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1.
2. _I- -- -_____
ihis report was prepared as an account of w o ~ ksponsored by an ageocy of the
lJniEsdStates:Govctilment Neithat theunitedStatcsGoverrai,ient norany agency
ihereoi, nor any of thcrr employees, makes any warranty, mpress or implied, or
assumes any legal liability or responsibility for the accuracy, completcnrss, or
usefulness of any inforn-raiion, apparatus orodiict, or process disclosed, or
represents that its use would not infringe privately owasd rights 3cference herein
to any spcc~frl:commercial product,process, or s e ~ ~ ~ i c eby trade name,trademark,
rnanufactuict , or othceisriae, ~ O P Snot necessarily constitute or imply its
endorsement, recornmendation, or favoring by fire United Sta?cs@overnment or
any agency thereof Tne vicsals and opinions of authors nxpccsscd herern do riot
necessarily state or rcfivct those of the United Sta:es GOVCii-I:iiejat or any agency
thetcoi
- -_________-~
7. LIST OF FIGURES
e-composition-te data (Duhring chart)
eous LiBr and a t e mixtures . . . . . . . . . .
erature
erature
LiBr-water m . . . . . . . . . . . . . . . . . . .
aqueous t e r es . . . . . . . . . . . . .
i t r a t e mixture . . . . . . . .
mal conducti res . . . . . . . . . . . .
. . . . . . . . . . . . . . . . .
3
5
3 t comparison and ternary
t e mixtures . . . . . . . . . . . . . . . . . . . 1 3
4 a t i c representatio lated single-sta
rature heat pump a t e points . . . . . . . . . 15
ture boost as t e heat and
water tempera ternary
m i x t u r e s . . . . . . . . . . . . . . . . . . . . . . . . . 1 7
6 son of pure r e solution
t e and absorb or LiBr and
n i t r a t e mixt . . . . . . . . . . . . . . 1 9
7 son of pure re t e solution
rate and absorb for LiBr and
n i t r a t e mixt . . . . . . . . . . . . . . . . . . . . . 20
8 t of increasing xchanger surface
on COP for terna u r e s . . . . . . . . . . . . . 21
9 f increasing s o l u t i exchanger surface
on flow r a t e for ixtures . . . . . . . . . . 22
10 rison of COP-lift a heat release
orber UA for t e i s one-half
LiBr . . . . . . . . . . . . . . . . . . . . . . . . . . . 24
on of COP-lift and t release
when absorber UA f a r t is one-third
a t o f L i B r . . . . . . . . . . . . . . . . . . . . . . . . . . . 25
8.
9. ACKNOWLEDGMENTS
L
Appreciation is ex Stephen Kaplan, Hr,
Richlen, and man (Haifa Te
r support an ation is a
1 for typin LeRoy GLlliam
Sharon McCona s , and E. W.
orial skills.
i a l Programs.
document was prep U.S. Department of Ene
v i i
10.
11. EXECUTIVE SUKMARY
s report presen a computer si
at comparing th mance of 11th
nary nitrate aqu n a temperature a
In this study, the fallfn heat transfer coe
e-third. Due to a ed thermophy
nitrate mixtur be lower than th
t e s relied on
e results show t h nitrate mixture may be op
, which is a
er than wha ated with
potential for 1
than L i B r .
mental measu ing Eilm heat
perties are r
nitive investiga
i x
12.
13. ABSTRACT
A new aqueous ter ting of 53 wt %
and 19 w t % N
temperature
a computer prog
pump with LiB
ncentration-
mixtures as
he two f l u i d ere is a regio
omparison ca
cal data o in the temp
In the abse thermophysical
uess first app
w that the t
a 10% advantag advantage in t
s LiBr at hi ernary nitrat
lization at emperatures an
e l y i n the l o w a t temperature r
erforinance a
ure is suffic
d corrosion data.
xi
16. 2
2. WOWING MEDIA PROPERTIES
The pressure-composition-temperature (P-X-T) and the specific
enthalpy-composition-temperature(H-X-T)data for the working fluids are
critical pieces of information for heat pump cycle calculations. In the
case o f LiBr aqueous mixtures, these thermodynamic properties are well
documented between 50 and 350°F. The specific enthalpies of pure
refrigerant (water) and steam are available in steam tables. In the
case of the ternary nitrate mixtures, Ally has represented the exper-
imental B-X-T and H-X-T data by polynomial equations similar in form ts
s
the ones published €or LiBr in the ASHME Handbook of Fundamentals.
These equations €or LiBr and TNMs will be shown later with their atten-
dant Duhring and specific enthalpy plots. The main facility provided by
these equations is that they can easily be incorporated in a c~mputer
program e
5
2.1 EQUATIONS DESCRIBING I?-X-T
The P-X-Tdata for TNMs and LiBr mixtures are superimposed on one
another in Fig. 1. The relationship between the saturation temperature
of the pure refrigerant (pure water in each ease) and the temperature of
the mixture of known concentration, X (wt % ) , can be represented for
either working fluid by an equation of the form,
t = A(X)tf + B(X) , (1)
where t and t t are the mixture and pure refrigerant saturation tempera-
tures expressed in degrees Fahrenheit, respectively, and A axid B are
polynomial functions of the concentration, X. Of course, the functional
dependence of A and B on X will be different for the two mixtures as is
seen by their respective expressions in Fig. 1. The equilibrium vapor
pressure of water above the mixture is given by a van’t Hoff type of
equation,
E
2 ’
+ -Dp ~ c + -...-
( t t + 4 5 9 . 6 7 ) (t’ + 4 5 9 . 6 7 )
Loglo
where C, D, and E are constants that must be the same f o r both mixtures
because they share a common refrigerant between them. The reasons why
Eq. (2) is used for both L i B r and TNMs are explained in detail
elsewhere.
5
18. 4
2.2 EQUATIONS DESCRIBING SPECIFIC ENT
The specific H-X-Tdata and correlations for aqueous LiBr are
reproduced from the ASHFZAE Fund entals Handbook in Fig. 2a. Figure 2b
show3 the H-X-Tdata for the ternary nitrate mixture. The experimental
data are correlated with an equation of the form,
4
w =: a ( X ) I- /3(X)t , ( 3 )
where cr and /3 are polynomials in the solute (ternary s a l t ) cancentra-
tion, X (wt % ) , and t is the solution temperature. Details regarding
this correlation are re orted in ref. 5.
2.3 VISCOSITY, SPECIFIC GRAVITY, AND THERMAL CONDUCTIVITY DATA
The narrow scope of thermaphysical and transport data available in
the literature and the sparse amounts o f data available for the ternary
nitrate mixture were a serious handicap during the preparation of this
report. Viscosity, specific gravity, thermal conductivity, etc., data
€or aqueous LiBr mixtures are available up to 100°C (212”F), but proper-
ties at temperatures up to 180°C (356°F) were needed for this study. In
the absence of experimental data, estimated values were obtained by
extrapolation (Figs. 2c,d,e). Perhaps the only source of data far the
aqueous ternary nitrate fluid is ref, 3 , which contains adequate data on
viscosity, lacks considerable data on specific gravity, and is severely
deficient on thermal conductivity, for which only two values of 0.31 and
0.33 W/rn2-K are quoted at salt concentrations of 86.7 wt % and
83.7 wt % , respectively. These va ues are themselves obtained through a
recommended power law equation. The lack of specific gravity data is
not very severe because thermal expansion,
4
is small over the temperature range of interest. But the error on ther-
m a l conductivity could deviate substantially from the estimated value of
0.31 to 0.33 W/m2*K.
20. 35
E
W ( X , f ) = a(X) + P(X)t
4.516 - 8.649
x 10-5)x2
t = SQLUTIQN TE
F i g . 2 . ( b ) Specific enthalpy-composition-temperature for aqueous
ternary n i t r a t e mixtures.
23. 9
0.2 I I I I I I I I I
1 20 20 4Q 120 140 1
RE ("C)
Fig. 2. ( e ) Thermal. conductivity of L i B r mixtures.
24. Operation o f a single-stage temperature amplifier heat pump was
simulated using a program developed by Grossman and Michekson.
The criteria for evaluating absorption fluids from a practical
standpoint are (a) the coefficient of performance, (b) the temperatmre
lift and boost temperatures, (c) the flow rates of refrigerant,
(d) potential corrosion problems, ( e ) crystallization limits, (f) film
heat transfer coefficients, ( g ) mass transfer rate of sorbate into sor-
bent, and (h) M area per unit capacity, The coefficient of perfor-
mance, refrigerant flow rates, and film heat transfer coefficient are
directly related to the size of a particular heat pump unit and are
therefore reflected i n capital costs. High COP, heat, and refrigerant
transfer rates reduce heat pump size. Corrosion by working fluids is a
strong determinant of hardware useful life expectancy, and its reduction
OK elimination is obviously preferred. Crystallization is another
important operating parameter because it determines the acceptable range
of concentration and temperature of the circulating fluid before onset
of crystallization. Once crystallization BCCUKS, the system ma
be shut down. Mixtures in which crystallization occurs at law ternpera-
tures are generally preferred over those in which crystallization occurs
at higher temperatures.
First, consider the heat transfer coefficient. The absorber i s the
focus of attention because it is here that the sorbate (refrigerant) is
absorbed into the sorbent, thereby releasing heat. At least three
resistances to heat transfer are involved between the refrigerant vapor
and the process stream being produced, the largest of which is resis-
tance due ta the film resistance between the sorbent and the tube wall.
The other two resistances are the resistance to heat transfer offered by
the metal tube wall and that between the wall and the utility stream.
These three resistances in series are combined to yield a single overall
heat transfer coefficient, U as shown below,
6
0
1II_
9
DO xw Do 1
*o -
+- E-Dihi km r, 0
+ -- --
L
where D and D are the outside and inside diameters of the tube, x i s
the tube wall thickness, k is the metal thermal conductivity, D is the
logarithm mean diameter of the tube, and ho is the film heat transfer
coefficient. The term, represents the resistance to heat transfer
0 i - F B
M L
1
hO
25. sorber tubes,
st two term
the f i l m he
e value a€
esistance . at transfer
ause it implie
than 2000
eous beca
termination efficients i
t be determi
ue to the de
alue of f i l fficient was u
nitrate f l u i approximation.
ablished the heat transfer
data. The s procedure
, Due to the v , and ther
the film heat t t for the te
d to be about ha1 lutions. Th
a t transfer co ated using e
ing the Q V ~ r coefficient
n as one-half d a t h i r d set
e scenario heat transfer
s transfer coe ure of the r:
e the r e f r i ct with the
ed will be equilibrium v
se that the
the rate of m
l y during the orbent and re
er. Suppose t h ncentration i
of m a s s t r then equilibr
is absorbed t. If t h i s rat
rbed will be. 1
mount, resuE
pressure, eac solution (eq
ntrations eo erent temper
and t h e i r di as subcoolin
ent way to
e viscosities
nary n i t r a t e s ,
LiBr solution ow t h a t subco
g an effect r additive for
used in type I T S . Without an
26. 12
additive, LiBr mixtures typically have 10°C or greater subcooling for
low-pressure absorbers. Due to lack of experimental data, the extent of
subcooling cannot be quantified; but as explained above, sorbates of
higher viscosities will absorb sorbe ts slower than those lower
viscosities.
Based on the potential COP and temperature l i f t s shown in Fig. 3 ,
10°C of subcooling Ear the ternary nitrate s approximately equal to the
advantage that this f l u i d has over lithium romide in terms of tempera-
ture lift capability.
Since actual heat, mass transfer, and subcooling data are not yet
available for the ternary nitrates and since the computer model used in
this study does not account €OK any subcooling, the simplifying assump-
tion sf no subcooling for the t e r n a ~ g ~nitrate and LiBr mixtures is used.
having
28. 14
4 . RESULTS
A schematic of the single-stage temperature amplifier heat p u p
considered far the simulation study is shown in Fig. 4 . The waste heat
source input to the desorber and evaporator at positions 10 and 1,
respectively, is stea at a prescribed (input) temperature. This waste
heat source temperature is an input parameter in the program which can
arbitrarily be changed. The waste heat streams leaving the desorber and
evaporator at positions 11 and 2, respectively, is saturated water at
e pressure as their ~ e s p e ~ t i v einlet streams. Therefore, no
pressure gradient is assumed between state points 10 and 11 and 1 and 2,
respectively, and all the latent heat of vaporization from the waste
stream i s supplied to the desorber and evaporator. In the condenser,
cooling water at a prescribed temperature is introduced at 1 3 and exits
at 14. The temperature at 1 3 and the cooling water mass flow rate are
fixed. In the absorber section, the process stream enters at state
paint 3 at a prescribed temperature at its saturated condition
(condensed water). As it goes through the absorber, it picks up suffi-
cient heat to leave the absorber at 9 as saturated steam, The purpose
of the recuperator is to make the absorption cycle more efficient, and
the effectiven s s of the recuperator plays a major role in determining
the cycle COP.
The overall heat transfer coefficients times area (UA) in each of
the five primary equipments used in the simulation appear in Table 1.
These were obtained from a prototype test unit at QRNL used to monitor
the performance of LiBr aqueous mixtures.
8
Equipment UA
Btu/rn"F W/K 10-3
Desorber 166.7 5.27
Recuperator 8 3 . 3 2 . 6 3 4
Condenser 500 15.81
Abs orber 216.7 -+ 108.3 -3. 7 2 , 2 6.852 -+ 3 . 4 3 + 2 . 2 8
Evaporator 833 2 6 . 3 4
A cursory inspection of Fig. 1 shows that there is a small region
o f overlap between LiBr and ternary mixture solutions, At temperatures
below 65°C (=150"F), the TNMs will certainly present crystallization
problems, but LiBr is still suitable for heat pump applications without
imminent threat of crystallization. It is believed that LiBr/M,O may be
used at higher temperatures and concentrations than have been reported.
30. EM LIB% l! B EQUAL ABS0
The computer simulated performanees of % i B r and TNMs for two sets
o f waste heat and cooling water temperatures are shorn in Pig. 3 . Con-
sider the case where the waste heat and cooling water temperatures are
105°C (221°F) and 55°C (131"F), respectively, and the absorber UA is
6852 W/K. With LiBr, one can $0 from 10 to 42°C lifts because the con-
centrations and crystallization curves on the Duhring chart (Fig. 1)
allow it, With TNMs, the lower lifts of less than 3k"C are not possible
because the smallest concentration in the Duhring plat is 70 wt %, and
the crystallizatian curve is very near. Hence, with TNMs the range of
temperature lifts varies from 34 to 52°C. Similar arguments apply to
the case of the waste heat and cooling water temperatures being 140 and
70"C, respectively.
Considering the coefficient of performance, a camparison of the
~ U K V ~ Sin Fig. 3 shows that the COP values are higher fer TNM than they
are f o r LiBr. However, the question of how much of an advantage in COP
is afforded by the TNM over LiBnr becomes quite mbiguous as the tenpera-
t u ~ elift is varied. At low l i f t s (37 to 4O"C), the predicted COP of
the TNM is about 10% higher than that f o ~LiBr, assuming no subcooling.
A s the lift is increased from 42 to S2"C, the COB for the LiBr mixture
drops off to zero; whereas that far TNM keeps decreasing but is,
nevertheless, a finite value until a lift of 52"C, when it too becomes
zero. Therefore, between 42 and 52°C temperature lift, the COPS of the
TNM are infinitely greater than that of LiBr. The culprit is the pre-
cipitous fall in COP with temperature lift because AC approaches zero.
Therefore, a valid region of temperature lifts f o r comparison of COPS
for the two fluids is one ranging from low lifts up to the point where
the precipitous fall in COB begins to OCCUK. Based on the simulation
study and in light of the above discussion, it may be appropriate to say
that the predicted COP of the T is approximately 10% higher than that
for LiBr mixtures.
Two further queries arise from the results shown in Fig. 3 . They
are (i) why are the temperature lifts higher f o r TNMs? and (ii) why are
the COPS higher than they are f o r LiBr?
The answer to the first query is fairly straightforward. In
Fig. 1, the slope of the equilibrium vapor pressure versus solution tem-
perature plot i s flatter for the TNMs than those for LiBr, and this
flatness helps to reach out Eurther in the solution temperature field.
From the Duhring chart, it is an easy matter to determine the maximum
boost temperature possible (AC = 0 ) for a given waste heat and cooling
water temperature. This information is shown in Fig. 5. It can be seen
from Fig. 5 that in the comon operating temperature regimes, the tem-
perature boost and, consequently, the temperature lift of the TNMs are
potentially greater than they are for LiBr mixtures.
The second question, relating to higher COPS for the TNMs, does not
seem to have an overtly obvious answer. Since the definition o f COP is
Q /Q + Q,, higher COP values clearly indicate higher numerator values
A D
32. 18
with respect to the denominator, Q, + Q,. If the values of QD -+ Q
could be held Constant, then the higher COP values are associated wit!
Ahigher Q values. Then one could investigate the factors affecting Q
and from there be able to draw definite conclusions regarding the two
working fluids. However, the computer program6 used in the simulation
study did not permit the desired 'bevel of freedom in fixing Q and Q,,
and could only approximately be held constant f o r the t w o working
fluids. The results are shown in Fig. 6. For waste heat at 140°C
(284°F) and a condensing temperature of 70°C (158"F), the dilute solu-
tion flow rate (curve 2) for the two fluids is almost identical in the
region of overlap. The refrigerant flow rate (curve 1) is slightly
higher for the TNMs than it is for L i B r , and this explains why the
absorber capacity, Q, (curve 3 ) , is also higher. The same behavior is
obtained f o r a different set of waste heat 105°C (221°F) and condensing
water 55°C (131°F) conditions as shown in Fig. 7.
A s mentioned earlier, the primary purpose o f focusing attention on
the ternary nitrate mixtures i s because they have the potential to
operate at up to 260°C (500°F) with minimal corrosion of mild steel.
A
D
they
4 . 2 EFFECT OF SOLUTIQN HI AT EXCHANGER UA ON COP OF 9:
Et is well-known that the coefficient of performance of a heat pump
is sensitive to the effectiveness of the solution heat exchanger, other
things being equal. The effectiveness increases with the heat exchange
surface area. Figure 8 shows the improvement in COP by increasing the
surface area in the solution heat exchanger from 7 . 7 4 m2 to 17.0 m2.
The waste heat source and cooling water temperature are 140°C (284°F)
and 70°C (158"F), respectively. The COP increases by approximately 32%
from its value of 0.31 corresponding to a solution heat exchanger area
of 7.74 m 2 - Figure 9 shows what effect the change in solution heat
exchanger has on the refrigerant. and dilute solution flow rates and the
absorber heat release.
The mast dramatic change i s observed in the dilute solution flow
rate as the solution heat exchanger area is increased from 7.74 m2 to
1 7 . 0 m 2 * The pure refrigerant too decreases, but the decrease is less
than 10%. The significance of this is that the concentration difference
between the concentrated and dilute solutions is greater when
A = 7 . 7 4 m2 than it is when A 5 17.0 m2.
The change in solution heat exchanger area also influences the
total. quantities o f heat delivered to the evaporator and desorber and
that rejected in the absorber, Since there is only a 10% change in the
pure refrigerant flow rate, the heat input to the evaporator also
changes in the same proportion. The desorher and absorber heat
increases with increasing solution heat exchanger area. The net result
is higher COP as shown in Fig. 8.
33. C
-1
8
-*- LITHIUM BROMIDE
< -TERNARY NITRATES/H,U
CONDENSING WATER
70°C (158OF)
4 1O C (19.8OF)
AT IN EQUIPMENT-
ion flow rate
and absorber heat release for LiBr and ternary n i t r a t e mixtures.
34. 20
F i g . 7 . Comparison of pure refrigerant, d i l u t e solution f l o w r a t e
and absorber heat release f o r LiBr and ternary n i t r a t e mixtures.
37. 23
e computer simu d s a t i s f a c t o r
maximum a t s region is s
that the d i f ation between
ed stream a
was not possible
t h i s l i m i t a t
hes its maxi
oftware in t
4 . 3 NCE OF ABSORB CE
e case of th discussed i n Se
ransfer coe d t o be about
and down to
se i n the
era11 heat t
actual decv
er resistan
i t s influen n t . For the
t o deal with
cipated decrease
t r a t e is s long w i t h the
fts below rature <180°C
ncentration € w t % , f o r whi
Lithium bromi
COP of 0 . 4 , a oost temperat
rature) of u
ty. At lift
d the absorbe
the absorber
ween the t
r i n favor o
f TNM has pro t o believe t h
er coeffici n lower. To i
the absorber UA was - t h i r d that
ted r e s u l t s f o r fluids are
for 11fts 540 her COP than
er absorber
e r COP than
re is sufficient
e conclusions t o . 10 and 11 are t h a t (i) LiB
COPS and highe
38. 24
ORNL-DWG 878450
8 0.4
k-
z
w
2 0.3
0"
00
G o
u.
8- 0.2h
$- 0.1
--- LITHIiJ
.-.*p TERNARY NITRATE, UA = 6.85x io3W / K-
TERNARY NITRATE, UA = 3.43 x io3W / K
WASTE HEAT :I- 140°C: (284°F) -
WATER :::I- 7OoC (158°F)
ENT -11"C (20°F)
HEAT RELEASE
-
EXTRAPOLATION
.I-
O 10 20 30 40 50 60 70 80 90 100
TH - TM, TEMPERATURE LIFT ("C)
7
e-%
c.-
E
6 3A
W
QY
I
' E
0 3
X
F i g . 10. Comparison of COP-lift and absorber heat release w h e n
absorber UA for ternary nitrate i s one-half that of L i B r ,
39. 0.5
0.4
0.3
0.2
0.1
0.
OFM-DWQ 878451
I I I i I 1-(I- LITHIUM BROMIDE, UA = 6.85X IO31 W/KI
n
c
(216.7 Btu/min. O F )
% - TERNARY NITRATE, UA = 6.85 X IO3 W/K -/ 6 ‘E
EXTRAPOtATiON
ER THAN 70 wt %
UNAVAILABLE
40. 26
heat release through the absorber at lifts greater than 40°C and high
boast temperature using w a s t e heat at 140°C (284°F) even when the absar-
ber UA is assumed as low as one-third its value for L i B r , and (iii) the
film heat transfer coefficient is a strong determinant o f the perfor-
mance and needs to be known accurately.
41. 27
NS
U ~ O U Sternar containing a s
s than LiBr rature rang
era11 heat nt is reduc
Br. In lo
etitive w i
ure than has
both fluids
cap overcome
ired i n futur or both flui
sorber film icient and t
e critical ation which
t to the othe
advantage tha
42.
43. 29
1.
2.
3.
4 .
5 .
6 .
7 .
8.
9 .
10.
B. A. Phillips, '' d Residential
ch and Devel
F. C. Hayes and R. J ation of Adva
onference, R ent on Hea
Laboratory, A
W. F. Davidson and ew High Tempe
Sub/85-22013/1,
, 1985 Fundame Society.of Hea
and Air-Condi , pp. 17.71-1
of Aqueous
n t t o Chemi L/TM-10258,
ssman and E. ion Heat P
s , Part 1: S imu1ation
RNL/Sub/83-4 ational Lab
t Blab, Chem. , 95-105 (1977).
ez-Blanco a l e and Perfo
tion Heat P
National Lab
rmann, Personal
R. C. DeVault, Persona. S.
44.
45. 31
APPENDIX
Lithium Bromi
solution con
=: 1.63 x 5
e viscosity, v
3ckness, 6 -
Reynolds Nllmbe
e, 6 = 3.206
(Fig. 2e) =: 0
t transfer c
ernary Nitra
e r solution tern
olution conc
tic viscosity, Y =
kness, 6 -
eynolds Number
, 6 = 4.159 x
1 conductivity o == 0.33 W/meK
transfer co 7 9 3 . 4 W/m2.K
%
46.
47. 33
1-5, M.
6 , V.
7 . R.
8. R.
9 , F.
21. M.
22. R.
2 3 . F.
24. J .
BUTION
R. Ally H. A. McLain
D. Baxter V. C . Mei
D. R. Miller
M. Olszewski
. H. Perez-B1
. B. K. Seiver
R. €3. Shelt
J. J. Tomlin
C. D. West
T. J. Wilban
Central Rese
Document Re
C. Maiensch OWL Patent
49. W. J.
UTION
Bierman ve, Fayettev
J . M. C a l m , E arch Institut
1 0 4 1 2 , Palo A
5 essor of Corn
tsburgh, PA
52. G. Douglas Ca lley Authori
53. s Office, U.S.
54. D. C. Erickson, C o . , 627 R i d
lls, I D 8340
Annapolis, MD
55. R. J , Fiskum nergy Conve
ranch, CE-1 , U.S. Depa
000 Indepen hington, DC
48. 34
56. J. Gilbert, Dames 6 Moore, Inc., 7101 Wisconsin Avenue,
Suite 700, Bethesda, MD 20814
57. S . M. Gillis, Dean, Graduate School, Duke University,
4875 Duke Station, Durham, NC 27706
58. G. Grossman, Technion-Israel Institute of Technology, Faculty
of Mechanical Engineering, Haifa, Israel
59. W. T. Hanna, Battelle Columbus Laboratories, 505 King Avenue,
Columbus, OH 43201
60. F. C. Hayes, Trane Company, 3600 Pamel Creek Road, LaCrosse,
WP 54601
61. F. R. Kalhamer, Vice President, Electric Power Research
Institute, B.U. Box 10412, Palo Alto, CA 94303
62. A . Karp, Energy Management Q Utilization Division, Electric
Power Research Institute, 3412 Hillview Avenue, P a l o Alto,
CA 94303
63. R. E. Kasperson, Professor, Government and Geography,
Graduate School o f Geography, Clark University, Worcester,
MA 01610
64. R. Macriss, Institute of Gas Technology, 3424 South State
Street, Chicago, IL 60616
65. L. A . McNeely, 7310 Steinmeier Drive, Indianapolis, IN 46250
66. D. K. Miller, Borg-Warner Air Conditioning Inc.,
P.O. Box 1592, York, PA 17'405
67. J. I. Mills, EGG-Idaho Inc., P.O. Box 1625-WCB, Idaho Falls,
ID 83415
68. R. L. Perrine, Professor, Engineering and Applied Science,
Civil Engineering Department, Engineering I, Room 2066,
University o f California, Los Angeles, CA 90024
69. B. A . Phillips, Phillips Engineering Co., 721 Pleasant
Street, St. Joseph, MI 49085
7 0 . R. Radermacher, University of Maryland, Department o f
Mechanical Engineering, College Park, MD 20342
71. R. C. Reinmamn, Carrier Corp., P , O . Box 4808, Syracuse,
Ny 13221
72. S . L. Richlen, Office of Industrial Programs, CE-141,
5F-O35/FORS, U . S . Department of Energy, 1000 Independence
Avenue SW, Washington, DC 20585
49. 35
73. U. Rockenfelle Company, 1453 Road,
Boulder City,
74. J. D. Ryan, 0 and Comuni
CE-132, GF-21 rnent of Ene
Independence on, DC 2058
75. D. S. Severso titute, 8800
Avenue, Chica
a76. S. V. Shelton hanical Engi
Institute of , GA 30332
77. J. J. Tuzson, tute, 8800 We
Avenue, Chicag
78. G. C. Vliet, T fversity of Te
TX 78712
79. PI. Wahlig, La oratory, Univ
fice of Assi Energy Resear
California, B
ent, DOE-ORO, 30
P.O. Box 6 2 ,
