锅炉汽水阻力计算书-手算版

,,,汽水阻力计算书,,技术文件号:,,

,,,,,共5页第2页,,

序号,名称,符号,单位,公式,数值,备注,

一,设计数据,,,,,,

1,总给水量,G,kg/h,,10000,100000,

2,额定压力,P,Mpa,表压,3.82,3.82,

3,给水温度,tgs,℃,,104,104,

4,进口水密度,ρ,Kg/m3,1008.6263+(-0.2811*t)+(-0.0021921)t2,800.0,955.6821464,

5,负荷变量系数,m,,,1.0,1,

6,实际给水量,Gs,kg/h,m*G,10000,100000,

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二,高温过热器阻力,,,,,,

7,高过出口集箱规格,DxS,mm,设计取定,273x16,273X16,

8,高过出口集箱内径,dn1,m,,0.241,0.241,

9,过热蒸汽流量,Ggg,kg/h,,10000,100000,

10,出口蒸汽温度,tck,℃,查热力计算知,450,450,

11,进口蒸汽温度,tjk,℃,查热力计算知,330.0,330,

12,平均蒸汽温度,tpj,℃,,390.0,390,

13,出口蒸汽压力,"P""",MPa,前面计算,3.82,3.82,

14,进口蒸汽压力,P',MPa,"先假定,后校核",3.96,3.96,

15,平均蒸汽压力,Pcp,Mpa,"(P′+P"")/2",3.89,3.89,

16,平均蒸汽比容,Vcp,m3/kg,"查《水蒸汽性质表》按3.99MPa,t=390℃",0.072,0.0722,

17,蒸汽平均密度,ρpj,kg/m3,1/Vcp,13.850,13.85041551,

18,管子横向排数,Z1,,几何尺寸,100,100,

19,管圈数,n,,,1.0,,

20,管子内径,dn,m,取用φ38x3.5,0.031,0.031,

21,管子流通截面积,fZ,m2,Z1*π*dn^2/4,0.075,0.0754385,

22,蒸汽平均流速,WS,m/s,Ggg/(ρpj*fz*3600),2.657,26.58530532,

23,集箱进入管子的入口阻力系数,ζjxr,,查标准表2-4,0.8,0.8,

24,管子的绝对粗糙度,k,mm,按2-21条选定,0.060,0.06,

25,折算摩擦阻力系数,λ0,1/m,1/［4*dn(lg(3700*dn/k)^2］,0.749,0.748956763,

26,此路蒸汽流经管长,L,m,查图纸(取平均数),31.174,31.174,23.34797812

27,管子弯头角度,,,查图纸9个180°弯头2个90°（取内管圈）,,9个180°，2个90°,

28,弯头阻力系数之和,ζwt,,按R/din=4.194(2.42)查表2-9、2-100.3+8x0.193x2+2x0.137x2,3.164,3.164,

29,管子进入集箱的出口阻力系数,ζjxc,,查标准表2-5,1.1,1.1,

30,过热器的阻力系数,ζgg,,ζjxr+ζwt+ζjxc+L*λ0,28.412,28.41197812,

31,过热器流动阻力,Pld3,MPa,ζgg*ωs^2*ρpj/2,0.001,0.14,

32,高温过热器进口压力,P',MPa,"p""+Pld3",3.821,3.96,

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三,喷水式减温器阻力,,,,,,

33,喷水式减温器阻力,Pld4,MPa,按《蒸汽锅炉减温器》第105页,0.05,0.05,蒸汽经过减温器的压力损失小，一般为0.5公斤/cm2

34,低温过热器出口蒸汽压力,"P""",MPa,,3.871,4.01,

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四,低温过热器阻力,,,,,,

35,低过出口集箱内径,dn1,m,取用φ273x16,0.241,0.241,

36,过热蒸汽流量,Gdg,kg/h,,5000,95000,

37,出口蒸汽温度,tck,℃,查热力计算知,386.6,386.6,

38,进口蒸汽温度,tjk,℃,查热力计算知,254.7,254.7,

39,平均蒸汽温度,tpj,℃,(tck+tjk)/2,320.7,320.65,

40,出口蒸汽压力,"P""",MPa,由上知,3.871,4.01,

41,进口蒸汽压力,P',MPa,"先假定,后校核",4.180,4.175,

42,平均蒸汽压力,Pcp,Mpa,"(P′+P"")/2",4.026,4.092032459,

43,平均蒸汽比容,Vcp,m3/kg,"查《水蒸汽性质表》按4.104MPa,t=320.7℃",0.0603,0.05891,

44,蒸汽平均密度,ρpj,kg/m3,1/Vcp,16.584,16.97504668,

45,管子横向排数,Z1,,设计取定,101,101,

46,管圈数,n,,,1.0,,

47,管子内径,dn,m,取用φ38x3.5,0.031,0.031,

48,管子流通截面积,fZ,m2,Z1*π*dn^2/4,0.076,0.076192885,

49,蒸汽平均流速,WS,m/s,Gdg/(ρpj*fz*3600),1.099,20.4030789,

50,管子的绝对粗糙度,k,mm,按2-21条选定,0.060,0.06,

51,折算摩擦阻力系数,λ0,,1/［4*dn(lg(3700*dn/k)^2］,0.749,0.748956763,

52,此路蒸汽流经管长,L4,m,查图纸（取平均值）,49.295,49.295,36.91982362

53,管子弯头角度,,,查图纸21个180°弯头90°、60°弯头各一个,,21个180°，1个90°，一个60°,

54,弯头的局部阻力系数,ζwt,,按R/din=4.194(2.42)查表2-9、2-10与2-1110x0.3+11x0.193x2+0.137x2+0.112x2,7.744,7.744,

55,集箱进入管子的入口阻力系数,ζjxr,,查标准表2-4,0.8,0.8,

56,管子进入集箱的出口阻力系数,ζjxc,,查标准表2-5,1.1,1.1,

57,低温过热器的阻力系数,ζdg,,ζjxr+ζwt+ζjxc+L4*λ0,46.564,46.56382362,

58,低温过热器流动阻力,Pld5,MPa,ζdg*ωs^2*ρpj/2,0.00,0.164520884,

59,低过进口蒸汽压力,P',MPa,"p""+Plds",3.872,4.17,

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五,饱和蒸汽引出管阻力,,,,,,

60,低温过热器进口集箱,DxS,mm,设计取定,219x16,219*16,

61,集箱内径,dn,m,设计取定,0.187,0.187,

62,引出管规格,dxS,mm,设计取定,133x6,133*6,

63,引出管长度,L,m,设计取定,5.6,5.6,

64,饱和蒸汽温度,t,℃,查热力计算知,255,255,

65,出口蒸汽压力,"P""",MPa,由上知,3.872,4.17,

66,进口蒸汽压力,P',MPa,"先假定,后校核",4.20,4.2,

67,平均蒸汽压力,Pcp,Mpa,"(P′+P"")/2",4.036,4.186792901,

68,平均蒸汽比容,Vcp,m3/kg,"查《水蒸汽性质表》按4.3MPa,t=255℃",0.0462,0.0464,

69,蒸汽平均密度,ρpj,kg/m3,1/Vcp,21.645,21.55172414,

70,管子根数,n,,,6,6,

71,管子内径,dn,m,取用φ133x6,0.121,0.121,

72,管子流通截面积,fZ,m2,n*π*dn2/4,0.069,0.06895911,

73,蒸汽平均流速,WS,m/s,Gdg/ρpj*fz*3600,1.860,17.75609407,

74,管子的粗糙度,k,mm,按2-21条选定,0.06,0.06,

75,折算摩擦阻力系数,λ0,,1/［4*dn(lg(3700*dn/k)^2］,0.138,0.137751539,0.771408619

76,连接管弯头总局部阻力系数,ζwt,,R/dn=400/121=3.3062个90°弯头查表2-9与2-102x0.141=0.282,0.282,0.282,

77,连接管到锅筒出口阻力系数,ζc,,表2-5,1.0,1,

78,连接管入口阻力系数,ζr,,表2-4,0.7,0.7,

79,连接管入口集箱阻力系数,ζjx,,0.7n2(dn/djx)4=0.7x100x(99/187)4,4.417,4.417490212,主蒸汽引出管和过热蒸汽引出管都有5中阻力系数

80,总阻力系数,∑ζdg,,ζjx+ζwt+ζc+ζr+L*λ0,7.171,7.170898831,

81,阻力损失,△P,MPa,∑ζdg*Ws2*ρpj/2,0.000,0.024362424,

82,连接管进口压力,P',MPa,"p""+△P",3.872,4.20,

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六,锅筒出口到高温过热器出口集箱的阻力损失,,,,,,

83,总阻力损失,△P,MPa,p′-p″,0.052,0.38,

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七,省煤器引出管及锅筒进水管阻力,,,,,,

84,水流量,Gs2,kg/h,额定给水量+1%的排污量-5%的喷水量,10000,96000,

85,省煤器出口集箱规格,dxs,mm,设计取定,219x16,219*16,

86,进水管规格,dxs,mm,设计取定,89x4.5,89*4.5,

87,进水管内径,dn,m,设计取定,0.050,0.08,

88,进水管数量,n,根,设计取定,1,4,

89,进水管计算长度,L,m,设计取定,700.0,19,

90,介质温度,t',℃,查热力计算知,40.0,244.8,

91,介质出口水压力,P',MPa,前面计算,1.000,4.20,

92,介质进口水压力,"P""",MPa,"先假定,后校核",2.000,4.22,

93,平均介质压力,Pcp,Mpa,"(P′+P"")/2",1.500,4.208974113,

94,平均介质比容,Vcp,m3/kg,"查《水蒸汽性质表》按4.311MPa,t=244.8℃",0.00125,0.00124,

95,管子的绝对粗糙度,k,mm,按2-21条选定,0.060,0.06,

96,进水管摩擦阻力系数,λy,1/m,查线算图2-8,0.23,0.23,

97,进水管介质流通面积,fy,m2,n*π*dn^2/4,0.002,0.020096,

98,排污量,Dpw,kg/h,热力计算1%D,0,1000,

99,锅炉进水管介质流速,Wy,m/s,(D+Dpw)xVcp/(3600xfy),1.768,1.662575195,

100,进水管进口局部阻力系数,ζyr,,表2-4,0.7,0.7,

101,进水管弯头局部阻力系数,ζwt,,R/dn=300/80=3.754个90°弯头按表2-114x0.2=0.8,0.800,0.8,

102,进水管出口局部阻力系数,ζjc,,表2-5,1.0,1,

103,进水管总阻力系数,∑ζ1,,ζjc+ζwt+ζyr+L*λy,163.500,6.87,

104,进水管阻力损失,△P1,MPa,∑ζ1*Wy2/(2*Vcp),0.205,0.007657159,

105,总损失,△P,MPa,△P1+△P2,0.205,0.007657159,

106,省煤器引出管进口压力,"P""",MPa,P'+△P,1.205,4.21,

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八,省煤器阻力,,,,,,

107,省煤器集箱规格,DxS,mm,设计取定,219x16,219*16,

108,蛇形管规格,dxs,mm,设计取定,32x3,32*3,

109,蛇形管内径,dn,m,设计取定,0.026,0.026,

110,蛇形管根数,n,,设计取定,1,74,

111,介质流通截面积,fn,m2,nxπdn2/4,0.0005,0.03926884,

112,进口介质温度,t',℃,查热力计算知,40.0,104,

113,出口介质温度,"t""",℃,查热力计算知,40.0,244.8,

114,平均介质温度,tcp,℃,"(t'+t"")/2",40.0,174.4,

115,管子的绝对粗糙度,k,mm,按2-21条选定,0.060,0.06,

116,折算摩擦阻力系数,λ0,,1/［4*dn(lg(3700*dn/k)^2］,1.036,0.93606097,

117,蛇形管长度,L,m,结构特性,600.0,169,

118,介质出口水压力,P',MPa,前面计算,1.205,4.21,

119,介质进口水压力,"P""",MPa,"先假定,后校核",4.300,4.3,

120,平均介质压力,Pcp,Mpa,"(P′+P"")/2",2.752,4.252802692,

121,平均介质比容,Vcp,m3/kg,"查《水蒸汽性质表》按4.355MPa,t=174.4℃",0.00112,0.00112,

122,排污量,Dpw,kg/h,热力计算1%D,100,1000,

123,介质流速,Ws,m/s,(D+Dpw)xVcp/(3600xfn),5.860,0.768491704,

124,蛇形管进口阻力系数,ζr,,表2-4,0.80,0.8,

125,中间集箱蛇形管进口阻力系数,ζz,,表2-4、2-5ζr+ζc,3.6,3.6,

126,蛇形管弯头阻力系数,ζwt,,"R/dn=60/26=2.308表2-9表2-104个90°弯头,2个60°弯头,29个180°弯头4x0.141x2+2x0.114x2+29x0.198x2",13.068,13.068,

127,省煤器总阻力系数,∑ζ,,ζwt+ζc+ζr+ζz+L*λ0,639.324,175.6623039,

128,省煤器总阻力损失,△P,MPa,∑ζ*Ws2/(2*Vcp),9.8001,0.046313641,

129,省煤器进口集箱压力,Pv,MPa,P'+△P,11.005,4.25,

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九,重位压差（锅筒至省煤器