Incineration of Contaminated Soils in an Electrodynamic Balance

Chapter 3

Incineration of Contaminated Soils in an Electrodynamic Balance 1

1

1,3

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M . Flytzani-Stephanopoulos , A. F. Sarofim , L. Tognotti , H. Kopsinis , and M . Stoukides 2

2

1

Department of Chemical Engineering, Massachusetts Institute of Technology, Cambridge, MA 02139 Department of Chemical Engineering, Tufts University, Medford, MA 02155 2

Understanding contaminant evolution from landfill soils is important in several in-situ remediation processes as well as in thermal treatment and incineration of contaminated top soils. To delineate the rate-limiting processes in the absence of interparticle effects, single surrogate soil particles are examined in this work. The adsorption-desorption characteristics of toluene and carbon tetrachloride on single, surrogate soil particles have been studied using an electrodynamic balance (EDB) under ambient conditions (P=latm; T=298K). The EDB offers high mass sensitivity (∆m~10 g) in the absence of external mass transfer limitations and interparticle effects. In this work, three types of solid particles, 100-170μm in diameter, were examined, namely montmorillonite, a clay, and two synthetic chars, Spherocarb and Carbopack, of very different pore structures. Three different values of relative pressures, P/P were tested for each liquid by changing the saturator bath temperatures. Significant differences were identified among the various solid– organic compound pairs examined in adsorption-desorption sequences in the EDB. These are strongly correlated with differences in the solid pore structures. -9

o,

At the present time, alternatives to conventional hazardous waste treatment methods are actively being sought in response to stringent landfill regulations and associated high landfill costs. Incineration is a proven solution for treating

3

Current address: Department of Chemical Engineering, University of Pisa, Pisa, Italy

0097-6156/91/0468-0029$06.25/0 © 1991 American Chemical Society Tedder and Pohland; Emerging Technologies in Hazardous Waste Management II ACS Symposium Series; American Chemical Society: Washington, DC, 1991.

30

EMERGING TECHNOLOGIES IN HAZARDOUS WASTE MANAGEMENT II

top soils containing organic contaminants and well-designed incineration systems provide the highest overall degree of destruction of hazardous waste streams (1). Among other soil treatment methods, currently under development, are the in-situ decontamination by vacuum extraction and air stripping, and thermal desorption of contaminants by heating the soil to temperatures well below those typical in incinerators. The latter solution is more easily accepted by the public than incineration. Overall, significant growth in the use of incineration and other thermal soil treatment methods is anticipated in the near future (1, 2). A typical incinerator system consists of a primary combustor, where contaminants are primarily volatilized and partially burned, and the secondary combustion chamber where the thermal destruction is completed (3). More than 20% of the total hazardous wastes generated in the U.S. can be considered incinerable (1, 4). According to the experience gained to date, rotary kiln incinerators seem to show superior applicability and versatility compared to the other existing types (1, 2). A rotary kiln incinerator consists of a cylindrical refractory-lined shell mounted on a slight incline. The shell rotates to provide for transfer of waste and to enhance mixing. Wastes undergo partial volatilization followed by destructive distillation and partial combustion. Following the primary combustor, an afterburner is used where the gas phase oxidation reactions are completed. Transient phenomena involving rapid release of waste vapor into the kiln environment may occur during the batch-mode operation of a rotary kiln and may cause failure of the incinerator system. Such phenomena, called "puffs", are frequently encountered and have been studied by a number of investigators (5-7). In the rotary kiln the solids can be considered as a bed of many layers of particles that are being slowly stirred (3). In kilns operated at lower temperatures, the soil is picked up and dropped by baffles known as flights in order to augment the contacting between the soils and the gas stream. Contaminants may exist either adsorbed onto the internal pore structure of the particles or adsorbed on the external surface of the particles or as a liquid phase within the bed (3). Hence, both intraparticle and interparticle effects contribute to the high complexity of the rotary kiln system (3, 6). Numerous particles with variable properties are involved and the isolation of individual effects is not always easy. It is clear that a fundamental study of the evolution of contaminants from soil particles can contribute significantly to understanding the transport of hazardous chemicals in soils and the processes limiting the operation of rotary kilns. In particular, it would be very helpful if the characteristics of a single particle reactor were first examined because in this configuration interparticle effects are eliminated. To this end, an electrodynamic balance (EDB) appears to be a very useful tool. The EDB consists of electrodes that can suspend a single charged particle in space, here modified to permit particle heating by a

Tedder and Pohland; Emerging Technologies in Hazardous Waste Management II ACS Symposium Series; American Chemical Society: Washington, DC, 1991.

3.

FLYTZANI-STEPHANOPOULOS ET AL.

Incineration ofContaminated Soils

C 0 laser, temperature measurement by a two- or three-color infraredpyrometer and continuous particle weighing by a position-control system (8, 9). 2

The above apparatus has been used successfully in a number of applications including measurement of temperature and weight of charcoal particles undergoing oxidation (10, 11), measurement of adsorptivities and heat capacities of single particles (12) and measurement of buoyancy forces at low Grashof numbers. Recently, the same device has been used as a basic tool in developing a novel droplet imaging system that offers unique capabilities for characterizing size, mass, density and composition of individual droplets (17). The EDB has also been used to obtain water activities in single electrolyte solutions (18). In the present communication we report data on adsorption and desorption characteristics of two organic compounds; namely, toluene and carbon tetrachloride on single particles of surrogate soils in the EDB.

Experimental A schematic diagram of the E D B system is shown in Figure 1. The electrodynamic balance is a chamber that can hold a single charged particle suspended in space by means of electric fields (19, 20). The balance consists of two endcap electrodes and a ring electrode. A D C potential is applied across the endcap electrodes and a A C voltage is applied to the ring electrode. The EDB can measure the diameter, mass, density, excess charge and surface area of a single levitated particle (21). A 5mW He-Ne laser illuminates the particle for position sensing and a 5-20W C 0 laser is used for particle heating. An optical microscope is used for viewing the particle and for manual particle position control (Figure 1). Additional details on the experimental apparatus and procedure can be found elsewhere (8-10, 21). 2

The EDB was used to measure the relative weight change of a suspended particle during adsorption and desorption of organic vapors at room temperature. A single, dry particle was suspended in the chamber, through which a finite dry nitrogen flowrate was maintained. The particle was degassed before the adsorption runs by heating it with the C 0 laser. The voltage was then adjusted in order to balance the particle at its correct position. Under no flow conditions, the voltage required to levitate the particle is recorded as V . Prior to an adsorption experiment, the particle is balanced in dry nitrogen flow at a selected flowrate. The required voltage is recorded as V , i.e. the initial voltage (t=0) at zero adsorption. For the adsorption experiments, a dry nitrogen stream saturated with the organic vapor (toluene or carbon tetrachloride) was introduced into the E D B chamber. Saturation of the nitrogen stream took place by passing it through a bubbler holding the organic liquid at a constant temperature. 2

nf

Q


31

32


Figure 1. (a) Expanded view of the electrodynamic balance, (b) Crosssectional view of the electrodes in the electrodynamic balance.


3.

Incineration ofContaminated Sods 33

FLYTZANI-STEPHANOPOULOS E T AL.

00 Analog Sarvo Systam

Log A / B

PMT

computer

(d)

s ι

analoq

>

t

processing

4

5

MICRON

MICRON

-

ι I I ι 1 1 « 1

analoq processing

1 j

\\ 2 MICRON

particle

chop per

Figure 1 (continued), (c) Position control system for the electrodynamic balance, (d) Temperature measurement system.


34


The balancing voltage V gradually increases during adsorption to reach a final constant value recorded as V . Using the above definitions one can calculate (2) particle weight changes: a

Û

ο _

α Ο _ χ

where n^, is the mass of the dry solid particle, n^ is the sum of n ^ plus the mass of organic adsorbed, and \ is the maximum amount (in grams) of contaminant adsorbed per gram of solid particle. In order to determine potentially different solid-hydrocarbon affinities and the effect of pore structure, three types of solids have been examined in this work with two types of organic adsorbates, namely toluene and carbon tetrachloride. A porous clay, montmorillonite, and two synthetic char particles, namely "Spherocarb" and "Carbopack" were used. The physical properties of these materials are given below (9): Material

(S) (C) (M)

Diameter (um)

Surface Area (m /g)

Bulk Density

Porosity

125-150 150-180 90-125

860 (1050*) 10.4 192

.63 .95 .65

.525 .615 .802

2

S: Spherocarb; C: Carbopack; M : Montmorillonite. * determined by high-pressure C 0 adsorption-desorption measurements in the EDB (22) 2

Three different saturator temperatures were used, - 25, 0 and -21° C - and thus the ratio P/P of the partial pressure of the organic vapor over its vapor pressure P at 25°C (which was always the temperature in the electrodynamic balance chamber) was varied. For toluene the P/P values were 1.0, 0.23 and 0.05 for saturator temperatures 25, 0 and -21°C, respectively, while for carbon tetrachloride the corresponding P/P values at the same saturator temperatures were 1.0, 0.29 and 0.08, respectively. G

c

G

G

A series of adsorption and desorption experiments with different nitrogen flowrates were run to establish the importance of external mass transfer. Using flowrates in the range of 14-28 seem no significant differences in the rates of adsorption-desorption were measured (8, 9). Thus, the recorded weight changes in the EDB were free of gas-film diffusion limitations.


3. FLYTZANI-STEPHANOPOULOS ET AI^

Incineration of Contaminated Soils

Results Figure 2 shows results for toluene adsorption on a Spherocarb particle of ΠΟμπι diameter for P/P = 1 and for a total volumetric flowrate maintained at 21.4 seem. Figure 3 depicts the desorption profile of toluene at room temperature in dry nitrogen. An initial slow decrease in V / V is observed which probably corresponds to the slowly diminishing vapor pressure of toluene in the chamber during the initial displacement of the saturated gas from the chamber. This is followed first by a fast and then a slow decrease in V / V . G

0

Q

In order to compare the rates of adsorption and desorption in various experiments the data were normalized using as a variable the fractional attainment Y of the maximum adsorption, where Y = (V - V ) / ( V - V G

a

o )

Figure 4a compares the X values for Spherocarb, montmorillonite and Carbopack particles during adsorption of toluene at P/P = 1. Figure 4b shows a similar comparison during desorption of toluene from each type solid. In this case normalized data are shown. Each experimental point in these figures corresponds to an average value from at least three particles examined. Figures 5a and 5b show the data from carbon tetrachloride adsorption and desorption on the three types of particles again for P/P = 1. Each curve shown in Figures 4 and 5 can provide information about the characteristic time of either the adsorption or the desorption of the organic compound from the particle. The times required for the particles to adsorb 50% and 90% of the maximum amount that can be adsorbed under these conditions were defined as r and r , respectively. Similarly, the times required to desorb 50% and 90% of the adsorbed compound were defined as τ and r respectively. Table I contains X values for several experiments as well as average values of the above denoted characteristic times. a

G

G

0 3 a

09a

05ά

0 9 d

a

Experiments were also conducted with the saturator temperature kept at 0°C while the temperature in the electrodynamic balance chamber (and therefore the solid particle temperature as well) was kept at 25°C. In this case, the relative pressure for toluene was P / P = 0.23, while for CC1 the relative pressure was higher, P/P = 0.29. Results for adsorption and desorption of either compound on montmorillonite and Spherocarb particles are shown in Table II. Results with Carbopack are not shown because the adsorbed amount was very low. Table III contains similar results for montmorillonite and Spherocarb particles with the saturator temperature kept at -21°C. At this temperature the ratio P/P for CyHg was 0.05 and for CC1 it was 0.08. Typical experimental results for all three saturator temperatures employed are shown in Figures 6a and 6b and Figures 7a and 7b, respectively, for the CjHg. Spherocarb and CyHg-montmorillonite pairs. Similar results are shown in Figures 8a and 8b and 9a and 9b, respectively, for the adsorption and desorption of CC1 on Spherocarb and montmorillonite. 0

4

Q

Q

4

4


35


1.05 1.04

Τ = 298 Κ P/Po = 1.0 d = 170 μηι flow rate = 21.4 seem

1.031.02-

ι

ο

1.01 1.00

—τ

«

1

1

20

1

40

•

1

1

60

1

1

80

—

100

120

t (mini

Figure 2. Adsorption of Q H g on Spherocarb particle. 1.05 bo 1.04 1.031.02-

Τ = 298 Κ d = 170 μηι dry Ν2 flow rate = 21.4 seem

1.01 1.00

—ι

0

1

20

1

1

40

1

1

1

1

60 80 t (min)

1

1

100

«

1

«

120

1—

140

Figure 3. Desorption of Q H g from Spherocarb particle.


3.

Incineration of Contaminated SoUs 37

FLYTZANI-STEPHANOPOULOS ET AL.

0.10·

ο ο ο ο • •

0.08 H 0.06 -I

>

0

>

O

4

i

· m 0.02 Η ^ • "Η

Ρι 0.00-Ρ

Β

Β

•

Β

Montmorillonite Spherocarb Carbopack

Θ

Η

Π

_ •

1

ο

ο

1

1 80

•

"

1 40

1

1 120 t (min).

τ-

ι

160

200

Figure 4a. Average adsorption curves of QHg for different materials; Τ = 298 K, P/P = 1.0. 0

1.0dry Ν2 flow rate = 21.4 seem Τ = 298 Κ

ο _ o > râ

0.8-

ο >

0.4-

0.6 H

•

ο ο,

• ο Ξ °

0.20.0

—f 40

«

1

1

80

Montmorillonite Spherocarb Carbopack

1

120

»

1—

160

200

t (min)

Figure 4b. Average desorption curves of QHg for different materials.


38


0.4

0.3-

• Montmorillonite • Spherocarb A Carbopack

C

> >

0.2-1 •

o.H

0.0·

ι

1

1

10

j

20

1

;

1

30 t (mini

1

'

40

1

50

60

Figure 5a. Average adsorption curves of CC1 for different materials; Τ = 298 K, P/P = 1.0. 4

c

1.0

• Montmorillonite • Spherocarb A Carbopack

0.8 ο

>

0.6-

CO

> ο

0.4-

*

> 0.2 0.0

•

•• ·

dry N2 flow rate = 21.4 seem Τ = 298 Κ

•

—τ— 10

, 20 t (min)

30

40

Figure 5b. Average desorption curves of CC1 for different materials. 4


3. FLYTZANI-STEPHANOPOULOS ET A L


Table I. EDB Data of Ambient Adsorption (at P/P = 1) And Desorption of Toluene and Carbon Tetrachloride on Various Solid Paricles 0

Solid-Adsorbate

Xa (g Liq/g Solid)

'ΟΛ

(min)

7

'0.5d

' 0.9d

(min)

0.9a

(min)

(min)

S-QHg

0.029 0.061 0.048 0.045 0.025 0.045

8

45

140

>200

M-QHg

0.130 0.070 0.100 0.075

13

47

17

>40

C-CyHg

0.009 0.017

16

62

15

32

S-CC1

0.109 0.092 0.107 0.087

2

7

5

>30

0.292 0.290 0.272 0.347 0.260 0.280 0.360

2

17

3

11

0.012 0.012 0.012

1

2

0.5

4

M-CC1

C-CC1

4

4

S: Spherocarb; M : Montmorillonite; C: Carbopack


1.5-2.0

39

40


TABLE II.

P/Po

0.23

0.29

EDB Data of Ambient Adsorption (at intermediate P/Po values) and Desorption on Single Solid Particles SolidAdsorbate

Xa (g liq/g solid)

S-C^Hg

0.021 0.018 0.013 0.009 0.017

10

35

25

50

M-C^Hg

0.060 0.050 0.052 0.050

16

45

14

25

S-CC1

0.045 0.054 0.054 0.053 0.066

3

1

4

0.188 0.198 0.178 0.172 0.164

5

1

5

4

M-CC1

4

'ftSd

' 0.5a

(min)

(min)

'0.9d

(min) (min)





TABLE III. EDB Data of Adsorption (at low P/Po values) and Desorption of Toluene and Carbon Tetrachloride on Single Solid Particles P/Po

SolidAdsorbate

Xa (g liq/g solid)

0.05

S-QHg

0.008 0.011 0.012 0.004 0.016 0.014

M-C^Hg

S-CC1

0.08

4

M-CC1

4

τ (min)

r (min)

r (min)

4

10

3

8

0.015 0.021 0.025 0.026

5

20

4

10

0.041 0.026 0.048 0.061

2

3

1

4

0.086 0.085 0.086

2

4

1

5

0 Λ

0 9 a

0Sd



f (min) 09d

41

42


0.05 η

Τ = 298 Κ Β

0.040.03-

Β

Β

Ρ/Ρο = 1.0 • Ρ/Ρο=0.23 • Ρ/Ρο=0.05

Β

• •

0.02- ο H

•••

Λ

0.01 -

Β

Φ

•· · π

0.00- ?•

1

I

1

1

40

80

1

1

1

120

1-

160

200

t (min) Figure 6a. Spherocarb-QHg adsorption curves for different relative pressures. 0.05

Τ = 298 Κ ι 0.04

•

• •

•

4.2% 1.6% 1.1%

• • B

°

B

Β

•

•

•

>

•

0.01 0.00

40

80

120

160

200

t (min) Figure 6b. Spherocarb-CyHg desorption curves for the different adsorbed amounts of Q H g shown in Figure 6a.



Incineration of Contaminated Soils 43

0.10 Β

Β

Β

•

Β

Β

0.08

c

> X ο

Β

Β

••

Β

0.06

Β

>

Β

"

Β

•

• •·

•

•

#

Β

Ρ/Ρο=1.0 Ρ/Ρο=0.23 Ρ/Ρο=0.05 Τ = 298 Κ

•

•·

r 120

" Γ ' Ί 40 80 t (min)

0

» 160

Figure 7a. Montmorillonite-QHg adsorption curves for different relative pressures. 0.10Τ = 298 Κ

9.4% • 5.3% • 2.2%

Β

0.08 H c

> 0.06> > 0.040.02 -f · 0.00·

ι 10

ι 20

1

t (min)

ι 30

40

50

Figure 7b. Montmorillonite-QHg desorption curves for the different adsorbed amounts of Q H g shown in Figure 7a.


44


0.12Β

Q

Β

Β

Β

I Β Β

c

5l 0.06 ο

> > 0.04

Β • •

>•

Ρ/Ρο=1.0 Ρ/Ρο=0.29 Ρ/Ρο=0.08 Τ = 298 Κ

0.02 • 0.00 20

10

30 t (min)

40

50

Figure 8a. Spherocarb-CCl adsorption curves for different relative pressures. 4

0.12 τ = 298 Κ

Β

1

•

Β

0.08

•

Β

9.8% 5.4% 4.4%

Β *

tS 0.04

0.00

•

Β

• ··1—

0

Β Β

Β Θ

20 t (min)

10

Β

30

40

Figure 8b. Spherocarb-CCl desorption curves for the different adsorbed amounts of CC1 shown in Figure 8a. 4

4


3.


FLYTZANI-STEPHANOPOULOS ET A L

0.4-

Τ = 298 Κ 0.3·

Β

Β

1

Β

Β

Β

m o* 0.2 H •

•

•

0.1 Hi Β

•

• • •

•

Ρ/Ρο=1.0 Ρ/Ρο=0.29 Ρ/Ρο=0.08

• · ··

0.0

ι

·

10

1

20

«

1

«

30 t (min)

1

•

40

1

50

"~

60

Figure 9a. Montmorillonite-CCl adsorption curves for different relative pressures. 4

Τ = 298 Κ I Β

ο

>

0.2

Β •

•

30.0% 18.0% 8.3%

Β >

Β Β »•

Β

• 0

Β

10

20 t (min)

Β

30

40

Figure 9b. Montmorillonite-CCl desorption curves for the different adsorbed amounts of CC1 shown in Figure 9a. 4

4


46


Discussion There are several observations to be made in discussing the experimental results obtained in this work: (a) time scales were long for both adsorption and desorption, indicating hindered diffusion of the contaminant in the solid (Table I); (b) time scales were longer for toluene than for carbon tetrachloride; (c) the amount of contaminant adsorbed increased with the relative pressure, P / P (Tables I-ΙΠ); (d) the particle-to-particle variability was greatest for Spherocarb (as indicated by variation in the values of X^ Tables I-ΠΙ); and (e) the desorption times for Spherocarb were significantly longer than the corresponding adsorption times at high P/P , but approached symmetry at low P / P (Tables M I ) . 0

9

Q

0

The amounts of toluene and carbon tetrachloride adsorbed on each type of solid particle at P/P = 1.0, corresponded to approximately monolayer coverage for Spherocarb, and slightly above monolayer coverage for the montmorillonite and Carbopack particles (9). Carbopack adsorbed the least amount of either organic compound, in agreement with its low surface area and large pores. The higher (approximately twofold) \ values for CC1 adsorption on all solids are commensurate with the density difference between CC1 (1.595 g/cm ) and CyHg (0.866 g/cm ). Montmorillonite adsorbed the highest amount of both CyHg and CC1 , even though it has a much lower surface area than Spherocarb (192 vs~1050 m /g). For either solid, the characteristic times of adsorption and desorption were much higher (min) than what would correspond to external film diffusion (10" -10" sec) or pore diffusion even of the Knudsen type (0.1-1 sec). Q

4

3

4

3

4

2

3

2

These results point to hindered diffusion in the smallest pores of the materials and capillary condensation in pores with radius in the range > 10 Â and < 250 Â as is well established in the literature (23). The pore size distribution of Spherocarb particularly supports this hypothesis. In earlier work carried out in this laboratory (24), Spherocarb particles were found to contain large vesicular pores (of radius r > 250 Â) in their interior. Large variability in macroporosity (indicated by a twofold density variation) was found, which can explain the particle-to-particle variability in adsorption reported here. Pore volume and pore surface distributions for Spherocarb (25) show the volume of micropores (r < 10 À) and mesopores (10 < r < 250 A) together not to exceed 33% of the total, while 90% of the surface area lies in micropores and 10% in mesopores. The low amounts and large time scales associated with contaminant adsorption on Spherocarb (Table I, Figures 2, 4a, 5a) can then be explained by condensation in the micropores interconnecting and leading to the vesicular macropores. Similar agreements hold for the observed diffusion transients involving slow migration of liquid molecules in the small pores. Montmorillonite is expected to have a much larger voidage fraction in the mesopore regime than




Spherocarb and a smaller fraction in the macropore, which can explain its higher 'adsorption' due to capillary condensation. In summary, the E D B was shown to be a useful tool for studying the fundamental processes of contamination and decontamination of porous soils. The ability of the EDB to study small weight changes on a single particle in the absence of external diffusion limitation and interparticle effects has been proven. Significant differences among various solids and contaminant compounds have been identified in this "first-generation" study. It is clear that a systematic study of the adsorption-desorption characteristics and their dependence on the physical and chemical properties of the soil particles is necessary. Work toward this goal is currently underway. Acknowledgements We gratefully acknowledge the Center for Environmental Management of Tufts University for support of this research under grant #CR-813481-02-0. The apparatus used at MIT has been developed with support from the Exxon Corporation. Literature Cited 1.

Oppelt, E.T. "Incineration of Hazardous Waste" J. Air Pollut Control Assoc. 1987, 37, p.558.

2.

Oppelt, E.T. "Hazardous Waste Destruction" Environ. Sci. Technol. 1986, 20, p.312.

3.

Lighty, J.S., Britt, R.M., Pershing, D.W., Owens, W.D. and Cundy, V.A. "Rotary Kiln Incineration II. Laboratory-Scale Desorption and Kiln-Simulator Studies-Solids" J. Air Pollut. Control Assoc. 1989, 39, p.187.

4.

"New Jersey Hazardous Waste Facilities Plan" New Jersey Waste Facilities Siting Commission, published by the Environmental Resources Management, Inc., p.170, Trenton, Ν.J., 1985.

5.

Linak, W.P., McSorley, J.A., Wendt, J.O. L. and Dunn, J.E. "On the Occurence of Transient Puffs in a Rotary-Kiln Incinerator Simulator: II. Contained Liquid Wastes on Sorbent"J. Air Pollut. Control Assoc. 1987, 37, p.934.

6.

Linak, W.P.,McSorley, J.A., Wendt, J.O.L. and Dunn, J.E. "Hazardous Waste Management - On the Occurence of Transient Puffs in a Rotary Kiln Incinerator I. Prototype Solid Plastic Wastes"J. Air Pollut. Control Assoc. 1987, 37, p.54.


48


7.

Wendt, J.D.L., Linak, W.P. and McSorley, J.A. Paper presented at the A F R C Int'l Symposium on Incineration of Hazardous Municipal and Other Wastes, Palm Springs, CA, Nov. 2-4, 1987.

8.

Tognotti, L., Flytzani-Stephanopoulos, M., Sarofim, A.F., Kopsinis, H . and Stoukides, M . "Study of Adsorption-Desorption of Contaminants on Soil Particles Using The Electrodynamic Thermogravimetric Analyzer" Environ. Sci. Technol. 1990, in print.

9.

Kopsinis, H . "Study of Adsorption-Desorption of Contaminants on Soil Particles Using the Electrodynamic Thermogravimetric Analyzer" MS Thesis, Tufts University, Medford, MA, 1990.

10.

Dudek, D.R. "Single Particle, High Temperature, Gas-Solid Reactions in an Electrodynamic Balance" PhD Thesis, Massachusetts Institute of Technology, Cambridge, MA, 1988.

11.

Bar-Ziv, E., Jones, D.B., Spjut, R.E., Dudek, D.R., Sarofim, A.F. and Longwell, J.P. "Measurement of Combustion Kinetics of a Single Char Particle in an Electrodynamic Thermogravimetric Analyzer" Comb. and Flame 1989, 75, p.81.

12.

Monazam, E.R., Maloney, D.J. and Lawson, L.O. "Measurements of Heat Capacities, Temperatures and Absorptivities of Single Particles in an Electrodynamic Balance" Rev.Sci.Instrum. 1989, 60, p.3460.

13.

Greene, W.M., Spjut, E.R., Bar-Ziv, E., Sarofim, A.F. and Longwell, J.P. "Photophoresis of Irradiated Spheres: Absorption Centers" J. Opt. Soc. Amer. 1985, 82, p.998.

14.

Greene, W.M., Spjut, E.R., Bar-Ziv, E., Longwell, J.P., and Sarofim, A.F. "Photophoresis of Irradiated Spheres: Evaluation of the Complex Index of Refraction" Langmuir 1985, 1, p.361.

15.

Spjut, R.E., Sarofim, A.F. and Longwell, J.P. "Laser Heating and Particle Temperature Measurement in an Electrodynamic Balance" Langmuir 1985, 1, p.355.

16.

Spjut, R.E., Bar-Ziv, E., Sarofim, A.F. and Longwell, J.P. "Electrodynamic Thermogravimetric Analyzer" Rev.Sci.Instrum. 1986, 57, p.1604.

17.

Maloney, D.J., Flashing, G.E., Lawson, L.O. and Spann, J.F. "An Automated Imaging and Control System for the Continuous


3. FLYTZANI-STEPHANOPOULOS ET AL.


Determination of Size and Relative Mass of Single Compositionally Dynamic Droplets" Rev. Sci. Instrum. 1989, 60, p.450. 18.

Cohen, M.D., Flagan, R.C. and Seinfeld, J.H. "Studies of Concentrated Electrolyte Solutions Using the Electrodynamic Balance I. Water Activities for Single-Electrolyte Solutions" J. Phys. Chem. 1987, 91, p.4568.

19.

Wuerker, R.F., Shelton, H. and Langmuir., R.V. "Electrodynamic Containment of Charged Particles" J. Appl. Phys. 1959, 30, p.342.

20.

Davis, E.J. and Ray, A.K. "Single Aerosol Particle Size and Mass Measurements Using an Electrodynamic Balance" J. Coll. Interf. Sci. 1980, 75, p.566.

21.

Arnold, S., Amani, Y . and Orenstein, A. "Photophoretic Spectrometer" Rev. Sci. Instrum. 1980, 51, p.1202.

22.

Bar-Ziv, E., Longwell, J.P. and Sarofim, A.F. "Determination of the Surface Area of Single Particles from High Pressure CO2 Adsorption-Desorption Measurements in an Electrodynamic Chamber" accepted for publication.

23.

Gregg, S.J. and Sing, K.S.W. "Adsorption, Surface Area and Porosity;" Academic Press: London, 1982; 2nd Edition, p.113.

24.

D'Amore, M., Dudek, R.D., Sarofim, A.F. and Longwell, J.P. "Apparent Particle Density of a Fine Particle" Powder Technology 1988, 56, p.129.

25.

D'Amore, M . personal communication.

RECEIVED April 5, 1991


Incineration of Contaminated Soils in an Electrodynamic Balance

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