Single-shell, two-tube pass heat exchanger with surface area 0.4 m? andoverall heat transfer coefficient of 1800 W/m2-K; saturated steam at 110°Ccondenses on one side while water at a flow rate of 0.35 kg/s enters at 17°C.Calculate (a) Outlet temperature of the water (b) Rate of condensation of steam.cp(water)=4179 J/kg. K.916 IThermodynamicsTABLE A-4Saturated water-Temperature tableInternal energy,Specific volume,m/kgEnthalpy.KJ/kgEntropy,kJ/kg - Kk/kgSa.SatSat.Sat.Sat.Sat.Sat.Sat.liquid, Evap., vapor,Sat.Temp.,liquid,liquid,Evap..liquid,Evap.,press.Pst kPavapor,vapor,vapor,T°CUphe0.0010000.0010000.00021.01942.0202374.92374.90.00121.02042.0220.0000 9.1556 9.15560.07630.1511 8.7488 8.89990.2245 8.5559 8.78030.2965 8.3696 8.66610.015100.61170.87251.2281206.00147.03106.322360.82346.62381.82388.72500.92489.12477.22500.92510.12519.28.9487 9.024915200.0010000.0010012.3392 0.0010022332.52318.42395.52402.32465.42453.51.705777.88562.98083.91362.98283.9152528.32537.457.762104.83125.73146.63167.53188.4325300.3672 8.1895 8.55670.4368 8.0152 8.45200.5051 7.8466 8.35170.5724 7.6832 8.25560.6386 7.5247 8.16333.16980.00100343.34032.8792304.32290.22276.02409.12415.92422.7104.83125.742441.72429.82546.54.24690.0010042555.62564.62573.53540455.6291 0.0010067.3851 0.0010089.595325.20519.51515.2512261.92247.72429.42436.1146.64167.53188.442417.92406.0-2394.00.0010102582.4209.332233.42219.12204.72190.35012.3522382.00.0010120.0010150.00101712.0269.56397.66706.19352442.72449.3209.342591.30.7038 7.3710 8.074815.7635560650.7680 7.2218 7.98980.83130.8937 6.9360 7.82960.9551 6.7989 7.754O230.24251.16230.26251.18272.122369.82357.72600.12608.819.9477.0769 7.90820.0010200.0010232455.92462.42468.925.043272.09293.042345.42333.02617.52626.17031.2025.03962175.8293.07313.9975802161.32146.62131.92475.32481.638.5970.0010260.0010290.0010324.12913.40532.8261314.032320.62308.02295.32282.52269.61.0158 6.6655 7.68121.0756 6.5355 7.61111.1346 6.4089 7.54351.19291.2504 6.1647 7.41512634.62643.047.41657.86870.183334.97355.96335.02356.0285902487.82117.02102.02494.02500.12651.42659.62667.66.2853 7.47820.0010360.0010402.35931.9808376.97398.00377.04398.099584.609101.42120.90143.38169.182087.02071.82056.42040.91000.0010430.0010470.0010521.67201.4186419.062506.0419.172675.62683.42691.12698.62706.02256.41.3072 6.0470 7.35422511.92517.7105440.15461.27440.28461.422243.11101150.0010560.0010601.20941.03600.891332229.72216.02202.11.3634 5.9319 7.29521.4188 5.8193 7.23821.4737 5.7092 7.18292523.32528.9482.42482.59503.81120198.67503.602025.31.5279 5.6013 7.1292125130135232.23270.28313.220.0010650.0010700.0010750.0010800.0010850.770120.668080.58179524.83546.10567.412009.51993.41977.32534.32539.52544.7525.07546.38567.752713.12720.12726.92188.12173.71.5816 5.4956 7.07711.6346 5.3919 7.0265140145361.53415.680.508500.446002549.62554.42159,12144.32129.21.6872 5.2901 6.97731.7392 5.1901 6.92941.7908 5.0919 6.8827588.771960.91944.2589.16610.642733.5610.192739.8150155476.16543.490.0010910.0010960.392480.34648631.66653.19674.791927.41910.31893.02113.82098.01.8418 4.9953 6.83711.89241.94262559.1632.18653.792745.92563.52567.82571.92575.72751.82757.52762.84.9002 6.79274.8066 6.7492160165170618.23700.93792.180.0011020.0011080.0011140.306800.272440.24260696.46718.201875.41857.5675.47697.24719.082082.02065.61.9923 4.7143 6.70672.04172048.82767.94.6233 6.6650175892.601002.81123.51255.20.0011210.21659740.021839.42579.4741.022031.72772.72.0906 4.5335 6.62420.0011270.0011340.0011410.0011490.001157761.92783.91763.05785.19807.434.4448 6.58411801851900.193841820.91802.11783.02582.82586.02589.02014.21996.21977.92777.22781.42.13922.1875 4.3572 6.54472.2355 4.2705 6.50592.28310.173902785.32788.82792.00.15636806.00828.18850.461954.1847 6.46781398.81554.90.140890.127211763.61743.72591.72594.2829.78852.261959.01939.82002.3305 4.0997 6.4302

TS=110°CT1=17°CT2 =?m˙=0.35kg/secCp=4179j/kg-kU= 1800w/m2-k∆T= log mean temp difference

Single-shell, two-tube pass heat exchanger with surface area 0.4 m2 and overall heat transfer coefficient of 1800 W/m2.K; saturated steam at 110°C condenses on one side while water at a flow rate of 0.35 kg/s enters at 17°C. Calculate (a) Outlet temperature of the water (b) Rate of condensation of steam. cp(water)=4179 J/kg. K. 016 Thermodynamics

Single-shell, two-tube pass heat exchanger with surface area 0.4 m2 and overall heat transfer coefficient of 1800 W/m2.K; saturated steam at 110°C condenses on one side while water at a flow rate of 0.35 kg/s enters at 17°C. Calculate (a) Outlet temperature of the water (b) Rate of condensation of steam. cp(water)=4179 J/kg. K. 016 Thermodynamics

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Chapter9: Heat Transfer With Phase Change

Section: Chapter Questions

Problem 9.31P

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Concept explainers

Heat Exchangers

Heat exchangers are the types of equipment that are primarily employed to transfer the thermal energy from one fluid to another, provided that one of the fluids should be at a higher thermal energy content than the other fluid.

Heat Exchanger

The heat exchanger is a combination of two words ''Heat'' and ''Exchanger''. It is a mechanical device that is used to exchange heat energy between two fluids.

Question

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Single-shell, two-tube pass heat exchanger with surface area 0.4 m? and
overall heat transfer coefficient of 1800 W/m2-K; saturated steam at 110°C
condenses on one side while water at a flow rate of 0.35 kg/s enters at 17°C.
Calculate (a) Outlet temperature of the water (b) Rate of condensation of steam.
cp(water)=4179 J/kg. K.
916 I
Thermodynamics
TABLE A-4
Saturated water-Temperature table
Internal energy,
Specific volume,
m/kg
Enthalpy.
KJ/kg
Entropy,
kJ/kg - K
k/kg
Sa.
Sat
Sat.
Sat.
Sat.
Sat.
Sat.
Sat.
liquid, Evap., vapor,
Sat.
Temp.,
liquid,
liquid,
Evap..
liquid,
Evap.,
press.
Pst kPa
vapor,
vapor,
vapor,
T°C
Up
he
0.001000
0.001000
0.000
21.019
42.020
2374.9
2374.9
0.001
21.020
42.022
0.0000 9.1556 9.1556
0.0763
0.1511 8.7488 8.8999
0.2245 8.5559 8.7803
0.2965 8.3696 8.6661
0.01
5
10
0.6117
0.8725
1.2281
206.00
147.03
106.32
2360.8
2346.6
2381.8
2388.7
2500.9
2489.1
2477.2
2500.9
2510.1
2519.2
8.9487 9.0249
15
20
0.001000
0.001001
2.3392 0.001002
2332.5
2318.4
2395.5
2402.3
2465.4
2453.5
1.7057
77.885
62.980
83.913
62.982
83.915
2528.3
2537.4
57.762
104.83
125.73
146.63
167.53
188.43
25
30
0.3672 8.1895 8.5567
0.4368 8.0152 8.4520
0.5051 7.8466 8.3517
0.5724 7.6832 8.2556
0.6386 7.5247 8.1633
3.1698
0.001003
43.340
32.879
2304.3
2290.2
2276.0
2409.1
2415.9
2422.7
104.83
125.74
2441.7
2429.8
2546.5
4.2469
0.001004
2555.6
2564.6
2573.5
35
40
45
5.6291 0.001006
7.3851 0.001008
9.5953
25.205
19.515
15.251
2261.9
2247.7
2429.4
2436.1
146.64
167.53
188.44
2417.9
2406.0
-2394.0
0.001010
2582.4
209.33
2233.4
2219.1
2204.7
2190.3
50
12.352
2382.0
0.001012
0.001015
0.001017
12.026
9.5639
7.6670
6.1935
2442.7
2449.3
209.34
2591.3
0.7038 7.3710 8.0748
15.763
55
60
65
0.7680 7.2218 7.9898
0.8313
0.8937 6.9360 7.8296
0.9551 6.7989 7.754O
230.24
251.16
230.26
251.18
272.12
2369.8
2357.7
2600.1
2608.8
19.947
7.0769 7.9082
0.001020
0.001023
2455.9
2462.4
2468.9
25.043
272.09
293.04
2345.4
2333.0
2617.5
2626.1
70
31.202
5.0396
2175.8
293.07
313.99
75
80
2161.3
2146.6
2131.9
2475.3
2481.6
38.597
0.001026
0.001029
0.001032
4.1291
3.4053
2.8261
314.03
2320.6
2308.0
2295.3
2282.5
2269.6
1.0158 6.6655 7.6812
1.0756 6.5355 7.6111
1.1346 6.4089 7.5435
1.1929
1.2504 6.1647 7.4151
2634.6
2643.0
47.416
57.868
70.183
334.97
355.96
335.02
356.02
85
90
2487.8
2117.0
2102.0
2494.0
2500.1
2651.4
2659.6
2667.6
6.2853 7.4782
0.001036
0.001040
2.3593
1.9808
376.97
398.00
377.04
398.09
95
84.609
101.42
120.90
143.38
169.18
2087.0
2071.8
2056.4
2040.9
100
0.001043
0.001047
0.001052
1.6720
1.4186
419.06
2506.0
419.17
2675.6
2683.4
2691.1
2698.6
2706.0
2256.4
1.3072 6.0470 7.3542
2511.9
2517.7
105
440.15
461.27
440.28
461.42
2243.1
110
115
0.001056
0.001060
1.2094
1.0360
0.89133
2229.7
2216.0
2202.1
1.3634 5.9319 7.2952
1.4188 5.8193 7.2382
1.4737 5.7092 7.1829
2523.3
2528.9
482.42
482.59
503.81
120
198.67
503.60
2025.3
1.5279 5.6013 7.1292
125
130
135
232.23
270.28
313.22
0.001065
0.001070
0.001075
0.001080
0.001085
0.77012
0.66808
0.58179
524.83
546.10
567.41
2009.5
1993.4
1977.3
2534.3
2539.5
2544.7
525.07
546.38
567.75
2713.1
2720.1
2726.9
2188.1
2173.7
1.5816 5.4956 7.0771
1.6346 5.3919 7.0265
140
145
361.53
415.68
0.50850
0.44600
2549.6
2554.4
2159,1
2144.3
2129.2
1.6872 5.2901 6.9773
1.7392 5.1901 6.9294
1.7908 5.0919 6.8827
588.77
1960.9
1944.2
589.16
610.64
2733.5
610.19
2739.8
150
155
476.16
543.49
0.001091
0.001096
0.39248
0.34648
631.66
653.19
674.79
1927.4
1910.3
1893.0
2113.8
2098.0
1.8418 4.9953 6.8371
1.8924
1.9426
2559.1
632.18
653.79
2745.9
2563.5
2567.8
2571.9
2575.7
2751.8
2757.5
2762.8
4.9002 6.7927
4.8066 6.7492
160
165
170
618.23
700.93
792.18
0.001102
0.001108
0.001114
0.30680
0.27244
0.24260
696.46
718.20
1875.4
1857.5
675.47
697.24
719.08
2082.0
2065.6
1.9923 4.7143 6.7067
2.0417
2048.8
2767.9
4.6233 6.6650
175
892.60
1002.8
1123.5
1255.2
0.001121
0.21659
740.02
1839.4
2579.4
741.02
2031.7
2772.7
2.0906 4.5335 6.6242
0.001127
0.001134
0.001141
0.001149
0.001157
761.92
783.91
763.05
785.19
807.43
4.4448 6.5841
180
185
190
0.19384
1820.9
1802.1
1783.0
2582.8
2586.0
2589.0
2014.2
1996.2
1977.9
2777.2
2781.4
2.1392
2.1875 4.3572 6.5447
2.2355 4.2705 6.5059
2.2831
0.17390
2785.3
2788.8
2792.0
0.15636
806.00
828.18
850.46
195
4.1847 6.4678
1398.8
1554.9
0.14089
0.12721
1763.6
1743.7
2591.7
2594.2
829.78
852.26
1959.0
1939.8
200
2.3305 4.0997 6.4302

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F1 Vegetable oil at a flow rate of 10 kg/s (p=920 kg/m³; u=5x10-3 Pa.s; k=0.14 W/m K; cp-2.1 kj/kg K) from 51 pieces of 1.2 mm thick stainless steel plates It will be heated from 20°C to 50°C in a plate heat exchanger consisting of Heating will be carried out using steam at 121°C. The plate width (w) is 0.3 m and the clearance between the plates is 3 mm. The effective area is 1.5 times the projected area. The heat transfer coefficient for the steam side is 12000 W/m².K. Calculate the required plate length since the heat exchanger is operated in series flow order (Pressure drop must be determined)