锅炉水动力计算样板

1、、锅炉规范1.额定热功率Q 58 MW2.额定工作压力P 1.25MPa3.出水温度t130 C4.回水温度t 锅炉结构特性70 C回路名称前墙水冷壁后墙水冷壁侧墙水冷壁对流管束回路元件上升管下降管上升管下降管上升管下降管引出管上升管下降管管径mm（）60 x 4$ 219x8（）60 x 4$ 219x84 60 x 4$ 219x8$ 159x64 51 x 34 51 x 3根数nn5825823224864576截面积f2 m0.12320.06470.12320.06470.0680.06470.06791.3740.916截面比0.5250.5250.9510.9990.667管子

2、长度lim2.37813.89.73712.011.2612.85.197.248.31l2m8.3998.712I3m5.631回路高度him1.6811.223.3411.511.4111.650.248.48.4h2m8.008.16h3m1.54弯管半径Rmm200800200800200800500160160弯头角度弯头个数ani1-70°1-30°1-1101-45°2-35°1-60°1-90°1-24°1-25°1-20°1-48.51-30°1-55°1-12

3、76;1-40°1-20°1-28°1-29°1-78°1-15°1-30°1-15°1-70°三、各回路局部阻力系数:名称符号公式及来源前墙水冷壁后墙水冷壁侧墙水冷壁对流管束上升管下降管上升管下降管上升管下降管引进管上升管下降管入口阻力系数r表2.表50.70.50.70.50.70.50.70.50.5出口阻力 系数匕c表91.01.11.01.11.11.11.01.01.0弯头阻力 系数wK良0.250.180.350.170.160.20.170.120.12总局部阻 力系数£ jbr

4、+ 孔+ -w1.951.782.051.771.861.81.871.621.62四、各受热面热量分配1 .炉膛辐射受热面热负荷：ql=121.9kw/m22 .前墙I区段辐射受热面积：H fqi =5.4m2前墙皿区段辐射受热面积：H fq2 = 52.5m2前墙用区段辐射受热面积：H fq3 = H fqd = 35.2m23 .后墙I区段辐射受热面积：H e = 22.1m2后墙皿区段辐射受热面积：H fh2 = 40.5m24 .侧墙辐射受热面积：H命=68.2m25. 顶棚吸热不均匀系数：吁=0.66. 前、后、侧墙吸热不均匀系数："=呷=/：= Hf 0.6Hfqd =

5、1.075Hfq H fh H fc7. 燃烬室辐射受热面热负荷：qj =60.5kw/m28. 燃烬室前墙受热面热负荷：Hrjq = 14.6m2燃烬室后墙受热面热负荷：Hrjh = 48.5m29.各受热面热量分配名称符号单位前墙后墙侧墙对流管束省煤器下降管Qjkw0006110.93204.4上升区段QS1kw707.62896.08937.123389.7上升区段QS2kw6879.76190.5上升区段QS3kw2574.5引出管Qykw0五、各回路水循环计算：1. 下降管入口水温假设：n =70 Ctj2 =1 1 5tj3=92.5 Cj 1j 2j 32. 流量假设前墙回路：G

6、1 = 125000kg/hG2 =131000kg/hG3 -137000kg/h后墙回路：G1 = 125000kg/hG2 =131000kg/hG3 =137000kg/h侧墙回路：G1 = 70000kg/hG2 = 76000kg/hG3 = 82000kg/h对流管束回路：G1 = 800000kg/hG2 = 850000kg/hG3 = 900000kg/h前墙回路水循环计算名称符号单位计算公式及来源计算结果回路循环流量Gkg/h假设125000131000137000125000131000137000125000131000137000下降管入口水温tjc假设7092.5

7、115下降管平均水温tjc不受热7092.5115下降管水平均密度Pjkg/m3查表B1978.19963.86947.24下降管水速与jm/ sG/(3600fPj)0.54860.5750.613055680.58350.61020.566660.59380.6209下降管水粘度PPa?s查表C406.4乂10 顼306.310*243.510 顼下降管水雷诺数RejcodP/ 卜2.681勺052.81 区1052.938K1053.557勺053.727 乂1053.898乂 1054.474 乂 1054.689 乂 1054.903 乂105沿程阻力系数Aj查图及公式170.017

8、70.01770.01760.01740.01740.01730.01710.01710.017下降管总阻力系数"/ d + -jb2.9832.9832.9762.9632.9632.9652.9422.9422.936下降管流动阻力PidjPa£如苛/2439.1482.4526.3442.7486.2530.4447.3491.3536.1下降管重位压降PzwjPa口gh107668106090104261上升管出口水温It llctj +Q1/GCP74.8874.6574.4597.3897.I596.95II9.88II9.65II9.45nt “ l2ck +

9、 QJGCPI22.28II9.88II7.7I44.78I42.38I40. 2I67.28I64.88I62.7mt;ctp/GCPI40.02I36.8II33.88I62.52I59.3II56.38I85.02I8I.8II78.88上升管平均水温Itlc（t；+ti）/272.4472.3372.2394.9494.8394.73II7.44II7.33II7.23nl2c（ti” + t；）/298.5897.2796.08I2I.08II9.77II8.58I43.58I42.27I4I.08mtac（t2'+t；）/2I3I.I5I28.35I25.79I53.65I

10、50.85I48.29I76.I5I73.35I70.79上升管水平均密度IPikg/m3查表Bi976.72976.78976.85962.I4962.2I962.29945.3I945.4945.48nP2kg/m3查表Bi959.6596I.5496I.35942.4943.49944.42923.05924.26925.35mP3kg/m3查表Bi934.0I936.37938.499I3.669I6.369I8.7489I.04894.0I896.74上升管平均水温tsc（ti +t2 +t3）/3I00.7299.3298.03I23.22I2I.82I20.53I45.72I44

11、.32I43.03上升管水平均密度Pskg/m3查表Bi958.I4959.I4960.02940.6294I.79942.8692I.08922.36923.56上升管水速m/ sG/（3600fPs）0.294I0.30790.32I70.29960.3I360.32760.3060.32020.3345上升管水粘度Pa?s查表C279.9X10-6284X10-6288.2K10-6225.9X10'6228.6乂10-6231.1乂 10-6188.5乂10-6190.5乂 10-6192.3号0-6上升管雷诺数Re仍 dP/N5.235X1045.407X1045.572 x

12、1046.487 x1046.718 x1046.95x 1047.7754 x108.06x 1048.354 x104沿程阻力系数As查图及公式170.02530.02520.02520.02480.02470.02460.02430.02420.0241上升管总阻力系数制 / d + Ejb9.9339.9029.9029.7759.7449.7129.6189.5869.554上升管流动阻力PldsPa牟2/2411.6450.2491.9412.7451.2491.4414.8453.3493.6上升管重位压降IPzwlPa勒16097160981609915857158581585

13、9155791558115582nPzwlPagh2755027557275635741447423074303726227271772803mPzw3Papgha141101414614178138031384413880134611350613547有效压头SyxPaApzwj £ Apzws Apids1736.41590.81452.12057.31891.81741.62365.22184.72017.4后墙回路水循环计算名称符号单位计算公式及来源计算结果回路循环流量Gkg/h假设12500013100013700012500013100013700012500013100

14、0137000下降管入口水温tjc假设7092.5115下降管平均水温tjc不受热7092.5115下降管水平均密度Pjkg/m3查表B1978.19963.86947.24下降管水速%m/sG/(3600fPj)0.54860.5750.613055680.58350.61020.566660.59380.6209下降管水粘度Pa?s查表C406."0 顼306.3尺10*243.5又 10下降管水雷诺数RejedP/E2.681区1052.81_ 5乂102.938_ 5X103.557_ 5乂103.727_ 5X103.898”054.474_ 5X104.689_ 5X10

15、4.903 乂 105沿程摩擦阻力系数A查图及公式170.01770.01770.01760.01740.01740.01730.01710.01710.017下降管总阻力系数为/d +轧2.8162.8162.812.7992.7992.7932.7812.7812.775下降管流动阻力PidjPa£g/2414.5455.4496.9418.2459.3501.2422.8464.4506.7下降管重位压降ApzwjPaPgh110355108738106863上升管出口水温It llCtj +Q1 /GCP89.9589.0488.21112.45111.54110.71134

16、.95134.04133.21nt;ctJ + QGCP132.6129.74127.13155.1152.24149.63177.6174.74172.13上升管平均水温Itlc(tj +t；)/279.8979.5279.11102.48102.02101.61124.98124.52124.11nt;c(tE)/2111.28109.39107.67133.78131.89130.17156.28154.39152.67上升管水平均密度IPlkg/m3查表B1972.21972.48972.73956.82957.16957.47939.16939.54939.88nP2kg/m3查表B

17、1950.19951.66952.94931.72933.37934.87911.14912.95914.6上升管平均水温tsc(ti +t2)/295.6394.4693.39118.13116.96115.89140.63139.46138.39上升管水平均密度Pskg/m3查表Bi961.66962.47963.23944.77945.69946.54925.78926.82927.74上升管水速缶sm/sG/(3600fPs)0.29310.30690.32070.29830.31230.32630.30440.31870.333上升管水粘度Pa?s查表C296.1M0'629

18、9.9M0'6303.4乂10-6236.3M0'6239M0'6241.4M0'6195.7M0'6197.5"0-6199.2乂10-6上升管雷诺数ResedP/E4.954区1045.1224 勺045.2944 乂1046.2024 又1046.4264 '1046.6534 又1047.4884 区1047.7774 乂1048.0654乂 104沿程阻力系数查图及公式170.025440.025370.02530.024940.024850.024760.024430.024310.0242上升管总阻力系数3以/d11.07

19、611.05111.02610.89810.86610.83510.71710.67510.636上升管流动阻力PldsPa£"/2457.5500.9546.2458.1501.1546459.7502.5547.1上升管重位压降IPzwlPa%hi318553186431872313513136231372307723078430796np zw1Pap2gh2760627618076282745847471674836729367308173213有效压头SyxPaAPzwj - ZAPzws - APlds1980.51810.11654.82344.92158.9

20、19842695.32495.52306.9侧墙回路水循环计算名称符号单位计算公式及来源计算结果回路循环流量Gkg/h假设700007600082000700007600082000700007600082000下降管入口水温tjc假设7092.5115下降管平均水温tjc不受热7092.5115下降管水平均密度Pjkg/m3查表B1978.19963.86947.24下降管水速与jm/ sG/(3600fPj)0.30720.33360.35990.31180.33850.36530.31730.34450.3717下降管水粘度PPa?s查表C406.410 顼306.310*243.5乂

21、10顼下降管水雷诺数Rej切dP/卜1.501_ 5乂 101.63_ 5X101.759乂 1051.992”052.162_ 5X102.334_ 5乂 102.506_ 5乂 102.72_ 5X102.935_ 5X10沿程摩擦阻力系数查图及公式170.018850.018740.018630.018420.018270.018120.017970.017790.0176下降管总阻力系数兀l / d + -jb2.9892.9822.9752.9612.9522.9432.9332.9222.91下降管流动阻力SdjPa，g/2138162.3188.5138.7163189.3139

22、.9164.2190.4下降管重位压降ApzwjPapgh111794110156108257上升管出口水温ts“Ctj +Q/GCP125120.64116.93147.5143.14139.43170165.64161.93上升管平均水温tsC(tj'+t；)/297.595.3293.47120117.82115.97142.5140.32138.47上升管水平均密度Pskg/m3查表B1960.38961.87963.17943.31945.02946.47924.04926.06927.67上升管水速钏m/ sG/(3600fPs)0.29770.32280.34780.30

23、310.32850.35390.30950.33520.3611上升管水粘度pPa?s查表C290K 10-6297.1K10-6303.2X10-6232.1X10-6237K10-6241.2乂 10-6193.1乂 10-6196.1乂10-6199.1乂 10-6上升管雷诺数RescodP/ P5.127X1045.434X1045.745X1046.406X1046.811X1047.221乂 1047.701乂 1048.231X1048.749X104沿程阻力系数查图及公式170.025350.025240.025140.02490.024770.024630.024460.02

24、4280.0241上升管总阻力系数”/d+%7.3497.3257.3047.2527.2247.1937.1577.1187.079上升管流动阻力PldsPa12312.8367.1425.5314.2368.3426.3316.7370.3428.1上升管重位压降PzwsPaPgh107497107664107810105587105778105940103430103656103836引出管平均水温tycts125120.64116.93147.5143.14139.43170165.64161.93引出管水平均密度Pykg/m3查表B1939.14942.77945.72919.469

25、23.45926.84897.59901.93905.65引出管水速m/ sG/(3600fPy)0.30490.32980.35470.31150.33670.36190.3190.34470.3704引出管水粘度Pa?s查表C222.6号0-6230.9号0-6239.1乂 10-6186乂 10-6192.2乂 10-6197.5乂10-6159.6乂 10-6164.3乂 10-6168.2x 10-6引出管水雷诺数ReycodP/ N1.8874乂 101.9794乂 102.0624乂 102.2644X 102.3784乂 102.4974乂 102.6374X 102.7824

26、乂 102.9324X 10沿程摩擦阻力系数查图及公式170.01920.019140.019080.018950.018870.018790.01870.01860.0185引出管总阻力系数EE” / d + -jb2.5482.5462.5442.5392.5362.5332.532.5272.523引出管流动阻力PldyPa芽2/2111.2130.5151.3113.3132.7153.7115.5135.4156.7引出管重位压降ApzwyPaPgh2211.12219.72226.62164.82174.22182.22113.32123.52132.3有效压头SyxPap zwj

27、 七 pzws 七 p zwy1661.91412.71180.61976.71702.81453.82281.51971.81703.9对流管束水循环计算名称符号单位计算公式及来源计算结果回路循环流量Gkg/h假设800000850000900000800000850000900000800000850000900000下降管入口水温tjc假设7092.5115下降管出口水温tjctj +Q/GCP76.5876.1975.8599.0898.6998.35121.58121.19120.85下降管平均水温tjc(tj +tj)/273.2973.172.9395.7995.695.4311

28、8.29118.1117.93下降管水平均密度Pjkg/m3查表1976.21976.32976.42961.55961.68961.8944.65944.8944.93下降管水速您m/sG/(3600fPj)0.24850.2640.27950.25230.2680.28380.25680.27280.2888下降管水粘度PPa?s查表C389.3乂10-6390.3乂10-6391.2区10-6295.6乂10-6296.2乂 10-6296.7乂 10-6236乂 10-6236.4次 10-6236.8乂 10-6下降管水雷诺数Rej切dP/ P2.7418X1042.9057X104

29、3.0695K1043.6111勺043.8285勺044.0479勺044.5228 尺1044.7972勺045.0707勺04沿程摩擦阻力系数%查图及公式170.0280.027860.027720.027250.027070.026880.026470.026240.026下降管总阻力系数，/d+'b6.908.6.8826.8556.7676.7336.6976.7196.5766.53下降管流动阻力PidjPaAfV/2208.2234.1261.4207.1232.5259.4206.2231.2257.3下降管重位压降ApzwjPa电h80444804538046179

30、2367924679256778437785577866上升管出口水温tsCt+Q/GCP101.7699.8998.23124.26122.39120.73146.76144.89143.23上升管平均水温tsC(tj'+t；)/289.1788.0487.04111.67110.54109.54134.17133.04132.04上升管水平均密度Pskg/m3查表B1966.17966.9967.56949.88950.77951.54931.38932.37933.24上升管水速钏m/sG/(3600fPs)0.16240.17770.18810.17030.18070.1912

31、0.17360.18430.195上升管水粘度pPa?s查表C290-6X10297.1-6X10303.2-6X10232.1-6 X10237-6乂 10241.2-6乂 10193.1-6乂 10196.1-6乂10199.1-6乂 10上升管雷诺数Res切 dP/E2.23934 X102.34564 K102.45424K102.83574勺02.98084勺03.1274X103.45024 X103.6354勺03.81844尺10沿程阻力系数查图及公式170.02890.028810.028670.028160.027970.027780.027360.027110.02687

32、上升管总阻力系数研 / d + %6.3846.3616.3386.2546.2226.1916.1226.0816.041上升管流动阻力pidsPaAfV/286.497.1108.586.196.6107.786.096.3107.2上升管重位压降pzwsPa%h796167967679731782747834778411767497683176903有效压头SyxPapzwj Apzws Aplds741.6679.9621.5875.9802.4737.31008927.7855.8六、绘制特性曲线确定循环工作点，得计算结果汇总表:名称符号单位前墙后墙侧墙对流管束下降管入口水温tjc1

33、01.57回路循环流量Gkg/h176072.5179864.9110572.91178603上升管出口水温t；C151.28145.08136.38123.13106.04上升管平均水温tsC126.43123.33118.98114.59103.81上升管平均密度Pskg/m3937.96940.53944.11947.56955.82上升管水速您sm/ s0.42320.43120.47840.25150.3739七、水阻力计算:序号名称符号单位公式及计算结果（一）省煤命郃分（假设切=0.3m/ s）1集箱内径djxm0.2032管子直径dnm0.063流通截面积f2 m.2 .,mdn /4 (n=30)0.08484循环水量Gkg/h假设900005入口水温t.C设计706出口水温t“Ct' + Q/GCP100.667平均水温tc(t*t")/285.338水的平均密度pkg/m3查表B1968.689水的平均动力粘度pPa?s查表C .-6333.13。1010平均水速om/ sG/(3600 fP)0.304311雷诺数RecodP/E5.3081 ”0412管内壁绝对粗糙度kmm查 4.4.10.2513沿程摩擦阻力系数z查图及公式170.030714管子长度lm34.215入口阻力系数tr查表 5 (X 1.2)0.