道内介质的温度 t=95输入保温层平均温度 tp=70输入保温材料的导热系数 W/m1=0.048输入管道外径 mdw=0.219输入管道周围空气温度tk=28输入保温层表面到周围空气的放热系数 W/(m2k)h=0.034单位表面允许最大散热量 qq=93设管道主保温层外径为d1:d1=0.3527则保温层厚度为:m=0.0668注:当预先定出管道或设备的表面最大允许散热损失时,其保温层的经济厚度为:1=0.0048(三).通过控制温度降时的保温层厚度计算管道内的介质流量 kg/hG=35输入介质平均比热 kj/(kg)C=896输入介质始端温度 t1=95输入介质终端温度 t2=70输入管道输送长度 mL=1000输入平面保温层到周围空气的放热系数 W/(m2k)h1=0.344输入管道支吊架局部保温系数K1=1.2输入当(t1-tk)/(t2-tk)2时TRUE设管道主保温层外径为d1:d1=0.2266则保温层厚度为:m=0.0528当(t1-tk)/(t2-tk)2时FALSE设管道主保温层外径为d1:d1=0.1228则保温层厚度为:m=0.0009(四).直埋管道的保温层厚度计算土壤的导热系数 W/mt=1.74土壤层温度 tt=5埋管深度 mh=1.2设管道主保温层外径为d1:d1=0.0310则保温层厚度为:m=-0.0450备 注tw1=33.4+0.028(t50)(或者根据工艺要求直接输入)tp=(t+tw1)/2h=11.63+6.950.5d1/dwln(d1/dw)=21(t-tw1)/hdw(tw1-tk)见后面附表1见后面附表1=(d1-dw)/2=(x-1)dw/2此计算方法计算保温层厚度时,外表面温度未知,平均温度查附表2查附表3查附表4ln(d1/dw)=23.141(t-tk)/qh1=2.69dw1.211.35tw11.73/q1.5室内取0.086,室外取0.344吊架室内1.10,室外1.15;支架室内1.15,室外1.20当(t1-tk)/(t2-tk)2时,用下面公式计算：ln(d1/dw)=23.141(tp-tk)LK1/GC(t1-t2)h1=(d1-dw)/2当(t1-tk)/(t2-tk)2时，用下面公式计算：ln(d1/dw)=23.141(t2-tk)LK1/GC(t1-tk)h1=(d1-dw)/2一般可取1.74W/m一般可取5管管 道道 保保 温温 层层 厚厚 度度 的的 计计 算算 方方 法法(三三种种方方法法)lnd1=1(tw1-tt)ln(dw)+1(t-tw1)ln(4h)/t(tw1-tt)+1(t-tw1)=(d1-dw)/2附附表表1 1:x与与xlnx函函数数表表(当当x=15时时的的xlnx)值值xxlnxxxlnxxxlnxxxlnx10.0001.420.4992.141.632.863.0021.0050.0051.430.5122.151.6482.873.0211.010.010051.440.5262.161.6652.883.0451.0150.015151.450.5392.171.6812.893.0651.020.02021.460.5522.181.6992.93.0851.0250.2531.470.5652.191.722.913.1041.030.03041.480.582.21.7352.923.131.0350.03561.490.5942.211.7562.933.151.040.04071.50.6072.221.7712.943.171.0450.0461.510.6222.231.7912.953.191.050.05121.520.6372.241.8052.963.211.0550.05651.530.652.251.8252.973.241.060.06171.540.6652.261.8412.983.251.0650.0671.550.6792.271.8612.993.271.070.07241.560.6952.281.8833.291.0750.07771.570.7082.291.8993.013.311.080.08311.580.7222.31.923.023.341.0850.08851.590.7372.311.9353.033.361.090.09461.60.7512.321.9553.043.381.0950.09941.610.7652.331.973.053.41.10.10481.620.7822.341.993.063.421.1050.111.630.7992.352.0073.073.441.110.11621.640.8152.362.0273.083.461.1150.121.1.650.8272.372.0423.093.481.120.127.1.660.8422.382.0623.13.51.1250.13271.670.8562.392.083.113.531.130.1381.680.8722.42.13.123.551.1350.1431.690.8892.412.123.133.571.140.14921.70.9022.422.143.143.591.1450.15451.710.9162.432.163.153.611.150.16071.720.9322.442.183.163.641.1550.16651.730.9492.452.1953.173.661.160.17211.740.9652.462.2173.183.681.1650.17721.750.982.472.2333.193.71.170.18461.760.9942.482.2553.23.721.1750.1891.771.0112.492.273.213.741.180.1951.781.0292.52.293.223.761.1850.2011.791.042.512.313.233.781.190.2071.81.0592.522.3283.243.811.1950.2131.811.0812.532.3443.253.831.20.2181.821.0892.542.373.263.851.2050.251.831.1082.552.3853.273.881.210.231.841.1212.562.4053.283.91.2150.2361.851.1382.572.4253.293.921.220.2421.861.1522.582.4443.33.941.2250.2451.871.1692.592.4623.313.961.230.25451.881.1852.62.483.323.981.2350.2611.891.2052.612.5033.3341.240.2661.91.222.622.5213.344.031.2450.2721.911.2342.632.543.354.051.250.2791.921.2512.642.563.364.071.2550.2851.931.272.652.583.374.091.260.2911.941.2882.662.63.384.121.2650.2981.951.3022.672.623.394.141.270.341.961.3182.682.643.44.161.2750.3091.971.3352.692.663.414.181.280.3161.981.3512.72.683.424.21.2850.3221.991.3692.712.73.434.231.290.32821.3862.722.723.444.251.2950.3342.011.4012.732.743.454.271.30.342.021.4192.742.763.464.31.310.3542.031.4392.752.783.474.321.320.3672.041.4552.762.83.484.341.330.382.051.4712.772.823.494.361.340.3892.061.4882.782.843.54.381.350.4052.071.5072.792.863.514.41.360.4172.081.522.82.883.524.421.370.4322.091.5422.812.9013.534.451.380.4452.11.5592.822.9213.544.471.390.4572.111.5792.832.943.554.51.40.472.121.5922.842.9613.564.521.410.4852.131.612.852.983.574.55附附表表2:保保 温温 层层 平平 均均 温温 度度 tp周围空气温度()介 质 温 度100150