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Adsorptive Bubble Separation and Dispersed Air Flotation

111

Fig. 10. De-inking flotation process system for waste paper purification and recycle ( 123 ).

adjust the pH. Then the slurry is conditioned with a fatty acid soap, which selectively coats the calcium carbonate particles with an insoluble soap making them hydrophobic and collectable. In the flotation machine, which mixes as well as disperses fine air bubbles into the slurry, the coated particles attach to the bubbles so that they can float to the surface and be removed from the machine. The clay and silt, which are still water-wetted, remain in the slurry ( 124).

12.2.2. Mechanism of Froth Flotation

Many theories have been advanced concerning the mechanisms involved in surfacing the mineral particles so as to create a hydrophobic hydrocarbon film on the mineral surface, and many investigations have been carried out to define these mechanisms. When froth flotation is used in an aqueous medium that carries the solids to be separated (together with dispersed air bubbles and possibly an organic liquid) a threeor possibly a four-phase system must be considered. In most froth flotation processes, the solid particles are initially completely water-wetted, and the solid–liquid interface must be replaced by

112

Lawrence K. Wang

a solid–gas interface by using suitable reagents. Studies of the changes in thermodynamic properties such as free energy and chemical potentials have done much to advance the understanding of flotation ( 124).

Whether the adsorption of the reagent at the surface of the solid is by physical adsorption, chemisorption, or chemical reaction, there is a definite correlation between the flotability of most minerals and the solubility of the compound formed by the collector agent and the compound to be floated. Theory postulates the formation of an insoluble metal organic compound at the particle surface. For example, in the use of xanthates for the collection of sulfides, it has been shown that the insoluble metal xanthate formed with lead and copper results in a floatable particle. With the more soluble zinc xanthate, zinc sulfide is not floatable unless it is activated by the addition of copper sulfate. Although the actual reactions may be more complex, the following simplified reactions of an organic compound with a polar–nonpolar configuration such as a xanthate are indicative:

2 RCOSSNa + PbS

Pb(RCOSS)2

+ Na2 S

(31)

ZnS + CuSO4

CuS + ZnSO4

 

(32)

2 RCOSSNa + CuS

Cu(RCOSS)2

+ Na2 S

(33)

The organic portion, R, in the xanthate is generally obtained from alcohols ranging

from ethyl to amyl (C2H5OH to C5 H 11OH).

The mechanism for surfacing (collecting) the carbonate and oxide compounds by the use of fatty acid or fatty acid soaps can also be described by the formation of insoluble organic metallic compounds at the surface of the particles. The use of an oleic acid soap (NaO2H33C18 ) for the flotation of limestone (CaCO3) demonstrates the basic chemistry:

2 NaO2H33 C 18 + CaCO3 Ca(O2H33C18 )2 + Na2CO3

(34)

13. ANALYTICAL METHODS AVAILABLE FOR PROCESS MONITORING

Influent concentrations and residual concentrations of cationic surfactants, anionic surfactants, cationic polyelectrolyte, anionic polyelectrolyte, proteins, colloids, oxygen, ozone, detergents, suspended solids, and so on, in the adsorptive bubble separation systems can be determined by the analytical methods reported in the literature (82,127–149).

14. GLOSSARY

Important flotation process terminologies are briefly introduced in this section (1,75,124).

Activators: Activators selectively react with particles to cause the collector to surface. The classic example, as mentioned above, is the use of copper sulfate for the activation of zinc sulfide so that it can be collected by standard sulfide mineral collectors. Another example is the surfacing of lead carbonate, copper carbonate, and copper oxide with the use of sodium sulfide so that collection is also possible by the sulfide collectors.

Air Dissolving Tube or Retention Tank: A metal tank in which the water flow and compressed air are held under high pressure for several minutes to allow time for the air to dissolve into water.

Adsorptive Bubble Separation and Dispersed Air Flotation

113

Air to Solid (A/S) Ratio: A/S is the ratio of the pounds (or kilograms) of air available for flotation and the pounds (or kilograms) of suspended solids to be floated. The A/S ratio is independent of flotation surface area.

Clarified Effluent: The liquid being discharged from the flotation unit.

Collectors: Collector reagents are used to provide a water-repellent surface on the particles to be floated in order to obtain adherence to the air bubbles. The collectors are classified according to their cationic or anionic reaction and type of minerals to be floated. The anionic types of collectors react with the metal portion (cation) in the compound to be floated, whereas the cationic types react with anion portions.

Degree of Treatment: The desired or required degree of treatment depends on objectives. It may meet the effluent discharge standards, or the requirements for water reuse, or the quantity/quality of recovered material.

Depressants: Depressants act to prevent the surfacing of the collector on a particle. An example is the use of zinc sulfate in preventing zinc sulfide from floating while allowing lead sulfide to be collected. Sodium silicate not only aids in the dispersion of slimes or colloidal material, but depresses silica and silicates. The cyanide ion aids in selectively assisting in the activation of lead sulfide but depressing pyrite (iron sulfide) and zinc sulfide. Lime concentrations at a relatively high pH 10–12 depress pyrite, allowing the copper or zinc sulfide mineral to float. Organic colloids such as starch, glue, and tannins act as dispersants, and an excess can prevent any collection. In controlled amounts, they are used to depress carbonaceous material, clays, talc, and calcium carbonate.

Design Flow: Feed or influent to be applied to the flotation unit for design purpose. It can be obtained by examining existing or expected flow data.

Float or Floated Sludge: The concentrated material scooped or skimmed from the top of the flotation unit. The concentration is measured in percent solids, or mg/L.

Flocculating Agent or Flocculant or Coagulant: Any chemical that can convert soluble or colloidal substances to insoluble flocs.

Flotation Aid: Any chemical that produces coagulation, breaks an emulsion, and/or aids in the adsorption of air bubbles by the liquid or particles to be removed.

Flotation Chamber or Flotation Tank: A tank where the water enters and the air comes out of solution in minute bubbles throughout the entire volume of liquid for flotation of impurities.

Froths: A frothing agent is used to form a stable yet brittle froth at the surface of the flotation machine so that the froth can be removed from the slurry along with the attached particles, thus accomplishing a separation of the hydrophobic and wetted particles. The froth generated should be able to support the particles, but should also readily break down when removed from the flotation machine so as not to interfere with subsequent processing. Frothing agents function by reducing the surface tension of the water. Compounds used are generally heteropolar. They contain an organic nonpolar radical that repels water and a polar portion that attracts water. Used in limited quantities, the heteropolar molecules are aligned at the gas–liquid interface with the polar end toward the water and the nonpolar end toward the air. This monomolecular film tends to retain the size of the bubble formed by the flotation machine and prevents the bubbles from breaking as they

114

Lawrence K. Wang

burst through the top of the water layer. A wide variety of organic compounds could function to a greater or lesser degree as frothing compounds, but the number that are low in cost, readily available, effective in low concentrations, and essentially free of collector properties is limited. Initially, most frothers contained a hydroxyl (OH) polar group and had limited water solubility. Compounds included in this group are amyl alcohol (C5 H11OH), cresol (CH3C6H4OH) in cresylic acid, and terpineol (C10H 17 OH) in fine oil.

Hydraulic Loading: The hydraulic loading rate of the flotation unit is expressed in GPM/ft2 of flotation area. The influent loading rate is the influent flow divided by the surface area. The total hydraulic loading rate is the influent flow plus the recycle flow divided by the surface area.

Influent or Feed: The wastewater, process water, or sludge being delivered to the flotation unit. The concentration of impurities is generally measured in mg/L, and flow in GPM or MGD, or m3/d.

Influent Characteristics: The nature and solids concentration of the influent stream and information relating to its source. They are necessary to determine what design parameters should be used.

Modifiers: Modifying agents may act as selective depressants, selective activators, pH regulators, or they may reduce the harmful effects of colloidal material or soluble salts. Often one compound may perform several functions. Depending on the particle separation desired and the character of the slurry, the pH required may be from 1.0 to 12.5 or higher. Lime, soda ash, caustic, or acids are used for pH adjustment. The pH adjustment may act as an activator to aid in collector surfacing or as a selective depressant by preventing collector surfacing. As an example, soda ash (Na2CO3) may be an activator for some sulfides, a depressant if present in excess in calcite flotation, or a pH regulator.

Operating Cycle: The operational time of the flotation unit in hours/day. In most cases for industrial waste the operating cycle is determined by the production schedule.

Recycle Percentage: This applies to a flotation unit operating with effluent recycle. The recycle percentage is the percentage of the influent flow that is recycled.

Solids Loading: Loading of the flotation unit in pounds (dry solids) per ft2 of effective flotation surface area per hour of operation (lb/ft2/h), or in kilograms per m2 of effective flotation surface area per hour of operation (kg/m2/h).

NOMENCLATURE

a 1 a2 a3, a4

A

e

A

s

ai

b 1 b2 b3 b4 d

dr/dL

E

Eb

constants

the equilibrium contact angle, degree

cross-sectional area of bubble separation reactor, cm2 the activity of the ith component

constants

the effective average bubble diameter, cm

the rate of variation of the surface tension of the solution with bulk concentration

the solute surface excess (g-mole/cm2 ) in equilibrium with L

the surface excess value (g-mole/cm2 ) in equilibrium with drain concentration Lb

Adsorptive Bubble Separation and Dispersed Air Flotation

115

E

i

the surf

 

ace excess value (g-mole/cm2

) in equilibrium with the influent

 

 

 

 

 

 

 

 

feed concentration Li

Ethe surface excess of the solute, g-mole/cm2, or mg/cm2

x

the surf

 

ace excess, which is essentially the concentration the component

Exi

 

 

 

 

i at the interface, g-mole/cm2

f

the surf

 

ace to volume ratio of gas bubbles (cm–1 ); for the simple mode 6/d

 

 

 

for stripping mode 6.59/d

Kan equilibrium constant for surface adsorption, cm

Kan equilibrium constant for surface adsorption, g-mole/cm2

Lthe bulk surface active solute concentration, g-mole/cm3 , or mg/cm3

L

b

the surf

 

ace active solute or solid concentration in the drain, g-mole/cm3

 

 

 

or mg/cm3

 

 

L

i

the surf

 

ace active solute or solid concentration in the feed, g-mole/cm3

 

 

 

or mg/cm3

 

 

Lthe surface active solute or solid concentration in the net overhead, g-

n

 

mole/cm3 , or mg/cm3

Lt

the surf

 

ace active solute or solid concentration in the collapsed foam

 

 

 

phase, g-mole/cm3, or mg/cm3

Ni

the number of bubbles of radius ri

NTU

the number of transfer units in the foam based on the upflow stream

Qthe volumetric rate of liquid upflow in a foam separation reactor, cm3/s.

Qthe volumetric rate of air, cm3/s

Q

a

the volumetric liquid flow rate of bottom drain, cm3

/s

b

Q

the volumetric liquid flow rate of influent feed, cm3

/s

i

Qthe volumetric liquid flow rate of net overhead, cm3/s

Q

n

the volumetric liquid flow rate of top overhead, cm3

/s

t

 

 

 

rthe surface tension of the solution, dyne/cm

r

the ef

 

fective average bubble radius, cm the bubble radius averaged by the

 

e

ratio of the third moment (volume) to the second moment (surface area)

 

ri

the radius of the ith bubble, cm

Rf

external reflux factor

rLG

the average surface tensions (i.e., interfacial tensions) of the liquid–gas

 

interface, dyne/cm

rSG

the average surface tensions (i.e., interfacial tensions) of the solid–gas

 

interface, dyne/cm

rSL

the average surface tensions (i.e., interfacial tensions) of the solid–liquid

 

interface, dyne/cm

Rthe universal gas constant, dyne-cm/(g-mole K)

S

b

the residual collector concentration in the drain, mg/cm3

S

the collector concentration in the feed, mg/cm3

i

S

the collector concentration in the foam phase, mg/cm3

t

 

 

Tthe absolute temperature, K

Ttemperature in °C

c

buoyancy component, cm/s

UB

UR

relative bubble velocity, cm/s

116

 

 

 

Lawrence K. Wang

V

b

the residual liquid volume in the separation column, cm3

V

the initial volume, cm3

i

V

the collapsed foam (as liquid) volume from the batch process, cm3

t

y

ef

 

fective concentration of solute in the upflow within a foam separation

 

 

 

 

 

 

reactor on a gas-free basis of liquid, g-mole/cm3

y

 

the effective concentration of solute, in equilibrium with Lt in the

 

 

upflow within a foam separation reactor on a gas-free basis, g-mole/cm3

REFERENCES

1. L. K. Wang, Theory and Applications of Flotation Process . Lenox Institute of Water

Technology (formerly Lenox Institute for Research), Lenox, MA. Technical Report No. LIR/l1-85/l58, 1985. U.S. Department of Commerce, National Information Service, Springfield, VA. NTIS-PB86-194198/AS. 1985.

2.L. K. Wang, Y. T. Hung, and N. K. Shammas (eds.). Physicochemical Treatment Processes The Humana Press, Totowa, NJ, 2005.

3. L. K. Wang, N. K. Shammas, and Y. T. Hung (eds.). Biosolids Treatment Processes The Humana Press, Totowa, NJ, 2006.

4.L. K. Wang, N. K. Shammas, and Y. T. Hung (eds.). Advanced Biological Treatment Processes. The Humana Press, Totowa, NJ, 2006.

5. M. Krofta and L. K. Wang, Potable Water treatment by dissolved air flotation and filtration, J. Am. Water Works Assc. 74 304–310 (1982).

6. M. Krofta and L. K. Wang, Application of dissolved air flotation to the Lenox Massachusetts Water Supply: water purification by flotation, J. N. Engl. Water Works Assc. 249–264 (1985).

7.M. Krofta and L. K. Wang, Application of dissolved air flotation to the Lenox Massachusetts Water Supply: sludge thickening by flotation or lagoon, J. N. Engl. Water Works Assc. 265–284 (1985).

8.M. Krofta, L. K. Wang, L. L. Spencer, and J. Weber, Separation of algae from lake water by dissolved air flotation and sand filtration, Proceedings of the Water Quality and Public

Health Conference, Worcester Polytechnic Institute, Worcester, MA, USA, pp. 103–110,

1983 (NTIS-PB83-219550).

9.L. K. Wang and P. J. Koldziej, Removal of trihalomethane precursors and coliform bacte-

ria by Lenox Flotation-Filtration Plant, Proceedings of the Water Quality and Public

Health Conference Worcester Polytechnic Institute, Worcester, MA, USA, pp. 17–29, 1983 (NTIS-PB83-244053).

10. L. K. Wang, Investigation and design of a denitrification filter, Civil Engineering for

Practicing and Design Engineers, Vol. 3, pp. 347–362, 1984 (NTIS-PB82-199803).

11. M. Krofta and L. K. Wang, Development of innovative Sandfloat systems for water purification and pollution control, ASPE J. Eng. Plumbing 1–16, (1984) (Recipient of 1982 Pollution Engineering Five Star Award) (NTIS-PB83-107961).

12. M. Krofta and L. K. Wang, Tertiary treatment of secondary effluent by dissolved air flotation and filtration, Civil Engineering for Practicing and Design Engineers, Vol. 3, pp. 253–272, 1984 (NTIS-PB83-17l165).

13. M. Krofta and L. K. Wang, Wastewater treatment by biological-physicochemical two-stage process system Proceedings of the 41st Industrial Waste Conference Lewis Publishers Inc., Chelsea, MI, 1986, pp. 67–72.

14. M. Krofta and L. K. Wang, Flotation technology and secondary clarification, Technical Association of the Pulp and Paper Industry Journal ( TAPPI J. ), 70 92–96 (1987).

15. M. Krofta, D. Guss, and L. K. Wang, Development of Low Cost Flotation Technology and

Systems for Wastewater Treatment. Proceedings of the 42nd Industrial Waste Conference

Purdue University, W. Lafayette, IN, USA, May, 1987.

Adsorptive Bubble Separation and Dispersed Air Flotation

117

16. M. Krofta and L. K. Wang, Development of a total closed water system for a deinking plant, Proceedings of the American Water Works Association Water Reuse Symposium III,

San Diego, CA, Vol. 2, pp. 881–898, August, 1984.

17. M. Krofta and L. K. Wang, Total Closing of Paper Mills with Reclamation and Deinking

Installations. Proceedings of the 43rd Annual Purdue Industrial Waste Conference Purdue University, IN.

18. M. Krofta and L. K. Wang, Potable Water Pretreatment for Turbidity and Color Removal by Dissolved Air Flotation and Filtration for the Town of Lenox, Massachusetts U.S. Dept. of Commerce, National Technical Information Service, Springfield, VA., Report No. PB82-182064, 48 p., Oct. 1981.

19. Editor, Water and the industrial launderer: pretreatment, Industrial Launderer pp. 57–70

May, 1983.

20. K. Ng, L. Gutierroz, and C. Walden, Detoxification of kraft pulp mill effluents by foam separation, Pulp & Paper Canada, 80 87–92 (1979).

21. J. H. Voith, The injector cell––a low energy flotation machine, TAPPI J. 73–76 (1982). 22. L.R. Van Vuuren, Dispersed air flocculation flotation for stripping of organic pollutants

from effluents, Water Res. 2 177–183 (1968).

23. L. K. Wang, M. H. S. Wang, S. Yaksich, and M. L. Granstrom, Water treatment with multiphase flow reactor and cationic surfactants, J. Am. Water Works Assc. 70 522–528 (1978).

24. V. Kondratazicius, Removal of synthetic surface-active agents from waste waters of tanneries, Kozk. Obur. Prom. (USSR) 11 18–18 (1969).

25.M. Krofta and L. K. Wang, Wastewater treatment by biological-physicochemical twostage process system: recent developments, Proceedings of the 41st Annual Purdue Industrial Waste Conference Purdue University, W. Lafayette, Indiana USA, May 13–16, 1986.

26. M. Krofta and L. K. Wang, Development of innovative flotation-filtration systems for water treatment, part C: an electroflotation plant for single families and institutions,

Proceedings of the American Water Works Association Water Reuse Symposium III, San Diego, CA, Vol. 3, pp. 1251–1264, August, 1984.

27. F. Barrett, The electroflotation of organic wastes, Chemistry and Industry, 880–882 (1976). 28. D. Rogers, Deep tank aeration/flotation clarification adds a new treatment dimension,

Industrial Wastes 10–17 (1983).

29. P. E. Wace, Foam Separation Process Design, Chemical Engineering Progress Symposium Series, 65 (91), 18–19 (1969).

30. R. B. Greives, Foam separations for industrial wastes: process selection, Proceedings of the 25th Industrial Waste Conference Purdue University, IN, pp. 398–405 (1970).

31.N. London, et al, Fractionation of an enzyme by foaming, Notes Vol. 75, p. 1746 (April 5, 1953).

32. S. E. Charm, The separation and purification of enzymes through foaming, Anal. Biochem. 15 498–508 (1966).

33. R. W. Schnepf and E. L. Gaden Jr., Foam fractionation of proteins: concentration of aqueous solutions of bovine serum albumin, J. Biochem. Microbiol. Tech. Enginr. 1 (1), 1–8 (1959).

34.C. T. Wallace and D. F. Wilson, Foam Separation as a Tool in Chemical Oceanography

Naval Research Laboratory Report 6958, 20 pages (Nov. 1969).

35.V. Kevorkian and E. L. Gaden Jr., Froth-frothate concentration relations in foam fraction-

ation, J. Am. Inst. for Chem. Engineers 3, 180 (1957).

36. L. C. Hargis and L. B. Rogers, Enrichment and fractionation by foaming, Separation Science 4(2), 119–127 (1969).

37. R. K. Wood and T. Tran, Surface adsorption and the effect of column diameter in the continuous foam separation process, The Canad. J. Chem. Engineer. 322–326 (1966).

38.I. Sheiham and T. A. Pinfold, Some parameters affecting the flotation of cationic surfactants, Separation Science 7(1), 25–41 (1972).

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Lawrence K. Wang

39.

C. I. Harding, F

 

oam Fractionation in Kraft Black

Liquor Oxidation Ph.D. Thesis,

 

 

 

University of Florida, Gainesville, FL (1963).

 

40.

Georgia Kraft Company, F

 

oam Separation of Kraft

Pulping Wastes Water Pollution

 

 

Control Research Series, DAST-3, U.S. Department of the Interior, Federal Water Pollution

 

Control Administration (1969).

 

41.

D. T. Michelsen, T

 

reatment of Dyeing Bath Waste Streams by Foaming and Flotation

 

 

 

Techniques Project Report of Water Resources Research Center, Virginia Polytechnic

 

Institute and State University, Virginia, December, 1970.

42.

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mendations for adsorptive bubble separation methods, Separation Science 2 401 (1967).

43.

M. H. S. Wang, Separation of Lignin from Aqueous Solution by Adsorptive Bubble

 

Separation Processes Ph.D. Thesis, Rutgers University, New Brunswick, NJ, 1972.

44.M. H. S. Wang, M. L. Granstrom, T. E. Wilson, and L. K. Wang, Removal of lignin from water by precipitate flotation, Proceedings of American Society of Civil Engineers, Journal of Environmental Engineering Division, 100 (EE3), 629–640, June 1974.

45. L. J. King, Pilot Plant Studies of the Decontamination of Low Level Process Waste by a Scavenging Precipitation Foam Separation Process U.S. Atomic Energy Commission,

ORNL-3808, 57 pages, 1968.

46. B. H. Davis, and F. Sebba, The removal of radioactive caesium contaminants from simple aqueous solutions, J. Appl. Chem. 17 40–43 (1967).

47. E. J. Hahne and T. A. Pinfold, Precipitate flotation: flotation of silver, uranium and gold,

J. Appl.Chem. 19 57–59 (1969).

48. J. A. Lusher and F. Sebba, Separation of aluminum from beryllium in aqueous solutions by precipitate flotation, J. Appl. Chem. 16 129–132 (1966).

49. A. J. Rubin and J. D. Johnson, Effect of pH on ion and precipitate flotation systems, Anal. Chem. 39 298–302 (1967).

50. E. J. Mahne and P. A. Pinfold, Precipitate flotation: separation of palladium from platinum, gold, silver, iron, cobalt and nickel, J. Appl. Chem. 18 140–142 (1968).

51. R. B. Grieves and D. Bhattacharyya, Foam separation of cyanide complexed by iron,

Separation Science 3(2), 185–202 (1968).

52. D. Bhattacharyya, Foam Separation Processes Ph.D.Thesis, Illinois Institute of Technology, IL, 1966.

53. R. E. Wilson and M. H. S. Wang, Removal of lignin by foam separation processes,

Proceedings of the 25th Industrial Waste Conference Purdue University, IN, pp.

731–738 1970.

54. M. H. S. Wang, M. L. Granstrom, T. E. Wilson, and L. K. Wang, Lignin separation by continuous ion flotation: investigation of physical operational parameters, Water Resources Bulletin 10(2), 283–294 (1974).

55. B. Karger and B. Rogers, Foam fractionation of organic compounds Separation Science 33(9), 1165–1169 (1961).

56. B. L. Karger, Foam fractionation under total reflux. Separation Science 38(6), 764–767 (1966). 57. R. B. Grieves, Optimization of the ion flotation of dichromate Journal of the Sanitary Engineering Division, Proceedings of the American Society of Civil Engineers, p. 515,

June 1969.

58. R. B. Grieves, Continuous dissolved air ion flotation of hexavalent chromium, J. Am. Insti. Chem. Engineers 13(6), 1167–1170 (1967).

59. B. L. Karger and D. G. DeVivo, General survey of adsorptive bubble separation processes,

Separation Science 3(5), 393–424 (1968).

60. A. J. Rubin, Microflotation of bacteria, Proceedings Southern Water Resources and

Pollution Control Conference, 14 222 (1965).

61. A. A. Rubin, Microflotation: new low gas flow-rate foam separation technique for bacteria and algae, Biotechnol. Bioeng 8 135 (1966).

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62. A. J. Rubin, Microflotation: coagulation and foam of separation of aerobatic aerogenes,

Biotechnol. Bioeng. 10 89 (1968).

63. O. Henderson, The Effect of pH on Algae Flotation Ph.D. Thesis, Univeristy of North Carolina, Chapel Hill, NC, 1967.

64. B. Dobias and V. Vinter, Flotation of microorganisms, Folia. Microbiology 11 314 (1966). 65. E. Cassell and A. J. A. Rubin, Removal of organic colloids by microflotation, Proceedings of the 23rd Industrial Waste Conference, Purdue University, IN, pp. 966–977, 1968.

66. A. N. Dolzhenkova, (USSR), Improved apparatus for microflotation, Obogashch. Rud. 13 (3), 52–53 (Russ) (1968).

67.A. P. Pikkat-Ordynskaya, Flotation separation of monomineral fractions of galena, pyrite, chalcopyrite, Sphalerite, quartz and feldspar, Aktsessornye Miner. Izrerzhennykh Porod. 75–77 (Russ) (1968).

68. A. N. Kozhukhovskaya, (USSR), Selective flotation of microlite and rutile, Nauch. No 19, 105–111 (Russ) (1968).

69.L. V. Katashin, Flotation of Pyrochlore from Slimes Left After Gravitational Concentration of Rare Metal Carbonatite Ores Nauch. Tr., Irktsk, Gos. Nauch Issled. Inst. Redk. Isvet.

Metal., No. 19 (1968).

70. N. Onoprienko, Flotation of iron oxides, Izr. Vyssh. Ucheb. Zaved., Gorn. Zh. 12(1), 157 (1969). 71. L. K. Wang, P. Leonard, M. H. S. Wang, and D. W. Goupil. Adsorption of disssolved organics from industrial effluents on to activated carbon, J. Appl.Chem. Biotechnol. 25

491–502 (1975).

72.L. K. Wang, Treatment of tannery effluents by surface adsorption, J. Appl. Chem. Biotechnol. 25 475–490 (1975).

73.L. K. Wang, Evaluation and Development of Physical-Chemical Techniques for the Separation of Emulsified Oil from Water Report No. 189, Calspan Corporation, Buffalo, NY, 31 pages, May 1973; Selected Water Resources Abstract 6(21), W73–l3642, p. 90, November 1973.

74.Y. S. Kim and H. Zeitlin, The separation of zinc and copper from seawater by adsorption colloid flotation, Separation Science 7(1), 1–12 (1972).

75. L. K. Wang, Environmental Engineering Glossary Calspan Corporation, Buffalo, New York, 439 pages, 1974.

76. D.O. Harper, Bubble and Foam Fractionation PhD Thesis, University of Cincinnati, Cincinnati, OH 1967.

77. L. K. Wang, Continuous Bubble Fractionation Process, PhD Thesis, Rutgers University, New Brunswick, NJ, 1972.

78.B. T. Kwon and L. K. Wang, Solute separation by continuous bubble fractionation, Separation

Science 6(4), 537–552, 1971. Selected Water Resources Abstracts, 6(21), W73–l3638, p. 89, November 1973.

79.L. K. Wang, Continuous bubble fractionation, Environmental Lett. 3(4), 251–265 (1972),

4(3), 233–252 (1973); 5(2), 71–89 (1973).

80.B. L. Karger, A. B. Caragay, and S. B. Lee, Studies in solvent sublation: extraction of methyl orange and rhodamine B, Separation Science 2(1), 39–64 (1967).

81.I. Sheiham and T. A. Pinfold, The solvent sublation of hexadecyl-trimethyl-ammonium chloride, Separation Science 7(1), 43–50 (1972).

82. APHA, AWWA, WEF, Standard Methods for the Examination of Water and Wastewater,

American Public Health Association, Washington DC, 2005.

83.M. Krofta, L. K. Wang, and H. Boutroy, Development of a New Treatment System Consisting of Adsorption Flotation and Filtration U.S. Dept. of Commerce, National Technical Information Service, Springfield, VA, Report No.PB85-209401/AS, 28 pages, October, 1984.

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