Dobe Tubo Exel

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Tabla y ResultadosTabulacin de Datos y Resultados ExperimentalesTabla N 1: Condiciones de LaboratorioTemperatura (C)21Densidad (Kg/L)0.99802Tabla N 2: Especificaciones del Intercambiador de calorLongitud (m)2.88Dimetro nominal(pulg)(m)Externo 2pulgD12.070.525Interno 1 pulgdi1.380.035do1.660.042Area Total (m2)0.381Tabla N 3: Temperaturas experimentales de los fluidos a una presin de 9psicaudal (LPM)Fluido CalienteFluido FroLiq. - Vap.Temperatura entrada T1Temperatura salida T2Temperatura entrada t1Temperatura salida t2Temperatura C C C C C67.5108.0102.021.030.089.049108.0104.021.032.094.030108.0105.021.036.097.015108.0107.021.044.097.0Tabla N 4: Datos obtenidos para el clculo de los flujos masicos a una presin de 9psiBaldeAmarilloBlancoverdeazulPeso0.580.9630.6780.52Flujo calienteFlujo friCorridaCaudal (LPM)w (Kg)t (s)w (Kg)t (s)mc (Kg/h) (rotametro)167.58.860300.00011.878.444041.986.905300.76012.3049.697.290300.5008.2185.922497.350360.1007.7507.912934.186.530300.0207.9357.755.930300.50012.2413.023305.935300.2807.4313.3101796.445.175300.0107.613.0506.110300.00011.69515.0604155.000360.0005.50519.560898.224.690300.0104.68215.7604.610300.1007.36626.42Tabla N 4A: Datos obtenidos para el clculo de los flujos masicos a una presin de 9psiFlujo calienteFlujo friCorridaCaudal (LPM)w (Kg)t (s)w (Kg)t (s)mc (Kg/h) (rotametro)Flujo de CondensadoFlujo Cond promedioFlujo FrioFlujo Frio promedio167.58.340300.00011.1928.444041.98100.0804773.8396.325300.76011.6269.6975.70885.6314319.2574501.6406.770300.5007.2555.9281.1054411.8242496.770360.1007.0727.912934.1867.6813218.6096.010300.0206.9727.7572.11567.9633238.6063191.7605.350300.50011.27713.0264.0933118.0653304.972300.2806.9113.3101796.4459.6081868.9714.497300.0107.0213.05053.96258.4451936.5522123.6475.147300.00010.73215.06061.7642565.4184304.420360.0504.98519.5601796.4444.194917.4853.727300.0104.00415.76044.72345.753914.619914.4714.030300.1006.68826.4248.344911.310Tabla N 5: Valores calculados de flujo masicoCaudalFlujo prom. condensado (Kg/h)Flujo de vapor sat. (Kg/h)Flujo de liquido sat. (Kg/h)Flujo de agua (Frio) (Kg/h)Flujo de agua (Kg/h) (rotametro)67.585.63185.964501.644041.984967.96368.483191.762934.183058.44559.002123.651796.441545.75346.36914.471796.44Tabla N 6: Calores ganados y perdidos por los flujos masicosCaudalQc (KJ/h)Qh (KJ/h)Qp (KJ/h)67.5151910194610427004913477515440019625301125101327512024115172482103884-68598Tabla N 7: Calculo de los coeficientes de pelcula para el tubo interno del intercambiadorCaudalVelocidad de masa (Kg/m2-h)ReynoldsN Prhi(KJ/h m2 K)hio(KJ/h m2 K)67.541834164.64E+046.0017426145224930368503.43E+045.8713672113933018592962.19E+045.62948079001518592962.39E+045.1298488207Tabla N 8: Coeficientes de Pelcula para superficie externa del tubo interno del intercambiadorCaudalho(KJ/h m2 K)Th (C)Tw (C)67.5453210244.4149466810449.1730461110557.2515465510759.65Tabla N 9: Coeficientes globales de transferencia de calor y factor de incrustamientoCaudalMLTD (C)UD (KJ/h m2 K)UC (KJ/h m2 K)RD (h m2 K/ KJ)67.579.49112934545.96E-044979.45100233116.96E-043077.8584029118.47E-041574.46130129704.32E-04Tabla N 10: ResumenCaudalUD (KJ/h m2 K)UC (KJ/h m2 K)RD (h m2 K/ KJ)67.5112934545.96E-0449100233116.96E-043084029118.47E-0415130129704.32E-04Tabla N 11: Tiempo vs. Peso de chorroTiempo por chorro9.071Corrida 1Corrida 2Corrida 3ChorroPesoTiempoPesoTiempoPesoTiempo00.0000.0000.0000.0000.0000.00010.6319.0710.5329.0710.5769.07110.63151.4360.53242.8590.57642.87121.26360.5071.06551.9301.15151.94221.263102.8711.06585.7171.15185.74331.894111.9421.59794.7881.72794.81431.894154.3071.597128.5761.727128.61442.526163.3782.130137.6472.303137.68542.526205.7432.130171.4342.303171.48653.157214.8142.662180.5052.879180.55753.157257.1792.662214.2932.879214.35763.789266.2503.195223.3643.454223.42863.789308.6143.195257.1513.454257.22974.420317.6853.727266.2224.030266.30074.420360.0503.727300.0104.030300.100

Calculos AuxiliaresCalculos AuxiliaresUso de tablas de los diversos librosTabla A : Flujos masicos del liquido saturado a la salida de la Trampa de VaporCorridaCaudal (LPM)m (Kg/h)167.585.63101085.63101024967.96319067.96319033058.44485658.44485643045.75341945.75341945.753419Tabla B : Calculo del Flujo masico a la entrada de la Trampa de VaporCaudalm2 (Kg/h)H1H2H3m1 (Kg/h)m3 (Kg/h)67.585.63427.61419.062675.6085.960.3349.067.96436.06419.062675.6068.480.5230.058.44440.28419.062675.6059.000.5530.045.75448.74419.062675.6046.360.61Tabla C : Datos para interpolarADB(B-A)*(F-D)/(C-A)+DCFCaudalT(C)H1(kJ/Kg)T(C)H2(kJ/Kg)T(C)H3(kJ/Kg)102427.61100419.061002675.6067.5102427.61100419.061002675.60102427.61100419.061002675.60104436.06100419.061002675.6049104436.06100419.061002675.60104436.06100419.061002675.60105440.28100419.061002675.6030105440.28100419.061002675.60105440.28100419.061002675.60107448.74100419.061002675.6030107448.74100419.061002675.60107448.74100419.061002675.60Tabla D : Para el calculo del QCCaudalTm (C)C (KJ/Kg K)(t2 - t1) (K)Qc (KJ/h)67.525.504.189.01519104926.504.1811.01347753028.504.1815.01125101532.504.1723.0172482Tabla E : Interpolacin para la capacidad calorficaCaudalT(C)C (KJ/Kg K)25.004.176067.525.504.175930.004.175025.004.17604926.504.175730.004.175025.004.17603028.504.175330.004.175025.004.17601532.504.174530.004.1750Tabla F : Calculo del QhCaudalQh (KJ/h)Q latente (KJ/h)Q sensible (KJ/h)Q latente (KJ/Kg)C (KJ/Kg K)(T1 - T2)Tm (C)67.519461019355310582251.742.056.00105.00491544001538375632246.492.054.00106.00301327511323873642243.862.063.00106.5015103884103789962238.612.061.00107.50Tabla G : Interpolacin para el calor latente y la capacidad calorficaCaudalT(C)Q latente (KJ/Kg)T(C)C (KJ/Kg K)100.002257100.002.02967.5102.002252105.002.051106.852239111.852.080100.002257100.002.02949104.002246106.002.055106.852239111.852.080100.002257100.002.02930105.002244106.502.057106.852239111.852.080100.002257100.002.02915107.002239107.502.061106.852239111.852.080Tabla H : apap (m2)9.66E-04Tabla I : Calculo del ReCaudalGp (Kg/m2 - h)Densidad (Kg/m3)di (m)Velocidad (m/h)Viscosidad (Kg/m - h)Re67.541834169983.51E-0241913.164.64E+044930368509973.51E-0230453.103.43E+043018592969963.51E-0218672.982.19E+041518592969933.51E-0218732.732.39E+04Tabla J : calculo de la Densidad y la Viscosidad a TmCaudalT(C)Densidad (Kg/m3)T(C)Viscosidad (Kg/m - h)26.8599726.853.0867.525.5099825.503.1631.8599331.852.7726.8599726.853.084926.5099726.503.1031.8599331.852.7726.8599726.853.083028.5099628.502.9831.8599331.852.7726.8599726.853.081532.5099332.502.7331.8599331.852.77Tabla K : calculo del PrCaudalT(C)Pr26.855.8367.525.506.0031.855.2026.855.834926.505.8731.855.2026.855.833028.505.6231.855.2026.855.831532.505.1231.855.20Tabla L : Para el calculo del hiCaudalTm (C)Viscosidad (Kg/m - h)K (KJ/m h K)hi.uw^0.14hio.uw^0.1467.525.503.162.2018842157024926.503.102.2114704122533028.502.982.221009984161532.502.732.24104608717Tabla LL : calculo del KCaudalT(C)K26.852.212025.502.2031.852.2326.852.213026.502.2131.852.2326.852.214528.502.2231.852.2326.852.216532.502.2431.852.23Tabla MCaudalTh (C)tc (C)Tw (C)Tf (C)AT (C)Tc (C)67.510225.5063.7582.8838.25105.004910426.5065.2584.6338.75106.003010528.5066.7585.8838.25106.501510732.5069.7588.3837.25107.50Tabla N : caudal 20 LPMIteraciones1234Twi (C)63.7544.4844.4144.41Tf (C)82.8873.2473.2173.20T (K)38.2538.2538.2538.25K (KJ/h m K)2.422.402.402.40 (Kg /h m)1.221.351.351.35 (Kg/ m3)970977977977 ( KJ/Kg)2252225222522252ho(KJ/h m2 K)4660453345324532w (Kg /h m)1.481.751.751.75hi(KJ/h m2 K)17832174281742617426hio(KJ/h m2 K)14860145231452214522Twi+1 (C)44.4844.4144.4144.41Tabla Tf (C)T(C)K (KJ/h m K)T(C) (Kg /h m)T(C) (Kg/ m3)T(C)w (Kg /h m)81.852.4281.851.2381.8597181.851.2382.8882.882.4282.881.2282.8897063.751.4886.852.4386.851.1786.8596786.851.1781.852.4281.851.2381.8597181.851.2373.2473.242.4073.241.3573.2497744.481.7586.852.4386.851.1786.8596786.851.1781.852.4281.851.2381.8597181.851.2373.2173.212.4073.211.3573.2197744.411.7586.852.4386.851.1786.8596786.851.17Tabla O : caudal 30 LPMIteraciones1234Twi (C)65.2549.2949.1749.17Tf (C)84.6375.6475.5975.59T (K)38.7538.7538.7538.75K (KJ/h m K)2.422.402.402.40 (Kg /h m)1.201.321.321.32 (Kg/ m3)969976976976 ( KJ/Kg)2246224622462246ho(KJ/h m2 K)4668454645464546w (Kg /h m)1.461.681.681.68hi(KJ/h m2 K)13943136731367213672hio(KJ/h m2 K)11619113951139311393Twi+1 (C)49.2949.1749.1749.17Tabla PTf (C)T(C)K (KJ/h m K)T(C) (Kg /h m)T(C) (Kg/ m3)T(C)w (Kg /h m)81.852.4281.851.2381.8597181.851.2384.6384.632.4284.631.2084.6396965.251.4686.852.4386.851.1786.8596786.851.1781.852.4281.851.2381.8597181.851.2375.6475.642.4075.641.3275.6497649.291.6886.852.4386.851.1786.8596786.851.1781.852.4281.851.2381.8597181.851.2375.5975.592.4075.591.3275.5997649.171.6886.852.4386.851.1786.8596786.851.17Tabla Q : caudal 45 LPMIteraciones1234Twi (C)66.7557.3857.2557.25Tf (C)85.8879.6979.6279.62T (K)38.2538.2538.2538.25K (KJ/h m K)2.422.412.412.41 (Kg /h m)1.181.261.271.27 (Kg/ m3)968972973973 ( KJ/Kg)2244224422442244ho(KJ/h m2 K)4700461146114611w (Kg /h m)1.441.571.571.57hi(KJ/h m2 K)9595948294809480hio(KJ/h m2 K)7996790179007900Twi+1 (C)57.3857.2557.2557.25Tabla RTf (C)T(C)K (KJ/h m K)T(C) (Kg /h m)T(C) (Kg/ m3)T(C)w (Kg /h m)81.852.4281.851.2381.8597181.851.2385.8885.882.4285.881.1885.8896866.751.4486.852.4386.851.1786.8596786.851.1781.852.4281.851.2381.8597181.851.2379.6979.692.4179.691.2679.6997257.381.5786.852.4386.851.1786.8596786.851.1781.852.4281.851.2381.8597181.851.2379.6279.622.4179.621.2779.6297357.251.5786.852.4386.851.1786.8596786.851.17Tabla S : caudal 65 LPMIteraciones1234Twi (C)69.7559.8359.6559.65Tf (C)88.3880.9180.8280.82T (K)37.2537.2537.2537.25K (KJ/h m K)2.432.412.412.41 (Kg /h m)1.151.251.251.25 (Kg/ m3)966972972972 ( KJ/Kg)2239223922392239ho(KJ/h m2 K)4767465746554655w (Kg /h m)1.401.541.541.54hi(KJ/h m2 K)9978985098489848hio(KJ/h m2 K)8315820882078207Twi+1 (C)59.8359.6559.6559.65Tabla TTf (C)T(C)K (KJ/h m K)T(C) (Kg /h m)T(C) (Kg/ m3)T(C)w (Kg /h m)81.852.4281.851.2381.8597181.851.2388.3888.382.4388.381.1588.3896669.751.4086.852.4386.851.1786.8596786.851.1781.852.4281.851.2381.8597181.851.2380.9180.912.4180.911.2580.9197259.831.5486.852.4386.851.1786.8596786.851.1781.852.4281.851.2381.8597181.851.2380.8280.822.4180.821.2580.8297259.651.5486.852.4386.851.1786.8596786.851.17

Grfico10000.63142857140.53242857140.57571428570.63142857140.53242857140.57571428571.26285714291.06485714291.15142857141.26285714291.06485714291.15142857141.89428571431.59728571431.72714285711.89428571431.59728571431.72714285712.52571428572.12971428572.30285714292.52571428572.12971428572.30285714293.15714285712.66214285712.87857142863.15714285712.66214285712.87857142863.78857142863.19457142863.45428571433.78857142863.19457142863.45428571434.423.7274.034.423.7274.03

Corrida 1Corrida 2Corrida 3Tiempo (s)Peso (Kg)Grafica 1 : Tiempo vs. Peso por chorro

Grfico20.57985714290.5798571429000.57985714290.5798571429000.57985714290.5798571429000.57985714290.5798571429000.57985714290.5798571429000.57985714290.5798571429000.57985714290.57985714290

PesoTiempo (s)Peso (Kg)Grafica 1 : Peso vs Tiempo

Para graficaTiempo por chorro9.071PesoTiempo4.059320.037Corrida 1Corrida 2Corrida 3PromedioChorroPesoTiempoPesoTiempoPesoTiempoPesoTiempo00.0000.0000.0000.0000.0000.0000.0000.00010.6319.0710.5329.0710.5769.0710.5809.07110.63151.4360.53242.8590.57642.8710.58045.72021.26360.5071.06551.9301.15151.9421.16054.79121.263102.8711.06585.7171.15185.7431.16091.43931.894111.9421.59794.7881.72794.8141.740100.51031.894154.3071.597128.5761.727128.6141.740137.15942.526163.3782.130137.6472.303137.6852.319146.23042.526205.7432.130171.4342.303171.4862.319182.87853.157214.8142.662180.5052.879180.5572.899191.94953.157257.1792.662214.2932.879214.3572.899228.59863.789266.2503.195223.3643.454223.4283.479237.66963.789308.6143.195257.1513.454257.2293.479274.31774.420317.6853.727266.2224.030266.3004.059283.38874.420360.0503.727300.0104.030300.1004.059320.037Tiempo por chorro9.071Corrida 1Corrida 2Corrida 3ChorroPesoTiempoPesoTiempoPesoTiempo00.0000.0000.0000.0000.0000.00010.6319.0710.5329.0710.5769.07110.63151.4360.53242.8590.57642.87121.26360.5071.06551.9301.15151.94221.263102.8711.06585.7171.15185.74331.894111.9421.59794.7881.72794.81431.894154.3071.597128.5761.727128.61442.526163.3782.130137.6472.303137.68542.526205.7432.130171.4342.303171.48653.157214.8142.662180.5052.879180.55753.157257.1792.662214.2932.879214.35763.789266.2503.195223.3643.454223.42863.789308.6143.195257.1513.454257.22974.420317.6853.727266.2224.030266.30074.420360.0503.727300.0104.030300.100Datos de Grfica 1PromedioEspaciosPesoTiempo00.5800.00010.58024.61810.00024.61820.00049.23620.58049.23630.58073.85530.00073.85540.00098.47340.58098.47350.580123.09150.000123.09160.000147.70960.580147.70970.580172.32770.000172.32780.000196.94680.580196.94690.580221.56490.000221.564100.000246.182100.580246.182110.580270.800110.000270.800120.000295.418120.580295.418130.580320.037130.000320.037

Hoja1DOBLE TUBOTABLA DE DATOS Y RESULTADOSTABLA N1Condiciones de LaboratorioT ambiente (C)18.1TABLA N2(A) Temperatura experimentales de los fluidos a 4psi y 30 LPMFLUIDO FRIOFLUIDO CALIENTET entrada de agua (T1)Tsalida de agua(T3)T entrada de vapor (T2)T salida de vapor (T4)CFCFCFCF2373.43493.2106222.8102215.62373.43493.2106222.8102215.62373.43493.2106222.8102215.6TABLA N3(B) Temperatura experimentales de los fluidos a 4psi y 60 LPMFLUIDO FRIOFLUIDO CALIENTET entrada de agua (T1)Tsalida de agua(T3)T entrada de vapor (T2)T salida de vapor (T4)CFCFCFCF2373.42984.2106222.8102215.62373.42984.2106222.8101213.82373.42984.2106222.8101213.8TABLA N4(C) Temperatura experimentales de los fluidos a 8psi y 30 LPMFLUIDO FRIOFLUIDO CALIENTET entrada de agua (T1)Tsalida de agua(T3)T entrada de vapor (T2)T salida de vapor (T4)CFCFCFCF2373.43595112233.6108226.42373.43595112233.6109228.22373.43595112233.6109228.2TABLA N5Calculos de los flujos masicos del condensadoobtenidos del balance de la Trampa de vapor (A)LPMFlujo frioFlujo calienteCondensado(lb/h)(lb/h)(lb/h)303958.64123.55124.01303958.64130.89131.38303958.64125.13125.60TABLA N6Calculos de los flujos masicos del condensadoobtenidos del balance de la Trampa de vapor (B)LPMFlujo frioFlujo calienteCondensado(lb/h)(lb/h)(lb/h)607917.27147.16147.71607917.27130.62130.87607917.27138.96139.22TABLA N7Calculos de los flujos masicos del condensadoobtenidos del balance de la Trampa de vapor (C)LPMFlujo frioFlujo calienteCondensado(lb/h)(lb/h)(lb/h)303958.64124.60126.50303958.64121.63123.71303958.64128.37130.57

Hoja2Tabla de vapor saturado(KERN)EntalpiaEntalpiaEntalpiaEntalpiaTemperaturaliq satvap satPresionliq satvap sat(F)(Btu/lb)(Btu/lb)(psia)(Btu/lb)(Btu/lb)212180.071150.414.696180.071150.4220188.131153.415181.111150.8230198.23115720196.161156.3240208.34116025208.421160.630218.821164.1Calculo de flujos calorificosDensidad del agua (23C)0.99757Calculos de los flujos masicos del condensado obtenidosCorriente de liquidaCorriente de vaporCorriente de vapordel balance de la Trampa de vapor (A)Cp(BTU/lb*F):1Cp(BTU/lb*F):0.45(BTU/lb)969.6LPMFlujo frioPeso aguaFlujo calienteEntalpiaEntalpiaEntalpiaCondensado Temp. FriaQ ganado Temp. FriaQ sensibleQ latenteQ cedidoQ perdidomfcalientemcLiq satVap sat(T3-T1)* fluido frio(T2-T4)*fluido calient*fluido calient*fluido calienthacia el amb(lb/h)(Kg)(lb/h)H1 (Btu/lb)H2 (Btu/lb)H3 (Btu/lb)(lb/h)(F)(BTU/h)(F)(BTU/h)(BTU/h)(BTU/h)(BTU/h)303958.641.868123.55183.70180.071150.4124.0119.878381.017.2401.79120239.44120641.2342260.21303958.641.979130.89183.70180.071150.4131.3819.878381.017.2425.67127384.28127809.9549428.94303958.641.892125.13183.70180.071150.4125.6019.878381.017.2406.95121784.27122191.2243810.21Calculos de los flujos masicos del condensado obtenidosCorriente de liquidaCorriente de vaporCorriente de vapordel balance de la Trampa de vapor (B)Cp(BTU/lb*F):1Cp(BTU/lb*F):0.45(BTU/lb)969.6LPMFlujo frioPeso aguaFlujo calienteEntalpiaEntalpiaEntalpiaCondensado Temp. FriaQ ganado Temp. FriaQ sensibleQ latenteQ cedidoQ perdidoFfcalienteFcLiq satVap sat(T3-T1)* fluido frio(T2-T4)*fluido calient*fluido calient*fluido calienthacia el amb(lb/h)(Kg)(lb/h)H1 (Btu/lb)H2 (Btu/lb)H3 (Btu/lb)(lb/h)(F)(BTU/h)(F)(BTU/h)(BTU/h)(BTU/h)(BTU/h)607917.272.225147.16183.70180.071150.4147.7110.885506.567.2478.58143218.81143697.3958190.83607917.271.975130.62181.88180.071150.4130.8710.885506.569530.01126888.77127418.7941912.22607917.272.101138.96181.88180.071150.4139.2210.885506.569563.83134983.96135547.7850041.22Calculos de los flujos masicos del condensado obtenidosCorriente de liquidaCorriente de vaporCorriente de vapordel balance de la Trampa de vapor (C)Cp(BTU/lb*F):1Cp(BTU/lb*F):0.45(BTU/lb)969.6LPMFlujo frioPeso aguaFlujo calienteEntalpiaEntalpiaEntalpiaCondensado Temp. FriaQ ganado Temp. FriaQ sensibleQ latenteQ cedidoQ perdidoFfcalienteFcLiq satVap sat(T3-T1)* fluido frio(T2-T4)*fluido calient*fluido calient*fluido calienthacia el amb(lb/h)(Kg)(lb/h)H1 (Btu/lb)H2 (Btu/lb)H3 (Btu/lb)(lb/h)(F)(BTU/h)(F)(BTU/h)(BTU/h)(BTU/h)(BTU/h)303958.641.884124.60194.59180.071150.4126.5021.685506.567.2409.85122651.90123061.7537555.19303958.641.839121.63196.41180.071150.4123.7121.685506.565.4300.62119950.47120251.0834744.52303958.641.941128.37196.41180.071150.4130.5721.685506.565.4317.29126603.51126920.8041414.24Dimensiones de la Tuberia de Acero 2-1 plg.IPSPropiedades del fluido frio a Tm83.3FPropiedades del vapor a Tm219.2Fdi (plg):1.38di (pie)0.115Viscosidad (lb/(pie-h))2.00134Cp(BTU/lb-F)1Viscosidad (lb/(pie-h))0.03025Cp(BTU/lb-F)0.45Area de flujo (ap) pie20.0104Densidad (g/cm3)0.996k(BTU/pie-h-F)0.35398Densidad (g/cm3)k(BTU/pie-h-F)14.2196531792DI (plg):2.067DI (pie):0.1723DE (plg):1.66DE (pie):0.138(A) Calculo para los fluidos a 4psi y 30 LPMFLUIDO FRIO: Calculo del hi y hioFLUIDO FRIO: Calculo del ho( coeficiente de pelicula en el tubo interior)( coeficiente de pelicula en el anulo)VelocidadNumero deNumero dehihioVelocidadNumero deNumero dehihiode masa (Gp)ReynoldsPrandtde masa (Gp)ReynoldsPrandtlb/(pie2-h)BTU/h-pie2-FBTU/h-pie2-Flb/(pie2-h)BTU/h-pie2-FBTU/h-pie2-F381117.6921899.595.65439.31365.21381117.6921899.595.65439.31365.21381117.6921899.595.65439.31365.21Dimensiones de la Tuberia de Acero 2-1 plg.IPSPropiedades del fluido frio a Tm78.8FPropiedades del vapor a Tm219.2Fdi (plg):1.38di (pie)0.115Viscosidad (lb/(pie-h))2.1145Cp(BTU/lb-F)1.01Viscosidad (lb/(pie-h))0.03025Cp(BTU/lb-F)0.45Area de flujo (ap) pie20.0104Densidad (g/cm3)0.99678k(BTU/pie-h-F)0.35128Densidad (g/cm3)k(BTU/pie-h-F)14.2196531792DI (plg):2.067DI (pie):0.1723DE (plg):1.66DE (pie):0.138(B) Calculo para los fluidos a 4psi y 60 LPMFLUIDO FRIO: Calculo del hi y hioFLUIDO FRIO: Calculo del ho( coeficiente de pelicula en el tubo interior)( coeficiente de pelicula en el anulo)VelocidadNumero deNumero dehihioVelocidadNumero deNumero dehihiode masa (Gp)ReynoldsPrandtde masa (Gp)ReynoldsPrandtlb/(pie2-h)BTU/h-pie2-FBTU/h-pie2-Flb/(pie2-h)BTU/h-pie2-FBTU/h-pie2-F762235.3941455.226.08744.17618.65762235.3941455.225.65744.17618.65762235.3941455.225.65744.17618.65Dimensiones de la Tuberia de Acero 2-1 plg.IPSPropiedades del fluido frio a Tm84.2FPropiedades del vapor a Tm219.2Fdi (plg):1.38di (pie)0.115Viscosidad (lb/(pie-h))1.9795Cp(BTU/lb-F)1.01Viscosidad (lb/(pie-h))0.03025Cp(BTU/lb-F)0.45Area de flujo (ap) pie20.0104Densidad (g/cm3)0.99591k(BTU/pie-h-F)0.3545Densidad (g/cm3)k(BTU/pie-h-F)14.2196531792DI (plg):2.067DI (pie):0.1723DE (plg):1.66DE (pie):0.138(C) Calculo para los fluidos a 8psi y 30 LPMFLUIDO FRIO: Calculo del hi y hioFLUIDO FRIO: Calculo del ho( coeficiente de pelicula en el tubo interior)( coeficiente de pelicula en el anulo)VelocidadNumero deNumero dehihioVelocidadNumero deNumero dehihiode masa (Gp)ReynoldsPrandtde masa (Gp)ReynoldsPrandtlb/(pie2-h)BTU/h-pie2-FBTU/h-pie2-Flb/(pie2-h)BTU/h-pie2-FBTU/h-pie2-F381117.6922141.215.64443.47368.67381117.6922141.215.64443.47368.67381117.6922141.215.64443.47368.67