N I STIR 89-3932

NONTOXIC HEAT TRANSPORT FLUIDS

FOR SPACECRAFT TWO-PHASE

THERMAL CONTROL SYSTEMS

Patricia J. Giarratano

James F. Welch

National Institute of Standards and Technology

U.S. Department of Commerce

Boulder, Colorado 80303-3328

January 1990

NISTIR 89-3932

NONTOXIC HEAT TRANSPORT FLUIDS

FOR SPACECRAFT TWO-PHASE

THERMAL CONTROL SYSTEMS

Patricia J. Giarratano

James F. Welch

Chemical Engineering Science Division

Center for Chemical Technology

National Measurement Laboratory

National institute of Standards and Technology

Boulder, Colorado 80303-3328

January 1990

Sponsored by

Lyndon B. Johnson Space Center

Houston, Texas 77058

UNITED STATES

DEPARTMENT OF COMMERCE, Robert A. Mosbacher, Secretary

NATIONAL INSTITUTE OF STANDARDS

AND TECHNOLOGY, Raymond G. Kammer, Acting Director

CONTENTS

LIST OF TABLES ......... V

NOMENCLATURE AND DEFINITIONS vii

Nomenclature vii

Subscripts viii

Definitions ............... ix

Conversion Factors . . . xi

SUMMARY xiii

ABSTRACT ................. 1

INTRODUCTION .............. .......... 1

APPROACH . 3

Computer Database 3

Selection of Fluids for Evaluation 4

Rank Fluids Falling within Temperature Ranges 4

Calculate Relative Ranking, WF****, of Each Fluid for Each

Parameter 5

Assign a Weight Factor to Each of the Ranking Parameters . . 6

AuxHilary Parameters 7

Survey Commercial Suppliers of Heat Transport Fluids ...... 7

RESULTS AND DISCUSSION ............. 8

Results of Existing Fluids Study (PPDS) 8

Results of Commercial Survey 10

CONCLUSIONS AND RECOMMENDATIONS 11

Develop a New Substance .................................. 11

Investigate the Possibility of Using a Mixture of Existing

Fluids 12

Investigate the Catalytic Converter Technology 12

REFERENCES 13

TABLES 15

APPENDIX A DETAILS OF CALCULATION . A1

Background A1

Flow Regime and Heat Transfer Correlations A1

Boiling . A2

Condensation . A3

Two-phase Pressure Drop A4

iii
Calculation Procedure . A5

Detail on Calculation of Ranking Factors, (WF****) A7

WFFOMB and WFLTF A7

WFNBP and WFPVAP . A8

WFTMP and WFDEN A8

Figure A1 Assumed Geometry and Conditions for Evaluating

Thermal Performance Parameters, FOMB, FOMC. ....... A10

Supplement Al Computer Program for Calculation of Thermal

Performance Parameters All

APPENDIX B SUMMARY LIST OF COMPANIES CONTACTED B1

List of Companies Contacted by Telephone B1

Foreign Companies Contacted by Correspondence B4

Companies Specializing in CFC Production Contacted by

Correspondence B6

IV
1

2

3

4

5

6

7

8

9

10

LIST OF TABLES

Description Page

Top Ranked Fluids for

Temperature Range 1,

Tbulk = 200 K 18

Top Ranked Fluids for

Temperature Range 1,

Tbulk = 250 K 19

Top Ranked Fluids for

Temperature Range 1,

Tbulk - 300 K 20

Top Ranked Fluids for

Temperature Range 1

,

Tbulk “ 350 K 21

Top Ranked Fluids for

Temperature Range 2

,

Tbulk = 275 K 22

Top Ranked Fluids for

Temperature Range 2

,

Tbulk - 290 K 23

Top Ranked Fluids for

Temperature Range 2

,

Tbulk = 305 K 24

Top Ranked Fluids for

Temperature Range 2

,

Tbulk = 320 K 25

Comparison of Ranking Factors

for Water and Ammonia with those

for the Top Ranked Fluids 26

Product of Reduced Temperature

and Pressure for Top and Bottom

Ranked Fluids in Temperature Range 2

(Ranking on the Basis of Thermal

Performance) 27-34

Summary of Responses from Commercial

Suppliers of Heat Transport Fluids 35-42

V

NOMENCLATURE AND DEFINITIONS

Nomenclature

c

p

D

F

G

AH

h

k

L

LTF

APsat

PCRIT

Pr

PRED

PVAP

Re

S

ATsat

TCRIT

TRED

v

WF

WFDEN

WFFOMB

WFLTF

WFNBP

WFPVAP

WFTMP

x

X tt

Oi

M-P

a

$

1

2

$

2

lo

Specific heat at constant pressure,

J/(kg-K)

Diameter, m

Correction factor in Chen boiling

correlation

Mass velocity, kg/(s-m2

) Latent heat of vaporization, J/kg

Heat transfer coefficient, W/(m2 -K)

Thermal conductivity, W/(m-K)

Length, m

Liquid transport factor , ap ^AH/p-^ , W/m2

Ps$t.Twall “" psat , Tbulk' Pa

Critical pressure, Pa

Prandtl number=C

pp/k

PVAP/Pcrit

Vapor pressure at T^]^

Reynolds number=DG/p

Correction factor in Chen boiling

correlation

Wall superheat = Twall -Tbulk , K

Critical temperature, K

Tbul)$/Tcrit 3 Specific volume, m

J /kg

Weight factor

Ranking factor for the liquid density

Ranking factor for figure of merit for

boiling

Ranking factor for the liquid transport

factor

Ranking factor for normal boiling-point

temperature

Ranking factor for vapor pressure at the

bulk temperature

Ranking factor for the normal meltingpoint temperature

Quality (mass fraction vapor)

Martinelli-Nelson correlating parameter

Volume fraction vapor

Viscosity, (N-s)/m2 or Pa-s

Density, kg/m3

Surface tension, N/m

Two-phase friction multiplier based on

pressure gradient for liquid-alone flow

Two-phase friction multiplier based on

pressure gradient for total flow,

assumed liquid

Vll
Coefficients in Equations (A9) and (A10)

AF = -0.188 321 1071E+02

BF = 0.580 694 7 612E+01

CF = -0.551 671 5499

DF = 0. 166 927 8 595E-01

AS = 0.994 610 2006

BS = 0.591 353 4234

CS = 0.554 849 7826E-01

DS = -0.586 330 4243E-02

Subscripts

bp

bulk

c

cond

crit

f

g

1

mix

mp

NuB

red

sat

tp

tt

v

wall

boiling-point

evaluated at bulk (saturation)

conditions

convection

condensation

critical

liquid

vapor, gas

liquid

two-phase mixture

melting-point

nucleate boiling

normalized by critical property

saturation

two-phase

turbulent-turbulent

vapor

evaluated at wall temperature

viii
Definitions

Coefficient of Performance for Boiling (COPB)-

Ratio of the heat flux required to completely vaporize the

liquid, flowing at a fixed Reynolds number, to the pumping

power per unit surface area required to move the fluid

through the pipe for a fixed L/D and D.

Coefficient of Performance for Condensation (COPC)-

Ratio of the heat removed to completely condense the vapor,

flowing at a fixed Reynolds number, to the pumping power per

unit surface area required to move the fluid through the

pipe for a fixed L/D and D

,

Density of the Liquid (DEN)-

Density of the liquid at the bulk temperature and

corresponding vapor pressure, kg/m3 *

Figure of Merit for Boiling (FOMB)-

Ratio of an integrated-average forced-convection boilingheat-transfer coefficient in a pipe, over the length of

which complete vaporization of the liquid stream occurs due

to the application of a uniform heat flux, to the pumping

power per unit surface area required to move the two-phase

fluid through the pipe, (W/m2 -K) / (W/m2) =1/K.

Figure of Merit for Condensation (FOMC)-

Ratio of an integrated-average forced-convection

condensation-heat-transfer coefficient in a pipe, over the

length of which complete condensation of the vapor stream

occurs due to the removal of heat, to the pumping power per

unit surface area required to move the two-phase fluid

through the pipe, 1/K.

Liquid Transport Factor (LTF)

Ratio of properties (see nomenclature) that compares the

relative merits of the fluids for use in heat pipes in a

low-gravity field, W/m2

. Melting-point (TMP)

Temperature at which a solid melts at 101 kPa (1 atm), K.

Normal Boiling-point (NBP)

Saturation temperature at 101 kPa (1 atm) , K.

Operating Pressure (PVAP)-

Vapor pressure at the bulk temperature within the

temperature range, Pa.

ix
Ranking Factor (WF****)-

Value denoting the proximity to the preferred value for the

parameters FOMB, NBP, PVAP, TMP, LTF, DEN (may have a value

from 0 to 1 and the **** may be FOMB, NBP, etc.).

Weight Factor (WF)

Assigns a number to the relative importance of each

parameter considered relevant to the evaluation of a fluid.

x
Conversion of SI Units to Engineering Units

To obtain from multiply by

Atm Pa 9.860X10” 6

Btu/lbm J/kg 4.2992X10” 4

Btu/(lbm-°F) J/ (kg-K) 2 . 3885xl0“ 4

Btu/ (h-f

t

2 -°F) W/ (m2 -K) 1.7612X10” 1

Btu/ ( ft 2 -h) W/m23 . 1726X10” 1

CP Pa-s IxlO 3

ft m 3 .2808

lb f/f

t

N/m 6.8522xl0~ 2

lb f/ft2 Pa 2 . 089X10" 2

lbm/ft3 kg/mJ 6.248x10 ^ '

°F K tF=1.8tK

- 459.67

°F °C tp=1.8tc

+ 32

xi
'
SUMMARY

A search was conducted for an environmentally acceptable

heat transport fluid for use in a two-phase thermal control

bus of a manned spacecraft. A fluid having the following

general characteristics was sought: (1) nontoxic, (2)

nonflammable, (3) noncorrosive, (4) having long-term

stability, (5) catalytic decomposition resistant (at

temperatures of the order 573 K) , (6) possessing optimum

physical properties for efficient forced convection boiling

heat transfer, and (7) having a vapor pressure near 101 kPa

(1 atm) at room temperature.

The approach was to (1) develop a methodology to evaluate

and rank potential candidates for which thermodynamic and

transport properties were available, (2) perform the

evaluation for a wide range of fluids, and (3) survey the

commercial suppliers to establish the availablity or

unavailability of a suitable fluid.

The candidate fluids were restricted to those that could

operate in a two-phase system within certain temperature

ranges. The ranges were selected to cover temperature

extremes anticipated to exist in the internal and external

thermal control loops being considered for the thermal bus

of the Space Station.

Temperature range (1): freezing point less than 198 K (-

7 5°C ) and a critical temperature greater than 348 K (75°C) . Temperature range (2)

freezing point less than 273 K (0°C)

and a critical temperature greater than 322 K (49°C)

.

Many of the common refrigerants and hydrocarbons emerged as

top-ranked fluids for thermal performance and other relevant

parameters defined in our study. However, none of these

fluids met all the other stringent reguirements of

nontoxicity, nonflammability, and stability at high

temperatures. Further, the responses from commercial

suppliers , queried world-wide, revealed no commercially

marketed heat transport fluid that satisfies all specified

requirements

.

Based on the results of the study, we recommend the

following

1. Investigate the feasibility of the development of a new

substance

.

a. In order to more clearly specify the range of

thermodynamic and transport properties desired, complete a

more detailed statistical analysis of the relationship

between the physical properties and FOMB. This should be

done in consultation and cooperation with chemists

xiii
contemplating the possible molecular structures for the

fluid *

2. Investigate the possibility of using a mixture of

existing fluids.

3. Investigate the catalytic converter technology for

possible new concepts that would eliminate the high

temperature thermal stability constraint on the candidate

fluid

.

XIV
NONTOXIC HEAT TRANSPORT FLUIDS FOR SPACECRAFT TWO-PHASE

THERMAL CONTROL SYSTEMS

NASA Contract T-4528P

Patricia J. Giarratano, James F. Welch

This report summarizes an investigation to determine

the availability of a nontoxic, nonflammable,

noncorrosive and thermally stable heat transport

fluid suitable for two-phase thermal control systems

in manned spacecraft. Approximately 860 chemical

substances were sorted and ranked according to

parameters that were defined and calculated to

quantitatively evaluate fluids for the proposed

application. A methodology was developed for the

evaluation and ranking. A survey of world suppliers

of heat transport fluids was also conducted to

determine whether a suitable fluid is available. The

investigation did not identify a fluid that can meet

all the environmental and thermal property

requirements required for safe and efficient

performance in the spacecraft application.

Key words: commercial heat transport fluids; heat

transport; nontoxic fluids; spacecraft; thermal

control ; two-phase

INTRODUCTION

The Center for Chemical Engineering of the National

Institute of Standards and Technology conducted a search

for alternative nontoxic heat transport fluids for two-phase

thermal control systems for spacecraft, particularly those

serving life support systems or crew module systems. The

low vapor pressure of water, 2.48 kPa (0.36 psia) at 294 K

( 2 1°C) , and the relatively high freezing temperature (273 K)

make this otherwise desirable (from the point of view of

toxicity and other handling characteristics) heat transport

fluid less than ideal for the manned modules of spacecraft

if a failure condition should occur. The low vapor pressure

favors air leakage from the crew modules into the thermal

bus and thereby impairs operation of the system. Water's

relatively high freezing point may result in "freeze-up"

during "off-normal" conditions.

The high temperature catalytic converter in the crew

compartment presents an additional constraint on the

selection of the heat transport fluid for the thermal bus.

1
A suitable fluid must not be subject to catalytic

decomposition into toxic substance (s) when exposed to

temperatures in the order of 573 K (300°C)

.

Ultimately the development of a new, nontoxic, nonflammable,

stable heat transport fluid specifically for the spacecraft

application may be required. However, in view of the likely

high cost and complexity of the development and testing of

such a fluid, NASA requested an extensive evaluation of

existing substances, including commercially marketed heat

transport fluids, to establish the need and/or

specifications for the possible development.

Our approach to the problem was to develop a methodology to

provide a basis for quantitative evaluation of potential

heat transport fluids and apply the method to rank existing

fluids according to a weighted sum of relevant parameters

which are defined in the text. The emerging top ranked

fluids could then be subsequently evaluated for

environmental characteristics, including, for example,

toxicity, flammability, and thermal stability. The

methodology requires that the thermodynamic and transport

properties of saturated liquid and vapor at the operating

temperature be specified. Given these properties, the

method can be applied to predict the performance of existing

or new fluids which may be developed for the proposed

application

.

The parameter assigned the highest weight in the ranking

procedure was the thermal performance of the fluid. This

was defined as the ratio of an integrated average film

coefficient of heat transfer to the power consumed in

circulation through a uniformly heated (or cooled) pipe. A

similar approach for evaluation of media for single-phase

heat transfer systems was suggested by Parsons et al.[l] and

Carberry[2]. We applied the method to a simple two-phase

heat transfer system which is defined in the text and

appendix.

This study is concerned with the thermal control systems for

mannned spacecraft. A similar independent study has

recently been completed by McLinden[3] in which the

evaluation of fluids for two-phase heat transport was

performed for unmanned spacecraft application (for example,

external thermal control loop for Space Station) . The

results of the two investigations are consistent.

While the fluid property database that we employed in the

study is extensive (860 substances) , it is not allinclusive; therefore, a survey of known commercial suppliers

of heat transport fluids was conducted to ascertain the

availability of suitable fluids that were not in the

computer database.

2
APPROACH

An outline of the method employed in this study follows:

(1) Obtain computer database of themodynamic and

transport properties of fluids.

(2) Select fluids for evaluation,

(3) Rank the fluids according to a composite of

the ratio of heat transfer to pumping power, normal boilingpoint, vapor pressure at the selected operating temperature,

freezing point, liquid transport factor and density.

(4) Obtain toxicity, flammability and other

handling characteristics for top ranked fluids and eliminate

unsuitable materials.

(5) Contact commercial suppliers of heat transport

fluids for information on substances not contained in the

property database.

Computer Database

The thermodynamic and transport properties for approximately

860 fluids were obtained from the Physical Property Data

Service (PPDS) 1 computer Electronic Data Module [4]. This

database contains a wide variety of fluids, selected for

their industrial importance. It is particularly strong in

the hydrocarbon and simple organic (< 4 carbons) fluids.

The following fluid properties for saturated liquid and

vapor and physical constants were obtained for a range of

temperatures of interest:

(1) Density

(2) Heat capacity

(3) Latent heat of vaporization

(4) Thermal conductivity

(5) Viscosity

(6) Surface tension

(7) Vapor pressure

(8) Molecular weight

(9) Critical temperature

(10) Critical pressure

(11) Melting-point

(12) Normal boiling-point.

1 We use trade names to specify the computer database

adequately and do not imply endorsement by the National

Institute of Standards and Technology. Similar products by

other suppliers may work as well or better.

3
If any of these properties of a fluid were not available in

the PPDS database at the temperature of interest, then that

fluid was not included in the evaluation at that

temperature

.

Selection of Fluids for Evaluation

A review of prior NASA reports, [5-7], and discussion with

NASA JSC personnel established the range of temperatures of

interest. The evaluation of fluids was limited to those

that have;

Temperature Range (1); a freezing point less than 198 K (-

7 5°C) and a critical temperature greater than 348 K (75°C)

or

Temperature Range (2)

a freezing point less than 273 K

(0°C) and a critical temperature greater than 322 K (49°C)

.

For the Space Station application, Temperature Range (1)

represents a range of temperature that covers both infernal

and external thermal bus loop operating temperature

extremes. That selection criterion reduced the number of

fluids from 860 to 330.

Temperature Range (2) represents a narrower range of

temperature that covers the internal thermal bus loop

operating temperatures. This less restrictive temperature

range was satisfied by 659 fluids.

Rank Fluids Falling within the Temperature Ranges

Without regard to fluid toxicity or other handling

characteristics, we defined six parameters that provide the

basis for a quantitative evaluation/ranking of the fluids.

The parameters are evaluated at four different temperatures

within each range (200, 250, 300, and 350 K for Temperature

Range (1); 275, 290, 305, and 320 K for Temperature Range

(2)). The ranking parameters are:

(1) Ratio of an integrated-average forcedconvection-boiling heat transfer coefficient in a pipe, over

the length of which complete vaporization of the liquid

stream occurs due to the application of a uniform heat flux,

to the pumping power per unit surface area required to move

the two-phase fluid through the pipe. (FOMB, see appendix

for details.) This quantity characterizes the thermal

performance capability of the fluid. A high value is

preferred

.

4
(2) Operating pressure (PVAP - vapor pressure at

each of the four bulk temperatures within the temperature

ranges) . This quantity influences the pipe wall thickness

which in turn influences the mass of the system. A

favorable ranking is assigned to fluids having a vapor

pressure equal to 101 kPa (1 atm) . That operating pressure

would minimize the potential for leakage into or out of the

crew cabin module.

(3) Normal boiling-point (NBP - the saturation

temperature at 101 kPa) . A favorable ranking is assigned to

fluids having a normal boiling-point near 293 K (20°C)

.

(4) Freezing point (TMP) . A low value avoids the

possibility of freeze-up. A favorable ranking is assigned

to fluids having a low freezing point.

(5) Liquid transport factor (LTF) . This factor is

used to compare the relative merits of the fluids for use in

heat pipes in a zero-gravity field [8]. A large value of

LTF is preferred in the ranking scheme.

(6) Liquid density (DEN) . This quantity, like

operating pressure, influences the mass of the system. All

other criteria being equal in a ranking scheme, the lower

density receives a more favorable ranking.

Calculate Relative Ranking, WF****, of Each Fluid for Each

Parameter

For each parameter, a ranking of each fluid is calculated on

the basis of its proximity to the preferred value for that

parameter. For example the fluids having the highest value

of FOMB are given a ranking factor of 1, while the fluids

having the lowest values of FOMB are given a ranking factor

of 0 (or a very small number) . The ranking factors were

calculated using the statistical technique of calculation of

cumulative relative frequency [9]. This procedure

eliminates the need to scan the entire column of data to

determine a fluid's relative ranking within the column. It

also provides a means of placing the parameters on the same

basis so that an overall ranking of a fluid may be obtained

by addition of the ranking factors for all parameters. See

the appendix for more detail on calculating ranking factors

within each parameter column.

5
Assign a Weight Factor to Each of the Ranking Parameters

In order to assess the overall potential of a fluid as a

candidate alternative heat transport fluid, we have assigned

weight factors to the six parameters according to our

estimate as to the relative importance of that parameter in

the overall ranking. The weight factors assigned are:

Parameter Weight factor

FOMB 1.0

NBP 0.5

PVAP 0.4

TMP 0.3

LTF 0.2

DEN 0.1

With the above scheme, the maximum total ranking factor

possible for any fluid is 2.5; that is,

TOTAL = 1 . *WFFOMB + 0.5*WFNBP + Q.4*WFPVAP +

0 . 3 *WFTMP + 0 . 2 *WFLTF + 0.1*WFDEN

where the individual ranking factors ,WF****, ( *=any letter

in the parameter acronym) may be any value from 0 to 1

.

Since TOTAL is determined near the final stage of

calculations, it would be straightforward to redo the

calculation with different weight factors if others are

suggested in the future.

6
Auxilliary Parameters

Additional parameters which we consider to be ancillary to

the parameters described above were calculated but they

provide supplementary information for the ranking process.

The parameters (see appendix for calculation details) are:

(1) Ratio of integrated-average forced-convection

condensation-heat-transfer coefficient to the pumping power

required to move the two-phase fluid through the bus. (FOMC

- figure of merit for condensation.)

(2) Ratio of the heat flux required to completely

vaporize the entering liquid, flowing at a fixed Reynolds

number (2000 or 200 000)

,

to the pumping power per unit

surface area required to move the fluid through the pipe for

a fixed L/D and D (COPB - coefficient of performance for

boiling) . In an analagous fashion, the ratio of the heat

flux removed to completely condense the entering vapor,

flowing at a fixed Reynolds number (2000 or 200 000)

,

to the

pumping power per unit suface area required to move the

fluid through the pipe for a fixed L/D and D (COPC - coefficient of performance for condensation). Note:C0PB = COPC.

(3) The temperature difference at the pipe exit

between the inside pipe wall surface and the bulk fluid

(DELTB = vTboili , DELTC = vTcond$nsatio-) for complete

vaporization or condensation occunng in the pipe,

respectively.

)

Survey Commercial Suppliers of Heat Transport Fluids

Names of potential commercial suppliers of heat transport

fluids were compiled from a variety of sources [10-12].

Each of the companies was contacted by telephone or letter

requesting information on its products which might meet the

specified requirements. The list of companies contacted and

sample survey letters are included in the appendix.

7
RESULTS MID DISCUSSION

Results of Existing Fluids Study C^PDS)

The final ranking of the fluids in the PPDS database and

separation into categories" of Temperature Ranges 1 and 2 are

shown in Tables 1-4 and 5-8, respectively* Only the top

ranked (approximately fifty) fluids are presented for

conciseness. The rankings are for Re=2000 (the classical Re

where turbulent flow in a pipe commences) and L/D=100,

D=0.02 hu Results for Re=200 000 were also obtained but

because the rankings were not significantly different from

those at Re = 2000 for the same they are not

presented* A complete ranking of all ^fluids within the

temperature ranges at both Re numbers was delivered to NASA

in a Progress Report completed earlier* Tables 1-8 list in

decending order of total ranking number , TOTAL (max possible

= 2*5), the PPDS identity number (IDN) , the chemical formula

and abbreviated name (SPECIES) , and the relative ranking

factors ( WF****) for the parameters defined in the previous

sections

.

The weighting of the parameters and the assumption of a

linear weighted sum was arbitrary. However, for the

assumptions noted in the text in this regard, we can observe

the fluids that have the toprankings.

Many of the refrigerants (for example, IDN 485-

difluoromethane, 4 3 1-dichlorodifluoromethane, 492TM

difluoroethane, 369-chlorodifluoromethane) emerge as top

ranked fluids for all the bulk temperatures. This is not

surprising since these substances were specifically

developed as heat transport media. However, as was pointed

out by previous NASA investigations [5], these substances

are subject to decomposition into toxic gases if subjected

to high temperatures such as in a crew-cabin catalytic

converter.

Hydrocarbons (for example IDN 58-propene, 57-propane, 6-

butadiene, 60-propyne) also rank high among the fluids

tested, but because of their flammability, are not

considered a viable option.

8
Although we have not examined in detail the toxicity,

chemical stability or handling characteristics of the top

ranked fluids, there does not appear to be any substance

contained in the two temperature ranges that will emerge as

a candidate fluid for use in the manned spacecraft thermal

control systems. The top ranked fluids are either toxic

(either upon decomposition or outright) or flammable, or

both.

Table 9 was prepared from the complete ranking listings

which are not included in this final report. The table

illustrates how water and ammonia (fluids proposed for the

internal and external thermal bus loops of Space Station)

rank in the two temperature ranges, according to thermal

performance. We note that water (IDN 63) is ranked near the

bottom of the list for all the bulk temperatures in

Temperature Range 2 , although the ranking improves as the

temperature increases to 320 K. This ranking, in spite of

its attractiveness from the the point of view of toxicity

and handling, substantiates NASA's desire to replace it in

future thermal control system designs. Further, ammonia

(IDN 70) currently earmarked for use in the external thermal

control loop of Space Station ranks fairly high in the list

of fluids for both Temperature Ranges 1 and 2. The high

ranking, however, is offset by ammonia's unattractive

environmental and toxicological properties.

We mentioned in the introduction that McLinden[3] performed

an independent but similar investigation of "working fluids

for space-based two-phase heat transport systems." His

approach differed somewhat from ours, as his rating factors

were based on incremental system weights (or differences in

system weights between fluids) which arose because of, for

example, fluid weight, fluid dependent portion of components

weights, and an allowance for pumping power. However, all

but six of the 52 fluids top ranked in McLinden's scheme

appeared in the list of top ranked fluids in our study even

though the absolute order of the ranking was not identical.

Ammonia was ranked as the most favorable fluid and water as

the least favorable (Table 4 of McLinden's report) . The

results of the two studies are not inconsistent.

The functional relationship between fluid properties and

thermal performance ranking is complex. We observed a

correlation between low liquid viscosity and high ranking

for thermal performance. We expect this since a low

viscosity results in lower frictional pressure drop and

correspondingly lower pumping power. None of the other

properties show a pattern that would lead to a similar

statement except for proximity to thermodynamic critical

point. In general the fluids that rank the highest at a

given bulk temperature are nearer their thermodynamic

critical point than the lowest ranked ones. This can be

9
verified by noting the product of reduced temperature

(TRED=Tbulk/Tcr^ t ) and reduced pressure (PRED=PVAP/Pcr | t ) in

Table 10. A value of 1 indicates the thermodynamic critical

point. The fluids ranked highest appear to have the highest

value of this product; conversely, the lowest ranked fluids

have the smallest value. For supercritical fluids, the

correlation between proximity to thermodynamic critical

point and enhanced heat transfer coefficient has been

demonstrated [16]. A plot of the properties parameters that

occur in various single-phase forced-convection heat

transfer correlations peaks near the critical point (or

transposed critical points which exist above the critical

pressure) . The peak is made evident by enhanced heat

transfer coefficient. For the subcritical fluids and twophase heat transfer correlations of this study this seems

to be the case also. More extensive review and statistical

analysis would be required to substantiate the relationship

between proximity to critical point and high ranking. Since

FOMB (the value of which is related to the heat transfer

coefficient) is weighted the heaviest, the higher ranking

for fluids more near thermodynamic critical point is also

reflected in Tables 1-8. Further, the variation of

proximity to critical with temperature probably accounts for

the differences in ranking of the fluids for the different

bulk temperatures.

Again, because of the complexity of the functional

relationship between the properties parameters and heat

transfer coefficient (for forced convection boiling) a

detailed statistical analysis is required. Therefore, it is

difficult to specify the properties of an "ideal” fluid

which can be used as a basis for the development of a new

heat transport fluid without further analysis.

Results of Commercial Survey

A summary of some of the responses from manufacturers of

heat transport fluids is contained in Table 13. Not all

those contacted responded to the survey and in general

property data supplied was not sufficient to rank the fluids

quantitatively. However, as can seen from Table 13, the

primary obstacles to meeting the NASA requirements are that

the vapor pressure is low at room temperature and/or the

substances are toxic, flammable, or subject to decomposition

at high temperature, or a combination of all these. None of

the responses was encouraging enough to pursue detailed

property data for quantitative evaluation and ranking.

10
CONCLUSIONS AND RECOMMENDATIONS

This study leads to the conclusion that there is a need to

develop a nontoxic, nonflammable, stable heat transport

fluid for application to manned spacecraft , The following

outline is suggested for consideration:

Develop a New Substance

A more detailed statistical analysis of the relationship

between dominant physical properties and heat transfer

coefficient and pressure drop in the correlations for twophase forced-convection heat transfer is recommended. The

database and tools developed in this study can be applied in

this step. The analysis may provide guidance in the

development of a new optimum heat transport fluid, should

the development be feasible.

Since nontoxicity, nonflammability and chemical stability

at high temperatures are the qualities which are missing

from all the "good thermal performers," studies to formulate

candidate molecular structures having these attributes are

also recommended. Concurrent with this phase the

thermophysical properties of the proposed molecular

structure may be predicted using well-known group

contribution techniques or other suitable methods. The

methodology developed in our current study could then be

applied to rank the candidate fluid. A computerized expert

system could also be implemented to aid the likely iterative

process that will be necessary to zero in on a candidate

molecular structure.

11
Investigate the Possibility of Using a Mixture of Existing

Fluids

Establish a list of candidate nontoxic, nonflammable fluids.

Examine the appropriate boiling mixture heat transfer and

pressure drop correlations, using the results of the work

above to determine the dominant properties. Knowing this

will indicate which property to give most priority in trying

to find a combination of fluids, whose mixture will yield

properties that are required.

Investigate the feasibility of developing an expert system

to work backwards to find the mixture that yields the phase

equilibria and properties required.

Investigate liquid-liquid systems as an alternative to a

boiling (liquid-vapor) system.

Investigate the Catalytic Converter Technology.

The investigation of new technologies to replace or modify

the existing catalytic converter is recommended. New

concepts which would eliminate the high temperature thermal

stability constraint on candidate heat transport fluids are

needed. If the constraint were eliminated, some common

refrigerants would be viable candidates for the mannedspacecraft thermal bus application. Examples (see Tables 1-

8) are dif luoromethane ( IDN 485), chlorodifluoromethane ( IDN

369)

,

and dichlorodifluoromethane (IDN 431) . Possible new

concepts would include for example, low temperature

operation and/or selective absorption.

12
REFERENCES

[1] Parsons, P.W. , and Gaffney, B.J. "Comparing Fluids as

Heat Transfer Agents," Trans. Am. Inst. Chem. Engrs. 40,

655-673, 1944.

[2] Carberry, James J. "Media for Heat Transport," Chemical

Engineering, 225-228, June, 1953.

[3] McLinden, Mark O. "Working Fluid Selection for SpaceBased Two-Phase Heat Transport Systems," NBSIR 88-3812, U.S.

Dept, of Commerce, Gaithersburg, MD. , May 1988, issued

August 1988.

[4] PPDS , Physical Property Data Service, National

Engineering Laboratory in Association with the Institution

of Chemical Engineers, 165-171 Railway Terrace, Rugby,

Warwickshire, CV21 3 HQ, England.

[5] Rockwell-International Report, SSD84-0075, "High

Efficiency Automated Thermal Control System Study," May,

1984.

[6] Boeing Aerospace Co. Report, DRL No. T-1854, Item 2, No.

SE-973 T, "Development of a Protopype Thermal Bus for Manned

Space Station Compartments," September, 1985,

[7] Vought Corp. Design Information Release, DIR No . 2-

30320/CDIR-02 , "Alternate Fluid Trade Study for the Orbiter

Active Thermal Control Subsystem," March, 1980.

[8] Chi, S.W. "Heat Pipe Theory and Practice," Hemisphere

Publishing Corp., Washington and London, p. 160 , 1976.

[9] Ostle, Bernard and Mensing, Richard W. "Statistics in

Research," 3rd Ed., Iowa State University Press, 1975.

[10] Thomas Register of American Manufacturers Products and

Services, Thomas Publishing Co., New York, 1989.

[11] Cogan, Douglas G. , "Stones in a Glass House, CFCs and

Ozone Depletion," Investor Responsibility Research Center,

Washington, D.C., 1988.

[12] Japan Trade Directory, Japan External Trade

Organization, Publications Dept., Tokyo, 105, 1985.

[13] Collier, John G. "Convective Boiling and Condensation,"

2nd Ed.

,

McGraw-Hill Book Co.

,

New York, 1972

13
[14] Cuta, J.M., Michener Thomas E., Best, Frederick R. , and

Kachnik, Leo J. "Reduced Gravity Two-Phase Flow Experiments

in the NASA KC 135," Trans. Fifth Symp. on Space Power

Systems, 1988.

[15] Breber, G. , Palen, J.W., and Taborek, J. "Prediction of

Horizontal Tubeside Condensation of Pure Components Using

Flow Regime Criteria," J. Ht. Transf., 102:471-476, 1980.

[16] Giarratano, P.J., Arp, V.D., and Smith, R.V. "Forced

Convection Heat Transfer to Supercritical Helium,"

Cryogenics, 385-393, October, 1971.

14
TABLES

15
Table 1. Top-ranked fluids for Temperature Range 1 Tbulk = 200 K

IDN SPECIES WFFQMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

58 C3H6 PROPENE 1.000 0.494 0.778 0.991 0.836 0.988 2.121

57 C3H8 PROPANE 0.951 0.567 0.725 0.991 0.754 0.996 2.072

375 COS CARBONYL SULPHIDE 1.000 0.494 0.812 0.833 0.967 0.187 2.034

9 C4H8 BUT-1-ENE 0.770 0.903 0.478 0.991 0.754 0.952 1.957

485 CH2F2 DIFLUOROMETHANE(32) 0.951 0.494 0.800 0.797 0.820 0.171 1.938

369 CHCLF2 CHLORODIFLUOROMETHAN 0.902 0.603 0.704 0.903 0.705 0.127 1.909

8 C4H10 BUTANE 0.754 0.964 0.454 0.797 0.623 0.984 1.880

49 C4H8 2-METHYLPROPENE 0.754 0.903 0.482 0.833 0.623 0.952 1.868

431 CCL2F2 DICHLORODIFLUOROMETH 0.885 0.697 0.637 0.948 0.344 0.088 1.851

48 C4H10 ISOBUTANE 0.754 0.845 0.516 0.961 0.344 0.984 1.839

60 C3H4 PROPYNE 0.836 0.752 0.563 0.367 0.902 0.873 1.815

163 H2S HYDROGEN SULPHIDE 0.984 0.364 0.899 0.064 0.984 0.343 1.775

355 CH3CL CHLOROMETHANE(40) 0.836 0.752 0.580 0.276 0.967 0.203 1.740

154 CL2 CHLORINE 0.869 0.639 0.664 0.367 0.836 0.084 1.740

216 C3H9N TRIMETHYLAMINE 0.689 0.964 0.438 0.573 0.623 0.873 1.729

130 C2H3CL VINYL CHLORIDE 0.689 0.803 0.516 0.942 0.623 0.211 1.725

492 C2H4F2 1 , 1 - D I FLUOROETHANE(

1

0.803 0.752 0.571 0.573 0.623 0.203 1.724

436 C2CLF5 CHLOROPENTAFLUOROETH 0.885 0.603 0.700 0.276 0.820 0.084 1.722

70 NH3 AMMONIA 0.836 0.639 0.613 0.015 1.000 0.873 1.693

490 C2K3CLF2 1 -CHLORO- 1

, 1 -D I FLUOR 0.754 0.845 0.494 0.742 0.393 0.159 1.692

432 CBRCLF2 BROMOCHLORODIFLUOROM 0.689 0.903 0.468 0.961 0.262 0.040 1.672

7 C4H6 BUTA-1 ,3-DIENE 0.590 0.903 0.468 0.903 0.393 0.920 1.671

472 HBR HYDROGEN BROMIDE 0.967 0.270 0.943 0.064 0.705 0.036 1.643

467 BCL3 BORON TRICHLORIDE 0.689 1.000 0.397 0.488 0.623 0.120 1.630

649 C2H3BR VINYL BROMIDE 0.590 1.000 0.397 0.797 0.623 0.072 1.620

517 C4H80 ETHYL VINYL ETHER 0.590 0.964 0.319 0.573 0.967 0.550 1.620

177 C2H5CL CHLOROETHANE( 160) 0.525 1.000 0.397 0.797 0.754 0.235 1.597

311 C5H10 PENT- 1 -ENE 0.459 0.991 0.338 0.979 0.623 0.873 1.595

486 CH3BR BROMOMETHANE 0.689 0.964 0.424 0.197 0.820 0.052 1.568

313 C5H10 3-METHYLBUT- 1 -ENE 0.475 1.000 0.378 0.979 0.262 0.920 1.565

434 CHCL2F DICHLOROFLUOROMETHAN 0.525 0.991 0.405 0.797 0.623 0.100 1.556

64 C2H40 ACETALDEHYDE 0.459 1.000 0.352 0.694 0.967 0.494 1.551

193 C2H40 ETHYLENE OXIDE(EPOXY 0.508 0.991 0.385 0.533 0.967 0.279 1.539

42 C5H12 ISOPENTANE 0.459 0.991 0.352 0.961 0.279 0.952 1.534

578 C4H12SI TETRAMETHYLSILANE 0.590 0.991 0.352 0.367 0.557 0.813 1.529

554 CH5N METHYLAMINE 0.557 0.903 0.431 0.197 0.967 0.769 1.511

228 S02 SULPHUR DIOXIDE 0.689 0.845 0.458 0.015 0.967 0.088 1.501

109 C5H8 2-METHYLBUTA-1, 3-DIE 0.361 0.991 0.319 0.903 0.623 0.920 1.471

374 C2H6S ETHYL MERCAPTAN (ETH 0.344 0.964 0.319 0.918 0.754 0.343 1.414

312 C5H10 2-METHYLBUT- 1 -ENE 0.344 0.991 0.338 0.797 0.393 0.813 1.374

56 C5H12 PENTANE 0.361 0.964 0.319 0.742 0.393 0.920 1.363

435 C2CL2F4 1 , 2-D I CHLORO- 1

, 1 ,2,

2

0.475 0.964 0.431 0.197 0.820 0.100 1.363

483 CBR2F2 DIBROMODIFLUOROMETHA 0.426 1.000 0.364 0.833 0.148 0.024 1.354

97 C4H10O DIETHYL ETHER 0.344 0.964 0.319 0.573 0.623 0.649 1.315

423 C2H7N DIMETHYLAMINE 0.361 0.991 0.378 0.197 0.623 0.769 1.268

440 CCL3F TRICHLOROFLUOROMETHA 0.344 0.991 0.364 0.533 0.213 0.080 1.196

396 HF HYDROGEN FLUORIDE 0.459 1.000 0.397 0.064 0.148 0.195 1.186

373 CH4S METHANETHIOL 0.213 0.991 0.418 0.694 0.262 0.279 1.164

570 C2H6S DIMETHYLSULPHIDE 0.295 0.964 0.288 0.276 0.705 0.343 1.150

365 CS2 CARBON DISULPHIDE 0.213 0.903 0.288 0.533 0.836 0.151 1.122

16
Table 2. Top-ranked for Temperature Range 1, Tbulk = 250 K

IDN SPECIES WFFOMB WFN8P WFPVAP WFTMP WFLTF WFDEN TOTAL

9 C4H8 BUT- 1 -ENE 0.915 0.903 0.885 0.991 0.825 0.976 2.281

7 C4H6 BUTA-1 ,3-DIENE 0.894 0.903 0.870 0.903 0.841 0.928 2.225

48 C4H10 ISOBUTANE 0.915 0.845 0.927 0.961 0.619 0.984 2.219

49 C4H8 2-METHYLPROPENE 0.905 0.903 0.891 0.833 0.788 0.976 2.218

8 C4H10 BUTANE 0.894 0.964 0.845 0.797 0.767 0.976 2.204

130 C2H3CL VINYL CHLORIDE 0.915 0.803 0.942 0.942 0.878 0.223 2.174

57 C3H8 PROPANE 0.984 0.567 0.873 0.991 0.767 0.996 2.167

12 C4H6 1-BUTYNE 0.857 0.991 0.764 0.718 0.947 0.853 2.148

58 C3H6 PROPENE 0.995 0.494 0.838 0.991 0.841 0.992 2.141

6 C4H6 1,2-BUTADIENE 0.831 0.991 0.748 0.797 0.841 0.853 2.118

60 C3H4 PROPYNE 0.947 0.752 1.000 0.367 0.942 0.928 2.114

216 C3H9N TRIMETHYLAMINE 0.884 0.964 0.822 0.573 0.767 0.896 2.109

313 C5H10 3-METHYLBUT- 1 -ENE 0.815 1.000 0.700 0.979 0.598 0.928 2.101

373 CH4S METHANETHIOL 0.852 0.991 0.786 0.694 0.984 0.291 2.096

431 CCL2F2 DICHLORODIFLUOROMETH 0.963 0.697 0.965 0.948 0.429 0.084 2.076

492 C2H4F2 1 , 1 -DI FLUOROETHANE(

1

0.947 0.752 0.995 0.573 0.767 0.203 2.066

143 CH20 FORMALDEHYDE 0.963 0.803 0.976 0.197 0.995 0.522 2.065

369 CHCLF2 CHLORODIFLUOROMETHAN 0.979 0.603 0.873 0.903 0.741 0.112 2.060

432 CBRCLF2 BROMOCHLORODIFLUOROM 0.884 0.903 0.870 0.961 0.429 0.012 2.058

311 C5H10 PENT- 1 -ENE 0.767 0.991 0.637 0.979 0.767 0.896 2.054

177 C2H5CL CHLOROETHANE(160) 0.815 1.000 0.736 0.797 0.878 0.251 2.049

434 CHCL2F DICHLOROFLUOROMETHAN 0.831 0.991 0.756 0.797 0.767 0.084 2.029

649 C2H3BR VINYL BROMIDE 0.836 1.000 0.725 0.797 0.767 0.056 2.024

375 COS CARBONYL SULPHIDE 1.000 0.494 0.835 0.833 0.878 0.175 2.024

355 CH3CL CHLOROMETHANE(40) 0.947 0.752 1.000 0.276 0.958 0.203 2.017

109 C5H8 2-METHYLBUTA-1, 3-DIE 0.751 0.991 0.613 0.903 0.825 0.896 2.017

42 C5H12 ISOPENTANE 0.751 0.991 0.654 0.961 0.619 0.928 2.013

554 CH5N METHYLAMINE 0.873 0.903 0.865 0.197 0.989 0.793 2.007

64 C2H40 ACETALDEHYDE 0.772 1.000 0.678 0.694 0.968 0.490 1.995

193 C2H40 ETHYLENE OXIDE(EPOXY 0.815 0.991 0.740 0.533 0.984 0.291 1.992

490 C2H3CLF2 1 -CHLORO- 1

, 1 -DI FLUOR 0.884 0.845 0.905 0.742 0.429 0.151 1.992

170 C4H4 VINYL ACETYLENE 0.315 0.991 0.790 0.367 0.767 0.761 1.966

312 C5H10 2-METHYLBUT- 1 -ENE 0.746 0.991 0.627 0.797 0.741 0.853 1.965

70 NH3 AMMONIA 0.968 0.639 0.923 0.015 1.000 0.928 1.955

196 C2H20 KETENE 0.931 0.494 0.824 0.770 0.921 0.291 1.952

423 C2H7N DIMETHYLAMINE 0.825 0.991 0.753 0.197 0.926 0.853 1.952

485 CH2F2 DI FLUOROMETHANE(32) 0.963 0.494 0.795 0.797 0.825 0.171 1.949

517 C4H80 ETHYL VINYL ETHER 0.799 0.964 0.580 0.573 0.942 0.590 1.932

467 BCL3 BORON TRICHLORIDE 0.852 1.000 0.740 0.488 0.630 0.096 1.930

211 C3H5CL 2-CHLOROPROPENE 0.746 1.000 0.678 0.797 0.741 0.251 1.930

374 C2H6S ETHYL MERCAPTAN (ETH 0.704 0.964 0.594 0.918 0.921 0.378 1.920

154 CL2 CHLORINE 0.931 0.639 0.931 0.367 0.868 0.064 1.913

486 CH3BR BROMOMETHANE 0.857 0.964 0.817 0.197 0.921 0.032 1.912

56 C5H12 PENTANE 0.741 0.964 0.597 0.742 0.661 0.928 1.909

578 C4H12SI TETRAMETHYLSILANE 0.825 0.991 0.656 0.367 0.598 0.853 1.898

439 C2H2CLF3 1 -CHLORO- 2,2,2 -TR I FL 0.836 0.991 0.745 0.424 0.630 0.112 1.894

228 S02 SULPHUR DIOXIDE 0.884 0.845 0.896 0.015 0.963 0.064 1.868

97 C4H10O DIETHYL ETHER 0.741 0.964 0.594 0.573 0.810 0.689 1.863

483 CBR2F2 DIBROMODIFLUOROMETHA 0.746 1.000 0.682 0.833 0.392 0.000 1.847

117 C5H8 1,3- PENTAD lENE(CIS) 0.698 0.903 0.544 0.833 0.767 0.761 1.847

444 COCL2 PHOSGENE 0.815 0.991 0.319 0.718 0.825 0.064 1.825

17
Table 3. Top-ranked fluids for Temperature Range 1 Tbulk = 300 K

IDN SPECIES WFFOMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

9 C4H8 BUT-1-ENE 0.934 0.903 0.821 0.991 0.778 0.972 2.264

7 C4H6 BUTA- 1 ,3-DIENE 0.938 0.903 0.827 0.903 0.872 0.943 2.261

6 C4H6 1,2-BUTADIENE 0.889 0.991 0.905 0.797 0.893 0.892 2.253

311 C5H10 PENT- 1 -ENE 0.815 0.991 0.991 0.979 0.778 0.892 2.245

313 C5H10 3-METHYLBUT-1-ENE 0.852 1.000 0.967 0.979 0.560 0.928 2.237

12 C4H6 1-BUTYNE 0.872 0.991 0.891 0.718 0.893 0.857 2.204

49 C4H8 2-METHYLPROPENE 0.922 0.903 0.817 0.833 0.753 0.972 2.198

109 C5H8 2-METHYLBUTA-1, 3-DIE 0.794 0.991 0.967 0.903 0.798 0.892 2.196

42 C5H12 ISOPENTANE 0.794 0.991 1.000 0.961 0.613 0.948 2.195

8 C4H10 BUTANE 0.901 0.964 0.846 0.797 0.663 0.976 2.191

64 C2H40 ACETALDEHYDE 0.827 1.000 0.972 0.694 0.988 0.574 2.179

177 C2H5CL CHLOROETHANEC160) 0.852 1.000 0.917 0.797 0.893 0.267 2.163

48 C4H10 ISOBUTANE 0.938 0.845 0.786 0.961 0.498 0.988 2.162

312 C5H10 2-METHYLBUT- 1 -ENE 0.794 0.991 0.983 0.797 0.753 0.857 2.158

373 CH4S METHANETHIOL 0.877 0.991 0.875 0.694 0.988 0.295 2.157

216 C3H9N TRIMETHYLAMINE 0.901 0.964 0.857 0.573 0.778 0.928 2.146

374 C2H6S ETHYL MERCAPTAN (ETH 0.770 0.964 0.960 0.918 0.934 0.434 2.141

130 C2H3CL VINYL CHLORIDE 0.947 0.803 0.764 0.942 0.893 0.243 2.139

211 C3H5CL 2-CHLOROPROPENE 0.815 1.000 0.983 0.797 0.794 0.243 2.130

649 C2H3BR VINYL BROMIDE 0.852 1.000 0.943 0.797 0.778 0.056 2.129

434 CHCL2F DICHLCROFLUOROMETHAN 0.856 0.991 0.896 0.797 0.778 0.080 2.113

56 C5H12 PENTANE 0.774 0.964 0.950 0.742 0.753 0.928 2.102

193 C2H40 ETHYLENE OXIDE(EPOXY 0.852 0.991 0.899 0.533 0.988 0.295 2.094

517 C4H80 ETHYL VINYL ETHER 0.815 0.964 0.955 0.573 0.893 0.610 2.090

97 C4H10O DIETHYL ETHER 0.794 0.964 0.960 0.573 0.794 0.733 2.064

423 C2H7N DIMETHYLAMINE 0.885 0.991 0.873 0.197 0.938 0.857 2.062

117 C5H8 1 ,3-PENTADIENE(CIS) 0.761 0.903 0.899 0.833 0.794 0.781 2.060

432 C8RCLF2 BROMOCHLOROOI FLUOROM 0.901 0.903 0.832 0.961 0.296 0.020 2.035

554 CH5N METHYLAMINE 0.914 0.903 0.786 0.197 0.992 0.857 2.023

57 C3H8 PROPANE 0.988 0.567 0.638 0.991 0.498 0.992 2.022

170 C4H4 VINYL ACETYLENE 0.827 0.991 0.875 0.367 0.778 0.821 2.020

483 CBR2F2 DIBROMODIFLUOROMETHA 0.794 1.000 0.983 0.833 0.296 0.000 1.997

58 C3H6 PROPENE 0.996 0.494 0.613 0.991 0.560 0.992 1.996

467 8CL3 BORON TRICHLORIDE 0.856 1.000 0.923 0.488 0.560 0.096 1.993

60 C3H4 PROPYNE 0.955 0.752 0.705 0.367 0.872 0.948 1.992

493 C2H5BR BROMOETHANE 0.761 0.964 0.938 0.633 0.844 0.056 1.983

143 CH20 FORMALDEHYDE 0.971 0.803 0.713 0.197 0.996 0.661 1.982

422 C2H7N ETHYLAMINE 0.823 1.000 0.942 0.015 0.959 0.821 1.978

382 C3H5CL ALLYL CHLORIDE 0.728 0.903 0.899 0.770 0.893 0.227 1.972

578 C4H12SI TETRAMETHYLSILANE 0.815 0.991 1.000 0.367 0.296 0.892 1.969

182 C2H2CL2 VINYLIDENE CHLORIDE 0.733 0.991 0.980 0.694 0.613 0.143 1.965

486 CH3BR BROMOMETHANE 0.881 0.964 0.865 0.197 0.909 0.032 1.952

197 C2H402 METHYL FORMATE 0.765 0.991 0.976 0.276 0.959 0.191 1.945

116 C6H12 TRANS-4-METHYLPENT-2 0.728 0.803 0.817 0.833 0.778 0.821 1.944

492 C2H4F2 1 , 1 -DI FLUQROETHANE(

1

0.967 0.752 0.696 0.573 0.613 0.243 1.940

396 HF HYDROGEN FLUORIDE 0.877 1.000 0.965 0.064 0.663 0.207 1.935

570 C2H6S DIMETHYLSULPHIDE 0.765 0.964 0.943 0.276 0.938 0.343 1.929

827 C6H12 3,3-DIMETHYLBUT-1-EN 0.737 0.903 0.923 0.573 0.560 0.857 1.927

440 CCL3F TRICHLOROFLUOROMETHA 0.770 0.991 0.991 0.533 0.498 0.056 1.927

431 CCL2F2 DICHLORODIFLUOROMETH 0.955 0.697 0.689 0.948 0.247 0.096 1.922

196 C2H2Q KETENE 0.971 0.494 0.597 0.770 0.938 0.470 1.922

18
Table 4. Top-ranked fluids for Temperature Range 1, Tbulk = 350 K

IDN SPECIES WFFOMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

48 C4H10 ISOBUTANE 0.944 0.845 0.605 0.961 0.996 0.988 2.195

6 C4H6 1,2-BUTADIENE 0.908 0.991 0.680 0.797 0.829 0.920 2.173

7 C4H6 BUTA-1, 3-DIENE 0.944 0.903 0.630 0.903 0.697 0.952 2.153

109 C5H8 2-METHYLBUTA-1, 3-DIE 0.805 0.991 0.795 0.903 0.801 0.900 2.139

311 C5H10 PENT- 1 -ENE 0.837 0.991 0.764 0.979 0.578 0.900 2.137

313 C5H10 3-METHYLBUT- 1 -ENE 0.869 1.000 0.722 0.979 0.382 0.940 2.122

42 C5H12 ISOPENTANE 0.829 0.991 0.756 0.961 0.498 0.940 2.108

9 C4H8 BUT-1-ENE 0.936 0.903 0.625 0.991 0.382 0.968 2.108

64 C2H40 ACETALDEHYDE 0.857 1.000 0.713 0.694 0.972 0.622 2.107

432 CBRCLF2 BROMOCHLOROO I FLUOROM 0.908 0.903 0.633 0.961 0.996 0.028 2.103

12 C4H6 1-BUTYNE 0.845 0.991 0.676 0.718 0.829 0.900 2.082

374 C2H6S ETHYL MERCAPTAN (ETH 0.781 0.964 0.790 0.918 0.920 0.414 2.080

177 C2H5CL CHLOROETHANE(160) 0.869 1.000 0.689 0.797 0.801 0.275 2.071

373 CH4S METHANETH IOL 0.876 0.991 0.656 0.694 0.952 0.375 2.071

312 C5H10 2-METHYLBUT-1 -ENE 0.821 0.991 0.768 0.797 0.578 0.869 2.065

8 C4H10 BUTANE 0.920 0.964 0.646 0.797 0.299 0.968 2.056

56 C5H12 PENTANE 0.813 0.964 0.803 0.742 0.629 0.920 2.056

211 C3H5CL 2-CHLOROPROPENE 0.837 1.000 0.725 0.797 0.801 0.243 2.050

49 C4H8 2-METHYLPROPENE 0.936 0.903 0.625 0.833 0.299 0.968 2.044

117 C5H8 1 ,3- PENTAD I ENE (CIS) 0.765 0.903 0.845 0.833 0.761 0.801 2.037

517 C4H80 ETHYL VINYL ETHER 0.829 0.964 0.795 0.573 0.841 0.653 2.034

193 C2H40 ETHYLENE OXIDE(EPOXY 0.876 0.991 0.668 0.533 0.976 0.375 2.032

130 C2H3CL VINYL CHLORIDE 0.952 0.803 0.594 0.942 0.649 0.275 2.031

216 C3H9N TRIMETHYLAMINE 0.908 0.964 0.656 0.573 0.498 0.940 2.018

649 C2H3BR VINYL BROMIDE 0.857 1.000 0.710 0.797 0.649 0.052 2.015

578 C4H12SI TETRAMETHYLSILANE 0.813 0.991 0.761 0.367 0.996 0.920 2.014

97 C4H10O DIETHYL ETHER 0.821 C.964 0.786 0.573 0.697 0.761 2.004

434 CHCL2F DICHLOROFLUOROMETHAN 0.876 0.991 0.671 0.797 0.578 0.084 2.003

423 C2H7N DIMETHYLAMINE 0.912 0.991 0.648 0.197 0.912 0.900 1.999

492 C2H4F2 1 , 1 -DI FLUOROETHANEC

1

0.976 0.752 0.538 0.573 0.996 0.514 1.989

116 C6H12 TRANS-4-METHYLPENT-2 0.745 0.803 0.910 0.833 0.697 0.841 1.984

439 C2H2CLF3 1 -CHLORO-2,2, 2-TRI FL 0.880 0.991 0.656 0.424 0.996 0.131 1.978

382 C3H5CL ALLYL CHLORIDE 0.753 0.903 0.846 0.770 0.892 0.211 1 .973

46 C6H14 ISOHEXANE 0.717 0.803 0.923 0.942 0.578 0.869 1 .973

554 CH5N METHYLAMINE 0.936 0.903 0.577 0.197 0.992 0.900 1 .966

493 C2H5BR BROMOETHANE 0.781 0.964 0.817 0.633 0.892 0.052 1.963

444 C0CL2 PHOSGENE 0.884 0.991 0.568 0.718 0.649 0.072 1.960

490 C2H3CLF2 1 -CHLORO- 1

, 1 -DI FLUOR 0.904 0.845 0.597 0.742 0.757 0.175 1 .957

103 C6H12 HEX- 1 -ENE 0.713 0.803 0.942 0.833 0.649 0.841 1.955

57 C3H8 PROPANE 0.988 0.567 0.510 0.991 0.398 0.992 1.952

632 C6H12 2-METHYLPENT-1 -ENE 0.713 0.803 0.931 0.797 0.649 0.801 1.936

422 C2H7N ETHYLAMINE 0.880 1.000 0.684 0.015 0.944 0.841 1.932

827 C6H12 3,3-DIMETHYLBUT- 1 -EN 0.781 0.903 0.832 0.573 0.498 0.869 1.923

170 C4H4 VINYL ACETYLENE 0.845 0.991 0.671 0.367 0.578 0.841 1.918

518 C5H100 ETHYL ALLYL ETHER 0.665 0.752 0.960 0.961 0.697 0.622 1.915

58 C3H6 PROPENE 1.000 0.494 0.499 0.991 0.359 0.992 1.915

397 C5H120 ETHYL PROPYL ETHER 0.713 0.803 0.938 0.718 0.697 0.685 1.913

634 C6H12 2-ETHYLBUT- 1 -ENE 0.697 0.752 0.943 0.742 0.801 0.761 1.909

396 HF HYDROGEN FLUORIDE 0.916 1.000 0.707 0.064 0.841 0.227 1.909

431 CCL2F2 DICHLORODIFLUOROMETH 0.964 0.697 0.541 0.948 0.398 0.131 1.906

182 C2H2CL2 VINYLIDENE CHLORIDE 0.765 0.991 0.770 0.694 0.578 0.131 1.905

19
Table 5. Top-ranked fluids for Temperature Range 2, Tbulk = 275 K

IDN SPECIES WFFOMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

7 C4H6 BUTA-1 ,3-DIENE 0.951 0.942 0.971 0.950 0.909 0.964 2.373

9 C4H8 BUT-1 -ENE 0.951 0.942 0.960 0.995 0.850 0.982 2.373

10 C4H8 2-BUTENECCIS) 0.937 0.977 0.992 0.915 0.909 0.942 2.372

8 C4H10 BUTANE 0.941 0.977 0.992 0.897 0.775 0.984 2.349

6 C4H6 1,2-BUTADIENE 0.920 0.992 0.951 0.897 0.909 0.917 2.340

12 C4H6 1-BUTYNE 0.920 0.992 0.971 0.857 0.944 0.887 2.339

49 C4H8 2-METHYLPROPENE 0.941 0.942 0.955 0.915 0.799 0.982 2.327

11 C4H8 2-BUTENE(TRANS) 0.941 0.977 1.000 0.709 0.850 0.972 2.310

216 C3H9N TRIMETHYLAMINE 0.932 0.977 1.000 0.783 0.799 0.942 2.310

48 C4H10 ISOBUTANE 0.951 0.912 0.926 0.979 0.623 0.994 2.295

373 CH4S METHANETHIOL 0.918 0.992 0.982 0.845 0.986 0.338 2.291

111 C2H6Q METHYL ETHER 0.970 0.850 0.847 0.933 0.909 0.855 2.281

313 C5H10 3-METHYLBUT-1-ENE 0.890 1.000 0.897 0.988 0.623 0.942 2.264

423 C2H7N DIMETHYLAMINE 0.920 0.992 0.973 0.595 0.948 0.887 2.262

109 C5H8 2-METHYLBUTA-1, 3-DIENE (ISOP 0.890 0.992 0.816 0.950 0.850 0.942 2.262

130 C2H3CL VINYL CHLORIDE 0.951 0.882 0.912 0.970 0.909 0.286 2.258

554 CH5N METHYLAMINE 0.937 0.942 0.951 0.595 0.988 0.887 2.253

177 C2H5CL CHLOROETHANE(160) 0.890 1.000 0.942 0.897 0.909 0.316 2.249

66 C3H4 ALLENE 0.977 0.786 0.800 0.897 0.946 0.982 2.246

64 C2H40 ACETALDEHYDE 0.874 1.000 0.888 0.845 0.986 0.583 2.238

311 C5H10 PENT-1-ENE 0.857 0.992 0.838 0.988 0.799 0.917 2.236

170 C4H4 VINYL ACETYLENE 0.838 0.992 0.982 0.680 0.850 0.855 2.236

193 C2H40 ETHYLENE OX IDE (EPOXYETHANE) 0.890 0.992 0.951 0.763 0.986 0.338 2.227

60 C3H4 PROPYNE 0.972 0.850 0.852 0.680 0.927 0.964 2.223

42 C5H12 ISOPENTANE 0.855 1.000 0.852 0.979 0.674 0.964 2.220

649 C2H3BR VINYL BROMIDE 0.902 1.000 0.926 0.897 0.850 0.068 2.218

434 CHCL2F DICHLOROFLUOROMETHANE(21

)

0.895 0.992 0.961 0.897 0.799 0.109 2.215

143 CH20 FORMALDEHYDE 0.972 0.882 0.874 0.595 0.993 0.638 2.203

120 C5H10 2-PENTENE(CIS) 0.845 0.977 0.791 0.965 0.850 0.917 2.202

312 C5H10 2-METHYLBUT-1-ENE 0.848 0.992 0.831 0.897 0.799 0.917 2.197

121 C5H10 2-PENTENECTRANS) 0.848 0.977 0.796 0.915 0.850 0.917 2.191

97 C4H100 DIETHYL ETHER 0.890 0.992 0.806 0.783 0.850 0.773 2.191

57 C3H8 PROPANE 0.986 0.715 0.753 0.995 0.719 0.998 2.187

486 CH3BR BROMOMETHANE 0.920 0.977 0.995 0.595 0.944 0.046 2.179

58 C3H6 PROPENE 0.995 0.671 0.724 0.995 0.799 0.996 2.178

432 CBRCLF2 BROMQCHLQROD I FlUOROMETHANE (

1

0.932 0.942 0.973 0.979 0.419 0.026 2.172

517 C4H80 ETHYL VINYL ETHER 0.869 0.992 0.796 0.783 0.946 0.638 2.171

56 C5H12 PENTANE 0.845 0.977 0.800 0.869 0.775 0.964 2.166

211 C3H5CL 2-CHLOROPROPENE 0.852 1.000 0.878 0.897 0.799 0.316 2.164

374 C2H6S ETHYL MERCAPTAN (ETHANETHIOL 0.827 0.992 0.806 0.958 0.944 0.425 2.164

110 C5H10 2-METHYL -2- BUTENE 0.838 0.977 0.779 0.883 0.850 0.887 2.162

492 C2H4F2 1 , 1 -DI FLUOROETHANE( 152A) 0.970 0.850 0.842 0.783 0.799 0.286 2.155

467 BCL3 BORON TRICHLORIDE 0.918 1.000 0.939 0.741 0.623 0.129 2.153

422 C2H7N ETHYLAMINE 0.855 1.000 0.904 0.487 0.956 0.855 2.139

355 CH3CL CHLOROMETHANE(40) 0.956 0.850 0.852 0.634 0.965 0.268 2.131

578 C4H12SI TETRAMETHYLSILANE 0.874 1.000 0.858 0.680 0.576 0.917 2.127

117 C5H8 1 ,3-PENTAD I ENE(CIS) 0.822 0.942 0.739 0.915 0.850 0.809 2.114

490 C2H3CLF2 1 -CHLORO- 1

, 1 -DI FLUOROETHANE( 0.923 0.912 0.927 0.869 0.419 0.181 2.112

228 S02 SULPHUR DIOXIDE 0.941 0.912 0.926 0.445 0.977 0.109 2.108

70 NH3 AMMONIA 0.972 0.786 0.771 0.445 1.000 0.964 2.103

20
Table 6. Top-ranked fluids for Temperature Range 2, Tbulk = 290 K

IDN SPECIES WFFOMB UFNBP UFPVAP WFTMP WFLTF WFDEN TOTAL

6 C4H6 1,2-BUTADIENE 0.929 0.992 0.973 0.897 0.912 0.920 2.358

10 C4H8 2-BUTENE(CIS) 0.946 0.977 0.927 0.915 0.871 0.964 2.351

7 C4H6 BUTA-1, 3-DIENE 0.959 0.942 0.888 0.950 0.912 0.964 2.349

9 C4H8 BUT-1-ENE 0.957 0.942 0.878 0.995 0.826 0.980 2.341

12 C4H6 1-BUTYNE 0.921 0.992 0.955 0.857 0.925 0.893 2.330

8 C4H10 BUTANE 0.948 0.977 0.909 0.897 0.773 0.984 2.323

109 C5H8 2-METHYLBUTA-1, 3-DIENE (ISOP 0.906 0.992 0.904 0.950 0.852 0.940 2.313

313 C5H10 3-METHYLBUT-1 -ENE 0.906 1.000 0.989 0.988 0.605 0.940 2.313

49 C4H8 2-HETHYLPROPENE 0.953 0.942 0.877 0.915 0.807 0.980 2.309

311 C5H10 PENT-1-ENE 0.878 0.992 0.927 0.988 0.807 0.920 2.295

64 C2H40 ACETALDEHYDE 0.882 1.000 0.982 0.845 0.983 0.606 2.285

177 C2H5CL CHLOROETHANE(160) 0.906 1.000 0.980 0.897 0.912 0.324 2.281

11 C4H8 2-BUTENE(TRANS) 0.946 0.977 0.916 0.709 0.850 0.970 2.281

216 C3H9N TRIMETHYLAMINE 0.929 0.977 0.926 0.783 0.807 0.940 2.279

373 CH4S METHANETHIOL 0.921 0.992 0.942 0.845 0.983 0.342 2.278

48 C4H10 ISOBUTANE 0.959 0.912 0.852 0.979 0.605 0.994 2.270

423 C2H7N DIMETHYLAMINE 0.929 0.992 0.942 0.595 0.951 0.920 2.263

42 C5H12 ISOPENTANE 0.865 1.000 0.942 0.979 0.652 0.964 2.262

120 C5H10 2-PENTENE(CIS) 0.861 0.977 0.892 0.965 0.852 0.920 2.258

111 C2H60 METHYL ETHER 0.974 0.850 0.767 0.933 0.912 0.893 2.258

312 C5H10 2 -METHYL BUT- 1 -ENE 0.865 0.992 0.923 0.897 0.807 0.920 2.253

193 C2H40 ETHYLENE OX I DEC EPOXYETHANE) 0.906 0.992 0.971 0.763 0.985 0.342 2.250

97 C4H100 DIETHYL ETHER 0.906 0.992 0.899 0.783 0.850 0.785 2.245

121 C5H10 2-PENTENECTRANS) 0.861 0.977 0.894 0.915 0.850 0.920 2.243

649 C2H3BR VINYL BROMIDE 0.906 1.000 0.995 0.897 0.807 0.072 2.241

130 C2H3CL VINYL CHLORIDE 0.961 0.882 0.838 0.970 0.912 0.296 2.240

170 C4H4 VINYL ACETYLENE 0.897 0.992 0.942 0.680 0.850 0.861 2.230

554 CH5N METHYLAMINE 0.948 0.942 0.861 0.595 0.989 0.893 2.230

434 CHCL2F DICHLOROFLUOROMETHANEC21

)

0.906 0.992 0.961 0.897 0.807 0.111 2.228

211 C3H5CL 2-CHLOROPROPENE 0.865 1.000 0.973 0.897 0.850 0.324 2.225

110 C5H10 2-METHYL -2- BUTENE 0.858 0.977 0.878 0.883 0.852 0.893 2.223

374 C2H6S ETHYL MERCAPTAN (ETHANETHIOL 0.843 0.992 0.899 0.958 0.951 0.443 2.221

56 C5H12 PENTANE 0.861 0.977 0.897 0.869 0.773 0.964 2.220

517 C4H80 ETHYL VINYL ETHER 0.878 0.992 0.897 0.783 0.925 0.640 2.216

66 C3H4 ALLENE 0.981 0.786 0.721 0.897 0.925 0.980 2.214

422 C2H7N ETHYLAMINE 0.882 1.000 1.000 0.487 0.966 0.861 2.207

143 CH20 FORMALDEHYDE 0.974 0.882 0.791 0.595 0.994 0.688 2.178

117 C5H8 1,3-PENTADIENECCIS) 0.839 0.942 0.847 0.915 0.850 0.817 2.175

467 BCL3 BORON TRICHLORIDE 0.916 1.000 0.982 0.741 0.605 0.129 2.165

486 CH3BR BROMOMETHANE 0.927 0.977 0.926 0.595 0.942 0.046 2.158

60 C3H4 PROPYNE 0.931 0.850 0.775 0.680 0.912 0.964 2.149

167 C3H60 PROPYLENE OXIDEC1 ,2-EPOXYPRO 0.839 0.992 0.894 0.763 0.912 0.443 2.149

578 C4H12SI TETRAMETHYLSILANE 0.878 1.000 0.948 0.680 0.457 0.920 2.144

432 CBRCLF2 BROMOCHLOROD I FLUOROMET HANE (

1

0.938 0.942 0.892 0.979 0.391 0.026 2.140

57 C3H8 PROPANE 0.987 0.715 0.689 0.995 0.605 0.996 2.139

556 C3H9N ISOPROPYLAMINE 0.835 0.992 0.912 0.595 0.807 0.861 2.121

827 C6H12 3,3-DIMETHYLBUT-1 -ENE 0.835 0.977 0.870 0.783 0.605 0.920 2.119

58 C3H6 PROPENE 0.994 0.671 0.653 0.995 0.652 0.996 2.119

483 CBR2F2 D I BROMOD I F LUOROME T HANE ( 1 2B2

)

0.861 1.000 0.973 0.915 0.457 0.008 2.116

826 C6H12 2,3-DIMETHYLBUT-1-ENE 0.811 0.912 0.783 0.973 0.773 0.861 2.113

197 C2H402 METHYL FORMATE 0.843 0.992 0.912 0.634 0.968 0.235 2.111

21
Table 7. Top-ranked fluids for Temperature Range 2, Tbulk = 305 K

IDN SPECIES WFFOMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

109 C5H8 2-METHYLBUTA-1 ,3-DIENE (ISOP 0.893 0.992 0.992 0.950 0.842 0.936 2.333

6 C4H6 1,2-BUTADIENE 0.934 0.992 0.894 0.897 0.912 0.920 2.332

311 C5H1Q PENT- 1 -ENE 0.885 0.992 0.995 0.988 0.797 0.936 2.329

7 C4H6 BUTA-1, 3-DIENE 0.961 0.942 0.819 0.950 0.904 0.962 2.322

10 C4H8 2-BUTENE(CIS) 0.943 0.977 0.861 0.915 0.842 0.962 2.315

9 C4H8 BUT- 1 -ENE 0.961 0.942 0.813 0.995 0.760 0.978 2.306

120 C5H10 2-PENTENE(CIS) 0.865 0.977 0.980 0.965 0.842 0.920 2.295

313 C5H10 3-METHYLBUT-1 -ENE 0.908 1.000 0.942 0.988 0.588 0.962 2.295

12 C4H6 1-BUTYNE 0.916 0.992 0.877 0.857 0.912 0.920 2.295

42 C5H12 ISOPENTANE 0.879 1.000 0.985 0.979 0.627 0.962 2.288

64 C2H40 ACETALDEHYDE 0.900 1.000 0.942 0.845 0.980 0.616 2.287

121 C5H10 2-PENTENE(TRANS) 0.865 0.977 0.982 0.915 0.842 0.920 2.281

312 C5H10 2-METHYLBUT- 1 -ENE 0.865 0.992 1.000 0.897 0.760 0.920 2.274

97 C4H10O DIETHYL ETHER 0.893 0.992 0.989 0.783 0.842 0.791 2.268

8 C4H10 BUTANE 0.947 0.977 0.838 0.897 0.635 0.984 2.265

374 C2H6S ETHYL MERCAPTAN (ETHANETHIOL 0.850 0.992 0.989 0.958 0.943 0.469 2.265

110 C5H10 2 -METHYL -2- BUTENE 0.865 0.977 0.971 0.883 0.842 0.895 2.264

49 C4H8 2-METHYLPROPENE 0.955 0.942 0.810 0.915 0.686 0.978 2.260

373 CH4S METHANETHIOL 0.928 0.992 0.867 0.845 0.977 0.388 2.259

517 C4H80 ETHYL VINYL ETHER 0.885 0.992 0.985 0.783 0.912 0.646 2.257

56 C5H12 PENTANE 0.865 0.977 0.982 0.869 0.760 0.962 2.255

177 C2H5CL CHLOROETHANE( 160) 0.908 1.000 0.899 0.897 0.904 0.322 2.249

11 C4H8 2-BUTENE(TRANS) 0.947 0.977 0.842 0.709 0.797 0.968 2.241

423 C2H7N DIMETHYLAMINE 0.934 0.992 0.865 0.595 0.947 0.920 2.236

211 C3H5CL 2-CHLOROPROPENE 0.879 1.000 0.960 0.897 0.842 0.322 2.233

48 C4H10 ISOBUTANE 0.961 0.912 0.783 0.979 0.543 0.994 2.232

193 C2H40 ETHYLENE OX IDE (EPOXYETHANE ) 0.914 0.992 0.888 0.763 0.982 0.352 2.226

649 C2H3BR VINYL BROMIDE 0.914 1.000 0.918 0.897 0.797 0.070 2.217

111 C2H60 METHYL ETHER 0.973 0.850 0.700 0.933 0.842 0.895 2.216

117 C5H8 1,3-PENTADIENE(CIS) 0.842 0.942 0.939 0.915 0.842 0.831 2.215

130 C2H3CL VINYL CHLORIDE 0.963 0.882 0.767 0.970 0.904 0.304 2.213

554 CH5N METHYLAMI NE 0.953 0.942 0.779 0.595 0.988 0.920 2.204

167 C3H60 PROPYLENE OX I DE ( 1 ,2-EPOXYPRO 0.850 0.992 0.989 0.763 0.912 0.469 2.201

216 C3H9N TRIMETHYLAMINE 0.879 0.977 0.858 0.783 0.797 0.936 2.199

434 CHCL2F DICHLOROFLUOROMETHANE(21

)

0.914 0.992 0.878 0.897 0.760 0.109 2.193

170 C4H4 VINYL ACETYLENE 0.900 0.992 0.867 0.680 0.797 0.863 2.192

422 C2H7N ETHYLAMINE 0.900 1.000 0.912 0.487 0.965 0.863 2.190

66 C3H4 ALLENE 0.977 0.786 0.648 0.897 0.904 0.984 2.178

556 C3H9N ISOPROPYLAMINE 0.846 0.992 1.000 0.595 0.797 0.863 2.167

827 C6H12 3,3-DIMETHYLBUT-l-ENE 0.842 0.977 0.960 0.783 0.588 0.920 2.159

826 C6H12 2,3-DIMETHYLBUT- 1 -ENE 0.822 0.912 0.877 0.973 0.760 0.863 2.159

197 C2H402 METHYL FORMATE 0.850 0.992 1.000 0.634 0.965 0.237 2.154

493 C2H5BR BROMOETHANE 0.842 0.977 0.971 0.813 0.904 0.083 2.152

570 C2H6S DIMETHYLSULPHIDE 0.850 0.977 0.975 0.634 0.947 0.388 2.147

114 C6H12 4-METHYLPENT-1-ENE 0.828 0.912 0.888 0.970 0.635 0.895 2.147

382 C3H5CL ALLYL CHLORIDE 0.828 0.942 0.931 0.883 0.912 0.270 2.146

143 CH20 FORMALDEHYDE 0.973 0.882 0.710 0.595 0.992 0.702 2.145

115 C6H12 CIS-4-METHYLPENT-2-ENE 0.828 0.912 0.874 0.897 0.760 0.895 2.144

19 C5H8 CYCLOPENTENE 0.801 0.942 0.939 0.883 0.842 0.616 2.143

578 C4H12SI TETRAMETHYLSILANE 0.879 1.000 0.982 0.680 0.357 0.920 2.139

633 C6H12 3-METHYLPENT- 1 -ENE 0.828 0.912 0.888 0.970 0.588 0.895 2.137

22
Table 8. Top-ranked fluids for Temperature Range 2, Tbulk = 320 K

IDN SPECIES WFFOMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

6 C4H6 1,2- BUTADIENE 0.940 0.992 0.824 0.897 0.909 0.932 2.310

120 C5H10 2-PENTENE(CIS) 0.875 0.977 0.955 0.965 0.839 0.918 2.295

311 C5H10 PENT- 1 -ENE 0.887 0.992 0.918 0.988 0.750 0.932 2.290

7 C4H6 BUTA-1, 3-DIENE 0.962 0.942 0.747 0.950 0.873 0.964 2.288

10 C4H8 2-BUTENE(CIS) 0.942 0.977 0.791 0.915 0.819 0.964 2.282

109 C5H8 2-METHYLBUTA-1, 3-DIENE (ISOP 0.859 0.992 0.942 0.950 0.841 0.932 2.278

110 C5H10 2-METHYL -2- BUTENE 0.875 0.977 0.967 0.883 0.839 0.893 2.272

121 C5H10 2-PENTENE(TRANS) 0.875 0.977 0.951 0.915 0.791 0.918 2.268

12 C4H6 1-BUTYNE 0.917 0.992 0.810 0.857 0.909 0.918 2.268

313 C5H10 3-METHYLBUT-1 -ENE 0.911 1.000 0.874 0.988 0.569 0.956 2.266

42 C5H12 ISOPENTANE 0.887 1.000 0.909 0.979 0.624 0.956 2.264

64 C2H40 ACETALDEHYDE 0.901 1.000 0.870 0.845 0.978 0.626 2.260

374 C2H6S ETHYL MERCAPTAN (ETHANETHIOL 0.859 0.992 0.942 0.958 0.944 0.483 2.256

312 C5H10 2-METHYLBUT-1 -ENE 0.877 0.992 0.923 0.897 0.750 0.918 2.253

9 C4H8 BUT- 1 -ENE 0.958 0.942 0.739 0.995 0.634 0.976 2.248

517 C4H80 ETHYL VINYL ETHER 0.887 0.992 0.948 0.783 0.909 0.664 2.245

8 C4H10 BUTANE 0.948 0.977 0.771 0.897 0.624 0.982 2.237

56 C5H12 PENTANE 0.875 0.977 0.951 0.869 0.666 0.956 2.234

117 C5H8 1,3-PENTADIENE(CIS) 0.849 0.942 0.992 0.915 0.791 0.837 2.233

373 CH4S METHANETHIOL 0.924 0.992 0.796 0.845 0.976 0.402 2.228

177 C2H5CL CHLOROETHANE( 160) 0.911 1.000 0.831 0.897 0.879 0.326 2.220

49 C4H8 2-METHYLPROPENE 0.956 0.942 0.739 0.915 0.624 0.976 2.220

423 C2H7N DIMETHYLAMINE 0.940 0.992 0.786 0.595 0.946 0.918 2.211

211 C3H5CL 2-CHLOROPROPENE 0.887 1.000 0.883 0.897 0.839 0.326 2.209

193 C2H40 ETHYLENE OX IDE (EPOXYETHANE) 0.917 0.992 0.816 0.763 0.978 0.354 2.199

167 C3H60 PROPYLENE OXIDE( 1

, 2-EPOXYPRO 0.859 0.992 0.939 0.763 0.918 0.483 2.192

97 C4H100 DIETHYL ETHER 0.841 0.992 0.939 0.783 0.819 0.795 2.191

11 C4H8 2-BUTENECTRANS) 0.946 0.977 0.775 0.709 0.666 0.972 2.188

649 C2H3BR VINYL BROMIDE 0.917 1.000 0.858 0.897 0.750 0.070 2.186

111 C2H60 METHYL ETHER 0.976 0.850 0.632 0.933 0.791 0.918 2.184

115 C6H12 CIS-4-METHYLPENT-2-ENE 0.835 0.912 0.960 0.897 0.750 0.893 2.183

382 C3H5CL ALLYL CHLORIDE 0.835 0.942 0.995 0.883 0.918 0.272 2.180

130 C2H3CL VINYL CHLORIDE 0.964 0.882 0.704 0.970 0.841 0.326 2.178

826 C6H12 2,3-DIMETHYLBUT- 1 -ENE 0.825 0.912 0.961 0.973 0.666 0.869 2.177

554 CH5N METHYLAMINE 0.956 0.942 0.706 0.595 0.984 0.918 2.177

422 C2H7N ETHYLAMINE 0.917 1.000 0.838 0.487 0.958 0.869 2.176

116 C6H12 TRANS-4-METHYLPENT-2-ENE 0.833 0.882 0.942 0.915 0.791 0.893 2.173

114 C6H12 4-METHYLPENT-1 -ENE 0.833 0.912 0.971 0.970 0.569 0.893 2.171

19 C5H8 CYCLOPENTENE 0.807 0.942 0.992 0.883 0.839 0.626 2.170

827 C6H12 3,3-DIMETHYLBUT-1 -ENE 0.849 0.977 0.980 0.783 0.569 0.918 2.170

48 C4H10 ISOBUTANE 0.960 0.912 0.721 0.979 0.356 0.994 2.169

633 C6H12 3-METHYLPENT- 1 -ENE 0.825 0.912 0.971 0.970 0.569 0.893 2.163

493 C2H5BR BROMOETHANE 0.855 0.977 0.961 0.813 0.909 0.083 2.162

170 C4H4 VINYL ACETYLENE 0.901 0.992 0.800 0.680 0.750 0.869 2.157

434 CHCL2F DICHLOROFLUOROMETHANE(21

)

0.917 0.992 0.813 0.897 0.666 0.119 2.152

383 C3H7CL 1 -CHLOROPROPANE 0.825 0.942 1.000 0.845 0.841 0.326 2.151

118 C5H8 1 , 3-PENTAD I ENE (TRANS) 0.855 0.977 0.982 0.554 0.791 0.869 2.147

570 C2H6S DIMETHYLSULPHIDE 0.855 0.977 0.960 0.634 0.946 0.402 2.147

556 C3H9N ISOPROPYLAMINE 0.859 0.992 0.918 0.595 0.791 0.869 2.146

216 C3H9N TRIMETHYLAMINE 0.873 0.977 0.786 0.783 0.666 0.956 2.140

445 C3H802 DIMETHOXYMETHANE 0.835 0.977 0.980 0.709 0.839 0.402 2.136

23
Table 9. Comparison of ranking factors for water and ammonia with those for the top-ranked fluids.

I DM SPECIES WFFOMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

7 C4H6 BUTA- 1, 3-D I EWE 0.951 0.942 0.971 0.950 0.909 0.964 2.37

70 NH3 AMMONIA 0.972 0.786 0.771 0.445 1.000 0.964 2.10

63 H20 WATER 0.159 0.715 0.223 0.008 0.998 0.229 0.83

IDN SPECIES WFFOMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

6 C4H6 1,2-BUTADIENE 0.929 0.992 0.973 0.897 0.912 0.920 2.36

70 NH3 AMMONIA 0.981 0.786 0.685 0.445 0.998 0.970 2.08

63 H20 WATER 0.130 0.715 0.346 0.008 1.000 0.227 0.90

IDN SPECIES WFFOMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

109 C5H8 2-METHYLBUTA-1, 3-DIENE (ISOP 0.893 0.992 0.992 0.950 0.842 0.936 2.33

70 NH3 AMMONIA 0.982 0.786 0.602 0.445 0.996 0.968 2.04

63 H20 WATER 0.279 0.715 0.501 0.008 1.000 0.227 1.06

IDN SPECIES WFFOMB WFNBP WFPVAP WFTMP WFLTF WFDEN TOTAL

6 C4H6 1,2-BUTADIENE 0.940 0.992 0.824 0.897 0.909 0.932 2.31

70 NH3 AMMONIA 0.982 0.786 0.524 0.445 0.996 0.972 2.01

63 H20 WATER 0.374 0.715 0.648 0.008 1.000 0.225 1.22

24
Table 10. Product of reduced temperature and pressure for top and bottom ranked fluids in Temperature Range 2. (Ranking on the basis of thermal performance- FOMB)

top ranked by FOMB

275 K

IDN SPECIES TRED*PRED

482 CBRF3 BROMOTRI FLU0R0METHANE(13B1

)

0.1811

375 COS CARBONYL SULPHIDE 0.0801

155 HCL HYDROGEN CHLORIDE 0.2725

163 H2S HYDROGEN SULPHIDE 0.0893

58 C3H6 PROPENE 0.1011

485 CH2F2 DIFLUOROMETHANE(32) 0.1160

57 C3H8 PROPANE 0.0876

369 CHCLF2 CHLORODI FLUOROMETHANE(22) 0.0790

436 C2CLF5 CHLOROPENTAFLUOROETHANE( 1 15) 0.1165

472 HBR HYDROGEN BROMIDE 0.1141

66 C3H4 ALLENE 0.0517

70 NH3 AMMONIA 0.0276

143 CH20 FORMALDEHYDE 0.0235

60 C3H4 PROPYNE 0.0334

111 C2H60 METHYL ETHER 0.0375

431 CCL2F2 D I CHLORODI FLUOROMETHANEC 12) 0.0568

492 C2H4F2 1 , 1 -DI FLUOROETHANE( 152A) 0.0460

196 C2H20 KETENE 0.0932

355 CH3CL CHLOROMETHANEC40) 0.0272

154 CL2 CHLORINE 0.0324

130 C2H3CL VINYL CHLORIDE 0.0231

9 C4H8 BUT- 1 -ENE 0.0224

48 C4H10 ISOBUTANE 0.0309

7 C4H6 BUTA-1, 3-DIENE 0.0192

49 C4H8 2-METHYLPROPENE 0.0233

25
Table 10 (continued)

bottom ranked by FOMB

275 K

IDN SPECIES TRED*PRED

607 C7H7CL O-CHLOROTOLUENE 0.0000

680 C6H15N N-HEXYLAMINE 0.0000

67 C3H60 PROP-2-ENE-1-OL 0.0001

331 C7H14 CYCLOHEPTANE 0.0001

500 C9F20 PERFLUORONONANE 0.0001

279 C9H20 2,2,3,3-TETRAMETHYLPENTANE 0.0000

506 C6H5BR BROMOBENZENE 0.0000

711 C5H80 CYCLOPENTANONE 0.0000

426 C5H11N PIPERIDINE 0.0001

805 C4H5N PYRROLE 0.0000

371 C4H6CL2 1 ,3-DICHLOROBUTENE-2(TRANS) 0.0000

859 C10H16 ALPHA-PINENE 0.0000

229 C3H802 ETHYLENE GLYCOL MONOMETHYL E 0.0000

389 C2H2CL4 1 , 1 ,2,2-TETRACHLOROETHANE 0.0000

706 C8H14 CYCLOOCTENE 0.0000

385 C3H5CL3 1-2-3 TRICHLOROPROPANE 0.0000

39 C3H80 PROPAN-2-OL 0.0001

81 C6H100 CYCLOHEXANONE 0.0000

731 C4H9NQ MORPHOLINE 0.0000

59 C3H80 PROPAN- 1-OL 0.0000

390 C2HCL5 PENTACHLOROETHANE( 120) 0.0000

510 C10F18 PERFLUORODECALIN 0.0001

172 C4H100 BUTAN-2-OL(SECBUTANOL) 0.0000

171 C4H100 2-METHYLPROPAN- 1 -OL( ISOBUTAN 0.0000

189 C6H140 4-METHYL-2-PENTANOL 0.0000

714 C5H11N CYCLOPENTYLAMI NE 0.0001

512 C5H120 2-METHYLBUTAN-2-OL 0.0001

424 C6H13N CYCLOHEXYLAMINE 0.0000

26
Table 10. (continued)

top ranked by FOMB

290 K

IDN SPECIES TRED*PRED

482 CBRF3 BROMOTRI FLUOROMETHANEC 13B1

)

0.2842

375 COS CARBONYL SULPHIDE 0.1310

485 CH2F2 DIFLUOROMETHANE(32) 0.1914

58 C3H6 PROPENE 0.1619

163 H2S HYDROGEN SULPHIDE 0.1430

155 HCL HYDROGEN CHLORIDE 0.4180

57 C3H8 PROPANE 0.1417

436 C2CLF5 CHLOROPENTAFLUOROETHANEC 1 15) 0.1915

369 CHCLF2 CHLOROD I FLUOROMETHANE(22) 0.1310

472 HBR HYDROGEN BROMIDE 0.1777

70 NH3 AMMONIA 0.0490

66 C3H4 ALLENE 0.0885

143 CH20 FORMALDEHYDE 0.0424

196 C2H20 KETENE 0.1493

111 C2H60 METHYL ETHER 0.0645

492 C2H4F2 1 , 1 -DI FLUOROETHANEC 152A) 0.0793

431 CCL2F2 DICHLOROD I FLUOROMETHANE( 12) 0.0947

355 CH3CL CHLOROMETHANE(40) 0.0467

130 C2H3CL VINYL CHLORIDE 0.0402

154 CL2 CHLORINE 0.0540

48 C4H10 ISOBUTANE 0.0533

7 C4H6 BUTA-1, 3-DIENE 0.0342

9 C4H8 BUT- 1 -ENE 0.0396

49 C4H8 2-METHYLPROPENE 0.0409

554 CH5N METHYLAMINE 0.0237

228 $02 SULPHUR DIOXIDE 0.0254

27
Table 10 (continued)

bottom ranked by FOMB

290 K

IDN SPECIES TRED*PRED

229 C3H802 ETHYLENE GLYCOL MONOMETHYL E 0.0001

424 C6H13N CYCLOHEXYLAMINE 0.0001

91 C6H1203 2-ETHOXYETHYL ACETATE 0.0000

731 C4H9N0 MORPHOLINE 0.0001

505 C6H4CL2 1,2-DICHLOROBENZENE 0.0000

715 C7H7BR O-BROMOTOLUENE 0.0000

213 C6H1202 DIACETONE ALCOHOL 0.0000

367 C12H26 2,2,4,6,6-PENTAMETHYLHEPTANE 0.0000

363 C5H402 FURFURAL 0.0000

797 C9H10 INDANE 0.0000

385 C3H5CL3 1-2-3 TRICHLOROPROPANE 0.0000

81 C£H100 CYCLOHEXANONE 0.0000

509 C6H$I IODOBENZENE 0.0000

726 C5H10CL2 1 ,5-DICHLOROPENTANE 0.0000

390 C2HCL5 PENTACHLOROETHANE( 120) 0.0000

510 C 1 0F 1

8

PERFLUORODECALIN 0.0003

172 C4H1QO BUTAN-2-OL(SECBUTANOL) 0.0002

512 C5H120 2-METHYLBUTAN-2-OL 0.0002

793 C 1 0H 1

8

TRANS-DECALIN 0.0000

238 C5H9CL3 1,2,3-TRICHLORO-2-METHYLBUTA 0.0000

171 C4H10O 2-METHYLPROPAN- 1 -OL( ISOBUTAN 0.0001

189 C6H140 4-METHYL-2-PENTANOL 0.0001

714 C5H1 IN CYCLOPENTYLAMINE 0.0003

394 C5H120 PENTAN-1 -OL 0.0000

28
Table 10. (continued)

top ranked by FOMB

305 K

IDN SPECIES TRED*PRED

482 CBRF3 BROMOTRI FLUOROMETHANEC13B1

)

0.4283

485 CH2F2 D1FLU0R0METHANE(32) 0.3014

375 COS CARBONYL SULPHIDE 0.2059

58 C3H6 PROPENE 0.2478

163 H2S HYDROGEN SULPHIDE 0.2182

155 HCL HYDROGEN CHLORIDE 0.6196

436 C2CLF5 CHLOROPENTAFLUOROETHANEC 1 1 5

)

0.2998

57 C3H8 PROPANE 0.2188

369 CHCLF2 CHLORODI FLUOROMETHANE(22) 0.2066

472 HBR HYDROGEN BROMIDE 0.2674

70 NH3 AMMONIA 0.0820

66 C3H4 ALLENE 0.1440

196 C2H20 KETENE 0.2277

492 C2H4F2 1, 1-DIFLUOROETHANE(152A) 0.1294

143 CH20 FORMALDEHYDE 0.0723

111 C2H60 METHYL ETHER 0.1047

431 CCL2F2 DICHLORODI FLUOROMETHANEC12) 0.1499

355 CH3CL CHLOROMETHANE(40) 0.0759

130 C2H3CL VINYL CHLORIDE 0.0658

7 C4H6 BUTA-1, 3-DIENE 0.0573

154 CL2 CHLORINE 0.0857

48 C4H10 ISOBUTANE 0.0870

9 C4H8 BUT- 1 -ENE 0.0659

49 C4H8 2-METHYLPROPENE 0.0678

414 N02 NITROGEN DIOXIDE 0.0115

554 CH5N METHYLAMINE 0.0419

228 S02 SULPHUR DIOXIDE 0.0445

8 C4H10 BUTANE 0.0566

29
Table 10 (continued)

bottom ranked by FOMB

305 K

IDN SPECIES TRED*PRED

385 C3H5CL3 1-2-3 TRICHLOROPROPANE 0.0001

510 C10F18 PERFLUORODECALIN 0.0007

509 C6H5I IOOOBEHZENE 0.0000

620 C9H1802 N-PENTYL N-BUTYRATE 0.0000

62 C11H24 UNDECANE 0.0000

665 C9H180 METHYL N-HEPTYL KETONE 0.0000

789 C8H18S OCTANE- 1 -THIOL 0.0000

171 C4H100 2-METHYLPROPAN-1 -OL( ISOBUTAN 0.0003

797 C9H10 INDANE 0.0000

615 C9H1802 N-HEPTYL ACETATE 0.0000

420 C7H50CL BENZOYL CHLORIDE 0.0000

363 C5H402 FURFURAL 0.0000

582 C1()h3003SI4 DECAMETHYLTETRASILOXANE 0.0000

748 C9H1802 N-OCTYL FORMATE 0.0000

793 C10H18 TRANS-DECALIN 0.0000

847 C6H10O4 DIETHYL OXALATE 0.0000

726 C5H10CL2 1 ,5-DICHLOROPENTANE 0.0000

189 C6H140 4-METHYL-2-PENTANOL 0.0002

714 C5H11N CYCLOPENTYLAMINE 0.0008

757 C10H2002 N-PENTYL VALERATE 0.0000

238 C5H9CL3 1,2,3-TRICHLORO-2-METHYLBUTA 0.0000

394 C5H120 PENTAN-1-OL 0.0001

364 C6H1402 ETHYLENE GLYCOL MONO-N-BUTYL 0.0000

647 C2H3BR3 1 , 1 ,2-TRI BROMOETHANE 0.0000

415 C6H7N ANILINE 0.0000

104 C6H140 HEXAN-1-OL 0.0000

704 C10H20 CYCLODECANE 0.0000

588 C10H30O5SI5 DECAMETHYLCYCLOPENTASI LOXANE 0.0001

142 C8H180 2-ETHYLHEXANOL 0.0000

30
Table 10. (continued)

top ranked by FOMB

320 K

IDN SPECIES TRED*PRED

482 CBRF3 BROMQTR I FLUOROMETHANE( 13B1

)

0.6248

485 CH2F2 DIFLUOROMETHANE(32) 0.4567

58 C3H6 PROPENE 0.3657

375 COS CARBONYL SULPHIDE 0.3090

436 C2CLF5 CHLOROPENTAFLUOROETHANE( 1 15) 0.4510

163 H2S HYDROGEN SULPHIDE 0.3196

57 C3H8 PROPANE 0.3254

155 HCL HYDROGEN CHLORIDE 0.0660

369 CHCLF2 CHLOROD I FLUOROMETHANE(22) 0.3127

472 HBR HYDROGEN BROMIDE 0.3905

70 NH3 AMMONIA 0.1307

196 C2H20 KETENE 0.3335

492 C2H4F2 1 , 1 -D I FLUOROETHANEC 152A) 0.2014

66 C3H4 ALLENE 0.2215

111 C2H60 METHYL ETHER 0.1623

431 CCL2F2 D I CHLOROD I FLUOROMETHANEC 12) 0.2275

143 CH20 FORMALDEHYDE 0.1171

355 CH3CL CHLOROME THANE (40) 0.1177

130 C2H3CL VINYL CHLORIDE 0.1028

414 N02 NITROGEN DIOXIDE 0.0226

7 C4H6 BUTA- 1 ,3-DIENE 0.0911

48 C4H10 ISOBUTANE 0.1355

154 CL2 CHLORINE 0.1301

9 C4H8 BUT- 1 -ENE 0.1044

49 C4H8 2-METHYLPRQPENE 0.1066

31
Table 10 (continued)

bottom ranked by FQH8

320 K

ION SPECIES TRED*PRED

89 C12H24 DOOEC-1-ENE 0.0000

789 C8H18S OCTANE- 1 -THIOL 0.0001

700 C8H18Q3 DIETHYLENE GLYCOL DIETHYL ET 0.0000

394 C5H120 PENTAN- 1 -OL 0.0002

728 C9H13M N,N-DIMETHYL-P-TQLUIDINE 0.0000

28 C12H26 DODECANE 0.0000

748 C9H18Q2 N-OCTYL FORMATE 0.0000

566 C8H7N P-TOLUNITRILE 0.0000

751 C11H2202 N-OCTYL PROPIONATE 0.0000

757 C10H2002 N-PENTYL VALERATE 0.0001

141 T0H20O2 2-ETHYLHEXYL ACRYLATE 0.0000

419 C10H15N N # W-DIETHYLANILINE 0.0000

647 C2H3BR3 1,1,2-TRIBROMOETHANE 0.0000

364 C6H1402 ETHYLENE GLYCOL MONO-N-BUTYL 0.0000

104 C6H140 HEXAN-1-OL 0.0001

704 C10H20 CYCLODECANE 0.0000

415 C6H7N ANILINE 0.0000

696 C5H1203 DIETHYLENE GLYCOL MONOMETHYL 0.0000

588 C10H30O5SI5 DECAMETHYLCYCLOPENTASILOXANE 0.0001

392 C4CL6 HEXACHLOROBUTAD I ENE 0.0000

513 C8H180 OCTAN-2-QL 0.0000

142 C8H180 2-ETHYLHEXANOL 0.0001

4 ALPHANOL ALPHANOL 0.0000

829 C10H200 DECANAL 0.0000

405 C3H60CL2 2-3-DICHLOROPROPAMOL 0.0000

32
Table 11. Summary of responses from commercial suppliers of heat transfer fluids

COMPANY FLUID FLUID DESCRIPTION

3M FC72 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC84 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC 77 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC104 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC75 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC40 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC43 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC5311 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC70 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC5312 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC71 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

3M FC87 COMPLETELY FLUORINATED ORGANIC COMPOUNDS

AKZO CHEMICALS DEMEON 13/87 AZEOTROPE (13W%DIMETHYLETHER,87W%R12)

AUSIMONT GALDEN D/80 PERFLUORINATED LIQUID

AUSIMONT GALDEN D02 PERFLUORINATED LIQUID

AUSIMONT GALDEN D03 PERFLUORINATED LIQUID

AUSIMONT GALDEN D05 PERFLUORINATED LIQUID

AUSIMONT GALDEN DIO PERFLUORINATED LIQUID

AUSIMONT GALDEN D20 PERFLUORINATED LIQUID

AUSIMONT GALDEN D40 PERFLUORINATED LIQUID

AUSIMONT LS/215 PERFLUORINATED LIQUID

AUSIMONT LS/230 PERFLUORINATED LIQUID

AUSIMONT HS/260 PERFLUORINATED LIQUID

DOW CORNING SYLTHERM 800 MODIFIED DIMETHYLSILOXANE

DOW CORNING SYLTHERM XLT DIMETHYLSILOXANE POLYMER

DOW CORNING DC200 DIMETHYL, PHENYLMETHYL, AND TRIFLUOROPROPYL SILICONE FLUID

DOW CORNING DC510 D I METHYL, PHENYLMETHYL, AND TRIFLUOROPROPYL SILICONE FLUID

DOW CORNING DC550 DIMETHYL, PHENYLMETHYL, AND TRIFLUOROPROPYL SILICONE FLUID

DOW CORNING DC710 DIMETHYL, PHENYLMETHYL, AND TRIFLUOROPROPYL SILICONE FLUID

DOW CORNING DCFS1265 DIMETHYL, PHENYLMETHYL, AND TRIFLUOROPROPYL SILICONE FLUID

GENERAL ELECTRIC SF97-50 POLYDIMETHYLSILOXANE

GENERAL ELECTRIC SF96-100 POLYDIMETHYLSILOXANE

GENERAL ELECTRIC SF1154 COPOLYMER CONTAINING BOTH METHY AND PHENYL. UNITS

GENERAL ELECTRIC S F 1 147 LUBRICANT

GENERAL ELECTRIC F50 HIGH TEMP LUBRICANT

GENERAL ELECTRIC S F 1 265 POLYDIMETHYLDIPHENYLSILOXANE

HOECHST UK LTD HOSTINERT 130,175,216,272 PERFLUORINATED LIQ. COMPOSED OF CARBON, FLUORINE, .& OXYGEN ATOMS

MONSANTO THERMINOL LT SYNTHETIC AROMATIC FLUID

MONSANTO THERMINOL 44 MODIFIED ESTER BASED FLUID

33
Table 11. (continued)

COMPANY FLUID FLUID DESCRIPTION

MONSANTO THERMINOL 55 SYNTHETIC HYDROCARBON

MONSANTO THERMINOL 59 ALKYL SUBSTITUTED AROMATIC

MONSANTO THERMINOL 60 POLYAROMATIC COMPOUND

MONSANTO THERMINOL 66 MODIFIED TF.RPHENYHL MONSANTO THERMINOL 75 TERPHENYL/QUATERPHYNYL

MONSANTO THERMINOL VP1 EUTECTIC MIXTURE OF 73.5% DIPHELYOXIDE,26.5% BIPHENHYL

MULTITHERM IG2 SINGLE-CUT PARAFFINIC

MULTITHERM PG1 WHITE MINERAL OIL

UNION CARBIDE UCAR FOODFREEZE 35 PROPYLENEGLYCOL BASED

UNION CARBIDE UCARTHERM ETHYLENE-GLYCOL BASED

UNION CARBIDE UCAR TRITHERM INHIBITED TRIETHYLENE GLYCOL-BASED

UNION CARBIDE UCON 500 POLYALKALENE GLYCOL-BASED

UNION CARBIDE L-305 SILICON FLUID DIMETHYLPOLYSILOXANE

34
Table 1 1 . (continued)

FLUID PVAP

(3293 K or T shown)

NORMAL BOILING

POINT

FREEZING POINT FLASH POINT FIRE POINT

(kPa) (K) (K) (K) (K)

FC72 30.9 309 183 NON FLAMMABLE NON FLAMMABLE

FC84 10.5 353 178 NON FLAMMABLE NON FLAMMABLE

FC77 5.6 370 163 NON FLAMMABLE NON FLAMMABLE

FC104 3.9 374 208 NON FLAMMABLE NON FLAMMABLE

FC75 4.1 375 185 NON FLAMMABLE NON FLAMMABLE

FC40 0.4 428 216 NON FLAMMABLE NON FLAMMABLE

FC43 0.17 447 223 NON FLAMMABLE NON FLAMMABLE

FC5311 <0.013 488 253 NON FLAMMABLE NON FLAMMABLE

FC70 <0.013 488 248 NON FLAMMABLE NON FLAMMABLE

FC5312 <0.013 488 283 MON FLAMMABLE NON FLAMMABLE

FC71 <0.0026 526 306 NON FLAMMABLE NON FLAMMABLE

FC87 7 307 7 7 7 DEMEON 13/87 700 3 298 K 244 7 NON FLAMMABLE NON FLAMMABLE

GALDEN D/80 10.5 3298 K 357 7 NONFLAMMABLE NONFLAMMABLE

GALDEN D02 <.13 3298 K 448 ? NONFLAMMABLE NONFLAMMABLE

GALDEN D03 <.13 3 298 K 463 7 NONFLAMMABLE NONFLAMMABLE

GALDEN D05 <.13 3 298 K 503 ? NONFLAMMABLE NONFLAMMABLE

GALDEN DIO NIL 3 298 K 523 7 NONFLAMMABLE NONFLAMMABLE

GALDEN D20 NIL a 298 K 543 7 NONFLAMMABLE NONFLAMMABLE

GALDEN D40 NIL a 298 K NONE 3 1 ATM ? NONFLAMMABLE NONFLAMMABLE

LS/215 NIL 3 298 K 488 ? NONFLAMMABLE NONFLAMMABLE

LS/230 NIL 3 298 K 503 7 NONFLAMMABLE NONFLAMMABLE

HS/260 NIL a 298 K 533 ? NONFLAMMABLE NONFLAMMABLE

SYLTHERM 800 NIL 473 233 308 341

SYLTHERM XLT <0.27 443 180 320 7 DC200 NIL >373 233 272 TO 588 ? DCS 1

0

NIL ? 223 272 TO 588 ? DC550 NIL ? 233 272 TO 588 ? DC710 NIL ? 255 272 TO 588 7 DCFS1265 NIL ? 233 272 TO 588 ? SF97-50 NOT GIVEN NOT GIVEN 218 573 613

SF96-100 NOT GIVEN NOT GIVEN 206 848 948

SF1154 NOT GIVEN NOT GIVEN 233 823 923

SF1147 NOT GIVEN NOT GIVEN 213 753 873

F50 NOT GIVEN NOT GIVEN 173 823 913

SF1265 NOT GIVEN NOT GIVEN ? 7 7 HOSTINERT 130, 175,216,272 <0.1 TO 3 403 TO 545 <183 NON FLAMMABLE >923

35
Table 11. (continued)

FLUID PVAP NORMAL BOILING FREEZING POINT FLASH POINT FIRE POINT

(3293 K or T shown) POINT

(kPe) (K) (K) <K> (K)

THERMINOL IT 0.102 454 198 330 339

THERMINQL 44 NIL >473 211 480 499

THERMINOL 55 NIL >560 233 450 483

THERMINOL 59 NIL 588 205 423 443

THERMINOL 60 NIL 563 205 427 433

THERMINOL 66 NIL >616 247 450 466

THERMINOL 75 NIL >653 343 472 500

THERMINOL VP1 NIL >523 285 397 400

IG2 7.43588 K 621 255 500 533

PG1 56 3477 K 589 233 444 469

UCAR FOOD FREEZE 35 0.09 435 222 372 NOT GIVEN

UCARTHERM 0.16 437.5 248.4 400.7 NOT GIVEN

UCAR TRITHERM 0.48 416.4 220 NONE ? UCON 500 NIL >533 233 588 ? L-305 SILICON FLUID NIL >533 213 511 >573

36
fable 11 .(continued)

FLUID/COMMENTS

FC72

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC84

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC77

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC104

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC75

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC40

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC43

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC5311

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC70

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC5312

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC71

NON TOXIC BUT AT OR ABOVE 200 C THERMAL DEGRADATION MAY GENERATE HIGHLY TOXIC DECOMPOSITION PRODUCTS

FC87

NEW FLUID NOT IN BROCHURE, INFO FROM TELECON W/3M

DEMEON 13/87

NONTOXIC BUT STILL CONTAINS CFC , R12, WHICH MAY DECOMPOSE TO TOXIC SUBSTANCE.

37
Table 11. (continued)

FLUID/COMMENTS

GALDEN D/80

LOW TOXICITY, MAY BREAK DOWN AT HIGH TEMP

GALDEN D02

LOW TOXICITY, MAY BREAK DOWN AT HIGH TEMP

GALDEN D03

LOW TOXICITY, MAY BREAK DOWN AT HIGH TEMP

GALDEN DOS

LOW TOXICITY, MAY BREAK DOWN AT HIGH TEMP

GALDEN DIO

LOW TOXICITY, MAY BREAK DOWN AT HIGH TEMP

GALDEN D20

LOW TOXICITY, MAY BREAK DOWN AT HIGH TEMP

GALDEN D40

LOW TOXICITY, MAY BREAK DOWN AT HIGH TEMP

LS/215

LOW TOXICITY, MAY BREAK DOWN AT HIGH TEMP

LS/230

HS/260

LOW TOXICITY, MAY BREAK DOWN AT HIGH TEMP

SYLTHERM 800

LOW TOXICITY, DESIGNED FOR USE AS HIGH TEMP LIQ PHASE HEAT TRANSFER FLUID

SYLTHERM XLT

LOW TOXICITY, DESIGNED AS LIQUID PHASE HEAT TRANSFER FLUID

DC200

GENERAL PURPOSE SILICONE FLUID, MARKETED AS LOW FREEZE PT, VERY LOW VAP PRESS, AND HIGH FLASH PTS. (FLASH

POINTS VARY WITH VISCOSITY)

38
Table 11. (continued)

FLUID/COMMENTS

0C510

GENERAL PURPOSE SILICONE FLUID, MARKETED AS LOW FREEZE PT, VERY LOW VAP PRESS, AND HIGH FLASH PTS. (FLASH

POINTS VARY WITH VISCOSITY)

DC550

GENERAL PURPOSE SILICONE FLUID, MARKETED AS LOW FREEZE PT, VERY LOW VAP PRESS, AND HIGH FLASH PTS. (FLASH

POINTS VARY WITH VISCOSITY)

DC710

GENERAL PURPOSE SILICONE FLUID, MARKETED AS LOW FREEZE PT, VERY LOW VAP

PRESS, AND HIGH FLASH PTS. (FLASH POINTS VARY WITH VISCOSITY)

DCFS1265

GENERAL PURPOSE SILICONE FLUID, MARKETED AS LOW FREEZE PT, VERY LOW VAP PRESS, AND HIGH FLASH PTS. (FLASH

POINTS VARY WITH VISCOSITY)

SF97-50

DESIGNED AS DIELECTRIC FLUID;PUBLICATION INDICATES INDEFINITE OPERATION AT 150 C. THEREFORE, LIKELY

HIGH BOILING POINT. LOW TOXICITY

SF96-100

USED IN RADIATION ENVIRON. , HIGH BOILING POINT

SF1154

USED IN RADIATION ENVIRON. , HIGH BOILING POINT

SF1147

USED IN RADIATION ENVIRON. , HIGH BOILING POINT

F50

USED IN RADIATION ENVIRON. , HIGH BOILING POINT

SF1265

INTERNAL RELEASE AGENT FOR RESINS

HOSTINERT 130, 175,216,272

NON-TOXIC, MFR CLAIMS STABILITY AT HIGH TEMPERATURE

THERMINOL LT

39
Table 11. (continued)

FLUID/COMMENTS

THERMINOL 44

THERMINOL 55

THERMINOL 59

THERMINOL 60

THERMINOL 66

THERMINOL 75

SOLID AT ROOM TEMP

THERMINOL VP1

RELATIVELY HIGH POUR POINT

IG2

NONTOXIC, HIGH TEMP HT TRANSF FLUID

PG

1

NONTOXIC, HIGH TEMP HT TRANSF FLUID, FDA/USDA CERTIFIED

UCAR FOODFREEZE 35

USED IN FOOD PROCESSING

UCARTHERM

UCAR TRIT

L - 305 SILICON FLUID

40
APPENDIX A. DETAILS OF CALCULATION

Background

Forced-convection boiling (or condensation) in horizontal

tubes was considered to be the primary mechanism of heat

transfer for the calculations of this study. In order to

calculate the thermal performance ranking parameters, FOMB

and FOMC , it was necessary to select appropriate

correlations for the prediction of the boiling (or

condensation) heat transfer coefficient and the two-phase

pressure drop (and thus the corresponding pumping power

required to circulate the fluid) . The primary reference

source for the selection of correlations and for other twophase flow background information was Collier [13].

We tacitly assumed that the relative ranking of the fluids

for thermal performance is primarily dependent on the fluid

properties (as they arise in the heat transfer and pressure

drop correlations) and not on the system geometry and/or

boundary conditions chosen for thermal performance

evaluation. However, the effect of D, L/D, and Reynolds

number was initially examined for a few fluids. The results

showed that the relative ranking was essentially the same.

Therefore, in order to limit the number of data

files/records to a manageable size, we have performed the

detailed calculations and resulting ranking and sorting for

a uniformly heated pipe of diameter, D=0.02 m, and lengthto-diameter ratio, L/D=100. The results for two different

liquid Reynold numbers (2000 and 200 000 - turbulent flow

region) are included. These assumptions and others are

implied in Figure Al. We shall note additional assumptions

in the discussions to follow.

Flow Regime and Heat Transfer Correlations

As a saturated liquid flowing through a pipe is subjected to

a uniform heat flux, various flow patterns will develop in

the pipe. A particularly important flow pattern is annular

flow since it may occur over a wide range of mass quality (x

from 0.1 and below, up to 1) [13]. Also, this flow pattern

is one likely to dominate in zero-g [14]. Therefore, we

assumed this flow regime to be representative and sought

correlations applicable to it.

Al
Boiling

There are a number of correlations in the literature for

predicting the heat transfer coefficient in the regions of

saturated nucleate boiling and forced convective heat

transfer through a liquid film. These regions are usually

associated with the annular flow pattern. Collier [13],

however, has recommended the Chen correlation.

This correlation is a superposition one where it is presumed

that the contributions from nucleate boiling, hNu

, and

forced convection, hc , are additive; that is,

htp~hNuB+hc

where

r k- 0.79

l NuB = 0.00122 'P,l

0.45

Pi

0.49

0.5 0.29 A ttO . 24 0.24

a p. 1 AH p q

ATsat

0.24A Psat

0.75

and

0.023

(Al)

(A2)

(A3)

The correction factors F and S have been empirically

determined as:

(F) = (X tt ) ' and (S) = f

2 (Retp).

The Martinelli-Nelson parameter is defined as:

(A4)

(A5)

Xtt

2 (A6)

where the subscript "f" indicates the pressure gradient is

due to friction losses. xtt maY be approximated by

Xtt * [

1-x

X

0.9 10.5 ^1 1 0.4

P"V

(A7)

A2
The two-phase Reynolds number is defined as:

Retp = F

1 ' 25 Re1( (A8)

where

G(l-x)

D

Re-j^ = —-—

^1

The functions F and S are presented in graphical form [10].

We fit the curves in the graphs with equations of the form:

logiQ F = Ap+Bp (log^Q ( l/x-^-j- )

) +Cp (log^Q ( 1/x-^-j- ) ) ^ +

Dp (log 10 (l/x tt )

)

3 (A9)

S = Ag+Bs log 10 (Ret )+Cs (log10 (Ret ))

2 +D

s (log 10 (Ret ))

3 ^ ^ YA10

)

Condensation

The correlation used for condensation heat transfer, hcon(^

/ in horizontal tubes for annular flow was developed by

Breber, et al. [15]

hcond = hl (ltl 1

2

) °' 45 (All)

where

hx = 0.023(Re1 ) 0#8 (Pr1

)°* 4 (k1 /D)

,

(A12)

and is the two-phase friction multiplier which may be

expressed in the form

$

x

2 = l+(C/x tt )+(l/(x tt ) 2

) (A13)

For turbulent-turbulent gas-liquid flow, C=20.

A3
Two-phase Pressure Drop

A separated flow model of the two-phase vapor-liquid flow in

the pipe was assumed in the calculation of the two-phase

pressure drop. Collier [13] gives the following expression

for the particular case where a fluid is evaporated from a

liquid at the saturation temperature (x=0) to a vapor-liquid

mixture containing a mass quality xL, with a linear change

of x over a length L (dx/dz=constant)

A Ptp =A Pf+A Pa+A Pg (A14)

Apf= 2f foG V1 L

D

rX

L 2j *lo dx

0

Apa

A Pg

(1-*L> 2

(1-a)

1

L g sin 0

XL

rx

L

(p v«+pi (!-a) ) dx

J 0

( A15

)

( A16

(A17)

For complete vaporization of the liquid stream, and ignoring

the gravity term (g=0) , eq. (A14) becomes:

2 f f

o

G vi L r “,t» —— L

cl

»lo dX +G‘i (Vv

-V1 )( A18

)

where f fo is the friction factor when the total flow is all

liquid.

f fo

and

0.079

(GDAi-p 0 - 25

$ lo

2 =

*i

2 (l-x) 1 - 75

(A19)

(A20)

A numerical integration was performed for the term

f

1

®lo2dx -

J 0

The absolute value of the total two-phase pressure drop for

condensation was considered to be the same as that

calculated for boiling.

A4
Calculation Procedure

The Fortran computer program which performs these

calculations is given at the end of this appendix

(Supplement 1) ; The methodology for the calculations

follows

(1) Read the thermodynamic and transport properties for one

of the candidate fluids in the temperature ranges. These

data are stored in an array for four different bulk

temperatures within the ranges. If a property was not

available at the bulk temperature, then the calculations

were not performed for that fluid at that temperature. This

was frequently the case in Temperature Range 1 at 200 K.

(2) Perform an in-situ least squares fit of the vapor

pressure data for each fluid. This is required for the

iterative solution of the Chen correlation (Apsa£ term)

.

(3) Input the system geometry data, D, L/D.

(4) Call the calculation subroutine for each of the four

bulk temperatures. The calculations consist of the following

steps for each of two liquid Reynolds numbers (at entrance

to pipe, 2000 and 200 000)

(a) Calculate the mass velocity, G = ^Re/D

(b) Calculate the Martinelli correlating parameter, xtt' at

11 points along the tube (0.01 <= x <= 0.99, ten intervals

assuming that for a uniform heat flux, quality varies

linearly along the length of the tube) . Store the local

values in an array for later numerical integration to

calculate an average.

(c) Calculate the correction factor, F for the Chen

correlation.

(d) Calculate the two-phase Reynolds number, Rex.

p

=Re1 *F 1 • 25

, and the correction factor, S for the Chen correlation.

(e) Calculate the heat flux required to completely vaporize

the liquid stream over the length of the pipe.

^0 =

r G AH n +

L 4 (L/D)J

r 1*10 7 DG3

L 8L

(A21)

(f) Calculate the two-phase forced-convection boiling-heat

transfer coefficient using the Chen correlation; an

iterative procedure is required since ATsa^. and Appat are

not known. This calculation is done for each of tne 11

stations along the tube (0.01 =< x <=0.99) and the local

A5
values are stored in an array.

(g) Perform the same calculations as above for condensation,

and store the local values of heat transfer coefficient in

an array.

(h) Integrate the local boiling and condensing heat transfer

coefficients over the length of the tube to get an average

value. This average value is used in FOMB and FOMC.

(i) Integrate the local Martinelli correlating parameter,

over the length of the tube to get an average value.

This average value is used in calculating an average volume

fraction of vapor, a.

(j) Calculate the total two-phase pressure drop.

(k) Calculate the power per unit surface area required to

circulate the fluid through the tube. Here we used a

homogeneous model to calculate an average volume fraction,

a, and thus average density of the two-phase mixture.

i! 2 = l+(20/x tt )+(l/(x tt>

2

)

Pmix = apy+U-^Pl

and

(A22)

(A23)

(A24)

PUMPWR = AptpG/ ( 4 p mix L/D) (A25)

(l) Calculate the ratio of heat flux to pumping power per

unit surface area (COPB)

(m) Calculate the ratio of heat transfer coefficient to

pumping power per unit surface area (FOMB and FOMC)

.

(n) Print the output and repeat for the next fluid.

A6
Detail on Calculation of Ranking Factors/ (WF****)

We calculated the cumulative relative-frequency distribution

of the values of the parameters noted in the text. This

procedure eliminates the need to scan the entire column of

data within a column to determine the relative ranking of a

particular fluid. It also provides a means of putting the

parameters on the same basis so that an overall ranking of a

fluid may be obtained by addition of the ranking factors.

Because frequently the values of the parameters varied over

several orders of magnitude the logarithm of each value was

calculated and the cumulative relative-frequency determined

on this basis.

If for a certain parameter value, x, we tally and then sum

all the frequencies corresponding to parameter values which

are smaller than or equal to that x, we obtain the

cumulative frequency corresponding to that x. Division by

the total number of fluids yields the cumulative relative

frequency [9]. This number we have called "ranking factor"

and accordingly it varies between 0 and 1. A ranking factor

of 1 indicates that 100% of the parameter values are less

than or equal to that x. The task becomes one of forcing

the "preferred" value for each parameter to be the maximum

value so that the cumulative relative frequency represents

the proximity to the preferred value whether the preferred

value is the maximum value, (for example, FOMB, LTF) a fixed

value (for example, 101 kPa for PVAP, and 293 K for NBP) or

the minimum value (for example TMP, and DEN) . This was done

as described below:

WFFOMB and WFLTF (Ranking Factors for Figure of Merit for

Boiling and Liguid Transport Factor)

For these parameters the preferred value was the maximum

value. That is, the ratio of heat transfer coefficient to

required pumping power should be large and the liquid

transport factor should be large. In this case the

calculation of culumulative relative frequency was

straightforward and it was not required to force the

preferred value to be the maximum.

A7
WFNBP and WFPVAP (Ranking Factors for Normal Boiling-point

and Operating Pressure at Tbulk)

The preferred value for the normal boiling-point was 293 K

(20°C) . We chose this value because by definition, the

vapor-pressure at this temperature is 101 kPa (1 atm) . This

criterion (proximity to 1 atm at "room temperature") arises

from the concern for possible leakage into (or out of) the

thermal control loop and the crew modules which are

nominally maintained at 293 K and -101 kPa (1 atm)

.

Therefore, if the heat transport fluid in the thermal

control loop has a NBP near 293 K there is less potential

driving force for leakage into or out of the system.

For calculation of ranking factor, WFNBP, the NBP of each

fluid was divided by 293 K, and the logarithm of the ratio

was calculated. The desired value was therefore 0 (that is,

log 1=0) , and this implies NBP=293 K. For assignment of

ranking factor, we are interested in the proximity to 293 K,

not whether the NBP is greater than or less than 293 K. In

order to "force" the preferred value to the maximum value,

if log (NBP /293) > 0, then change its sign,

logiO (NBP/293 ) becomes -log1Q (NBP/293

)

and all values appear to be less than or equal to 0; 0 is

then the maximum value and the preferred value. Those

fluids having NBP furthest away from 293 K have large

negative numbers and by the cumulative relative frequency

calculation receive a ranking factor of 0 or a very small

number? those closest to 293 K have small negative numbers

and are assigned a ranking factor near 1.

For calculation of ranking factor, WFPVAP, the vapor

pressure at Tbulk of each fluid was divided by 101 kPa (1

atm) and the corresponding logarithm of the ratio

calculated. Analagous to the procedure for WFNBP

assignment, we determined the ranking factors, WFPVAP, for

each fluid.

WFTMP and WFDEN (Ranking Factors for Melting-point and

Liquid Density)

The preferred values for both these parameters is the

minimum value. A low melting-point (or freezing point)

minimizes the possibility of freeze-up in the lines under

off-normal conditions. All other factors being equal, a

small liquid density translates to a small system mass,

important in spacecraft application.

A8
The logarithm of each value was calculated and the

cumlulative relative frequency calculated. Since we want

the minimum value to receive a ranking factor of 1, then

set:

WF = 1. - CUM. REL. FREQ.

In this fashion, the fluids having the lowest melting-points

and liquid densities receive the highest ranking factor.

A9
Boiling

q

=

Uniform

Heat

Flux

; i o

CL 3

CO ©

il X

o

II X

o

o

o

CM

II <D CE

o

o

o

o

CM

.2 O

Q“.E 1* "j X

o

o o

CM O

II 2

CD o

CE CM

A10

Figure

A1

-

Assumed

Geometry

and

Conditions

for

Evaluating

Thermal

Performance

Parameters,

FOMB,

FOMC.
Supplement A1 . Computer Program for Calculation of Thermal Performance Parameters.

PROGRAM C0P1AVG

C THIS PROGRAM PERFORMS CALCS FOR ENVELOPE1 (USES AVG HT

C COEFFICIENT IN THE PIPE)

DIMENSION TBULK(4) ,RHOL(4) ,RHOV(4) , VISCL(4)

,

1 VISCV(4) ,CPL(4) ,CPV(4) , TCONL(4) ,TCONV(4)

,

2 SURTENC4) ,XLATHT (4) ,PSATB(4) ,TR(4) ,PR(4)

DIMENSION COEF(2),QUAL(3)

CHARACTER XNAME*32, FMLA*12,TEST*1

COMMON/DATA/TBULK, RHOL , RHOV, VI SCL , VI SCV, CPL

,

1 CPV,TCONL, TCONV, SURTEN, XLATHT , PSATB,

2 D,XLEN,TCRIT,PCRIT,TBP

COMMON/LSQ/COEF

Q**********************************

C READ SYSTEM PARAMETERS FROM UNIT 5 C READ PROPERTIES DATA FROM UNITS 6,7,8,9,10

C UNIT 6 WILL HAVE TRANSPORT PROPS ALONG SAT LINE AT T1 C UNIT 7 WILL HAVE PROPS ALONG SAT LINE AT T2

C UNIT 8 WILL HAVE PROPS ALONG SAT LINE AT T3

C UNIT 9 WILL HAVE PROPS ALONG SAT LINE AT T4

C UNIT 4 WILL HAVE PHYS PROP DATA INCLUDING NORMAL BP,

C MELTING POINT, TCRIT,PCRIT

C*********UN IT 12 WILL CONTAIN OUTPUT

C************* INPUT SYSTEM PARAMETERS

OPEN ( 1 2, F I LE="OUTPUT .DAT" , STATUS="UNKNOWN"

)

OPEN (4, F I LE="SORT ID . EN1", STATUS="OLD"

)

OPEN (6, FI LE="ENV1200.DAT",STATUS="OLD")

OPEN (7, FI LE="ENV1250.DAT",STATUS="OLD")

OPEN (8, F I LE="ENV1300.DAT", STATUS="OLD")

OPEN (9, FI LE="ENV1350.DAT", STATUS="OLD")

C*****READ INPUT DATA FROM FILES

NREAD=0

5 CONTINUE

NREAD=NREAD+1

WRITE(*,*)NREAD

C I F(NREAD.EQ.50)GO TO 2500

READ(4, 1500,END=2500,ERR=9004)

1 I D 1 ,XNAME, FMLA, FW,TMP,TBP,TCRIT,

1 PCRIT

C CLOSE (4)

READ (6, 1000,END=2500,ERR=9006) ID2, FMLA,

1 TBULK(1 ),RHOL(1 ),

1 RHOV( 1 )

, CPL ( 1 )

, CPV( 1 ), TCONLC 1 )

, TCONV( 1 )

,

2 VI SCL ( 1 ), VI SCV( 1 )

, XLATHT(1 )

, SURTEN( 1 ), PSATB( 1

)

C CLOSE (6)

I F C I D 1 .NE.ID2)THEN

WRITE(*,*)"ERROR, IDS NOT EQUAL"

GO TO 2500

ELSE

END IF READ (7, 1000,END=2500,ERR=9007) ID2 .FMLA.

All
1 T BULK ( 2 )

, RH0L(2)

,

1 RHOV(2),CPL(2),CPV(2),TCONL(2),TCONV<2),

2 VISCL(2),VISCV(2),XLATHT(2),SURTEN(2),PSATB(2)

C CLOSE (7)

IF(ID1.NE.ID2)THEN

WRITE(*,*)"ERROR, IDS NOT EQUAL"

GO TO 2500

ELSE

ENDIF

READ (8, 1000,END=2500,ERR=9008)ID2, FMLA,

1 TBULK(3),RHOL(3),

1 RHOV(3),CPL(3),CPV(3),TCONL(3),TCONV(3),

2 VISCL(3) , VISCV(3) f XLATHT (3),SURTEN(3) ,PSATB(3)

C CLOSE (8)

IF(ID1.NE.ID2)THEN

WRITE(*,*)"ERROR, IDS NOT EQUAL"

GO TO 2500

ELSE

ENDIF

READ (9, 1000,END=2500,ERR=9009)ID2, FMLA,

1 TBULK(4) , RHOL(4)

,

1 RHOV(4) , CPL(4) , CPV(4) ,TCONL(4),TCONV(4)

,

2 VISCL(4) , VISCV(4) ,XLATHT (4) ,SURTEN(4) , PSATB(4)

C CLOSE (9)

IF(ID1.NE.ID2)THEN

WRITE(*,*)"ERROR, IDS NOT EQUAL"

GO TO 2500

ELSE

ENDIF

1000 FORMAT (1X,I3,1X,A12,F6.1,F7.1,F8.2,2F5.2,F6.4,

1 F7.5,F7.3,F7.5,F7.1,F7.5,F7.1)

1020 FORMAT (16X,F6.1,F7.1,F8.2,2F5.2,F6.4,

1 F7.5,F7.3,F7.5,F7.1,F7.5,F7.1)

1500 FORMAT ( I3,3X,A32,2X, A12, F6.1,3F8.1,F8.0)

C CHECK TO SEE THAT VAPOR PRESSURES ARE REASONABLE

I F(PSATB(4) .LT .0. 1 )THEN

GO TO 5 ENDIF

DO 1625 1=1,4

I F ( PSAT B C I ).LT.0.1)THEN

GO TO 1625

ENDIF

I F(PSATB( I).GE.0.1)THEN

C CHECK TO SEE THAT ALL DATA ARE AVAILABLE FOR THE SUBSTANCE

C EXCEPT FOR CPV AND TCONV WHICH AREN'T USED IN CALCS

PROD=RHOL( I )*RHOV( I )*CPL( I ) 1*TCONL( I )*VISCL( I )*VISCV( I

)

2*XLATHT ( I )*SURTEN( I

)

ENDIF

I F(PROD . EQ .0 . )GO TO 5 1625 CONTINUE

WRITE(*,1610)ID1, FMLA,XNAME

1630 WRITE( 12, 1611)

WRI TE( 12, 1610) ID1, FMLA, XNAME

Cl 61 0 FORMAT (/, ' ID NO.=' , I3/1X,A12,A32)

1610 FORMAT (IX, I3,/1X,A12, A32)

1611 FORMAT ('++++++')

A12
C CONVERT KILOJOULES TO JOULES IN CP

DO 1550 1=1,4

CPL( I )=CPL( I )*1000.

CPV(I)=CPV(I)*1000.

1550 CONTINUE

C CONVERT KILOJOULES TO JOULES IN LATENT HEAT

DO 1560 1=1,4

XLATHT( I )=XLATHT( I )*1000.

1560 CONTINUE

C CONVERT CENTIPOISE TO PaS IN VISCOSITY

DO 1570 1=1,4

V I SCL ( I )=VISCL( I )*0.001

VISCV(I)=VISCV(I)*0.001

1570 CONTINUE

C CONVERT KILOPASCALS TO PASCALS

DO 1600 1=1,4

PSATB( I )=PSATB( I )*1 .E3

1600 CONTINUE

PCR1T=PCRIT*1.E3

C CALCULATE REDUCED TEMPERATURES AND PRESSURES

DO 1612 KK=1 ,4

TR(KK)=TBULK(KK)/TCRIT

PR(KK)=PSATB(KK)/PCRIT

C DO THE FOLLOWING FOR PRINTOUT CONVENIENCE

PSATB(KK)=PSATB(KK)/1000.

WRITE( 12, 1640)TBULK(KK) ,PSATB(KK) , RHOL(KK)

,

1 TR(KK),PR(KK)

C GET UNITS BACK AGAIN

PSATB(KK)=PSATB(KK)*1000.

1612 CONTINUE

C 1640 FORMAT ('TBULK (K)=' , F6. 1 ,2X,

C 1 'VAPOR PRESSURE <Pa)=' ,G10.3,2X,

C 2 'LIQUID DENSITY <KG/M3)=' ,G10.3,3X,/

C 3 'REDUCED TEMP=' ,G10. 3, 3X, 'REDUCED PRESS=' ,G10.3,/)

1640 FORMAT (F6.1,2X,F10.3,F10.3,F10.4,3X,F10.4,/)

C PERFORM LEAST SQUARES FIT OF VAPOR PRESSURE VS T C THE ARRAY C CONTAINS THE COEFFICIENTS OF THE FIT

C LOG P=C( 1 )+C(2)/T

C THIS WILL BE USED IN THE CALC OF PSAT CORRES TO TWALL

C WHICH IS NEEDED IN THE CHEN BOILING CORRELATION

CALL LSQ2D(COEF)

OPEN ( 5 , F

I

LE="SYSPAR . DAT" , STATUS="OLD"

)

1615 READ (5,*,END=2000,ERR=9005)D,XLOD

XLEN=XLOD*D

WRITE(12, 1605)D,XLOO

C 1605 FORMAT(3X,'D (M)=' , F8.3,3X, 'L/D=' , F8.3,//)

1605 FORMAT (3X, F8.3,3X, F8.3//)

DO 1950 1=1,4

A13
I F (PSATBC I ) - LT . 100. )THEN

GO TO 1950

ENDIF

C CALL SUBROUTINE FOR CALCULATIONS AND PRINTING

CALL CALC(TBULK( I ),RHOL( I ),

1 RHOV( I ),CPL( I

)

f CPV( I )

, TCONL ( I )

, TCONV( I )

,

2 VISCL( I

)

# VISCV( I

)

f XLATHT ( I ) ,SURTEN( I ), PSATBC I )

,

3 ID1)

1950 CONTINUE

GO TO 1615

2000 CLOSE (5)

GO TO 5 2500 CLOSE (12)

CLOSE (6)

CLOSE (7)

CLOSE (8)

CLOSE (9)

GO TO 10000

9004 WRITE(*,*)"ERROR IN TAPE 4"

READ (4, FMT=' (A)' )TEST

READ (6, FMT=' (A) # )TEST

READ(7,FMT='<A)')TEST

READ(8,FMT='(A)')TEST

READ (9, FMT=' (A) ' )TEST

GO TO 5 C GO TO 10000

9005 WRITE(*,*)"ERROR IN TAPE 5"

GO TO 5

C GO TO 10000

9006 WRITE(*,*)"ERROR IN TAPE 6"

READ (6, FMT=' (A)' )TEST

READ (7, FMT=' (A) ' )TEST

READ (8, FMT=' (A) ' )TEST

READ(9,FMT= / (A)')TEST

GO TO 5 C GO TO 10000

9007 WRITE(*,*)"ERROR IN TAPE 7"

READ (7, FMT= ; (A)' )TEST

READ (8, FMT=' (A) ' )TEST

READ (9, FMT=' (A) ' )TEST

GO TO 5 C GO TO 10000

9008 WRITE(* f *)"ERROR IN TAPE 8"

READ(8„FMT='(A)')TEST

READ (9, FMT=' (A)' )TEST

GO TO 5 C GO TO 10000

9009 WRITE(*,*)"ERROR IN TAPE 9"

READ (9, FMT=' (A) ' )TEST

GO TO 5 10000 CONTINUE

END

A14
***********************************************************

SUBROUT I NE CALC(TBULK, RHOL , RHOV, CPL , CPV, TCONL , TCONV,

1 VISCL,VISCV,XLATHT,SURTEN,PSATB, ID)

DIMENSION G(2),REL(2)

DIMENSION XHB(0:10),XHC(0:10),XTTS(0:10)

COMMON/DATA/DUM(48),D,XLEN,DUM2(3)

DATA REL/2.E03,2.E05/

DATA XMIN,XMAX/0.01 ,0.99/

DATA A,B,C,DD,ABAR < BBAR,CBAR,DBAR/0.9946102006E+00,

1 0.5913534234E+00,0.5548497826E-01,

2 - 0.5863304243E- 02, -0.1 883211 071 E+02,

3 0.5806947612E+Q1 , -0.5516715499E+00,

4 0. 1669278595E-01/

C**CALCULATE THE G(K) CORRESPONDING TO REYNOLDS

C** NUMBERS OF 10E4, 10E5, 10E6 —TURBULENT FLOW

C AND THEN CALCULATE THE AVG HEAT TRANSFER COEFF

DO 600 K=1 ,2

G(K)=VISCL*REL(K)/D

C CALCULATE THE HEAT TRANSFER COEF FOR 11 STATIONS (I.E.,

C FOR 0.01>=X<=0.99 TEN INTERVALS)

DO 135 J J=0, 10

XINTER=(XMAX-XMIN)/10.

X=XMIN+XINTER*REAL( JJ)

C CALCULATE THE XTTCMARTINELLI -NELSON CORRELATING PARAMETER)

XTT=< ( 1

. -X)/(X) )**0.9*(VISCL/VISCV)**0.

1

1 *(RHOV/RHOL)**0.5

C STORE XTT IN AN ARRAY XTTS(11) FOR LATER AVERAGING

XTTS(JJ)=XTT

C CALCULATE 1/XTT

XTT I NV= 1 ./XTT

C CALCULATE F THE CORRECTION FACTOR WHICH ACCOUNTS FOR

C INCREASED TURBULENCE DUE TO PRESENCE OF VAPOR

XX=ALOG(XTTINV)

F=A+B*XX+C*XX**2+

1 DD*XX**3

F=EXP( F) C CALCULATE THE TWO-PHASE RE NUMBER

C CALCULATE THE REYNOLDS NO. BASED ON LIQUID ALONE FLOW

C RELF

RELF=G(K)*(1. -X)*D/VISCL

RETP=RELF*F**1 .25

C CALCULATE SUPPRESSION FACTOR,

S

XX=ALOG(RETP)

S=ABAR+BBAR*XX+CBAR*XX**2

1 +DBAR*XX**3

125 CONTINUE

A15
C CALCULATE THE FORCED CONVECTION BOILING HEAT TRANSFER

C COEFFICIENT (ASSUMING ANNULAR FLOW MOOEL, I.E.

C SEPARATED FLOW MODEL)

C CHEN CORRELATION WILL BE USED

130 CALL HTBOIL(XHTPB,XHTFLX,TDELT,G(K),F,S,

1 CPL,VISCL,VISCV,TCONL,

2 RELF,D,XLATHT,SURTEN,RHOL,RHOV,TBULK, X,XLEN,PSATB)

C STORE THE LOCAL BOILING HEAT TRANSFER COEFF IN AN ARRAY

XHB( JJ)=XHTPB

C CALCULATE THE FORCED CONVECTION CONDENSATION HEAT TRANSFER

C COEFFICIENT (CORRELATION FOR BUBBLE FLOW OR ANNULAR

C FLOW INSIDE HORIZONTAL TUBES) REF: BREBER,PALEN, TABORED

C CALL HTCOND(XHTPC,XTT)

C STORE THE LOCAL CONDENSING HEAT TRANSFER COEFF IN C AN ARRAY

XHC( JJ)=XHTPC

135 CONTINUE

C INTEGRATE THE LOCAL BOILING HEAT TRANSFER COEFF OVER THE C LENGTH OF THE PIPE TO GET AN AVERAGE

VALUE XHAVGB

CALL S I MPSON(XHB„X INTER, XHAVGB)

C INTERGRATE THE LOCAL XTT OVR THE LENGTH OF THE PIPE

C TO GBT_^N AVERAGE VALUE XTTAVG

CALL SIMPSON(XTTS,XINTER, XTTAVG)

C INTEGRATE THE LOCAL CONDENSING HEAT TRANSFER COEFF OVER

C LENGTH OF THE PIPE TO GET AN AVERAGE VALUE XHAVGC

CALL SIMPSON(XHC,XINTER, XHAVGC)

C CALCULATE THE TOTAL TWO-PHASE PRESSURE DROP OVER

C THE HEATED LENGTH (REF COLLIER PAGE 37). THIS IS

C FOR COMPLETE VAPORIZATION OF THE FLUID I.E. X=0 TO 1

150 CALL DELTAPO . ,D,G(K),XLEN,DPTP,RHOL,

1 RHOV.VISCL)

C CALCULATE POWER PER UNIT SURFACE AREA REQUIRED

C TO CIRCULATE FLUID THROUGH PIPE

C USE HOMOGENEOUS MODEL TO CALCULATE AN AVERAGE VELOCITY

C OF THE TWO- PHASES I.E. CALC VMIX=G(K)/RHOMIX

C RHOMIX IS AVG VALUE IN PIPE BASED ON AVG ALPHA(AVG VOL

C FRACTION OF VAPOR IN THE PIPE)

C FIRST CALCULATE AN AVG ALPHA FROM PHILTTAVG USING XTTAVG

PH I LTTA=1 . +20 . /XTTAVG+( 1 . /XTTAVG**2

)

ALPHA=1 .-(1 ./SQRT(PHI LTTA)

)

200 RHOMIX=ALPHA*RHOV+( 1

. - ALPHA )*RHOL

250 PUMPPWR=DPTP*G(K)/(4.*RHOMIX*XLEN/D)

C

C CALCULATE RATIO OF BOILING HEAT FLUX INPUT

A16
C TO PUMPING POWER PER UNIT SURFACE AREA (COEFFICIENT OF

C PERFORMANCE FOR BOILING)

350 COPB=XHTFLX/PUMPPWR

C CALCULATE RATIO OF HEAT TRANSFER COEF TO PUMPING POWER PER C UNIT SURFACE AREA (FIGURE OF MERIT

FOR BOILING)

FOMB=XHAVGB/PUMPPWR

C CALCULATE THE CONDENSATION HEAT FLUX. THIS IS THE SAME AS

C BOILING HEAT FLUX SINCE WE CONSIDER TOTAL COND. FROM X=1

C TO X=0

CHTFLX=XHTFLX

TDELTC=CHTFLX/XHC(10)

C CALCULATE THE RATIO OF CONDENSATION HEAT TRANSFER COEF

C TO PUMPING POWER PER UNIT SURFACE AREA (FIGURE OF MERIT C FOR CONDENSATION)

FOMC=XHAVGC/PUMPPWR

C DIVIDE BY CONVENIENT FACTORS FOR PRINTOUT

IF(REL(K).EQ.2.E05)THEN

PCOPB=COPB*1.E03

PFOMB=FOMB*1.E03

PFOMC=FOMC*1.E03

ELSE

PCOPB=COPB

PFOMB=FOMB

PFOMC=FOMC

ENDIF

PXHTPB=XHAVGB/1.E3

PXHTPC=XHAVGC/1.E3

WRITE( 12,500)TBULK,PCOPB,

1 PXHTPB,TDELT,

1 PXHTPC,TDELTC,PFOMB, PFOMC

500 FORMAT (1X,F4.0,1X,F12.2,3X,

1 F8.2,1X,F6.2,1X,F8.2,1X,F6.2,1X,2(F12.2,1X))

600 CONTINUE

RETURN

END

A17
0 **********************************************************

SUBROUTINE HTBOIl(XHB,QO,DT,G,F,S,

1 CPL,VISCL,VISCV,TCONL,

2 RELF,D,XLATHT,SURTEN,RHOL,RHOV,TBULK,X,XLEN,PSATB)

C THIS SUBROUTINE CALCULATES THE FORCED CONVECTION

C BOILING HEAT TRANSFER COEFFICIENT

C CALCULATE HEAT FLUX, QO, FROM FIXED PARAMETERS:

C FLOWRATE AND LATENT HEAT

COMMON/SUBRT/XS , X F , XCPL , XVI SCL , XVI SCV, XTCONL , XRELF,

2 XD,XXLATHT,XSURTEN,XRHOL,XRHOV,XTBULK,XX,XXLEN,

3 XPSATB

EXTERNAL Q

XF=F

XS=S

XCPL=CPL

XVI SCL=VI SCL

XVISCV=VISCV

XTCONL=TCONL

XRELF=RELF

XD=D

XXLATHT=XLATHT

XSURTEN=SURTEN

XRHOL=RHOL

XRHOV=RHOV

XTBULK=TBULK

XX=X

XXLEN=XLEN

XPSATB=PSATB

C CALCULATE THE UNIFORM HEAT FLUX REQ'D TO COMPLETELY

C VAPORIZE THE FLUID IN THE PIPE LENGTH,XLEN

100 Q0=G*XLATHT/(4.*XLEN/D)+( 1 .E-7*D*G**3)/(8.*XLEN)

1 *((1./(RHOV**2))-(1./(RHOL**2)))

TGUESS1=0.

TGUESS2=100.

EPSXA=0.01

EPSXR=0.01

EPSYA=0.01

EPSYR=0.01

MODE =2

C ROOTM FINDS THE DELTAT IN THE CHEN CORRELATION THAT

C YIELDS THE CORRECT QO=HCALC*DELTAT

C AFTER ITERATION ON DELTAT, WE CALCULATE HEAT

C TRANSFER COEFFICIENT FROM QO/DELTAT

C DELTAT INITIALLY GUESSED BETWEEN 0&100 K

200 CALL ROOTM (DELTAT,TGUESS1 , TGUESS2,EPSXA,EPSXR,

1 EPSYA,EPSYR,Q, 00, INDEX, MODE)

DT=DELTAT

A18
300 XHB=Q0/DELTAT

RETURN

END

£************************A**********************************

SUBROUTINE DELTAP(X,D,G,L,DP,RHOL,RHOV,VISCL)

REAL L

EXTERNAL RINTPH

C CALCULATE TWO-PHASE PRESSURE DROP (REF COLLIER PAGE 37)

C INTEGRATE PHLOTT FROM 0 TO X

C USE V.ARP NUMERICAL ROUTINE FOR INTEGRATION

XLWR=0.

300 CALL INTGRL(PHIAVG,RINTPH,XLWR,X)

C CALCULATE FFO(FRICTION FACTOR FOR TOTAL FLOW

C CONSIDERED LIQUID)

400 F F0=0 . 079/( G*D/VI SCL )**0 . 25

C CALCULATE TWO-PHASE FRICTION PRESS. DROP

500 DPFTP=(2.*FFO*G**2*L/(D*RHOL) )*(PHIAVG/X)

C

C CALCULATE ACCELERATION PRESS. DROP

DPATP=(G**2)*((1./RHOV)-(1./RHOL))

C CALCULATE TOTAL TWO-PHASE PRESS. DROP

700 DP=DPFTP+DPATP

RETURN

END

A19
c*********************************************************

FUNCTION Q(DELTAT)

C THIS FUNCTION CALCULATES THE FORCED CONVECTION BOILING

C HEAT TRANSFER COEFFICIENT USING THE CHEN CORRELATION

COMMON/SUBRT/XS, XF,XCPL,XVISCL,XVISCV,XTCONL,XRELF f XD

1 XXLATHT,XSURTEN f XRHOL,XRHOV,XTBULK,XX,XXLEN,

2 XPSATB

COMMON/LSQ/COEF(2)

C CALCULATE SINGLE PHASE HTCOEFF BASED ON LIQUID ONLY

C CALCULATE REYNOLDS NO AND PRANDTL NUMBER

350 PRL=XCPL*XVISCL/XTCONL

400 XHCL=0.023*(XRELF)**0.8*PRL**Q.4*XTCONL/XD

C CALCULATE NUCLEATE POOL BOILING HT TRANS COEFF,XHNB

C CALCULATE PROPERTIES PARAMETER

550 XNUM=(XTCONL**0.79)*(XCPL**0.45)*(XRHOL**0.49)

600 XDENOM=(XSURTEN**0.5)*(XVISCL**0.29)*(XXLATHT**

1 0.24)*(XRHOV**0.24)

650 PROPS=XNUM/XDENOM

C CALCULATE DPSAT

C DPSAT IS PSAT AT TWALL - PSAT AT TBULK

C PSAT AT TBULK IS INPUT VAPOR PRESSURE DATA

C NEED TO GET PSAT AT TWALL

C CALCULATE TWALL

700 TWALL=XTBULK+DELTAT

IF{DPSAT.LT.1 . )THEN

DPSAT=1

.

ELSE

CONTINUE

ENDIF

PSATW=EXP(COEF( 1 )+COEF(2)/TWALL)

800 DPSAT=PSATW- XPSATB

820 IF(DELTAT.LE.O.)THEN

XHNB=0.

900

1000

850

ELSE

XHNB=0.00122*PROPS*DELTAT**0.24*DPSAT**0.75

ENDIF

XHTPB=XHCL*XF+XHNB*XS

Q=XHTPB*DELTAT

RETURN

A20
END

c******************************************************

FUNCTION RINTPH(XX)

C THIS FUNCTION IS THE ALGORITHM FOR INTEGRATING THE

C PRESSURE DROP CORRECTION FACTOR (PHLOTT)

COMMON/SUBRT/XS,XF,XCPL,XVISCL,XVISCV,XTCONL,XRELF,XD,

1 XXLATHT , XSURTEN , XRHOL , XRHOV, XTBULK, DUMMY , XXLEN

,

2 XPSATB

200 I F(XX.EQ.O. )THEN

PHLOTT=1

.

ELSEIF (XX.EQ.I.)TKEN

PHLOTT=0.

ELSE

250 AA=SQRT ( (XRHOV/XRHOL )

)

BB=(XVI SCL/XVI SCV)

BB=BB**0.

1

CC=(1.-XX)/XX

CC=CC**0.9

AAS=AA*AA

BBS=BB*BB

CCS=CC*CC

PHILTT=1.+(20./(CC*BB*AA))+(1./(CCS*AAS*BBS))

DXX=1 . -XX PHLOTT=(DXX**1 .75)*PHILTT

300 END IF RINTPH=PHLOTT

RETURN

END

Q********************************************************

SUBROUTINE HTCOND(XHC,XTT)

COMMON/SUBRT/XS,XF,XCPL,XVISCL,XVISCV,XTCONL,XRELF,XD,

1 XXLATHT, XSURTEN, XRHOL, XRHOV, XTBULK, XX, XXLEN,

2 XPSATB

C THIS SUBROUTINE CALCULATES THE FORCED CONVECTION

C CONDENSING HEAT TRANSFER COEFFICIENT INSIDE HORIZONTAL

C TUBES <REF:BREBER,PALEN,TABOREK)

C VALID FOR ANNULAR FLOW OR BUBBLE FLOW

C CALCULATE LOCAL PHILTT-TWO PHASE PRESS DROP CORRECTION

C PARAMETER USING CHISOLM CORRELATION

100 PHILTT=1.+(20./XTT)+(1./XTT**2)

A21
20 PRL=XCPL*XVISCL/XTCONL

30 XHC=0.023*(XTCONL/XD)*(XRELF**0.8)*PRL**0.4

1 *(PHILTT)**0.45

RETURN

END

A22
c***********************************************************

SUBROUTINE LSQ2D(C)

PARAMETER (NMAX=10)

DIMENSION XX(NMAX), YY(NMAX), C(50)

DIMENSION TBULK(4),RHOL(4),RHOV(4),VISCL(4),

1 VISCV(4),CPL(4),CPV(4),TCONL(4),TCONV(4),

2 SURTEN(4) ,XLATHT (4) ,PSATB(4)

COMMON /FITT/ XFUN(50), YFUN, NFUN, NWRITE

COMMON/DATA/TBULK, RHOL , RHOV, VI SCL , VI SCV, CPL

,

1 CPV, TCONL , TCONV, SURTEN ,XLATHT , PSATB,

2 D,XLEN, TCRIT,PCRIT,TBP

C OUTPUT WILL BE ON TAPE20

NWRITE=20

OPEN (20, 'LSQ2D.COF')

C USE DATA READ FROM TAPE 6 AND 7

NPTS=0

DO 10 1=1,4

C IF VAPOR PRESSURE IS LESS THAN O.lKPa THEN OMIT THAT

C POINT IN THE FIT (THIS MEANS WE DON'T HAVE DATA THERE

C AND/OR VAPOR PRESSURE IS TOO LOW ANYWAY)

C

I F ( PSATB ( I ) .LT . 100. )THEN

GO TO 10

ELSE

NPTS=NPTS+1

XX(NPTS)=TBULK( I

)

YY(NPTS)=PSATB( I

)

ENDIF

10 CONTINUE

NPTS=NPTS+1

XX(NPTS)=TBP

YY(NPTS)=1 .01E05

NPTS=NPTS+1

XX(NPTS)=TCRIT

YY(NPTS)=PCRIT

DO 40 N=1 ,NPTS

C CALCULATE INDIVIDUAL TERMS

CALL FGEN (XFUN, NFUN, XX(N))

C WEIGHTS

WT = 1. DO 30 < = 1, NFUN

30 XFUN(K) = XFUN(K) * WT

YFUN=ALOG(YY(N)) * WT

CALL FIT 40 CONTINUE

50 CONTINUE

JFUN=NFUN

CALL COEFF

C CONSTANTS MUST BE OBTAINED BEFORE CALLING STAT

DO 60 1=1 , JFUN

60 C( I )=XFUN( I

)

CALL STAT

A23
DO 70 1=1, NPTS

CALL PGEN(XFUN, NFUN, XX< I >

)

YCAIC=0.

DO 65 J=1, NFUN

YCALC=YCALC + XFUN(J)*C(J)

65 CONTINUE

YCALC=EXP(YCALC)

YD I F=YY( I )-YCALC

WRITEC20, 69) XX(I), YY(I), YCALC, YDIF

70 CONTINUE

CLOSE (20)

69 FORMAT (4G14.5)

RETURM

END

£******************* *************************

SUBROUTINE FGEN(F, N, X)

DIMENSION F(*)

C N MUST NOT EXCEED 50 (WITH THIS VERSION OF FITTER)

F ( 1 )=1 . F(2)=1./X

N=2

RETURN

END

A24
Q***********************************************************

Q**********************************************************

SUBROUTINE INTGRL (ANSWER, FUNC, XMIN, XMAX)

C OUTPUT

C ANSWER = INTEGRAL OF FUNC FROM XMIN TO XMAX

C INPUT

C XMIN, XMAX

C VERSION MARCH 13 1986, VDA NEWTON-COTES 7TH ORDER INTEGRATION

C IMPLICIT DOUBLE PRECISION (A-H, O-Z)

DIMENSION C(8)

EXTERNAL FUNC

DATA JMAX /8/

DATA C / 751., 3577., 1323., 2989.,

1 2989., 1323., 3577., 751./

H = (XMAX - XMIN)/REAL (JMAX-1)

ANSWER = 0. DO 10 J=1, JMAX

X = XMIN + H*REAL( J-1

)

YVALUE = FUNC (X)

ANSWER = ANSWER + C(J)*YVALUE

10 CONTINUE

ANSWER = ANSWER * (7.*H/17280.

)

RETURN

END

SUBROUTINE SIMPSON( FSUBI , STEP, ANS)

C THIS SUBROUTINE INTEGRATES THE ARRAY CONTAINED IN FSUBI

C OVER THE INTERVAL DEFINED IN THE MAIN PROGRAM

DIMENSION FSUBI (0: 10)

C USE SIMPSON'S RULE TO FIND THE AVG VALUE FOR FSUBI

ANS=( STEP/3. )*( FSUBI (0)+4.*( FSUBI ( 1 )+FSUBI (3)

1 +FSUBI (5)+FSUBI (7J+FSUBI (9) )+2.*( FSUBI (2)

2 +FSUBI (4)+FSUBI (6)+FSUBI (8)+FSUBI ( 10) )

)

RETURN

END

A25

APPENDIX B. SUMMARY LIST OF COMPANIES CONTACTED

List of Companies Contacted bv Telephone

1 . DOW CORNING HEAT TRANSFER FLUIDS

DEPT. A0021 BOX 0994

MIDLAND, MICHIGAN

48686-0994

PHONE 517-496-6000

2 . DOW CORNING

ADDRESS AS ABOVE

3.

MULTITHERM CORP.

125 S FRONT ST.

COLWYN, PA. 19023

1-800-225-7440

4.

GEORGE MANN AND CO.

DEPT 665

HARBORS IDE BLVD, PO BOX3066

PROVIDENCE, RI 02940

401-781-5600

5.

GENERAL ELECTRIC

SILICONE PRODUCTS DIV

SECTION TR84

WATERFORD, NY 12188

PHONE 518-233-2309

6 . 3M INDUSTRIAL CHEMICAL PRODUCTS DIV

3M CENTER BLDG X 236-2B-01

ST. PAUL, MINN. 55144

PHONE: 612-733-6282

PHONE: 612-736-5242

7.

MONSANTO CHEMICAL CO.

800 N. LINDBERGH BLVD.

ST. LOUIS, MO

PHONE: 800-433-6997

B1
8 . MAINSTREAM ENGINEERING CORP.

268 N BABCOCK ST

SUITE C

MELBQURN, FLORIDA

32935

PHONE I 407 -2 42 -7 003

9.

MOBIL OIL

150 E. 42ND ST

NEW YORK, NY

PHONE 1-800-662-4525

10 . SONNEBORN-WITCO

520 MADISON

NEW YORK, NY

11 . WALPEX TRADING CO., INC

NEW YORK, NY

PHONE 212-921-8260

12 . MQNTEOISQN-AUSXMONT

44 WHTPPAMY RD

MORRISTOWN , NEW JERSEY

07962

PHONE: 201-292-6250

13 . SUPER-TRQL DIV., ENERCON SYSTEMS INC

ELYRIA, OHIO

14.

EXXON

HOUSTON, TEXAS

PHONE: 1-800-443-9966

15.

STAUFFER CHEM CO

16.

AKZO CHEMIE

CHICAGO, ILLINOIS

PHONE: 312-906-7500

17.

PARK CHEMICAL CO

DETROIT, MICH

PHONE: 313-895-7215

B2
18.

EMERSON ELECTRIC CO

PITTSBURG, PA

PHONE: 412-967-3800

19.

E. H. KELLOG

MT. VERNON, N.Y.

PHONE: 914-664-3045

20 . UNION CARBIDE SILICONES

OLD RIDGEBURY ROAD

DANBURY, CONNECTICUT

PHONE: 1-800-331-9275

21 . UNION CARBIDE

NEW YORK

PHONE: 1-800-242-7226 OR 914-784-2278

22 . NORTON PETROLEUM CO.

290 POSSUM PARK RD.

NEWARK, DE

PHONE : 302-731-8220

23.

PARATHERM CORP.

1050 COLWELL LANE, BLDG #2

CONSHOHOCKEN, PA 19428

PHONE: 215 941-4900

24.

AMERICAN HYDROTHERM CO

MANHATTEN, NY

PHONE: 212 —889-7100

25.

KEMSTAR CORP

LOS ANGELES, CALIF.

PHONE : 213-391-8510

26.

DUPONT-BLOOMINGTON

PHONE: 302-774-1000

27.

AMETEC CORP

DELAWARE

PHONE: 302-995-0560

DUPONT-BLOOMINGTON 302-774-1000

B3
Foreign Companies Contacted bv Correspondence

Soken Chem. & Engineering Co. Ltd

Japan

Hoechst UK Ltd.

Great Britain

Wacker-Chemie

Germany

Rhone-Poulenc Ltd

Great Britain

Burmah-Castrol Ltd.

Ireland

Bayer UK Ltd.

Great Britain

Petrofina UK Ltd.

Great Britain

Hercules Ltd.

Great Britain

Degussa Ltd.

Great Britain

Esso Petroleum Co.

Great Britain

Huls Nederland

The Netherlands

B4
March 20, 1989

Hoechst UK Ltd.

Hoechst House

Salisbury Road

TW46JH Hounslow

Great Britain

Dear Sir or Madam:

I am currently associated with a research project for the

U.S. National Aeronautics and Space Administration (NASA)

.

We are searching for suitable heat transfer fluids that may

be used on manned spacecraft. If your company is a supplier

or manufacturer of heat transport media, would you please

forward this letter of inquiry to the appropriate

department.

The candidate heat transfer fluid (single component or

azeotropic mixture) is to operate two-phase (boiling system)

in a pumped-closed-loop thermal bus. Because of certain

environmental constraints, the fluid thermodynamic

properties must fall within certain limits.

Two other especially important requirements of the candidate

fluid are that it must be nontoxic and nonflammable. A list

of the requirements are:

(1) Freezing point less than 0°C.

(2) Vapor pressure at ambient temperature (approximately

20 &C greater than 1 atm.

(3) Critical temperature greater than about 50°C.

(4) Flash point greater than 205°C, fire point greater than

230°C.

(5) Nontoxic and will not decompose into toxic substance (s)

when subjected to high temperature, about 300°C. This is

not an operating temperature; this temperature may be

encountered in a failure condition on the surface of a

catalytic converter.

If your company can supply a fluid meeting the above

requirements, would you please send us a letter or brochure

containing the fluid's technical data, pricing and

availability. We would also be interested in fluids

approximately meeting the requirements.

B5
Companies Specializing in CFC Production Contacted by

Correspondence

Hoechst Aktiengesellschaft

Germany

Asahi Glass Co. Ltd.

Japan

Showa Denko KK. Ltd

Japan

E. I. du Pont de Nemours Co.

USA

Allied Signal Corp

USA

Essex Chemical Corp./Racon Inc.

USA

Pennwalt Corp.

USA

Akzo Chemical BV

The Netherlands

Daikin Industries Ltd.

Japan

Kali Chemie Aktiengesellschaft

Germany

Atochem SA

France

B6
March 27, 1989

Hoechst Aktiengesellschaft

Brueningstr. 38

Frankfurt, Hessen 6230

West Germany

Dear Sir or Madam:

The National Institue of Standards and Technology is

currently associated with a research project for the U.S.

National Aeronautics and Space Administration (NASA) . We

are searching for suitable heat transfer fluids that may be

used on manned spacecraft.

The candidate heat transfer fluid (single component or

azeotropic mixture) is to operate two-phase (boiling system)

in a pumped-closed-loop thermal bus. Because of certain

environmental constraints, the fluid thermodynamic

properties must fall within certain limits.

Two other especially important requirements of the candidate

fluid are that it must be nontoxic and nonflammable. A list

of the requirements are:

(1) Freezing point less than 0°C.

( 2 ) Vapor pressure at ambient temperature (approximately

20 t) C) greater than 1 atm.

(3) Critical temperature greater than about 50°C.

(4) Flash point greater than 205°C, fire point greater than

230°C.

(5) Nontoxic and will not decompose into toxic substance (s)

when subjected to high temperature, about 300°C. This is

not an operating temperature; this temperature may be

encountered in a failure condition on the surface of a

catalytic converter.

We are aware of your company's production of

chlorofluorocarbons which except for item (5) above might be

a suitable candidate. Therefore, we would like to know if

you can supply any alternative fluids which might be

considered for this application. Please provide any

relevant technical information that you have available for

our consideration. A telephone call or letter from your

technical or marketing department, if you require further

information, would be welcome.

B7
J
Contract T-4528P

Lyndon B. Johnson Space Center

NONTOXIC HEAT TRANSPORT FLUIDS FOR SPACECRAFT TWO-PHASE

THERMAL CONTROL SYSTEMS

Final Report

September 30 , 1989

Patricia J. Gikrratano

Op^nvestigator

James F. Welch

/t^U/Vu3\f*-/

DivosTonChief

Chemical Engineering Science Division

Larry L ./sparks

Director

Center for Chemical Engineering

Neil A. Olien

National Institute of Standards and Technology

Center for Chemical Engineering

Boulder, Colorado

80303

U.S. GOVERNMENT PRINTING OFFICE:! 9 9 0 -774-5 3 6 / 2 5 0 4 9
wm
IST-114A U.S. DEPARTMENT OF COMMERCE

}EV. 3-89) NATIONAL INSTITUTE OF STANDARDS AND TECHNOLOGY

BIBLIOGRAPHIC DATA SHEET

1. PUBLICATION OR REPORT NUMBER

NISTIR 89-3932

2. PERFORMING ORGANIZATION REPORT NUMBER

3. PUBLICATION DATE

January 1990

TITLE AND SUBTITLE

NONTOXIC HEAT TRANSPORT FLUIDS FOR SPACECRAFT TWO-PHASE THERMAL CONTROL SYSTEMS

AUTHOR(S)

Patricia J. Giarratano, James F. Welch

PERFORMING ORGANIZATION (IF JOINT OR OTHER THAN NIST, SEE INSTRUCTIONS)

U.S. DEPARTMENT OF COMMERCE

NATIONAL INSTITUTE OF STANDARDS AND TECHNOLOGY

GAITHERSBURG, MD 20899

7. CONTRACT/GRANT NUMBER

T-4528P

8. TYPE OF REPORT AND PERIOD COVERED

Report to Sponsor Sep 88-Sep 89

SPONSORING ORGANIZATION NAME AND COMPLETE ADDRESS (STREET, CITY, STATE, ZIP)

Lyndon B. Johnson Space Center

Houston, TX 77058

. SUPPLEMENTARY NOTES

DOCUMENT DESCRIBES A COMPUTER PROGRAM; SF-185, FIPS SOFTWARE SUMMARY, IS ATTACHED.

. ABSTRACT (A 200-WORD OR LESS FACTUAL SUMMARY OF MOST SIGNIFICANT INFORMATION. IF DOCUMENT INCLUDES A SIGNIFICANT BIBLIOGRAPHY OR

LITERATURE SURVEY, MENTION IT HERE.)

This report summarizes an investigation to determine the availability of a nontoxic,

nonflammable, noncorrosive and thermally stable heat transport fluid suitable for twophase thermal control systems in manned spacecraft. Approximately 860 chemical substances

were sorted and ranked according to parameters that were defined and calculated to

quantitatively evaluate fluids for the proposed application. A methodology was developed

for the evaluation and ranking. A survey of world suppliers of heat transport fluids

was also conducted to determine whether a suitable fluid is available. The investigation

did not identify a fluid that can meet all the environmental and thermal property

requirements required for safe and efficient performance in the spacecraft application.

!. KEY WORDS (6 TO 12 ENTRIES; ALPHABETICAL ORDER; CAPITALIZE ONLY PROPER NAMES; AND SEPARATE KEY WORDS BY SEMICOLONS)

commercial heat transport fluids; heat transport; nontoxic fluids; spacecraft;

thermal control ; two-phase

J. AVAILABILITY 14. NUMBER OF PRINTED PAGES

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WASHINGTON, DC 20402.

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