solubility of n2o in and density and viscosity of aqueous solutions of butan4

7252019 Solubility of N2O in and Density and Viscosity of Aqueous Solutions of Butan4

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Solubility of N2O in and Density and Viscosity of Aqueous Solutionsof 14-Butanediamine 2‑(Diethylamino)-ethanol and Their Mixturesfrom (29815 to 33315) K Zhicheng Xu Shujuan Wang and Changhe Chen

Key Laboratory for Thermal Science and Power Engineering of Ministry of Education Beijing Key Laboratory for CO2 Utilizationand Reduction Technology Department of Thermal Engineering Tsinghua University Beijing 100084 China

ABSTRACT Densities of and N2O solubilities in aqueoussolutions of 14-butanediamine (BDA) 2-(diethylamino)-ethanol (DEEA) and their aqueous mixtures were measuredat (29815 31315 and 33315) K and viscosities were measured at(29815 30315 31315 32315 and 33315) K The experimentscover the mole fraction ranges (195minus143 mol ) BDA

(201minus193 mol ) DEEA and (363minus167 mol ) BDA +(262minus222 mol ) DEEA in the blended solutions Theresults were compared with available data in the literature Theexperimental density and viscosity data were correlated using two semi empirical correlations in the literature as functions of temperature and concentration of BDA and DEEA

INTRODUCTION

Absorption of CO2 with amine-based absorbents is anestablished and proven technology1 Many solvents such asmonoethanolamine (MEA) methyldiethanolamine (MDEA)diethanolamine (DEA) and piperazine (PZ) have been appliedto capture CO22minus4 However this process always requires lots of

energy during solvent regeneration Recent years the novelprocess of biphasic system DMX and lipophilic solvents wereproposed with the energy consumption of DMX system beingestimatedto be23GJtCO2

5 6Dimethylcyclohexylamine (DMCA)dipropylamine (DPA) and DPA and DMCA blend 3-(methylamino)propylamine (MAPA) and DEEA blend and someother unspeci1047297ed amines in the literatures were studied for the

biphasic system7minus11

The previous researches have investigated CO2 absorption by some potential biphasic solvents The mixture of 875 mol BDA and 175 mol DEEA (2 M BDA+4 M DEEA) was foundto be a potential biphasic solvent and has 46 higher cyclicloading 48 higher cyclic capacity and 11 higher cyclicefficiency than 30 mass MEA The phase separation of thesolution after CO

2 absorption was due to the fast reaction rate of

CO2 with BDA and the limited solubility of DEEA in the reactionproducts of BDA and CO212minus14

As one of the most important issues in evaluating a solventkinetics parameters are typically derived from the experiments

based on mass transfer process and the data of physicaldiff usivity and solubility of CO2 in aqueous solvents solutions arerequired However due to the chemical reactions between CO2

and amine these properties are not possible to be measureddirectly15 It is suggested that using ldquoN2O analogy rdquo to estimatethe aforementioned physicochemical properties since N2Oresembles CO2 in molecular volume con1047297guration and electronicstructure and it is a nonreactive gas in amine conditions16minus18 as

shown in eq 1 Moreover densityand viscosity of aqueous solventsare also essential for the calculation of other physicochemicalproperties such as diff usivity gas solubility and reaction rateconstants

=‐

‐

‐

‐

⎛

⎝

⎜⎜

⎞

⎠

⎟⎟H H

H H CO Am

CO H O

N O H O

N O Am2

2 2

2 2

2

(1)

BDA has been widely investigated by evaluating the eff ect of chain length on the absorption and desorption capacity of

biamine and by measuring the vapor liquid equilibrium of pureBDA19minus22 However so far as we know there is still no literaturereporting the solubility of N2O in and density and viscosity of BDA aqueous solution

DEEA is usually blended with other activators (for examplepiperazine) to absorb CO2 because of its low reaction rate Thedensities of aqueous DEEA solutions were presented by Barbas et al and Lebrette et al23 24 which did not include theconcentrations needed in our kinetics study The viscosities of aqueous DEEA solutions were measured by Maham et al andLittel et al2526 The N2O or CO2 physical solubility in aqueousDEE A solution was obtained by Littel et al Vaidya and Liet al26minus29 which just covered limited concentrations around454 mol The solubility of N2O in and density and viscosity of BDADEEA mixtures have not been presented until now

In the present work N2O solubilities in and densities of aqueoussolutions of (195minus143 mol ) BDA (201minus193 mol ) DEEAand their aqueous mixtures were measured at (29815 31315 and33315) K with viscosities measured at (29815 30315 31315

Received December 27 2012 Accepted May 15 2013Published May 24 2013

Article

pubsacsorgjced

copy 2013 American Chemical Society 1633 dxdoiorg101021je301371p | J Chem Eng Data 2013 58 1633minus1640



32315 and 33315) K The results were compared with availabledata in the literatures The experimental data on density and

viscosity werecorrelated using twosemi empirical correlations in theliterature as functions of temperature and concentrations of BDA and DEEA

EXPERIMENTAL SECTION

BDA (ge

98 wt pure) and DEEA (ge

99 wt pure) were from Aladdin Reagent Company The BDA and DEEA structures areshown below

Distilled water was used for preparing experimental solutionsThe BDA and DEEA concentrations were determined by titration against 2 N H2SO4 using a Metrohm 809 Titrando autotitrator The N2O gas (99 vol pure) was supplied by BeijingHuayuan Gas Company

Density and Viscosity In this work thedensities of aqueoussolutions were measured by National Institute of Metrology (NIM) of China strictly following theJJG 1058-2010 veri1047297cationregulation of laboratory oscillation-type liquid density metersissued by General Administration of Quality SupervisionInspection and Quarantine of China (AQSIQ) using aDMA5000 density meter NIM is Chinarsquos highest researchcenter of metrology and the national technical center of legalmetrology The result of every point was the average value of six repeated trials

The viscosities of aqueous solutions were measured by a AampDSV-10 viscometer with a measurement range of 03minus1000mPamiddots The total accuracy of viscosity given by the manufactureris plusmn 1 Calibration of viscometer was done by measuring the

viscosity of Standard Liquid GBW13601 (1203) and GBW13603

(1203) produced by NIM and approved by AQSIQ The data forthe calibration are given in Table 1

It can be seen that viscosities from the measurements agree very well with the reference values for the standard liquid

Solubility of N2O TheN2O solubility apparatus consists of a

jacketed stirred glass reactor and a stainless steel gas holding vessel as shown in Figure 1 Before experiment the volume of thegas holding vesselwas measured by 1047297lling it upwithwater andcalculating the water volume Then the total volume of thereactor and the auxiliary pipe linking the reactor and valves no3minus6 were measured by adding into it a known amount of N2Ofrom the holding vessel The added N2O amount was calculated

by the amount diff erence in the gas holding vessel before andafter adding N2O into reactor The results show that the volumeof vessel V V was 2186middot10minus3 m3 while that of the reactor and theauxiliary V R was 5628middot10minus4 m3

The reactor was1047297rst vacuumed until the pressure was less than1 kPa and then the solution wassucked into it through valve no 3

The amount of solvent added (around half of reactor) into thereactor was calculated by measuring the weight of solvent before

and after the transference After the solution reached vaporliquid equilibrium at set temperature the pressure inside of thereactor P 1N2O was recorded The temperature of the reactor was

controlled by the circulating oil bath with an uncertainty of plusmn 01 K Then N2O gas was added to the reactor by shortly opening valve No 5 linking the reactor andthe vessel Consideringthat the open period for the reactor after the solution added was

very short and the good airtightness of the reactor the vaporedamount of the solvent should be very small and can be neglectedEquilibrium was then established after 6minus15 h (depending ontemperature) with an agitation speed of 450 rmin The reactorand vessel pressure were recorded by two pressure transducers(Druck PTX 7515 with uncertainty 02 of full scale (200 kPa))Two K-type thermocouples recorded temperatures in the reactor

and in the vessel respectively with an uncertainty of plusmn 01 KThe amount added ofN2O nN2O

added mol was calculated from the

pressure diff erence of the gas supply vessel before and afterfeeding N2O as

= ‐

⎛

⎝⎜⎜

⎞

⎠⎟⎟n

V

R

P

T z

P

T z

V

V

V

V N Oadded V

1 22

1

1

2

2 (2)

where P V1 and P V2 are the pressure of the vessel before and afterfeeding Pa T V1 and T V2 are the temperature of the vessel beforeand after feeding K z1 z2 represent the compressibility factor of gas before and after the feeding R is universal gas constant83145 Jmiddot(molmiddotK)minus1 The compressibility factor was calculatedusing the PengminusRobinson equation of state

The amount of N2O in the gas phase of the reactor nN2Og can becalculated by

=

minus

n

P V V

z RT

( )N Og N O R S

N O R 2

2

2 (3)

where T R is the reactor temperature after reaching equilibriumK and z is the compressibility factor of N2O after reachingequilibrium V S is the volume of added solvent which is thequotient of added solution amount and density m3 P N2O is the

N2O partial pressure and calculated by eq 4 Pa

= minus P P PN O 1N O 2N O2 2 2 (4)

Table 1 Viscosities of Standard Solutions for Calibration29315 K 1 atm (101325middot105 Pa)

viscosity μ (mPamiddots)

standard measurement ref deviation

GBW13601(1203) 184 18388 minus007

GBW13603(1203) 880 8793 003

Figure 1 Experimental setup of N2O solubility

Journal of Chemical amp Engineering Data Article

dxdoiorg101021je301371p | J Chem Eng Data 2013 58 1633minus16401634



where P 2N2O is the total pressure of reactor after reaching

equilibrium Pa The N2O amount in the liquid phase nN N2Ol can

then be expressed as the amount diff erence between added N2Oand N2O in the gas phase by

= minusn n nN Ol

N Oadded

N Og

2 2 2 (5)

The N2O concentration in the liquid phase C N2O can be

calculated by

=C

n

V

N ON Ol

S2

2

(6)

The solubility of N2O at diff erent pressures and temperatureshave been expressed as mass fraction w (kgkg) in this paperThentheN2O solubility was expressed by a Henry rsquos law constantH N2O according to eq 7 in this paper

= P H CN O N O N Ol

2 2 2 (7)

The units of C N2O and H N2O are molmiddotmminus3 and kPamiddotm3middotkmolminus1

All operating conditions including temperature and pressure were recorded using Kingview (652 version) software

Calibrations were done by measuring the solubility of N2O in water and in 30 mass MEA at diff erent temperatures from

(29315 to 33315) K and comparing the data with the literatureThe data of N2O pressure in gas phase and concentration inliquid phase are shown in Table 2 whereas the comparisons of Henry rsquos law constant H N2O with several literature references are

shown in Figures 2 and 31530 33minus37

It can be seen that the solubility of N2O in water and in30 mass MEA measured by this work agree very well withthe literature data The uncertainty is within 3 when lessthan 31315 K whereas the diff erences were about 7 at

(32315 and 33315) K w hen compared with the data of Versteeg and van Swaai j30

RESULTS AND DISCUSSION

Density The measured densities for the aqueous solutions of BDA DEEA and BDADEEA blends are presented in Table 3and Figures 4 and 5

Table 2 Measured N2O Solubilities (Mass Fraction w kgkg) in Water and 30 Mass MEA 29315 to 33315 K in This Work

T (K) 29315 29815 30315 31315 32315 33315

water P N2O (kPa) 1110 1509 1236 1503 1427 1817

w () 01338 01677 01219 01180 00952 00829

MEA P N2O (kPa) 1417 1555 1420

w () 01402 01195 00736a

The standard uncertainty of w measurement is plusmn 2

Figure 2 N2O solubility H N2O in water this work comparing with

literature data15 303334

Figure 3 N2O solubility H N2O in 30 mass MEA this work comparing

with literature data35minus37

Figure 4 Densities of aqueous BDA solutions measured and calculated by this work





For DEEA solutions the deviations are less than 03 whencompared with Barbas et al and Lebrette et al under the sameconditions2324 as shown in Figure 5

The densities of the binary and ternary mixtures decrease with increasing mole fractions of BDA and DEEA andtemperature in the mixture The experimental density data forthe binary and ternary mixtures were 1047297tted as a function of temperature and concentration of amine using the equationproposed by Liu et al31 as shown in eq 8 The correlationparameters were 1047297tted for lowest average absolute deviation(AAD) using LevenbergminusMarquardt and Universal Global

Optimization method in the 1STOPT software produced by 7D-Soft High Technology Inc

ρ middot middot

= + + +

times + +

+

minus minus

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k k

T x k x

k

T

k

T k x k x

( 10 (kg m )

( )

exp ( )

BDA DEEA 3 3

12

BDA 3 DEEA 42

56 BDA 3 DEEA

(8)

where ρ is the density of themixture T is thetemperature and xis themole fraction of BDA or DEEA k 1 to k 6 are the correlation

Table 3 Densities of Aqueous BDA (x1) DEEA (x2) and BDADEEA Blended Solutions at (29815 31315 and 33315) K and1 atm (101325middot105 Pa)

density ρamiddot10minus3 (kgm3)

10x1 (molmol)

T K 032 01952 04244 06965 10253 14336

29815 099704 0992346 0988532 0985772 0982813 0978544

31315 099222 0986497 0981237 0976817 0972197 096679133315 098320 0976433 0969713 0963518 0957323 0950667

10x2 (molmol)

T K 032 02012 04547 07875 12520 19329

29815 099704 0993744 0990151 0983322 0971858 0961569

31315 099222 0987552 0981577 0972648 0959656 0948632

33315 098320 0976860 0968366 0957191 0942334 0930379

10x110x2(molmol)

T K 0362914516 0874917499 1670322270 0679910198 0561805618 0871209376

29815 0962903 0948513 0930513 0967362 0979531 0973321

31315 0950135 0935423 0917399 0954889 0968135 0961226

33315 0932259 0917224 0899304 0937515 0952165 0944402aThe standard uncertainty of ρ measurement is plusmn 001

Figure 5 Densities of aqueous DEEA solutions measured and calculated by this work and compared with literature data 2324

Table 4 Correlation Parameters AADs SSE and R 2 for Densities of BDA DEEA and BDADEEA Blended Solutions

k 1 k 2 k 3 k 4 k 5 k 6 AADa SSEb R 2c

BDA 05635 64004 08865 minus14958middot104 27387 minus065421 146middot10minus3 459middot10minus5 09829

DEEA 05260 minus29200 minus001838 minus15151middot104 30754 372233 156middot10minus3 676middot10minus5 09889

BDA+DEEA 09686 minus14211 49035 19634middot105minus34675 011514 177middot10minus3 658middot10minus5 09917

a AAD = (1 N )Σi = 1 N ((| ρcali minus ρexpi|) ρexpi) bSSE = Σi = 1

N ( ρcali minus ρexpi)2 c The squared correlation coefficients





parameters k 3 is especially used to describe the interaction between the BDA and DEEA in the mixed solution Thecalculated parameters k the average absolute deviations(AADs) the residual sum of squares (SSEs) and the squaredcorrelation coefficients (R 2) are listed in Table 4

As shown in Figures 4 and 5 the calculated densities from thecorrelation eq 8 are in good agreement with the experimentaldata of this work and the data in literature The R 2 of thecorrelation for BDA DEEA and BDADEEA blended solutionsare 09829 09889 and 09917 respectively

Table 5 Viscosities of Aqueous BDA (x1) DEEA (x2) and BDADEEA Blended Solutions from (29815 to 33315) K and 1 atm(101325middot105 Pa)

viscosity μa (mPamiddots)

10x1 (molmol)

T K 032 01952 04244 06965 10253 14336

29815 089 186 264 350 553 792

30315 080 123 183 251 365 48731315 065 098 139 185 257 329

32315 055 080 110 140 186 229

33315 048 063 090 106 137 162

10x 2 (molmol)

T K 032 02012 04547 07875 12520 19329

29815 089 216 362 557 800 1161

30315 080 140 234 361 575 805

31315 065 112 166 242 376 527

32315 055 094 132 172 260 369

33315 048 075 103 124 187 253

10x110x2(molmol)

T K 0362914516 0874917499 1670322270 0679910198 0561805618 0871209376

29815 1350 1648 1528 1197 912 1005

30315 842 986 910 797 526 676

31315 542 613 600 518 370 454

32315 367 399 393 353 264 321

33315 247 261 254 243 189 230aThe standard uncertainty of μ measurement is plusmn6

Figure 6 Viscosities of aqueous DEEA solutions measured and calculated by this work and compared with literature data 25

Table 6 Correlation Parameters AADs SSE and R

2

for Viscosities of BDA DEEA and BDADEEA Blended Solutionsk 1 k 2 k 3 k 4 k 5 k 6 AADa SSEb R 2c

BDA 1290 07115 20806middot107minus401171 1238middot106

minus17178 01091 18350 09748

DEEA 4486 24061 16338middot106minus432448 131middot106

minus11926 008617 14616 09919

BDA+DEEA minus9751 minus09854 33713middot107minus403222 140middot106

minus11926 009759 13424 09726a AAD = (1 N )Σi = 1

N ((| μcali minus μexpi|) μexpi) bSSE = Σi = 1 N ( μcali minus μexpi)

2 c The squared correlation coefficients





Viscosity The measurements of viscosities in this work alsocomprise the aqueous solutions of BDA DEEA and the BDADEEA blends The experimental data are presented in Table 5 andFigures 6 and 7

For the DEEA solutions the experimental data of this work arecompared with literature data25 in Figure 6 for the same conditions

The viscosities of the binary and ternary mixtures increase withincreasing mole fraction of BDA or DEEA and decreasingtemperature The experimental viscosity data for the binary andternary mixtures were also 1047297tted by Liursquos equation as a function of temperature andconcentrations of BDA andDEEA31 shown as eq 9The correlation method was the same as for the density data

μ middot

= ++

++

times + + +

+

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k x k x

T k

x k x )

T

k

T

k

T k x k x

(mPa s)

1 ( ) (

exp ( )

BDA DEEA

1BDA 2 DEEA

3BDA 2 DEEA

2

2

4 52 6 BDA 2 DEEA

2

(9)

where μ is the mixture viscosity T is the temperature x is the molefractionofBDA orDEEA and k 1 to k 6 are thecorrelationparametersk 2 is especially used to describe the interaction between BDA andDEEA The calculated parameters and the average absolutedeviations (AADs) the residual sum of squares (SSEs) and thesquared correlation coefficients (R 2) are listed in Table 6

As shown in Figures 6 and 7 the calculated viscosities from

correlation eq 9 agree well with the experimental data in thispaper and in the literature The R 2 of the correlation for BDADEEA and BDADEEA blended solutions are 09748 09919and 09726 respectively

Solubility of N2O The solubility of N2O de1047297ned by eq 7 H N2O in BDA DEEA and BDADEEA solutions were presentedin

Figures 8 and 9 and the N2O solubility (mass fraction w kgkg) were listed in Table 7

Figure 10 compares the CO2 solubility data of DEEA calculated by N2O solubilit y data using eq 1 in this work andthe data in the literatures26minus29 under the same conditions Also

Figure 7 Viscosities of aqueous BDA solutions measured and calculated by this work

Figure 8 N2O solubility H N2O in aqueous BDA and DEEA solutions at

(29815 31315 and 33315) K

Figure 9 N2O solubility H N2O in aqueous BDADEEA blended

solutions at (29815 31315 and 33315) K

Figure 10 CO2 physical solubility H CO2 in aqueous DEEA solutions at

(29815 31315 and 33315) K in this work and compared withliterature27minus29





the solubility data of 201 mol DEEA at (31315 and 33315) K were repeated in Figure 10 to further veri1047297es the good accuracy and repeatability of the experiment system

Figures 8 and 9 indicate that the N2O solubility of BDA is higherthan DEEA at all of the measured concentrations The N2Osolubility in BDA solution increases with the increasing BDA concentration while that in DEEA solution decreases with theincreasing DEEA concentration TheN2O solubility in BDADEEA mixture decreases with the increasing DEEA concentration in themixtures

CONCLUSION

Densities viscosities and solubilities of N2O in BDA DEEA andBDADEEA aqueous solutions were measured with the amineconcentration of (195minus143 mol ) BDA (201minus193 mol )DEEA and (363minus167 mol ) BDA + (262minus222 mol )DEEA The densities and N2O solubilities were measured at(29815 31315 and 33315) K whereas the viscosities wereobtained at (29815 30315 31315 32315 and 33315) K Themeasurement results agreed well with the literature data

The densities and viscosities of the binary and ternary mixtures were correlated by two semiempirical correlations in the literatureThe correlated results are in good agreement with the experimentaland literature data within the range of temperature and amine

concentration in this work The N2O solubility in BDA solutionincreases with the increasing BDA concentration whereas that inDEEA solution decreases with the increasing DEEA concentrationThe N2O solubility in BDADEEA mixture decreases with theincreasing DEEA concentration in the mixture

AUTHOR INFORMATION

Corresponding Author

E-mail wangshujtsinghuaeducn

Funding

Financial support from Chinese MOST project ldquoKey Technol-ogy Research and Development on Advanced Coal Conversionand Power Generationrdquo (2010DFA72730) is greatly appreciated

NotesThe authors declare no competing 1047297nancial interest

REFERENCES

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(2) Bishnoi S Rochelle G T Absorption of carbon dioxide inaqueous piperazine methyldiethanolamine AIChE J 2002 48 2788minus2799

(3) DerksP WJ Dijkstra HB S Hogendoorn J A Versteeg GFSolubility of carbon dioxide in aqueous piperazine solutions AIChE J

2005 51 2311minus2327(4) Rinker E B Ashour S S Sandall O C Absorption of carbon

dioxide into aqueous blends of diethanolamine and methyldiethanol-amine Ind Eng Chem Res 2000 39 4346minus4356

(5) Raynal L Alix P Bouillon P A Gomez A de Nailly M F Jacquin M Kittel J di Lella A Mougin P Trapy J The DMX process An original solution for lowering the cost of post-combustioncarbon capture Energy Procedia 2011 4 779minus786

(6) Zhang X Studies on multiphase CO2 capture system [D] University of Dortmund Dortmund 2007

(7) Zhang J Agar D W Zhang X Geuzebroek F CO2 absorptionin biphasic solvents with enhanced low temperature solventregeneration Energy Procedia 2011 4 67minus74

(8) Tan Y H Study of CO2-absorption into thermomorphic lipophilicamine solvents [D] University of Dortmund Dortmund 2010

(9) Rojey A Cadours R Carrette P L Boucot P Method of deacidizing a gas by means of an absorbent solution with fractionatedregeneration through heating United States Patent US 20090199709 A1 2009

(10) Hu L Phase transitional absorption method United StatesPatent 7541001 2009

(11) Bruder P Svendsen H F Solvent comparison for postcombustion CO2 capture Paper presented at 1st Post CombustionCapture Conference Abu DhabiKingdom of Saudi Arabia May17minus192011

(12) Xu Z C Wang S J Chen C H CO2 Absorption by BDADEEA Biphasic Solvents J Eng Thermophys 2012 accepted

(13) Xu Z C Wang S J Chen C H Experimental Study of CO 2

absorption by MAPA DEEA BDA and BDADEEA mixtures JCombust Sci Technol 2013 19 103minus118

Table 7 Solubility of N2O (Mass Fraction w kgkg) in Aqueous BDA (x1) DEEA (x2) and BDADEEA Blended Solutions at(29815 31315 and 33315) K

10x1 (molmol)

0 01952 04244 06965 10253 14336

T K P N2OkPa w P N2OkPa w P N2OkPa w P N2OkPa w P N2OkPa w P N2OkPa w

29815 15090 01677 12980 01468 13350 01358 14320 01143 14320 01030 15540 01039

31315 15030 01180 15298 01111 14550 01009 16602 01001 16602 01053 13881 0083133315 18170 00829 14643 00882 14650 00868 14500 00863 14500 00791 15800 00827

10x2 (molmol)

0 02012 04547 07875 12520 19329


29815 15090 01677 13310 01281 15810 01566 13170 01385 12880 01638 12540 01962

31315 15030 01180 15660 01130 15439 01196 14097 01273 13094 01513 12468 01797

33315 18170 00829 17019 01104 14215 01025 14163 01141 13949 01501 11477 01457

10x110x2(molmol)

0362914516 0874917499 1670322270 0679910198 0561805618 0871209376


29815 12630 01798 12210 02022 11590 02628 14040 01548 14120 01281 15240 01788

31315 10740 01343 11750 01748 10740 02077 15110 01572 15030 01255 14590 01530

33315 13500 01513 12780 01765 11970 01993 13240 01282 13520 01065 14200 01360aThe standard uncertainty of w measurement is plusmn 2





(14) Xu Z C Wang S J Chen C H CO2 absorption by biphasicsolvents mixtures of 14-Butanediamine and 2-(Diethylamino)-ethanol Int J Greenhouse Gas Control 2013 16 107minus115

(15)Derks P WHogendoornK JVersteeg G F Solubility of N2Oin and Density Viscosity and Surface Tension of Aqueous PiperazineSolutions J Chem Eng Data 2005 50 1947minus1950

(16) Versteeg G F Van Dijck L A J van Swaaij W P M On thekinetics between CO2 and alkanolamines both in aqueous and non-

aqueous solutions An overview Chem Eng Commun 1996 144 113minus158(17) Laddha SS Diaz J M Danckwerts PV The N2O analogy the

solubilities of CO2 andN2O in aqueous solutionsof organic compoundsChem Eng Sci 1981 36 229minus230

(18) Sada E Kumazawa H Butt M A Solubility and diffusivity of gases in aqueous solutions of amines J Chem Eng Data 1978 23 161minus163

(19) Singh P Niederer J P M Versteeg G F Structure and activity relationships for amine based CO2 absorbents-I Int J Greenhouse GasControl 2007 1 5minus10

(20) Singh P Versteeg G F Structure and activity relationships forCO2 regeneration from aqueous amine-based absorbents Process Safty Environ Protect 2008 86 347minus359

(21) Singh P Niederer J P M Versteeg G F Structure and activity

relationships for amine based CO2 absorbents-II Chem Eng Res Des2009 87 135minus144(22) Ahmed N C Negadi L Mokbel I Jose J Phase equilibrium

properties of binary aqueous solutions containing ehtanediamine 12-diaminopropane 13-diaminopropane or 14-diaminobutane at severaltemperatures J Chem Thermodyn 2011 43 719minus724

(23) Barbas M J A Dias F A Mendonca A F S S Lampreia I MS Volumetric properties of aqueous binary mixtures of 2-diethyamine-thanolfrom 29815 to 30315 K Phys Chem Chem Phys 2000 2 4858minus4863

(24) Lebrette L Maham Y Teng T T Hepler L G Mather A G Volumetric properties of aqueous solutions of mono and diethyletha-nolamines at temperatures from 5 to 80 degC Thermochim Acta 2002 386 119minus126

(25) Maham Y Lebrette L Mather A E Viscosities and ExcessProperties of Aqueous Solutions of Mono and Diethylethanolamines atTemperatures between 29815 and 35315 K J Chem Eng Data 2002 47 550minus553

(26) Little R J Van Swaaij P M Versteeg G F Kinetics of carbondioxide with tertiary amines in aqueous solution AIChE J 1990 36 1633minus1640

(27)Vaidya P DKenigE Y Accelerationof CO2 reaction with NN-Diethylethanolamine in aqueous solutions by Piperazine Ind EngChem Res 2008 47 34minus38

(28) Vaidya P D Kenig E Y A Study on CO2 absorption Kinetics by aqueous Solutions of NN-Diethylethanolamine and N-Ethylethanol-amine Chem Eng Technol 2009 32 556minus563

(29) Li W Dong L Chen J Absorption kinetics of CO2 in aqueoussolutions of secondary and tertiary alkanolamines Chin J Process Eng2011 11 422minus428

(30) Versteeg G F van Swaiij W P M Solubility and Diffusivity of

Acid Gases (Carbon Dioxide and Nitrous Oxide) in Aqueous Alkanolamine Solutions J Chem Eng Data 1988 33 29minus34

(31) Liu J Z Wang S J Hartono A Svendsen H F Chen C HSolubility of N2O in and Density and Viscosity of Aqueous Solutions of Piperazine Ammonia and Their Mixtures from (28315 to 32315) K JChem Eng Data 2012 57 2387minus2393

(32) Watson J T R Basu R S Sengers J V An ImprovedRepresentative Equation for the Dynamic Viscosity of Water Substance J Phys Chem Ref Data 1980 9 1255minus1290

(33) Sun W C Yong C B Li M H Kinetics of the absorption of carbon dioxide into mixed aqueous solutions of 2-amino-2-methyl-l-propanol and piperazine Chem Eng Sci 2005 60 503minus516

(34)SamantaA Roy SBandyopadhyay S S Physical Solubility andDiffusivity of N2O and CO2 in Aqueous Solutions of Piperazine and (N-

Methyldiethanolamine + Piperazine) J Chem Eng Data 2007 52 1381minus1385

(35) Li M H Lai M D Solubility and Diffusivity of N2O and CO2 in(Monoethanolamine + N-Methyldiethanolamine + Water) and in(Monoethanolamine +2-Amino-2-methyl-1-propanol + Water) JChem Eng Data 1995 40 486minus492

(36)TsaiTCKoJJWangHMLinCYLiMHSolubilityof Nitrous Oxide in Alkanolamine Aqueous Solutions J Chem Eng Data

2000 45 341minus

347(37) Ying J Dag A E Yi W Measurements and Correlation of Physical Solubility of Carbon Dioxide in (Monoethanolamine + Water) by a Modified Technique Ind Eng Chem Res 2012 51 6958minus6966





32315 and 33315) K The results were compared with availabledata in the literatures The experimental data on density and

viscosity werecorrelated using twosemi empirical correlations in theliterature as functions of temperature and concentrations of BDA and DEEA

EXPERIMENTAL SECTION

BDA (ge

98 wt pure) and DEEA (ge

99 wt pure) were from Aladdin Reagent Company The BDA and DEEA structures areshown below

Distilled water was used for preparing experimental solutionsThe BDA and DEEA concentrations were determined by titration against 2 N H2SO4 using a Metrohm 809 Titrando autotitrator The N2O gas (99 vol pure) was supplied by BeijingHuayuan Gas Company

Density and Viscosity In this work thedensities of aqueoussolutions were measured by National Institute of Metrology (NIM) of China strictly following theJJG 1058-2010 veri1047297cationregulation of laboratory oscillation-type liquid density metersissued by General Administration of Quality SupervisionInspection and Quarantine of China (AQSIQ) using aDMA5000 density meter NIM is Chinarsquos highest researchcenter of metrology and the national technical center of legalmetrology The result of every point was the average value of six repeated trials

The viscosities of aqueous solutions were measured by a AampDSV-10 viscometer with a measurement range of 03minus1000mPamiddots The total accuracy of viscosity given by the manufactureris plusmn 1 Calibration of viscometer was done by measuring the

viscosity of Standard Liquid GBW13601 (1203) and GBW13603

(1203) produced by NIM and approved by AQSIQ The data forthe calibration are given in Table 1

It can be seen that viscosities from the measurements agree very well with the reference values for the standard liquid

Solubility of N2O TheN2O solubility apparatus consists of a

jacketed stirred glass reactor and a stainless steel gas holding vessel as shown in Figure 1 Before experiment the volume of thegas holding vesselwas measured by 1047297lling it upwithwater andcalculating the water volume Then the total volume of thereactor and the auxiliary pipe linking the reactor and valves no3minus6 were measured by adding into it a known amount of N2Ofrom the holding vessel The added N2O amount was calculated

by the amount diff erence in the gas holding vessel before andafter adding N2O into reactor The results show that the volumeof vessel V V was 2186middot10minus3 m3 while that of the reactor and theauxiliary V R was 5628middot10minus4 m3

The reactor was1047297rst vacuumed until the pressure was less than1 kPa and then the solution wassucked into it through valve no 3

The amount of solvent added (around half of reactor) into thereactor was calculated by measuring the weight of solvent before

and after the transference After the solution reached vaporliquid equilibrium at set temperature the pressure inside of thereactor P 1N2O was recorded The temperature of the reactor was

controlled by the circulating oil bath with an uncertainty of plusmn 01 K Then N2O gas was added to the reactor by shortly opening valve No 5 linking the reactor andthe vessel Consideringthat the open period for the reactor after the solution added was

very short and the good airtightness of the reactor the vaporedamount of the solvent should be very small and can be neglectedEquilibrium was then established after 6minus15 h (depending ontemperature) with an agitation speed of 450 rmin The reactorand vessel pressure were recorded by two pressure transducers(Druck PTX 7515 with uncertainty 02 of full scale (200 kPa))Two K-type thermocouples recorded temperatures in the reactor

and in the vessel respectively with an uncertainty of plusmn 01 KThe amount added ofN2O nN2O

added mol was calculated from the

pressure diff erence of the gas supply vessel before and afterfeeding N2O as

= ‐

⎛

⎝⎜⎜

⎞

⎠⎟⎟n

V

R

P

T z

P

T z

V

V

V

V N Oadded V

1 22

1

1

2

2 (2)

where P V1 and P V2 are the pressure of the vessel before and afterfeeding Pa T V1 and T V2 are the temperature of the vessel beforeand after feeding K z1 z2 represent the compressibility factor of gas before and after the feeding R is universal gas constant83145 Jmiddot(molmiddotK)minus1 The compressibility factor was calculatedusing the PengminusRobinson equation of state

The amount of N2O in the gas phase of the reactor nN2Og can becalculated by

=

minus

n

P V V

z RT

( )N Og N O R S

N O R 2

2

2 (3)

where T R is the reactor temperature after reaching equilibriumK and z is the compressibility factor of N2O after reachingequilibrium V S is the volume of added solvent which is thequotient of added solution amount and density m3 P N2O is the

N2O partial pressure and calculated by eq 4 Pa

= minus P P PN O 1N O 2N O2 2 2 (4)

Table 1 Viscosities of Standard Solutions for Calibration29315 K 1 atm (101325middot105 Pa)

viscosity μ (mPamiddots)

standard measurement ref deviation

GBW13601(1203) 184 18388 minus007

GBW13603(1203) 880 8793 003

Figure 1 Experimental setup of N2O solubility








= minusn n nN Ol

N Oadded

N Og

2 2 2 (5)


calculated by

=C

n

V

N ON Ol

S2

2

(6)


= P H CN O N O N Ol

2 2 2 (7)











T (K) 29315 29815 30315 31315 32315 33315

water P N2O (kPa) 1110 1509 1236 1503 1427 1817

w () 01338 01677 01219 01180 00952 00829

MEA P N2O (kPa) 1417 1555 1420

w () 01402 01195 00736a














ρ middot middot

= + + +

times + +

+

minus minus

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k k

T x k x

k

T

k

T k x k x

( 10 (kg m )

( )

exp ( )

BDA DEEA 3 3

12

BDA 3 DEEA 42

56 BDA 3 DEEA

(8)




10x1 (molmol)

T K 032 01952 04244 06965 10253 14336

29815 099704 0992346 0988532 0985772 0982813 0978544

31315 099222 0986497 0981237 0976817 0972197 096679133315 098320 0976433 0969713 0963518 0957323 0950667

10x2 (molmol)

T K 032 02012 04547 07875 12520 19329

29815 099704 0993744 0990151 0983322 0971858 0961569

31315 099222 0987552 0981577 0972648 0959656 0948632

33315 098320 0976860 0968366 0957191 0942334 0930379

10x110x2(molmol)

T K 0362914516 0874917499 1670322270 0679910198 0561805618 0871209376

29815 0962903 0948513 0930513 0967362 0979531 0973321

31315 0950135 0935423 0917399 0954889 0968135 0961226


















10x1 (molmol)

T K 032 01952 04244 06965 10253 14336

29815 089 186 264 350 553 792

30315 080 123 183 251 365 48731315 065 098 139 185 257 329

32315 055 080 110 140 186 229

33315 048 063 090 106 137 162

10x 2 (molmol)

T K 032 02012 04547 07875 12520 19329

29815 089 216 362 557 800 1161

30315 080 140 234 361 575 805

31315 065 112 166 242 376 527

32315 055 094 132 172 260 369

33315 048 075 103 124 187 253

10x110x2(molmol)

T K 0362914516 0874917499 1670322270 0679910198 0561805618 0871209376

29815 1350 1648 1528 1197 912 1005

30315 842 986 910 797 526 676

31315 542 613 600 518 370 454

32315 367 399 393 353 264 321




2



minus17178 01091 18350 09748


minus11926 008617 14616 09919


minus11926 009759 13424 09726a AAD = (1 N )Σi = 1










μ middot

= ++

++

times + + +

+

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k x k x

T k

x k x )

T

k

T

k

T k x k x

(mPa s)

1 ( ) (

exp ( )

BDA DEEA

1BDA 2 DEEA

3BDA 2 DEEA

2

2

4 52 6 BDA 2 DEEA

2

(9)









(29815 31315 and 33315) K











CONCLUSION




AUTHOR INFORMATION



Funding



REFERENCES

















10x1 (molmol)

0 01952 04244 06965 10253 14336


29815 15090 01677 12980 01468 13350 01358 14320 01143 14320 01030 15540 01039

31315 15030 01180 15298 01111 14550 01009 16602 01001 16602 01053 13881 0083133315 18170 00829 14643 00882 14650 00868 14500 00863 14500 00791 15800 00827

10x2 (molmol)

0 02012 04547 07875 12520 19329


29815 15090 01677 13310 01281 15810 01566 13170 01385 12880 01638 12540 01962

31315 15030 01180 15660 01130 15439 01196 14097 01273 13094 01513 12468 01797

33315 18170 00829 17019 01104 14215 01025 14163 01141 13949 01501 11477 01457

10x110x2(molmol)

0362914516 0874917499 1670322270 0679910198 0561805618 0871209376


29815 12630 01798 12210 02022 11590 02628 14040 01548 14120 01281 15240 01788

31315 10740 01343 11750 01748 10740 02077 15110 01572 15030 01255 14590 01530

































2000 45 341minus









= minusn n nN Ol

N Oadded

N Og

2 2 2 (5)


calculated by

=C

n

V

N ON Ol

S2

2

(6)


= P H CN O N O N Ol

2 2 2 (7)











T (K) 29315 29815 30315 31315 32315 33315

water P N2O (kPa) 1110 1509 1236 1503 1427 1817

w () 01338 01677 01219 01180 00952 00829

MEA P N2O (kPa) 1417 1555 1420

w () 01402 01195 00736a














ρ middot middot

= + + +

times + +

+

minus minus

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k k

T x k x

k

T

k

T k x k x

( 10 (kg m )

( )

exp ( )

BDA DEEA 3 3

12

BDA 3 DEEA 42

56 BDA 3 DEEA

(8)




10x1 (molmol)

T K 032 01952 04244 06965 10253 14336

29815 099704 0992346 0988532 0985772 0982813 0978544

31315 099222 0986497 0981237 0976817 0972197 096679133315 098320 0976433 0969713 0963518 0957323 0950667

10x2 (molmol)

T K 032 02012 04547 07875 12520 19329

29815 099704 0993744 0990151 0983322 0971858 0961569

31315 099222 0987552 0981577 0972648 0959656 0948632

33315 098320 0976860 0968366 0957191 0942334 0930379

10x110x2(molmol)

T K 0362914516 0874917499 1670322270 0679910198 0561805618 0871209376

29815 0962903 0948513 0930513 0967362 0979531 0973321

31315 0950135 0935423 0917399 0954889 0968135 0961226


















10x1 (molmol)

T K 032 01952 04244 06965 10253 14336

29815 089 186 264 350 553 792

30315 080 123 183 251 365 48731315 065 098 139 185 257 329

32315 055 080 110 140 186 229

33315 048 063 090 106 137 162

10x 2 (molmol)

T K 032 02012 04547 07875 12520 19329

29815 089 216 362 557 800 1161

30315 080 140 234 361 575 805

31315 065 112 166 242 376 527

32315 055 094 132 172 260 369

33315 048 075 103 124 187 253

10x110x2(molmol)

T K 0362914516 0874917499 1670322270 0679910198 0561805618 0871209376

29815 1350 1648 1528 1197 912 1005

30315 842 986 910 797 526 676

31315 542 613 600 518 370 454

32315 367 399 393 353 264 321




2



minus17178 01091 18350 09748


minus11926 008617 14616 09919


minus11926 009759 13424 09726a AAD = (1 N )Σi = 1










μ middot

= ++

++

times + + +

+

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k x k x

T k

x k x )

T

k

T

k

T k x k x

(mPa s)

1 ( ) (

exp ( )

BDA DEEA

1BDA 2 DEEA

3BDA 2 DEEA

2

2

4 52 6 BDA 2 DEEA

2

(9)









(29815 31315 and 33315) K











CONCLUSION




AUTHOR INFORMATION



Funding



REFERENCES

















10x1 (molmol)

0 01952 04244 06965 10253 14336


29815 15090 01677 12980 01468 13350 01358 14320 01143 14320 01030 15540 01039

31315 15030 01180 15298 01111 14550 01009 16602 01001 16602 01053 13881 0083133315 18170 00829 14643 00882 14650 00868 14500 00863 14500 00791 15800 00827

10x2 (molmol)

0 02012 04547 07875 12520 19329


29815 15090 01677 13310 01281 15810 01566 13170 01385 12880 01638 12540 01962

31315 15030 01180 15660 01130 15439 01196 14097 01273 13094 01513 12468 01797

33315 18170 00829 17019 01104 14215 01025 14163 01141 13949 01501 11477 01457

10x110x2(molmol)

0362914516 0874917499 1670322270 0679910198 0561805618 0871209376


29815 12630 01798 12210 02022 11590 02628 14040 01548 14120 01281 15240 01788

31315 10740 01343 11750 01748 10740 02077 15110 01572 15030 01255 14590 01530

































2000 45 341minus









ρ middot middot

= + + +

times + +

+

minus minus

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k k

T x k x

k

T

k

T k x k x

( 10 (kg m )

( )

exp ( )

BDA DEEA 3 3

12

BDA 3 DEEA 42

56 BDA 3 DEEA

(8)




10x1 (molmol)

T K 032 01952 04244 06965 10253 14336

29815 099704 0992346 0988532 0985772 0982813 0978544

31315 099222 0986497 0981237 0976817 0972197 096679133315 098320 0976433 0969713 0963518 0957323 0950667

10x2 (molmol)

T K 032 02012 04547 07875 12520 19329

29815 099704 0993744 0990151 0983322 0971858 0961569

31315 099222 0987552 0981577 0972648 0959656 0948632

33315 098320 0976860 0968366 0957191 0942334 0930379

10x110x2(molmol)

T K 0362914516 0874917499 1670322270 0679910198 0561805618 0871209376

29815 0962903 0948513 0930513 0967362 0979531 0973321

31315 0950135 0935423 0917399 0954889 0968135 0961226


















10x1 (molmol)

T K 032 01952 04244 06965 10253 14336

29815 089 186 264 350 553 792

30315 080 123 183 251 365 48731315 065 098 139 185 257 329

32315 055 080 110 140 186 229

33315 048 063 090 106 137 162

10x 2 (molmol)

T K 032 02012 04547 07875 12520 19329

29815 089 216 362 557 800 1161

30315 080 140 234 361 575 805

31315 065 112 166 242 376 527

32315 055 094 132 172 260 369

33315 048 075 103 124 187 253

10x110x2(molmol)

T K 0362914516 0874917499 1670322270 0679910198 0561805618 0871209376

29815 1350 1648 1528 1197 912 1005

30315 842 986 910 797 526 676

31315 542 613 600 518 370 454

32315 367 399 393 353 264 321




2



minus17178 01091 18350 09748


minus11926 008617 14616 09919


minus11926 009759 13424 09726a AAD = (1 N )Σi = 1










μ middot

= ++

++

times + + +

+

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k x k x

T k

x k x )

T

k

T

k

T k x k x

(mPa s)

1 ( ) (

exp ( )

BDA DEEA

1BDA 2 DEEA

3BDA 2 DEEA

2

2

4 52 6 BDA 2 DEEA

2

(9)









(29815 31315 and 33315) K











CONCLUSION




AUTHOR INFORMATION



Funding



REFERENCES

















10x1 (molmol)

0 01952 04244 06965 10253 14336


29815 15090 01677 12980 01468 13350 01358 14320 01143 14320 01030 15540 01039

31315 15030 01180 15298 01111 14550 01009 16602 01001 16602 01053 13881 0083133315 18170 00829 14643 00882 14650 00868 14500 00863 14500 00791 15800 00827

10x2 (molmol)

0 02012 04547 07875 12520 19329


29815 15090 01677 13310 01281 15810 01566 13170 01385 12880 01638 12540 01962

31315 15030 01180 15660 01130 15439 01196 14097 01273 13094 01513 12468 01797

33315 18170 00829 17019 01104 14215 01025 14163 01141 13949 01501 11477 01457

10x110x2(molmol)

0362914516 0874917499 1670322270 0679910198 0561805618 0871209376


29815 12630 01798 12210 02022 11590 02628 14040 01548 14120 01281 15240 01788

31315 10740 01343 11750 01748 10740 02077 15110 01572 15030 01255 14590 01530

































2000 45 341minus










10x1 (molmol)

T K 032 01952 04244 06965 10253 14336

29815 089 186 264 350 553 792

30315 080 123 183 251 365 48731315 065 098 139 185 257 329

32315 055 080 110 140 186 229

33315 048 063 090 106 137 162

10x 2 (molmol)

T K 032 02012 04547 07875 12520 19329

29815 089 216 362 557 800 1161

30315 080 140 234 361 575 805

31315 065 112 166 242 376 527

32315 055 094 132 172 260 369

33315 048 075 103 124 187 253

10x110x2(molmol)

T K 0362914516 0874917499 1670322270 0679910198 0561805618 0871209376

29815 1350 1648 1528 1197 912 1005

30315 842 986 910 797 526 676

31315 542 613 600 518 370 454

32315 367 399 393 353 264 321




2



minus17178 01091 18350 09748


minus11926 008617 14616 09919


minus11926 009759 13424 09726a AAD = (1 N )Σi = 1










μ middot

= ++

++

times + + +

+

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k x k x

T k

x k x )

T

k

T

k

T k x k x

(mPa s)

1 ( ) (

exp ( )

BDA DEEA

1BDA 2 DEEA

3BDA 2 DEEA

2

2

4 52 6 BDA 2 DEEA

2

(9)









(29815 31315 and 33315) K











CONCLUSION




AUTHOR INFORMATION



Funding



REFERENCES

















10x1 (molmol)

0 01952 04244 06965 10253 14336


29815 15090 01677 12980 01468 13350 01358 14320 01143 14320 01030 15540 01039

31315 15030 01180 15298 01111 14550 01009 16602 01001 16602 01053 13881 0083133315 18170 00829 14643 00882 14650 00868 14500 00863 14500 00791 15800 00827

10x2 (molmol)

0 02012 04547 07875 12520 19329


29815 15090 01677 13310 01281 15810 01566 13170 01385 12880 01638 12540 01962

31315 15030 01180 15660 01130 15439 01196 14097 01273 13094 01513 12468 01797

33315 18170 00829 17019 01104 14215 01025 14163 01141 13949 01501 11477 01457

10x110x2(molmol)

0362914516 0874917499 1670322270 0679910198 0561805618 0871209376


29815 12630 01798 12210 02022 11590 02628 14040 01548 14120 01281 15240 01788

31315 10740 01343 11750 01748 10740 02077 15110 01572 15030 01255 14590 01530

































2000 45 341minus









μ middot

= ++

++

times + + +

+

⎛

⎝⎜

⎞

⎠⎟

⎛

⎝⎜

⎞

⎠⎟

k x k x

T k

x k x )

T

k

T

k

T k x k x

(mPa s)

1 ( ) (

exp ( )

BDA DEEA

1BDA 2 DEEA

3BDA 2 DEEA

2

2

4 52 6 BDA 2 DEEA

2

(9)









(29815 31315 and 33315) K











CONCLUSION




AUTHOR INFORMATION



Funding



REFERENCES

















10x1 (molmol)

0 01952 04244 06965 10253 14336


29815 15090 01677 12980 01468 13350 01358 14320 01143 14320 01030 15540 01039

31315 15030 01180 15298 01111 14550 01009 16602 01001 16602 01053 13881 0083133315 18170 00829 14643 00882 14650 00868 14500 00863 14500 00791 15800 00827

10x2 (molmol)

0 02012 04547 07875 12520 19329


29815 15090 01677 13310 01281 15810 01566 13170 01385 12880 01638 12540 01962

31315 15030 01180 15660 01130 15439 01196 14097 01273 13094 01513 12468 01797

33315 18170 00829 17019 01104 14215 01025 14163 01141 13949 01501 11477 01457

10x110x2(molmol)

0362914516 0874917499 1670322270 0679910198 0561805618 0871209376


29815 12630 01798 12210 02022 11590 02628 14040 01548 14120 01281 15240 01788

31315 10740 01343 11750 01748 10740 02077 15110 01572 15030 01255 14590 01530

































2000 45 341minus








CONCLUSION




AUTHOR INFORMATION



Funding



REFERENCES

















10x1 (molmol)

0 01952 04244 06965 10253 14336


29815 15090 01677 12980 01468 13350 01358 14320 01143 14320 01030 15540 01039

31315 15030 01180 15298 01111 14550 01009 16602 01001 16602 01053 13881 0083133315 18170 00829 14643 00882 14650 00868 14500 00863 14500 00791 15800 00827

10x2 (molmol)

0 02012 04547 07875 12520 19329


29815 15090 01677 13310 01281 15810 01566 13170 01385 12880 01638 12540 01962

31315 15030 01180 15660 01130 15439 01196 14097 01273 13094 01513 12468 01797

33315 18170 00829 17019 01104 14215 01025 14163 01141 13949 01501 11477 01457

10x110x2(molmol)

0362914516 0874917499 1670322270 0679910198 0561805618 0871209376


29815 12630 01798 12210 02022 11590 02628 14040 01548 14120 01281 15240 01788

31315 10740 01343 11750 01748 10740 02077 15110 01572 15030 01255 14590 01530

































2000 45 341minus

































2000 45 341minus




solubility of n2o in and density and viscosity of aqueous solutions of butan4

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