2023年实验报告气汽对流传热综合实验.docx

气一汽对流传热综合实验1 .光滑套管换热器传热系数的测定数据记录与整理表传热管内径di =0.02 0 m有效长度Li=1.00m冷流体：空气（管内）热流体：蒸汽（管外）数据项目12345孔板压差PkPa0.2 71.051 .852. 5 83.41空气入口温度t.3 1.83 5.33 7.63 9.74 2.2空气出口温度t2C7 5.26 9.868.969.57 0 .9壁面温度Tw9 9.99 9.91 00.099.9100 . 0管内平均温度tm5 3.552.65 3.85 4.656.6空气密度Pmk g/ n?1.0811 .08 51.0801. 0781 .07 1空气导热系数朦*100W/m-2.8512.8 4 42. 8 532. 8582 . 872空气定压比热容C pmkJ / k g-1.0051.0 0 51 .0051. 0051. 005空气粘度gm* 1 0 0 000P a-s1.981.971.9 81.981 .99空气进出口温度差At43.434.531. 329.828.7平均温差 t m4 6 .44 7. 346.245.343. 420时空气流量V20m3/ h11. 79323.2 5 630. 8703 6.4554 1.9 11管内平均流量Vm3/h12.8 8 425.19433.44239. 45645.456平均流速um / s11.392 2.2729. 5734.8840.19传热量QW168.742 6 3. 27315 . 593 53.84390 .06对流传热系数«iW/m2-57 . 8788. 571 08.70124.30143.02雷诺数Re12436245 3 13225837 9 8 043 2 60努赛尔准数Nu4 0. 6 062.2976.2086.9 89 9.60Nu / P r0- 44 6.87971.0 078 8.03 6100. 54 9115.1372 .强化套管换热器传热系数及强化比的测定数据记录与整理表传热管内径di =0.020 m 有效长度Li= 1 .00 m冷流体：空气（管内）热流体：蒸汽（管外）数据项目12345孔板压差APkPa0 .15().6 71.151.7()2 . 23空气入口温度ti29.030. 130.93 1 .63 2. 2空气出口温度t2C9 0.785.18 2.681.98 2.4壁面温度Tw9 9.69 9.799.899.999.9管内平均温度tin59. 957.656. 856.85 7.3空气密度Pmkg/ m31 .0601.0681 .0 711 .0711. 069空气导热系数Xm*100W/m.2. 89 52.8792 . 87 42 .8 742.877空气定压比热容CpmkJ/kg-1 .0051. 0 051.0051 . 0051.005空气粘度pm*l 0 000Pas2.012.001. 991.9 92.00空气进出口温度差At6 1.755 . 05 1 .75 0.35 0. 2平均温差tm39.742.143. 043.142.620C时空气流量v20m3/ h8.7918.5824.342 9.593 3.89管内平均流量Vm3 / h9. 8372 0 .61 32 6.90232.6663 7.432平均流速um/s8 . 7 01 8.2 223. 7828.8 833. 09传热量QW1 79.6033 8.0 2392.16491.275 60.77对流传热系数GiW/m2-7 1 .991 27.77145.13181. 3920 9 .48雷诺数Re91761945825596310863 5373努赛尔准数Nu49. 738 8.761 0 1.01 26.23145.62Nu/P r 045 7.421 0 2.49116.761 45 . 921 68. 14Nuo3 1.9854. 3 766.047 5 .7382.98强化比Nu / Nuo1.561 . 631.531.671.7 53 .线性回归拟定准数关联式_ < R/n由N” = A Rem P”4可得PrQA -由线性拟合结果可求得:光滑套管换热器A= 0 .0581 m=0.7074强化套管换热器A= 0. 0 496 m =0,771