Predicted Values of the Viscosity and Thermal Conductivity Coefficients of Nitrous Oxide"

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<5 NBS TECHNICAL NOTE 693

NBS Pubii - cations

U.S. DEPARTMENT OF COMMERCE / National Bureau of Standards

Predicted Values of the Viscosity and Thermal Conductivity Coefficients

of Nitrous Oxide

QC 100 U5753 no. 693 1977 NATIONAL BUREAU OF STANDARDS

1 The National Bureau of Standards was established by an act of Congress March 3, 1901. The Bureau's overall goal is to strengthen and advance the Nation's science and technology and facilitate their effective application for public benefit. To this end, the Bureau conducts research and provides: (1) a basis for the Nation's physical measurement system, (2) scientific and technological services for industry and government, (3) a technical basis for equity in trade, and (4) technical services to promote public safety. The Bureau consists of the Institute for Basic Standards, the Institute for Materials Research, the Institute for Applied Technology, the Institute for Computer Sciences and Technology, the Office for Information Programs, and the Office of Experimental Technology Incentives Program.

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1 Headquarters and Laboratories at Gaithersburg, Maryland, unless otherwise noted; mailing address Washington, D.C. 20234. a Located at Boulder, Colorado 80302. m* t * iwi Predicted Values of the Viscosity and

Thermal Conductivity Coefficients

r of Nitrous Oxide 1

Howard J. M. Hanley

Cryogenics Division Institute for Basic Standards National Bureau of Standards Boulder, Colorado 80302

* L T J /

U.S. DEPARTMENT OF COMMERCE, Juanita M. Kreps, Secretary

Dr. Betsy Ancker-Johnson , Assistant Secretary for Science and Technology

NATIONAL BUREAU OF STANDARDS, Ernest Ambler, Acting Director

Issued March 1977 NATIONAL BUREAU OF STANDARDS TECHNICAL NOTE 693

Nat. Bur. Stand. (U.S.), Tech Note 693, 64 pages (March 1977)

CODEN: NBTNAE

U.S. GOVERNMENT PRINTING OFFICE WASHINGTON"; 1977

For sale by the Superintendent ot Documents, U.S. Government Printing Office , Washington, D.C. 20402

Order by SD Catalog No C 13. 46:693). Price $1.20 (Add 25 percent additional for other than U.S. mailing). 1

CONTENTS Page

Abstract 1

1. INTRODUCTION 1

2. DATA SURVEY 1

3. PREDICTION METHOD 2

3 . Summary 8

3.2 Kinetic Theory 8

3.3 The Behavior of the Thermal Conductivity Coefficient in the

Critical Region 9

4. COMPARISONS WITH DATA 10

5. TABLES 12

5.1 Assessment of Accuracy 12

6. MIXTURES 31

7. CONCLUSION 31

8. ACKNOWLEDGMENTS 31

9. REFERENCES 48 APPENDIX. Application of Statistical Mechanics 50

Note on Units

The results in this paper are given in British Engineering units at the specific request of the sponsor. Selected results, however, are also given in SI units to conform with the policy of the National Bureau of Standards to promote the SI system.

in LIST OF FIGURES Page

Figure 1. Top curve: 1 atm viscosity percent deviation plot

between values predicted from equation (20) and the

correlation equation (31) . Percent deviation is defined

as n[eq. (20)] -n[eq. (31) ]*100.0/n[eq. (31)]. Bottom

curve: 1 atm thermal conductivity deviations between

equation (21) and equation (31) 14

Figure 2. Dense gas and liquid isotherms for the thermal conduc-

tivity coefficient calculated from equation (21) (curves)

compared with the data of reference [19] (open and filled

circles) 16

Figure 3(a). Viscosity coefficient of dilute N„0: comparison between

kinetic theory values and equation (31) 58

Figure 3(b). Plot of the second virial, B, versus temperature. Data,

filled circles, from reference [30]. The curve is from

equation (9A) , while the triangles are results discussed

in the text 58 . .

PREDICTED VALUES OF THE VISCOSITY AND THERMAL CONDUCTIVITY COEFFICIENTS OF NITROUS OXIDE"

Howard J. M. Hanley

The viscosity and thermal conductivity coefficients of nitrous

oxide are calculated for temperatures between 180 and 900 K (330 to

1600°R) for pressures to 23 MPa (^ 3500 psi) . Tables of values are presented. Two mixtures with carbon dioxide are also discussed. These transport coefficients (for the pure fluid and for the mixtures) were predicted from thermodynamic data. Details of the prediction procedure are presented. Estimates of the accuracy of the tabular values are

+ 6% for the viscosity and + 8% for the thermal conductivity.

Key words: Carbon dioxide; corresponding states; mixtures; nitrous oxide; prediction; thermal conductivity; transport property; viscosity.

1. INTRODUCTION

In this report we discuss the transport coefficients — the viscosity coefficient (f)) and the thermal conductivity coefficient (A) — of nitrous oxide,

N~0. Tables of values are presented from 0.1 to 23 MPa (approximately 15 to

3500 psi) for temperatures between 180 and 900 K (approximately 330 to 1600°R) Two selected' mixtures of nitrous oxide and carbon dioxide are considered briefly,

Nitrous oxide is a common substance yet the transport coefficients have not been measured over a wide temperature and pressure range. In fact, the data are so scarce we prefer to obtain the coefficients by calculation [1]: the limited data are used only to check the procedure where possible.

2. DATA SURVEY

A bibliography of data sources for the thermodynamic and transport properties of nitrous oxide was prepared by the Cryogenic Data Center, National Bureau of Standards, Boulder, Colorado. The appropriate references for the

Contribution of the National Bureau of Standards, not subject to' copyright viscosity and thermal conductivity are as follows: viscosity coefficient ,

references [2]-[8]; thermal conductivity coefficient , references [9]-[23].

We have correlated the transport coefficients of several simple fluids

[Ar, 0„, N„ , CH, , C~H,] in a series of papers [24]. Criteria were set up to evaluate data critically, and an equation to represent the coefficients was proposed. Unfortunately, this procedure cannot be applied to nitrous oxide at this time because suitable data are not available for analysis. We have been able to find only two data sets for the dense gas and liquid, those from references [19] and [23], for the thermal conductivity. The other references cover the dilute gas only.

As remarked, therefore, we decided to present tables based on a prediction procedure, which will be outlined in the next section.

3. PREDICTION METHOD

The method used is an application of a procedure introduced in detail in reference [1]. An outline is given here.

As is well known, if classical two-parameter corresponding states applies to two fluids designated a and o, one can write the viscosity of one at a density

(p) and temperature (T) , in terms of the other:

= -« (i) n (p,t) n (p , t )(-*) (-«) lp o

Also for the thermal conductivity,

1/2/ c\2/3/^cvl/2 Vp.t) = up„_.(p t„ j\~\ \-a 1^1 (2) » vv| (7) (7)

In the above equations, M is the molecular weight, and p and T are the density and temperature respectively, for fluid o to correspond to the density and temperature for fluids a. The variables can be expressed in terms of the C C p° /p*~) /T The critical parameters, and T ; thus, p^ = p(p and T = T(T ). CXjO OCX \X y O (JUL coefficients r| and A also have to be scaled as shown in equations (1) and (2). o o It is common practise to calculate the coefficients for a given those for

o — which is then treated as a reference fluid.

Equations (1) and (2) can be extended for a mixture, x, if it is assumed that the mixture can be represented as an equivalent pure fluid — the one-fluid approximation — and that the mixture is "conformal," that is, all components obey the two-parameter corresponding states law. Hence one can write

1/2/ c\2/3/_c\l/2

T) T ; V?> " pa,o- a,o' V ,«(?)\tl \f>

and similarly for the thermal conductivity, A . Equation (3) can be derived under well-defined assumptions [25] . The derivation further yields a set of mixing rules:

Ct p and

C C 1 C C 1 T (pK ) = Z Z x x T (p ) (5) x x „ a MP ag

where x is the mole fraction of a. The mixing rule used in this work for the mass is M = Z x M (which differs slightly from that proposed in reference [25])

The a$ variables of equations (4) and (5) are given by

c C ly/2 T = F (t° T ) (6)

and

- c l 1 c ,-1/3 . 1 . c .-1/3 / \ = i , (p } (p + (p } (7) aS ^a3 2 aa> 2 33 where E, a and \\l D are binary interaction parameters, which are best obtained CXp Ctp from experiment.

The mixing rules, equations (6) and (7), are consistent with the mixing rules derived for thermodynamic properties using the one-fluid approximation.

If, therefore, the binary interaction parameters are assumed to be those valid

for thermodynamic properties , one has a procedure to predict the viscosity and thermal conductivity coefficients of mixture x, given the equivalent coefficients of the reference fluid.

Equations (l)-(3) are not general in that two-parameter corresponding states is invalid for polyatomic fluids, or for mixtures containing polyatomic molecules. The situation is, of course, paralleled with respect to the thermodynamic properties and has been discussed extensively in this latter context. For example, a recent approach due to Leland [26] and to Rowlinson [27], is of interest here. According to Leland and Rowlinson a third parameter, co — which can be taken as the Pitzer acentric factor — is introduced, but the framework of simple two-parameter corresponding states is preserved, if one considers the scaling functions

C C C f (T ; = /T ) h (P /P° ) (8) aa,o aa o aa,o aa,o o aa T aa,o

for fluid a with respect to o. The terms 6 and 6 are called shape factors r aa,o aa,o and are weakly varying functions of temperature and density:

6 = 1 (co -co = 1 + (co -co )G(T,p) + )F(T,p);

where co and co are acentric factors for fluids a and o, respectively. Using aa o the shape factors, the compressibility factor (for example) of a would be given

by the relation Z (p,T) = Z (ph , T/f ). With the appropriate expression 3 a o aa,o aa,o for the Helmholtz free energy, the thermodynamic properties of a are completely defined in terms of the properties of o.

It is a logical step to introduce shape factors into the viscosity and thermal conductivity expressions: for fluid a, therefore n n (p,t) = n (p' , t' ) FH (io) a o a,o a,o a,o where

"2/3 l/2 p' - = n = Ph ; T' T/f ; FH -£ ) h f ( , a,o aa,o a,o aa,o a,o fe)'"\M / aa,o aa,o

Similarly,

T A A = (p' , ) (p,T)K ' X T FH (12) a o a,o a,o a,o where

2/ 3 l/2_ FH* - U h" £ (13) a,o \M / "aa,oaa,o aa,o \M /V

And for mixtures,

T) T (14) \ ( P' = % ( x,o }

X A (p,T) = A (p' , T' ) FH (15) x o x,o x,o x,o

For mixing rules for h and f we take x,o x,o

h h (16) x,o =ZExxa a3,oD a 3

f h =EZxx D f h D (17) x,o x,o _ a 3 a3,o a3,o

with 1/2 f " (f f ) (18) a(3,o ^ag aa,o 3g,o and

3 1 ,1/3 1 ,1/3 I + 3l r h h *« -1 (19) a(3,o ag 2 aa,o 2 ;,oJ

An evaluation of equations (10), (12), (14) and (15) is discussed in reference [1]. In particular we were interested if these equations could be used to predict the transport coefficients of a or x, given values for the reference fluid. Specifically, one might hope that equations could be used

successfully if the shape factors, 9 and (J), and the mixing interaction

parameters, and \\) , were taken from a fit of thermodynamic (PVT) data. £ R R Unfortunately, the equations could not represent data satisfactorily if the above constraint was imposed.

We have, however, been able to propose a possible modification; we suggested that one should consider expressions of the form

n n n (p,T)K = n (p' , T» ) FH X (p,T) (20) a ' o a,o a,o a,o a,o and

A X 1 A (p,T) = A (p , T' ) FH X (p,T) (21) a o a,o a,o a,o a,o

with corresponding expression for the mixture. Note that equations (20) and (21) differ from those introduced earlier by the factor X or X„ . Based on how J a,o a,o equations (20) and (21) represent experiment, it turns out that X should be unity if fluids a and o follow classical two-parameter corresponding states, as in the case of the rare gases and their mixtures [25], but should be a function of temperature and density otherwise.

No formal equation is available for X but a possible expression was

determined in reference [1] . The expressions are based on a study of the Modified Enskog Theory. This theory has been discussed in detail in our previous work [28]. Following the arguments that are given in full in reference [1], we obtained for the pure fluid (with corresponding expressions for the mixture)

X^ (p,T) = Q G^ : X* (p,T) = Q G* (22) ot,o ot,o ot,o a,o 0L,O 0L,0

Q is function of p and T defined as a,o

- (pC/p)3] [1 1/exP = [(bp) /(bp) (23) n ]

where b is a term given by b = B + TdB/dT, with B the equilibrium second virial coefficient. G and G are ratios bgiven, respectively, by -,a,o, a,o n n n G = [] /[] and []/[]. The bracket expressions are [28] a,o a o a o

n [] = [1/bpx + 0.8 + 0.761 bpx]

(24) A [] = [1/bpx + 1.2 + 0.755 bpX ] with

- i < 25 > PR !;^ \3TJp

for fluids a or o. R is the gas constant.

Notice that the calculation of the correction factors X and X require only thermodynamic information for fluid a or x with respect to the reference fluid; for example, b [Equation (23)] can be obtained from the second virial

coefficient of the reference fluid, B , according to the expression o

(h B ) aa '° b (T) = h B + T d - (26) a aa,o o dT and similarly for the term bpx [equation (25)]. 3 . 1 Summary

To summarize the calculation procedure. To calculate the coefficients of

a fluid, a, or mixture, x, one needs (a) the viscosity and thermal conductivity

coefficients of a reference fluid, (b) the shape factors and, if necessary, the mixing parameters of the fluid with respect to the reference fluid; these quantities to be obtained from a fit of thermodynamic data. The viscosity and thermal conductivity of a or x follow from the equations

= 1 n n n VK(P,T) n (pK , T' ) FH x v(20)' a ' 'o a,o a,o a,o a,o

A ? A \ (p,T) = A (p , T ) FH X (21) a o a,o a,o a,o a,o

= n n n (p,t) n (p' , t' ) FH x (27) x o x,o x,o x,o x,o

A A X (p,T) = X (p' , T' ) FH X (28) x o x,o x,o x,o x,o

In this work a is, of course, nitrous oxide. Methane was chosen as the reference fluid and numerical values of the transport coefficients were those of the correlation of Hanley, Haynes and McCarty [24]. The equation of state for methane used here is due to Goodwin [29].

Shape factors for nitrous oxide with respect to methane, equation (8), were obtained by analyzing the PVT data of Couch, Kobe and Hirth [30]. The procedure is due to McCarty [31] and will not be described here.

3.2 Kinetic Theory

For consistency, the transport coefficients of nitrous oxide for all pressures and temperatures will be calculated by the method summarized in section 3.1. However, alternative approaChs are possible for the dilute gas since some data are available. In previous work on the dilute gas [32-34], we have used an empirical fit of data and/or calculated values via statistical mechanics and kinetic theory. This latter approach has several advantages, one of which is that statistical mechanics and kinetic theory allow an assessment to be made of systematic error by comparing independently measured properties through the pair potential function. For example, in references [32-34], we showed the transport properties of the rare gases, and oxygen and nitrogen were consistent with their respective second virial coefficients. As a matter of interest, nitrous oxide is briefly discussed along these lines in the Appendix.

3.3 The Behavior of the Thermal Conductivity Coefficient in the Critical Region

It is now well known that the thermal conductivity behaves anomalously in the vicinity of the critical point: in fact the coefficient will approach infinity as the density and temperature approach their critical values. An account of this phenomenon is given in reference [35], and it is considered in our previous data correlations of argon, oxygen, nitrogen and methane [24]. Undoubtedly, nitrous oxide will also display the anomaly.

The anomaly can be calculated directly and is discussed in reference [35] but it is included indirectly in our corresponding states procedure as follows.

The thermal conductivity is given by equation (21)

X X A (p,T) = A (p , T ) FH X (p,T) (21) a o a,o a,o a,o a,o

where a E NO and o E CH , but A can be separated into two terms, the , conductivity in the absence of a critical point anomaly, A', and the anomaly

itself, A : o

c A = A' + A (29) o o o

Hence

A A C A A A = A' FH X + A FH X (30) a o a,o a,o o a,o a,o n Since we have incorporated A in the methane correlation, A will have an r o a equivalent contribution.

4. COMPARISONS WITH DATA

Comparisons between our calculated values of the transport properties of

nitrous oxide and data are restricted to the dilute gas region, and to one data

set for the thermal conductivity [19]. First the dilute gas.

We attempted to assess the accuracy of the dilute gas viscosity data using

the arguments discussed in reference [24]. Data from references [6] and [7] were selected as the most reliable with an estimated accuracy of + 3%.

The dilute gas thermal conductivity data were also evaluated as far as

possible. Data from references [10], [14] and [18] were selected as the more

reliable with an estimated accuracy of + 6%.

Following the procedure of our previous work [24], the selected viscosity

and thermal conductivity data were fitted to an empirical function for computation convenience

X 2/3 1/3 1/3 n° = GV(1)T + GV(2)T + GV(3)T + GV(4) + GV(5)T

(31) 2/3 4/3 5/3 + GV(6)T + GV(7)T + GV(8)T + GV(9)T

and similarly for A°, but with coefficients GT(i)(i = 1...9) replacing GV(i)

in equation (31). n and X refer to the dilute gas viscosity and thermal conductivity coefficients, respectively. Values of GV and GT are listed in

table 1.

10 Table 1. Values of the coefficients of equation (31) for the dilute gas

viscosity, n, , and the dilute gas thermal conductivity, A . Units: temperature in K, n. in ug/(cm*s) and A in mW/(m*K).

GV(1 .2546211337E+07 GV(2 -.1670382040E+07 GV(3 .2898185505E+06 GV(4 .3474760268E+05 GV(5 -.1674096936E+05 GV(6 .1445438546E+04 GV(7 .8767956930E+02 GV(8 -.1932828150E+02 GV(9 .7959594290E+00

GT(1 -.1550251226E+07 GT(2 •9682908726E+06 GT(3 -.2120883669E+06 GT(4 .1779303821E+05 GT(5 -.9793550977E+03 GT(6 •3480491811E+03 GT(7 -.6424000898E+02 GT(8 .4582750314E+01 GT(9 -.1120206739E+00

11 Figure 1 displays a deviation plot between the experimental data fitted to equation (31), and our estimates from equations (20) and (21), with the pressure set at one atmosphere. Our representation of the dilute gas viscosity coefficient can be considered satisfactory, the thermal conductivity less so. for both coefficients systematic differences are observed but it is not clear whether they are caused by errors in the procedure, or are due to errors in the data. A possible reason for the deviations in the thermal conductivity is that our method does not take into account correctly the contribution of the internal degrees of freedom of nitrous oxide. This problem is under further investigation.

We next compared our predicted conductivities for nitrous oxide with the dense gas and liquid data of reference [19]. The result is shown in figure 2.

It is seen that the calculated values are within about 5%, or less, of the measured values.

5 . TABLES

Tables of values for the viscosity and thermal conductivity coefficients

of nitrous oxide were generated from equations (20) and (21) . Tables 2 and 3 give the results in the SI system of units, tables 4 and 5 in engineering units.

For convenience, saturated liquid values are listed separately as table 6 .

5.1 Assessment of Accuracy

An estimation of the accuracy of the tabular values is clearly difficult and has to be based mainly on how well the prediction method can represent other fluids for which reliable data are available. For nitrogen, ethane, propane, butane and carbon dioxide, and their mixtures, we were generally able to predict the coefficients to within about 6% using methane as the reference fluid. Here we have represented the dilute gas viscosity data to 3% and the dilute gas thermal conductivity data to 10%. The dense gas thermal

* The number of significant figures for an entry are more than the accuracy of the calculations warrant (see Section 5.1). Extra figures are included to facilitate interpolation if required.

12 conductivity measurements of reference [19] have been represented to within 6%.

Based on the above two factors, and our experience in evaluating data for fluids similar to nitrous oxide, we estimate the viscosity to be accurate to + 6% and the thermal conductivity to be accurate to + 8%. In the critical region this latter figure should be increased to + 20%. As in our previous work, these assessments refer to an accuracy estimation on a 2a basis.

13 .

Figure 1. Top curve: 1 atm viscosity percent deviation plot between values

predicted from equation (20) and the correlation equation (31) . Percent deviation is defined as n[eq. (20)] - n[eq. (31) ]*100. 0/n [eq. (31)].

Bottom curve: 1 atm thermal conductivity deviations between equation (21) and equation (31)

14 1 •

•

1 1

•

- • — <

• >-

CO • o - o — CO — > •

•

— • —

1 m—

N0I1VIA3Q lN33U3d

15 Figure 2. Dense gas and liquid isotherms for the thermal conductivity coefficient calculated from equation (21) (curves) compared with the data of reference [19] (open and filled circles).

16 300

PRESSURE, atm

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H "0 J- X> CO CD <\l <7> ro XI o> ro p*. X) CD in ^4 in rt (NJ PJ pj ^J pj ro ro ro 4- m in X) vO r>- *-< cn HCU CO CP X) PJ •o in 4> J3 o J3 J- PJ CD p. ro CP a 3 cp CT> CO CP pj ro PJ ro P» (M o o pj in CO CP rt H -4 PO XI CO rt fO PJ in ro rt in CD 4- CP in rt rt pj PJ pj PJ ro ro fO J- in in XI X> X)

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PJ ro in r» CD PJ in rt 4- CO pj o C3 4- 0» ro CO o rt PJ PJ pj pj ro ro ro in in in X) X) PJ

^ CD o CD cd o C3 CD "3 CD CD CD «o PJ X> o 4- CO pj -O CD * CO pj X) 4- PJ J3 CD PJ PJ ro ro to m in in X3 X) P» CO CO CP

19 -2 Table 4. The viscosity coefficient of nitrous oxide. Pressure in 10 psi

[i.e., pressure in psi is obtained by multiplying by 100.0], temperature in degrees Rankine, viscosity coefficient in 10 lb/(ft.s) [i.e., to obtain X] in lb/(ft.s), multiply the entries by 10 ].

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24 Table 5- The thermal conductivity coefficient of nitrous oxide. -2 Pressure in 10 psi [i.e., to obtain the pressure in psi multiply by 100.0], 3 temperature in degrees Rankine, thermal conductivity in 10 BTU/(ft. hr. °R) _3 [i.e., to obtain A in BTU/(ft. hr. °R) , multiply the entries by 10 ].

25 1 i

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rv i-i ro in ro rw *4 m C3 v0 o» CO I*. S. K |v K. CO 1-1 o O CO CO rv vO <0 J- CM CM H in

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CM CO J- r- i-4 CO CM <0 o J- o» CO t4 o o a* co CO rv <0 V0 m in ro CM i-l T-l

ro ro o in r». cr CO CO CO CO CM o o"> in rv ro o o CO »-l rv -t CM CO CD in in CO o in in in CM

CO tv , «-l ro O CO CM o> ^ .* CT> N. N. -D >0 V0 kD JD >0 rv t4 o O CO CO rv V0 in i-l i-l

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27 t

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CM * in r- CO <7> o CM ro in r^ CO o CM ro m CM CM CM CM CM ro ro ro fO ro ro

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Ha)

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r>- o i-l CM ro in CO o CM ro in CM H CM CM CM CM CM CM CM CM ro ro ro ro ro ro

CM i-l a o CM in in ro i-i CO >0 ro CT> co in i-i a o 1-1 ro 10 a in i-i CO i0 in CO CM

eo i-l CM ro in CO o iH ro in r^ i-i — —1 CM CM CM CM CM CM CM CM ro ro ro ro ro ro

i-l CM m CO iH CM ro ro CM CJ> ro o i-l «o CO o CD ro ro CM CM ro m o

US O -4 CM in 10 CO •4 ro in 9> t4 i-l i-l CM CM CM CM CM CM CM CM ro ro ro ro ro

i-l CM in CJ» O CM CM o CO CM i-4 N. O in in

IS CO CM ro in 10 CO CT> i-i ro m r^ 0> H ro i-t i-l CM CM CM CM CM CM CM CM ro ro ro ro ro

cc O o CO o CO co co eo CD CD a o o o CO

29 Table 6. Saturated Liquid Transport Coefficients for NO

T T n

°F °R lb-mass/f f s BTU/hr«ft«°F

127.03 332.64 .25188E-03 .11312E+00

• 99.99 359.68 .19866E-03 .10210E+00

• 50.0 409.66 .13464E-03 .84157E-01 40.0 419.67 .12516E-03 .80840E-01 22.0 437.67 .10998E-03 .75034E-01

• 4.0 455.67 .96711E-04 •69392E-01 5.0 464.67 •90656E-04 .66617E-01 14.0 473.67 .84921E-04 .63863E-01 23.0 482.67 .79464E-04 .61126E-01 32.0 491.67 .74250E-04 .58405E-01 41.0 500.67 .68980E-04 .55536E-01 50.0 509.67 .63901E-04 .52725E-01

59.0 518.67 58956E-04 .50018E-01 68.0 527.67 ,54078E-04 .47495E-01 77.0 536.67 .49158E-04 .45266E-01 86.0 545.67 .44106E-04 .43498E-01

95.9 555.57 , 38150E-04 .42357E-01

30 6 . MIXTURES

Equations (27) and (28) were used to generate tables for two mixtures of

nitrous oxide with carbon dioxide: compositions C0„ (12%) - N„0 (88%) and

C0„ (6%) - N„0 (0.94%), respectively. The results are tables 7-10. Since carbon dioxide is so similar to nitrous oxide, our accuracy assessments for pure nitrous oxide are probably valid for mixtures. No data are available for comparisons.

7. CONCLUSION

We have predicted the transport coefficients of nitrous oxide, and of

nitrous oxide/carbon dioxide mixtures using a significant modification of the corresponding states procedure. Tabular values have been listed. Data available

for comparisons are scanty. More, and more reliable, data will be required if

the accuracy of the tables is to be improved.

8 . ACKNOWLEDGMENTS

We are very grateful to R. D. McCarty for his help with the PVT calculations,

to P. M. Holland for valuable discussions on the statistical mechanical

calculations reported in the Appendix, and to Karen Bowie for her help in preparing the manuscript.

This work was supported by the Air Force Weapons Laboratory, Kirtland Air Force Base, New Mexico, Contract No. 76-258. Also (in part) by the Office of Standard Reference Data.

31 1 1 1 « 1 i

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