SHELL & TUBE CONDENSER DESIGN

STEP - 1TO CALCULATE HEAT LOAD

INPUT DATA :

9)SP.GR. OF SHELL SIDE FLUID10) LATENT HEAT OF VAPORISATION (Kcal/KG ° C)11) FLOWRATE OF SHELL SIDE FLUID (Kg/Hr)

12) FLOWRATE OF TUBE SIDE UTILITY FLUID (Kg/Hr)

13) FLOWRATE OF TUBE SIDE UTILITY FLUID (m3/Hr)

STEP - 2TO CALCULATE LMTD FOR COUNTER CURRENT FLOW : HOT FLUID IN 41 HOT FLUID OUTCOLD FLUID OUT 35 COLD FLUID INDIFFERENCE 6 DIFFERENCE

STEP - 3OVERALL HEAT TRANFER COEFFICIENT CONSIDERATION.

CONSIDERED= 50 244 Kcal/M2.hr.°C

STEP - 4HEAT TRANSFER AREA CALCULATIONINPUT DATA1) HEAT LOAD 2) LMTD

3) OVERALL HEAT TRANSFER COEFFICIENT

Heat Transfer Area ( M2 )

STEP - 5

AREA OF THE CONDENSER REQUIRED(CONSIDERING 20 % DIVERSITY)

NOTE: DO NOT CHANGE THE FIGURES WHICH ARE COLOURED

1) SHELL SIDE FLUID (vapourizing fluid)2) TUBE SIDE FLUID (utility)

1) Cp OF SHELL SIDE FLUID HOT FLUID( Kcal/Kg OC)

2) Cp OF TUBE SIDE FLUID COLD FLUID( Kcal/Kg OC)

5) TEMP. OF HOT FLUID INLET ( OC )

6) TEMP. OF HOT FLUID OUTLET ( OC )

7) TEMP. OF COLD FLUID INLET ( OC )

8) TEMP. OF COLD FLUID OUTLET ( OC )

BTU/HrM2OK

SHELL & TUBE CONDENSER DESIGN

waterwater

1

0.35

41 105.8 ºF

35 95 ºF

30 86 ºF

35 95 ºF1.32 COLD FLUID

87792 Total Boile up

42089 Kg/Hr

42 m3/Hr

3530

5

73656 Kcal/Hr 5.4848149

244

55.037199

66.04

Kcal/Hr-M2-OC

M2

M2

Common Solvent Data Sheet

Solvent

1 t

orr

5 t

orr

10

to

rr

40

to

rr

60

to

rr

10

0 t

orr

20

0 t

orr

40

0 t

orr

50

0 t

orr

60

0 t

orr

1 Acetic Acid 118.1 -17.2 6.3 17.5 43 51.7 63 80 99 105 110

2 Acetic Anhydride 139.6 1.7 24.8 36 62.1 70.8 82.2 100 119.8 126 133

3 Acetone 56.5 -59.4 -40.5 -31.1 -9.4 -2 7.7 22.7 39.5 46 51

4 Acetonitrile 81.75 -47 -26.6 -16.3 7.7 15.9 27 43.7 62.5 68 74

5 Benzene 80.1 -36.7 -19.6 -11.5 7.6 15.4 26.1 42.2 60.6 67 73

6 Carbon Bisulfide 46.3 -73.87 -53.8 -43.94 -21.16 -13.6 -5.1 10.4 28 34.57 39.5

7 Chloroform 61.3 -58 -39.1 -29.7 -7.1 0.5 10.4 25.9 42.7 48 54

8 Cyclohexane 80.7 -45.3 -25.4 -15.9 6.7 14.7 25.5 42 60.8 68 73

9 DMF 152.8 19.3 32.47 62.85 72.91 86.48 106.7 129.3 137.2 143.83

10 EDC 84 -44.5 -24 -13.6 10 18.1 29.4 45.7 64 70 76

11 Ethanol 78.4 -31.3 -12 -2.3 19 26 34.9 48.4 63.5 68 72

12 EPH 117.9 -16.5 5.6 16.6 42 50.6 62 79.3 98

13 Ethyl Acetate 77 -43.4 -23.5 -13.5 9.1 16.6 27 42 59.3 64 70

14 FFA 146 14.5 27.59 57.48 67.38 80.74 100.62 124.88 130.62 137.17

15 Formaldehyde -19.5 -88 -70.6 -65 -57.3 -46 -33 -32 -27

16 IPA 82.5 -26.1 -7 2.4 23.8 30.5 39.5 53 67.8 70 77

17 MDC 39.75 -70 -52.1 -43.3 -22.3 -15.7 -6.3 8 24.1 30 34

18 Methanol 64.7 -44 -25.3 -16.2 5 12.1 21.2 34.8 49.9 55 59

19 MIPA 33 -82.17 -62.99 -53.49 -31.65 -24.42 -14.66 -0.14 16.11 21.76 26.55

20 Mono Chloro Benzene 132 -13 10.6 22.2 49.7 58.3 70.7 89.4 110 117 123

21 MTBE 55.2 -68.32 -47.75 -37.56 -14.14 -6.38 4.07 19.65 37 43.15 48.28

22 n-Butanol 117.5 -1.2 20 30.2 41.5 60.3 70.1 84.3 100.8 106 111

23 n-Hexane 68.7 -34.5 -25 -2.3 5.4 15.8 31.6 49.6 56 61

24 Petroleum Ether 60-80

25 Phenol 182 40.1 62.5 73.8 100.1 108.4 121.4 139 160 168 172

26 Pyridine 115.4 -18.9 2.5 13.2 38 46.8 57.8 75 95.6 108 108

27 THF 66 -61.58 -40.34 -29.81 -5.62 2.39 13.19 29.28 47.29 53.55 58.85

28 Toluene 110.6 -26.7 -4.4 6.4 31.8 40.3 51.9 69.5 89.5 97 102

29 Water 100 1.2 11.2 34 41.5 51.6 66.5 79.41 86.3 92.13

30 o-Xylene 139.3 -15.86 9.97 22.78 52.2 61.94 75.08 94.65 116.55 124.16 130.61

31 m- Xylene 144 -12.93 13.2 26.15 55.9 65.76 79 98.84 120.99 128.69 135.21

32 p- Xyleme 137-138

33 Aniline 184 35 58 69.4 97 106 119 140 162

34 Carbon t Chloride 76.7 -50 -30 -20 4.3 12.3 23 38.3 57.8

35 Di Ethyl Ether 34.6 -74 -57 -48 -28 -22 -12 2.2 17.9

36 Dimethyl Sulfoxide 189 33 60 73 103 114 125 146 178

37 Dioxane 101 -36 -13 -1.2 25 33.8 45.1 62.3 81.8

38 Ethelene Glycol 197 53 78 92 120 130 142 159 179

39 Formamide 211 71 96 110 138 147 158 176 194

40 Methyl Acetate 57.8 -57 -39 -29 -8 -0.5 9.4 24 40

41 NitroBenzene 211 44 72 84.9 115 129 140 161 186

42 Propanol -1 97.8 -15 5 14.7 36 43.5 52.8 66.8 82

43 Heptane 98 -34 -13 -2 22 31 42 59 78

44 Glycerine 290 126 154 167 198 208 220 240 263

Sr.No.

B.P. in oC at

Atm Pr.

Common Solvent Data Sheet7

00

to

rr

Sp.Gr.

115 1.053 96.75 0.522 39 1.15 2.07 16.7 60.05 infinite

138 1.082 96.44 0.236 48.8 0.91 3.52 -73 102.09 12

55 0.78 124.3 0.538 -18 0.33 2 -94.6 58.08 infinite

79 0.783 173.68 0.541 6 0.38 1.5 0.41 41.05 infinite

78 0.8787 103 0.419 -11 0.65 5.5 78.11 0.18

43.9 1.263 59.35 - -30 NA -108.6 76.13

59 1.484 59.01 0.231 none 0.57 4.12 -63.5 119.4 0.82

78.5 0.7781 93.81 0.44 -18 0.98 2.9 6.6 54.16 0.0052

149.6 0.945 137.81 0.486 58 0.82 -61 73.1 infinite

82 1.2569 77.33 0.3015 13 0.9 3.35 -40 98 NIL

76 0.789 204.26 0.68 13 1.2 1.62 -112 46.07 infinite

1.183 97.95 -25.6 92.53

74 0.901 94.26 0.457 -4.4 0.46 3.05 -82.4 88.1 7.7

142.87 1.03 infinite

-24 0.815 60 -92 30.03 Very soluble

80 0.785 159.35 0.67 -11.7 0.34 2.07 -101 60.1 infinite

37.5 1.3255 77.077 0.2888 None 0.44 2.93 -96.7 84.94 2

63 0.7915 269.79 0.605 12 ..65 1.1 -97.8 32.04 infinite

30.72 0.692 119.09 0.65 0.498 59.111

129 1.107 78.3 0.311 29 0.8 -45.2 112.56 0.049

52.75 0.747 78.196 0.508 -28 0.35 3.04 -109 88.15 4.8

114 0.81 141.26 0.687 35 294 -79.9 74.12 7.45

66 0.6591 80.48 0.527 -18 0.31 2.97 -94 86.17 0.001

0.635 -40 2.5

178 1.071 0.561 79 2.8 40.6 94.11 8.2

113 0.982 107.36 0.431 20 0.88 -42 79.1 infinite

63.47 0.889 92.414 -17.22 2.5 -108 72.1 Fully Miscible

107 0.866 88.17 0.325 4.4 0.59 3.14 -95 92.13 0.06

97.22 0.99 540 0.99 NA 0.89 0 18 100

136.22 0.88 81.86 0.4 27 0.85 3.6 -47.4 106.1 NIL

140.89 0.87 81.86 0.4 32 0.6 3.6 -25 106.4 0.02

0.86 81.86 0.4 27 0.65 3.6 13-14 106.1 NIL

1.032 103 0.512 70 3.8 -6.2 93.13 3.8

46 0.2 -22.6 153.84

0.713 123 0.473 -40 0.24 74.12 6.9

1.101 178 0.7 85 1.99 78 Fully Miscible

1.034 102 0.4 12 1.3 9.5-10.5 88 Fully Miscible

1.113 191 0.573 >110 20.9 62 Fully Miscible

1.134 112 0.595 154 3.8 2 45.04 Fully Miscible

0.932 98 0.4 -9 0.37 -98.7 74.08 24.5

1.196 79 0.339 87 1.86 5.7 123.11 0.19

0.804 164 0.582 15 1.72 60.1 Fully Miscible

0.684 87.18 0.518 -1 0.41 9.6 100.21 0.005

1.261 124.17 0.4 160 945 92.09 Fully Miscible

Latent Heat

(Cal /gm)

Sp. Heat Cp

(Kcal/Kg-oC)

Flash Point (Close Cup)

(oC)

Viscosity in CP (25

oC)

Vap. Density (Kg/m3)

Melting point (oC)

Mol. Wt.

Solubility in water at 20 oC (%

w/w)

Basis of Drying Oven Operation:

1. Wet solid product is put into Tray Oven; oven is sealed closed.2. Heat input is applied to oven;3. Cooling fluid is circulated through acetone condenser;4. vacuum pump is started;

• As the wet solid is heated in the oven, the vapor pressure of the acetone increases and the acetone starts to vaporize at the lower, partial vacuum pressureproduced by the vacuum pump;

• The vacuum pump works to maintain the set partial vacuum that is controlled by allowing atmospheric air to "bleed" into the vacuum pump suction. The vacuum pump - under ideal conditions - would not not normally have to continue to operate after extracting all non-condensables from the system. However,in the real world situation, there will be air infiltration into the partial vacuum system through the oven door seals, the gaskets, equipment and piping joints, etc., etc.

• These air infiltrations try to defeat the vacuum created and, as a consequence, the vacuum pump is left to continue to operate - although at a reduced capacity by allowing the atmospheric air to bleed in and keep the pump working at capacity.

• The partial vacuum is really set by the temperature of the cooling fluid in the acetone condenser. The acetone has to be cooled and condensed at a temperaturethat corresponds to the acetone vapor pressure equal to the partial vacuum setting. This allows the acetone to condense and drop out of the condenser as a liquid and not be "sucked" (extracted) out of the system by the vacuum pump.

• If the temperature of the condensed acetone is sufficiently cold, there will little or undetected losses of acetone exiting in the vacuum pump exhaust to atmosphere.• The addition of heat into the oven accelerates the rate of acetone evaporation and speeds up the drying process; the price to pay for this capacity increase is

the cold energy that has to be inputted into the condenser as the coolant fluid.

Tray Oven

Acetone Condenser

Heat Input

Acetone Liquid

Coolant Fluid Out

As the wet solid is heated in the oven, the vapor pressure of the acetone increases and the acetone starts to vaporize at the lower, partial vacuum pressure

The vacuum pump works to maintain the set partial vacuum that is controlled by allowing atmospheric air to "bleed" into the vacuum pump suction. The vacuum pump - under ideal conditions - would not not normally have to continue to operate after extracting all non-condensables from the system. However,in the real world situation, there will be air infiltration into the partial vacuum system through the oven door seals, the gaskets, equipment and piping joints, etc., etc. These air infiltrations try to defeat the vacuum created and, as a consequence, the vacuum pump is left to continue to operate - although at a reduced capacity

The partial vacuum is really set by the temperature of the cooling fluid in the acetone condenser. The acetone has to be cooled and condensed at a temperaturethat corresponds to the acetone vapor pressure equal to the partial vacuum setting. This allows the acetone to condense and drop out of the condenser

If the temperature of the condensed acetone is sufficiently cold, there will little or undetected losses of acetone exiting in the vacuum pump exhaust to atmosphere.The addition of heat into the oven accelerates the rate of acetone evaporation and speeds up the drying process; the price to pay for this capacity increase is

Vacuum Pump

Coolant Fluid Out