Microsoft word - sk_bvb_icwrdm 2008

Separation of Carboxylic Acids from Waste Water via Reactive
Extraction
Sushil Kumara, B. V. Babub*
aLecturer, Chemical Engineering Group,
Birla Institute of Technology and Science (BITS), Pilani- 333031, Rajasthan, India.
Email: [email protected]
bDean-Educational Hardware Division & Professor, Chemical Engineering Group,
Birla Institute of Technology and Science (BITS), Pilani, -333031, Rajasthan, India.
Phone: +91-01596-245073 Ext. 259; Fax: +91-01596-244183.
Email: [email protected]
Homepage: http://discovery.bits-pilani.ac.in/discipline/chemical/BVb/
*Corresponding Author

ABSTRACT
The separation (or removal) of organic residues from aqueous waste streams released from
industries is important and essential from the points of view of pollution control and recovery
of useful materials. The disposal of waste waters containing most widely-used industrial
organic acids such as acetic acid, formic acid and propionic acid has been recognized as a
significant expense to the industry and environment. This paper presents a state-of-the-art
review on the development of techniques for the separation of carboxylic acids from waste
water. Available conventional techniques including fractional distillation, liquid extraction,
adsorption, precipitation, ion exchange, etc. have been discussed emphasizing the major
drawbacks of these methods. A new method – reactive extraction - for extracting carboxylic
acids from dilute aqueous solutions using a chemical extractant is described and compared
with the other conventional techniques. Reactive extraction is an efficient, economical, and
environmental friendly method for separation of acids from waste water streams.

Keywords: Waste Water; Carboxylic acids; Separation Processes; Reactive Extraction;
Extractant.

1. Introduction
Aqueous waste discharged from chemical plants typically contains low levels (a few percent or less) of small organic compounds such as carboxylic acids amines, alcohols and aldehydes. Whenver detailed characterization of industrial waste water streams has been carried out, one of the organic acids commonly found in significant concentrations is acetic acid. The concentration of these acids can differ significantly. Monocarboxylic acids such as formic acid, acetic acid or propionic acid are fundamental materials in the chemical industry. The organic acids are most widely used in the field of food and beverages as an acidulant and also in pharmaceutical and chemical industries. Carboxylic acids are classified by the chemical structure R-COOH. In this acid form, they are fully hydrocarbon soluble. Only those organic acids with a carbon count of five or less exhibit water solubility. However, an important characteristic of organic acids is that alkali metal salts of these compounds are readily soluble in water and insoluble in hydrocarbon media. Formic acid is used in the textile industry, in tanning, in rubber processing and in the manufacture of pharmaceuticals. Acetic acid is used in the synthesis of acetyl cellulose and plastics and also in the food industry, as well as in the printing and dyeing industries. Calcium and potassium salts of propionic acid are used in the food industry as preservatives (Cai et. al. 2001, Jaung and Wu, 1999). Processing in petrochemical plants, and wood pulping mills often generate aqueous effluent streams containing carboxylic acids, particularly acetic acid (Technical Bulletin, 1999). An aspect of high environmental importance is the recycling of acids from effluents rather than their neutralisation to form sludges for disposal. 2. The need for recovery of carboxylic acids
Advanced treatment of waste water streams containing significant amount of acetic acid and formic acid to meet future water quality standards has been recognized as a significant expense to the industry and environment. The cost of treatment of waste streams containing acetic acid using a conventional activated sludge biological treatment system is between 4 to 10 cents/kg depending on the concentration and sludge disposal system. In addition to treatment requirements, the discharge of acetic acid containing waste water represents the loss of valuable resource. Today acetic acid is one of the most important industrial organic acids and consumed worldwide, about half of it in USA. The global demand of acetic acid is around 6.5 million tonnes per year (Mt/a), of which approximately 1.5 Mt/a is met by recycling; the remainder is manufactured from petrochemical feedstocks or from biological sources (Acetic Acid, 2008). The largest single use of acetic acid is in the production of vinyl acetate monomer that is used for vinyl plastics, adhesives, textile finishes and latex paints and it is closely followed by acetic anhydride and ester production. This acetic anhydride is used for cellulose acetate and pharmaceuticals and plasticizers production. In households diluted acetic acid is often used in descaling agents. In the food industry acetic acid is used under the food additive code E260 as an acidity regulator. The principal use of formic acid is as a preservative and antibacterial agent in livestock feed. it is also widely used to preserve winter feed for cattle. In the poultry industry, it is sometimes added to feed to kill salmonella bacteria (Formic Acid, 2008). Most propionic acid produced is used as a preservative for both animal feed and food for human consumption. For animal feed, it is used either directly or as its ammonium salt. In human foods, especially bread and other baked goods, it is used as its sodium or calcium salt. Propionic acid is also useful as a chemical intermediate. It can be used to modify synthetic cellulose fibers. It is also used to make pesticides and pharmaceuticals. The esters of propionic acid are sometimes used as solvents or artificial flavorings (Kumar and Babu, 2008a). 3. Techniques for separation of carboxylic acid from waste water
As a result of a thorough waste characterization program and preliminary evaluation of the costs that would be associated with secondary treatment, the work toward developing removal and recovery of waste stream components is started in 1974. the separation of monocarboxylic acids from waste water has been important and essential from the points of view of pollution control and industrially for more than a century (Helsel, 1977). Several physical separation techniques such as liquid extraction, ultra filtration, reverse osmosis, electro-dialysis, direct distillation, liquid surfactant membrane extraction, anion exchange,
precipitation and adsorption have been employed to remove carboxylic acids from aqueous
solution.
3.1 Membrane processes
A potentially effective treatment of these waste solutions is to use membranes to remove and
recover the organic contaminants (Sirman et al 1991). Established membrane processes that
have been utilized for waste water treatment include ultra filtration, reverse osmosis (Timmer
et al 1994), electro-dialysis (Lee et al 1998), nanofilteration (Timmer et al 1994) and
pervaporation. The small size of the organics excludes the use of ultrafilteration and
microfilteration, and the osmatic pressure limitation from high salt content makes reverse
osmosis impractical. Supported polymeric liquid membrane can be effective for treating the
types of waste stream described above (Ho, 1999). Attractive features of this membrane
process include the ability to recover the acids in concentrated form for reuse or more
economical disposal of waste, low pressure (ambient) operation, simple scale-up using
commercial hollow fiber modules, and ease of in-situ regeneration of the polymeric liquid.
The process has shown treatment feasibility for several types of aqueous waste streams, but it
is not cost effective. In these processes, the problem of membrane fouling which requires
frequent cleaning of the dialyzer. It gives a higher extent of acids separation but with
increased power and energy consumption. The drawbacks are being of hindered
implementation, mainly complexity of operation and swelling in liquid surfactant membrane.
However, supported liquid membrane often suffers from membrane instability.
3.2 Distillation
Water is the lower boiling component and relative volatility of water to acetic acid is very
low. Although acetic acid and water do not form an azeotrope, it is necessary to have a large
number of equilibrium stages and a very high reflux ratio to obtain glacial grade acid by
simple distillation. As an alternative to fractionation, to reduce energy consumption,
azeotropic dehydration can be employed with addition of anther liquid. In this technique, the
entrainer carries the water overhead in the distillation column with the mixture being phase
separated after condensation and entrainer being returned to the column. It is effective only
for high concentration of acids (Helsel, 1977, Cockrem and Johnson, 1991).
3.3 Liquid-liquid extraction

For intermediate concentrations between 5 to 50%, liquid-liquid extraction is usually
employed, typically followed by azeotropic distillation. Pure solvents such as low molecular
weight esters, ethers, alcohols, ketones and hydrocarbons etc. are unable to give sufficient
distribution coefficients for carboxylic acids. The solvent extract stream, containing the acid
removed from waste stream and some dissolved water is sent to a distillation column where
solvent and water is taken overhead (Wardell and King, 1978 and Baniel 1982).
3.4 Adsorption
Carboxylic acids may be recovered by adsorption on solid adsorbent. Kawabata et al. (1982)
separated carboxylic acid by using a polymer adsorbent of pyridine skeletal structure and a
cross-linked structure. The polymer adsorbent showed good selectivity and high adsorption
capacity for carboxylic acids even in the presence of inorganic salts. The selected elutants
were aliphatic alcohol, aliphatic ketones and carboxylic esters. But the cost associated with
regeneration of commercial adsorbents make adsorption operation very expensive.
3.5 Precipitation
Pekham describes a process for the purification of lactic acid by precipitation. In the calcium
precipitation process, the separation and final purification stages account for up to 50% of the
production costs and produces a large quantity of solid waste. So, Conventional calcium
precipitation method is simple and reliable but it is expensive and unfriendly to the
environment as it consumes lime and sulphuric acid and also produces a large quantity of
calcium sulphate sludge as solid waste (Wasewar et al 2004).
4. Reactive extraction
Among various available alternate processes for removal of the bioproduct such as carboxylic acids from waster water stream, extraction is often the most suitable one (Kumar and Babu, 2008b) as shown in Fig. 1. Reactive extraction with a specified extractant giving a higher distribution coefficient has been proposed as a promising technique for the recovery of carboxylic and hydroxyl-carboxylic acids. Reactive Extraction is developed to intensify separation by solvent extraction and represents a connection between chemical (solute and extractant reaction) and physical phenomena (diffusion and solubilization of the system components). So a reactive extraction method has been proposed to be an effective primary separation step for the recovery of carboxylic acid from aqueous solution (Cascaval and Galaction 2004). Figure 1. Membrane based Solvent extraction system for separation of carboxylic acids
Advantages of this system include the need for relatively small volumes of solvent; low water miscibility in the system; high degree of phase separation in the system, which allows for smaller extraction equipment; and stability and high boiling point of solvent. After the extraction of organic acids, solvents are regenerated by stripping the acids for recycle in the extraction process. So, cost of separation of these useful products is reduced by using recycled solvents. For that reason the recovery of carboxylic acids, in particular acetic acid and propionic acid is economically advantageous. For example, total recovery costs for a 2% acetic acid stream of 0.0126 m3/s from which 90% of the acetic acid is recovered are given as 12.73 cent/kg. The recovery of other low molecular weight acids is suggested to make this method more economically attractive (Helsel, 1977). Reactive extraction strongly depends on various parameters such as the distribution coefficient, degree of extraction, loading ratio, complexation equilibrium constant, types of complexes (1:1, 2:1, etc.), rate constant of carboxylic acid-extractant reaction, properties of the solvent (extractant and diluent), type of solvent, temperature, pH and acid concentration (Kahya et al, 2001). The extraction of carboxylic acids is categories into three group: (i) acid extraction by solvation with carbon-bonded oxygen-bearing extractants (also inert aliphatic and aromatic hydrocarbons and some of their substituted homologs); (ii) acid extraction by solvation with phosphorus-bonded oxygen-bearing extractants and (iii) acid extraction by proton transfer or by ion pair formation, the extractant being high-molecular weight aliphatic amines (Kertes and King 1986). The distribution coefficients of carboxylic acids between the aqueous phases and organic phases with only first categorized solvents are very low as shown in table 2 (Schugeri, 1994). Table 2. Distribution coefficients (KD) of carboxylic acids between the water and
organic solvents at 25 oC
Carboxylic Acid
Organophosphoric derivatives such as tri-n-octyl phosphine oxide (TOPO), tri-n-butyl phosphate (TBP) and long-chain, aliphatic amines such as lauryl-trialkylmethylamine (Amberlite LA-2), tri-n-octylamine, tri-iso-octylamine, tri-n-(octyl-decyl)-amine (Alamine 336) and quaternary alkylammonium salt (Aliquat 336) are effective extractants for separation of carboxylic acids from dilute aqueous solution (Kertes and King 1986). Generally, extractants are dissolved in a diluent, an organic solvent that dilutes the extractant. It controls the viscosity and density of the solvent phase. However, the chemical structure of a diluent may have various effects connected with the formation of acid-amine complexes in the organic phase. The equilibrium behavior has been studied effectively by postulating the formation of various stoichiometric complexes of acid and extractant (Tamada et al, 1991). 4.1 Phosphorus bonded oxygen bearing extractants
Generally speaking, weak organic acids are extracted by organophosphorus compounds with
a significantly higher distribution ratio than by carbon-bonded oxygen donor extractants
under comparable experimental conditions. The basic donor properties of the phosphorus-
bonded oxygen extractants makes the solvation process to be specific, and the number of
solvating molecules per extracted acid is experimentally accessible (Kertes and King 1986).
The reactive extraction mechanism with organophosphorus based extractant can be expressed
by following interface equilibrium as given in eq. (1):
mR − COOH (aq) + nP(org)
So, Phosphorus based solvating extractants has opened new avenues in process development
and reduced energy and reagent consumption and several studies using these extractants have
been made. extraction equilibria of a number of organic acids, like acetic acid, glycolic acid,
lactic acid, pyruvic acid, butyric acid, succinic acid, fumaric acid, maleic acid, itaconic acid,
tartaric acid, citric acid and isocitric acid with tri-n-octylphosphine oxide in hexane has been
investigated by Hano et al. (1990). Al-Mudhaf et al., (2002) and Cai et al, (2001) using
phosphate based extractants showed that tri-n-octylphosphine oxide (TOPO) had a higher
distribution coefficient than tri-n-butyl phosphate (TBP). Wang et al., (2001) has used
Cyanex® 923 in kerosene to extract monocarboxylic acids and found that the distribution
ratios increased with an increase in the trialkylphosphine oxide concentration but decreased
with the carboxylic acid concentration in the aqueous phase. The study has been made to
examine the use of the organophosphine oxides, (Cyanex@921 and Cyanex@923) for the
extraction of formic, acetic and propionic acids from aqueous solutions (waste water stream)
by Wisniewski and Piezchalska (2005).
4.2 Aliphatic amine based extractants
Amines (tri and tertiary) are found to be effective extractants for carboxylic acids. The
amines have been favored because of lower cost and generally higher distribution coefficient.
Among different amines, extraction with primary amines is characterized by a large mutual
solubility of the aqueous and organic phase; secondary amines have the highest reported
distribution coefficient, but tend to form amides in the downstream regeneration by
distillation; quaternary amines extract acid at both acidic and basic pH via an anion exchange
mechanism, but are difficult to regenerate by back extraction with caustic. Consequently,
tertiary amines are the most attractive for extraction from aqueous stream on the basis of their
low aqueous solubility and intermediate basicity, providing reasonable extracting power
along with the possibility of stripping. The extractant must be diluted with an organic solvent
to provide suitable physical properties for use in an extraction process (Kertes and King
1986).

The reactive extraction mechanism with amine based extractant can be expressed by
following interface equilibrium as given in eq. (2):
mR − COOH (aq) + nNR (org) Hong and Hong (1999) carried out the Reactive extraction of lactic acid with mixed tertiary
amine extractants. The mixture of tripropylamine (TPA) and trioctylamine (TOA) dissolved
in 1-octanol/n-heptane was used in the reactive extraction of (L+) lactic acid in aqueous
solution. Malmary et al. (2001) proposed experimental and mathematical studies for recovery
of carboxylic acids from aqueous solutions by liquid-liquid Extraction with a triisooctylamine
diluent system. Tamada et al. (1991) studied the extraction of acetic acid, lactic acid, succinic
acid, malonic acid, fumaric acid, and maleic acid by Alamine 336, an aliphatic, tertiary amine
extractant, dissolved in various diluents. Matsumoto et al. (2001) studied the extraction of
organic acids using both amine based extractant – (tri-n-octylamine) and phosphorus based
extractant – (tri-n-butyl phosphate). The design of an amine extraction process requires
equilibrium data for the acid-amine (solvent) system used. Equilibria for propionic acid
extraction by trioctyl amine in various solvents hexanol, butyl acetate, and petroleum ether
have been determined by Wasewar and Pangarkar (2005. Kumar et al. (2006) has intensified
the recovery of propionic acid using reactive extraction. The conventional solvents, such as
simple hydrocarbon, ketone, kerosene oil and alcohol with or/and without Aliquat 336 are
used to recover the acids from aqueous solution using reactive extraction.
5. Conclusion
It is important to have an efficient and sustainable technology for the separation of carboxylic acids from the waste water stream from the points of view of pollution control and recovery of useful materials. Monocarboxylic acids such as formic acid, acetic acid or propionic acid are fundamental materials in the effluent of chemical industries. Several physical separation techniques such as liquid extraction, ultra filtration, reverse osmosis, electro-dialysis, direct distillation, liquid surfactant membrane extraction, anion exchange, precipitation and adsorption have been employed to remove carboxylic acids from aqueous solution. Some of these techniques are not environment friendly and others are not cost effective. Reactive extraction with a specified extractant has been proposed as a promising technique for seperation of carboxylic acids from waste water. Organophosphoric derivatives and long-chain, aliphatic amines have also opened up new avenues in recovery of carboxylic acids from waste stream with reduced energy and reagent consumption via reactive extraction. References
Acetic Acid, Wikipedia, free encyclopedia (database on Internet). [Updated September 20, 2008]. Available from: http://en.wikipedia.org/wiki/Acetic_acid Al-Mudhaf HF, Hegazi MF and Abu-Shady AI (2002), “Partition data of acetic acid between aqueous NaCl solutions and trioctylphosphine oxide in cyclohexane diluent”, Sep. Pur. Technol., Vol. 27, pp. 41–50. Baniel, A. M. (1982), “Process for the extraction of organic acids from aqueous solution”,. Cai W, Zhu S and Piao X (2001), “Extraction equilibria of formic and acetic acids from aqueous solution by phosphate-containing extractants”, J. Chem. Eng. Data, Vol. 46, pp. 1472–1475. Cascaval D. and Galaction A. I. (2004), “New Separation Techniques on Bioseparations 1. Reactive Extraction”, Chem. Ind., Vol. 58 (9), pp. 375-386. Cockrem, M. C. M., Johnson, P. D., (1991), U.S. Patent 5,210,296. Formic Acid, Wikipedia, free encyclopedia (database on Internet). [Updated September 20, 2008]. Available from: http://en.wikipedia.org/wiki/Formic_acid Hano T, Matsumoto M, Ohtake T, Sasaki K, Hori F and Kawano Y (1990), “Extraction equlibria of organic acids with tri-n-octylphosphine oxide”, J. Chem. Eng. Jap., Vol. 23, pp. 734–738. Helsel, R W (1977), “Removing Carboxylic Acids from Aqueous Wastes”, Chemical Engineering Progress, Vol. 73(5), p 55-59. HO, S. V. (1999), “A supported polymeric liquid membrane process for removal of carboxylic acids from a waste stream”, Environmental Progress, Vol. 18(4), pp. 273-279. Hong Y. K. and Hong W. H. (1999), “Reactive extraction of lactic acid with mixed tertiary amine extractants” Biotechnol. Techniques, Vol. 13, pp. 915–918. Juang R-S and Wu R-T (1999), “Extraction of acetate from simulated waste solutions in chloromycetin production”, Sep Pur Technol, Vol. 17, pp 225–233. Kahya E., Bayraktar E., Mehmeto G. U. (2001), “Optimization of Process Parameters for Reactive Lactic Acid Extraction”, Turk. J. Chem., Vol. 25, pp. 223-230. Kawabata, N., Yasuda, S., Yamazaki, T. (1982), US patent 4323702. Kertes, A.S. and King, C. (1986), “Extraction Chemistry of Fermentation product Carboxylic Acids”, Biotechnol. Bioeng., Vol. 28, pp. 269-282. King, C. J. (1992), “Amine-Based Systems for Carboxylic Acid Recovery: Tertiary Amines and the Proper Choice of Diluent Allow Extraction and Recovery from Water”, CHEMTECH, Vol. 5, pp. 285-291. Kumar S. and Babu B V (2008a), “Propionic Acid Production via Fermentation Route using Renewable Sources”, Chemical Industry Digest, Accepted (In Press). Kumar, S. and Babu B.V. (2008b), “Process Intensification for Separation of Carboxylic Acids from Fermentation Broths using Reactive Extraction”, Journal on Future Engineering & Technology, Vol. 3 (3), pp. 19-26. Kumar S., Babu B V and Wasewer K L. (2006) “Recovery of propionic acid using reactive extraction”, Proceedings of International Symposium & 59th Annual Session of IIChE (CHEMCON-2006), Vol. 1, pp. 196. Lee, E. G.; Moon, S.; Chang, Y. K.; Yoo, I.; Chang, H. N. (1998), “Lactic acid recovery using two-stage electrodialysis and its modeling”, J. Membr. Sci., Vol. 145, pp. 53-66. Malmary G., Albet J., Putranto A.M.H., and Molinier J. (2001), “Recovery of carboxylic acids from aqueous solutions by liquid-liquid Extraction with a triisooctylamine diluent system”, Brazil. J. Che. Eng., Vol. 18 (4), pp. 441-447. Matsumoto, M.; Otono, T.; Kondo, K. (2001), “Synergistic extraction of organic acids with tri-n-octylamine and tri-n-butylphosphate”, Sep. Purif. Technol., Vol. 24, pp. 337–342. Schugeri K. (1994), Solvent Extraction in Biotechnology, Springer-Verlag, Berlin. Sirman, T., Pyle, D. L., Grandison, A. S. (1991), “Extraction of organic acids using a supported liquid membrane”, Biochemical Society Transactions, Vol. 19 (3), pp. 274-279. Tamada, J. A., Kertes, A. S. and King, C. J. (1990), “Extraction of carboxylic acids with amine extractants. 1. Equilibria and Law of Mass Action Modeling”, Ind. Eng. Chem. Res., Vol. 29 (7), pp.1319-1326. Technical Bulletin, (1999), “Cyanex@923 extractant”, pp 1–16. Timmer, J. K. M., Kromkamp, J. and Robbertsen, T. (1994), “Lactic acid separation from fermentation broth by reverse osmosis and nanofiltration”, J. Membr. Sci., Vol. 92, pp. 185-197. Wang Y, Li Y, Li Y, Wang J, Li Z and Dai Y (2001), “Extraction equilibria of monocarboxylic acids with trialkylphosphineoxide”, J. Chem. Eng. Data, Vol. 46, pp. 831–837. Wardell, J. M. and King, C. J. (1978), “Solvent equilibria for extraction of carboxylic acids from water”, Journal of Chemical and Engineering Data, Vol. 23, pp. 144-148.
Wasewar K. L. (2005), “Separation of Lactic Acid: Recent Advances” Chem. Biochem. Eng. Wasewar, K. L., Pangarkar, V. G. (2006), “Intensification of Propionic Acid Production by Reactive Extraction: Effect of Diluents on Equilibrium”, Chem. Biochem. Eng. Q., Vol. 20, pp. 1–7. Wei Q., Zhenyu L., and Youyuan D. (2003), “Extraction of Monocarboxylic Acids with Trioctylamine: Equilibria and Correlation of Apparent Reactive Equilibrium Constant”, Ind. Eng. Chem. Res., Vol. 42 (24), pp. 6196 -6204. Wisniewski M. and Pierzchalska M (2005), “Recovery of carboxylic acids C1–C3 with organophosphine oxide solvating extractants”, J. Chem. Technol. Biotechnol., Vol. 80, pp. 1425–1430. Yang, S. T., White, S. A., Hsu, S. T. (1991), “Extraction of Carboxylic Acids with Tertiary and Quaternary Amines. Effect of pH”, Ind. Eng. Chem. Res., Vol. 30, pp. 1335-1342.

Source: http://seniorecho.wikispaces.com/file/view/Propionic%20Acid%20from%20Waste%20Water.pdf/212568182/Propionic%20Acid%20from%20Waste%20Water.pdf