Prediction of batch heat transfer coefficients for pseudoplastic fluids ...
Prediction of batch heat transfer coefficients for pseudoplastic fluids ... Prediction of batch heat transfer coefficients for pseudoplastic fluids ...
88 ql\fETI A = 6 T \--T -s L/kw (1+-12 1.Jhere l:l T"'I_S is the temperature difference bet1tJeen the measured point in the wall and the unkn01~ surface temperaturee If it is assumed that the wall resistance, L/~v' is negligible one could calculate the batch film coefricient using h' .,. ql-TET A6T 1 -J_b (4-13 hf can be calculated since all the variables can be measured or calcula ted. If equations 4-9 and 4-12 are equated~Ts_b ~he unknown variable in equation 4-10 ,can be calculated • b,T _ s b l/b_ III .6Tw_b l/h +L!kw and b,T s _ b = .6.T w _ b l+h L/lt w (4-15 Substituting 6T s _ b into equation L-1-- 1 0 (4-10 + hL) ~r (4-16 The group in the first set of parenthesis is equal to h'
and if' it is assumed that h' is almost equal to h equation 4-16 can be written h = hI (1 + h Y L/kw) (4-17 hI is calculated from equation ~--13. L is the average distance of the ther.nlocouple junction from the surface ~ 0.02 inches = 0.001667 feet. y~ is the thermal conductivity of' 316 stainless steel Substituting the values for L and kw (286) h = h' (1 + 0.0001774 hI) Apparent Vis~2sity of' the Batch The apparent viscosity of the batch is needed in the Reynolds nilluber, Prandtl number, and viscosity ratio. It can be calculated using equation 2-25. (2-25 The apparent viscosity is expressed in Ib .. /sec. f't if' K is expressed in Ib./ft. sec. n and N is expressed in rev. per. second .. The apparent viscosity of' the batch could also be expressed (4-19 based on the theoretical 8.-l1alysis d:i.scussed in Chapte,;,s{~~,Wjo0 \i".2t~;
- Page 59 and 60: 47 the highest heat tra...nsfer coe
- Page 61 and 62: 49 A pitched blade turbine gave coe
- Page 63 and 64: SI done on the correlation of heat
- Page 65 and 66: 5J evaluated at the wall temperatur
- Page 67 and 68: ss to (2-46 where ill is the consis
- Page 69 and 70: CHAPTER .2 DEVELOPMENT OF CORRELATI
- Page 71 and 72: momentum" mass" and energy may be ~
- Page 73 and 74: 61 Vr;> Jt.- ,,"Ii'\... ..", ::: (V
- Page 75 and 76: 63 Substitution of these dimensionl
- Page 77 and 78: l/(R + 1) and was able t@ elim.iE.a
- Page 79 and 80: 67 All of the variables and differe
- Page 81 and 82: 69 The average heat transfer coeffi
- Page 83 and 84: N"v = C Iv''' (;';~-"')&'i'~ (%t-n,
- Page 85 and 86: 73 Semi-Empirical Correlation i ..,
- Page 87 and 88: 75 7I1C1?/lfOCOUPLc .JuNe T/ON IMBE
- Page 89 and 90: 77 _I"---- / SCALE I ~~, .5 j t /Z.
- Page 91 and 92: also cop~ected to the pipes leading
- Page 93 and 94: 81 Ve8sel :J all th:l c]me 8 8 .) '
- Page 95 and 96: 83 potentiometer for varing the mot
- Page 97 and 98: 85 MATERIAL 7:0 STAIIJLESS STEEL /
- Page 99 and 100: 11 Wa.ll (Mi€1dl~) Same as #5 81
- Page 101 and 102: 89 shea.r ra.tes, tl?1ey a.re unaff
- Page 103: and if' lO"V'l$' a sm.all amount of
- Page 106 and 107: 94- was about 40-45 ndmutes .. Tke
- Page 108 and 109: 96 vThere N is in rev./sec .. and S
- Page 112 and 113: I {)D The generalized Reynolds n~mb
- Page 114 and 115: 02. CHAPTER !2. RESUI,TS Many heat
- Page 116 and 117: 01 TABLE 5-2 sutn~U{Y OF ADDITIONAL
- Page 118 and 119: 108 the batch than the other ticJO
- Page 120 and 121: 108 optimum impeller heights were u
- Page 122 and 123: 10 I r "'" , •• ,'., "",' """",
- Page 124 and 125: 112 correlations for the prediction
- Page 126 and 127: TABLE 5 - 4 Correlation Constants A
- Page 128 and 129: 1/6 Table 5-5 and 5-6. A measure of
- Page 130 and 131: TABLE S - 6 IMPELLER Correlation Co
- Page 132 and 133: 120 greater than 2.0. In this case
- Page 134 and 135: 12.2
- Page 136 and 137: TABLE 5 - 9 CORRELATION E t (a/n +1
- Page 138 and 139: TABLE 5 - 10 IMPELLER Correlation C
- Page 140 and 141: TABLE 5 - 11 CORRELATION G (1.30/61
- Page 142 and 143: 1.30 of the substantial improvement
- Page 144 and 145: 1.3 2. The probable error in the ca
- Page 146 and 147: 134 .,;' : :: :::: : ~ !~. , " . .'
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- Page 150 and 151: 38 the cooling of nitration liquors
- Page 152 and 153: 140 The average deviation of the me
- Page 154 and 155: 42 tween 0.25 and 0.58. L~~l had re
- Page 156 and 157: 144 transfer coefficients to non-Ne
- Page 158 and 159: 16 of fit and it may t...herefore b
88<br />
ql\fETI A = 6 T \--T -s<br />
L/kw<br />
(1+-12<br />
1.Jhere l:l T"'I_S is the temperature difference bet1tJeen the<br />
measured point in the wall and the unkn01~<br />
surface temperaturee<br />
If it is assumed that the wall resistance, L/~v'<br />
is<br />
negligible one could calculate the <strong>batch</strong> film coefricient<br />
using<br />
h' .,. ql-TET<br />
A6T 1 -J_b<br />
(4-13<br />
hf can be calculated since all the variables can be measured<br />
or calcula ted.<br />
If equations 4-9 and 4-12 are equated~Ts_b ~he<br />
unknown<br />
variable in equation 4-10 ,can be calculated •<br />
b,T _ s b<br />
l/b_<br />
III<br />
.6Tw_b<br />
l/h +L!kw<br />
and<br />
b,T s<br />
_ b = .6.T w _ b<br />
l+h L/lt w (4-15<br />
Substituting 6T s _ b into equation L-1-- 1 0<br />
(4-10<br />
+ hL)<br />
~r (4-16<br />
The group in the first set <strong>of</strong> parenthesis is equal to h'
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