-LEGAL
P I -
This m p r t was prepored
06
brhalf of tha Commission:
Mnkrr any warronry or reprorent&tion, expressed completeness,
any
or urefulnetr of the inform&ian
informotion.
---
on occount of Covernmnt sponrotad work.
nor ths Commission, nor any person acting on
A.
NOTICE
apporotur.
M
implied,
Neifhsr
the
United Slates,
with r e r p e t t o tha
~ctmocy,
contoined in tlrh report, or that the
“$8
of
method, or pracers d i n c b s e d in this mpott moy not rnktnpe
privately owned rights; or
8.
Aa+umcr any Itabllttiea w i t h respect ta the use of, mr fm doquger reauhing from the vse of
ony inlarmotion, apporofus, method, or prooars disclosed
A s w a d in the ebavs, ‘‘pe,sM actnng contmctw of the C a m m i r r ~ a n , r or
on bah-lf
in
thra report.
04 tha Commic6ton” fncludeb any employee
01
cmplayee of such eontracfor, IO the extant thut such employee
contfmc#w of the Commlmion, or employee of such controcior prmp<mws, disssminatcr,
provides occess to, rrny informottm pvrrvont t o h r a mmploymant of tontcoct wtth the Commirrron, or h i s employment with such contractor.
i i
i t
-1-
Introduction
me ix A ) .
f the riser (see
R i t w x CaLcylatiicsns ( coat h u e d ) ?
Where:
E[
-
= height of r i ~ e r f t (see Fig. I)
- lb/ft2
t?lP = pressure drop i n heat exchanger
a t
D
t a r p e r a t w e drop i n heat exchanger
fz
diameter of riser
- ft.
OF.
hk = loss due to el1st exftanh eat of reactor, e x i t and ea% of heat
- 1.6 velocity heads. Q = power output - y46,ooo Btu/sec 2 exchanger
&E = accel.
af g r a v i t y
C = specific heat
-
-
32.2 f t / s e c
0.52 Btu 'lb
P 1 = 20 f t (see' Ffg. I)
-
OF
i c t i o n factor * .02 0 = temperatwe coefficient of d e n s i t y 3 p = degsity of fuel = 123 1 b / f t
-
0.0121 lb/ft3
- OF
For an e i g h t f o o t diameter reactor t h e volume of t h e piping w i l l be
f o r each value of
D
EL&
H*
AP
and Qt
this
VOL
will be a min-Jslum a t same ~ & u e of
Ffg. 33 is a p l o t of p i p i n g volume veratls rises height for
At
= 2QQo and
values of n p of 10, 20, 30, 40, lb/ft'. Simflm pxots were made far 25Uo. The min value8 of g volume and &e associated r ts and d i & e t e r s are ed against heat ex& pressure drop i n Figs. I11 and
IV.
Heat Exchanger C,;lculations
On the baBis t h a t t h e heat exchanger is of the counterflow tube and shell
desTgn with the fuel i n t h e tubes tuLd t h a t the Mussel$ number over the range
-3-
Eeat Exchanger Galcdateons (continued w e derive the follow
inwestigafed I s Golastant and e q u a l t o k'",
ships (see Appendix B)).
LN = 286.5 Q k
At,
The v a l w e of t h e heat exchanger is:
'HE.
'tubes
Where :
L = length of tube
-
+
'Header
ft
N = nmber of tubes K = %herma1 conductivity of fuel.
3 . 5 Btu/hr
$t %enqeraturedrop in heat exchanger. OF &ta = average temperature differential. 0F = tube inside dia.
-
.05 f t .
= v i s e a s i t y of f u e l =
Q = heat output. C
P
IL-
p =
lb /hr
0.3.74
3tu/sec
specific heat of f u e l .
density of fuel
- ft -
Btu/lb
ltP3 l b / f t 3
-
-
OF
ft
0
F
From this we can calculate L, N, and heat exchanger volume against heat
att,.
The tenrperatwes used were: f u e l entering the heat exchanger a t 1210%' and leaving at 960'~ to 3.035%. The wall temperature was tasken as g ng from 850' to 1050째, giving t h e exchanger pmssure drop Sol: differetrt
following temperature cond$tions:
Fuel E x i t
8%
nta
la35
3-77
1010
200
1-72* 5 160.0
T m s e ture
.
me t0t;al voluble i
Of the sy'stera is e
of the; heat exchmgei'p
..
A-t
At,
%he voluae of. tibe pisfog plus
1u-h riser diweter, heat exc
r tube length and number
of'Lubes, and t o t a l trolume of the Systen sgalnat riser height.
On the basis of this preLiminary i reactors do not seem to be very attractive. ptmps seems to be more than baL a u k r O P heat hanger tubes of heat exchanger tabes can be s An Investigation e higher than comparable forced the cast of a natt.mil. convect fuel circulation
-----..
14 c
Distribution 1-3.
DTIEJ AEC
4. M.
J. Sklnner