Print version ISSN 0104-6632
Braz. J. Chem. Eng. vol.23 no.2 São Paulo Apr./June 2006
S. Lucas*; M. J. Cocero
Departamento de Ingeniería Química. Facultad de Ciencias. Universidad de Valladolid. Phone: +34 983 42 32 37 Fax: + 34 982 42 30 13 Prado de la Magdalena s/n, 47011. Valladolid , Spain. E-mail: email@example.com
In this paper a two-step integrated process consisting of CO2 supercritical extraction of volatile coffee compounds (the most valuable) from roasted and milled coffee, and a subsequent step of selective removal of pungent volatiles by adsorption on activated carbon is presented. Some experiments were carried out with key compounds from roasted coffee aroma in order to study the adsorption step: ethyl acetate as a desirable compound and furfural as a pungent component. Operational parameters such as adsorption pressure and temperature and CO2 flowrate were optimized. Experiments were conducted at adsorption pressures of 12-17 MPa, adsorption temperatures of 35-50ºC and a solvent flow rate of 3-5 kg/h. In all cases, the solute concentration and the activated particle size were kept constant. Results show that low pressures (12 MPa), low temperatures (35ºC) and low CO2 flowrates (3 kg/h) are suitable for removing the undesirable pungent and smell components (e.g. furfural) and retaining the desirable aroma compounds (e.g. ethyl acetate). The later operation with real roasted coffee has corroborated the previous results obtained with the key compounds.
Keywords: Coffee aroma; Supercritical extraction; Supercritical adsorption; Activated carbon; Supercritical CO2.
Roasted coffee contains volatile substances, constituting the characteristic fragrance. These volatile compounds are generally called aroma and almost 700 compounds have been reported in coffee (Ishii, 1987; Shibamoto, 1992). The desirable smell in coffee is produced by a delicate balance in the composition of volatiles. It is important to recover coffee volatiles that are released during production of soluble coffee and to put them back in to the liquid coffee extracts or dry products of the extract. This enhances the smell of coffee products and satisfies consumer preferences for such products.
The quality of soluble coffee has been improved by adding an aroma-absorbed coffee oil to coffee powder. In recent patents Jimenez and Liou (1998) and Furrer and Gretsch (2002) described several methods including supercritical technology.
Supercritical extraction-adsorption processes have been demonstrated to be a powerful tool for aroma recovery studies but efforts have been made in this field (Ramos et al., 1998; Sarrazin et al., 2000). In this paper a method of recovery and put-back of aromas to coffee based on an integrated process consisting of SCE and separation by adsorption is proposed. It is a two-step pilot plant comprising CO2 supercritical extraction of volatile coffee compounds (the most valuable fraction) from roasted and milled coffee and a subsequent step of selective recovery of these flavor chemicals and removal of pungent volatiles by adsorption on activated carbon. The adsorbent is regenerated by heating and the concentrate stream of volatile coffee compounds is recovered by absorption with 15 cm3 of coffee oil. The enriched coffee oil, analyzed by GC/MS, is sprayed on soluble coffee powders to improve the quality of the soluble coffee aroma before it is packed. More details about the experimental procedure are included in previous work (Lucas et al., 2004a).
In order to study and simplify the overall process several key compounds were selected from coffee aroma. In this paper ethyl acetate and furfural were chosen as key components. Ethyl acetate is a desirable volatile compound responsible for the fruity and brandy component of coffee aroma, and it is the most common ester present in several kinds of fruit (apples, grapes, etc.). On the other hand, furfural is an undesirable volatile compound with a pungent or foul smell. Lucas et al. (2004a) reported adsorption equilibrium data for both compounds.
MATERIAL AND METHODS
The granular activated carbon (CAL-Chemviron) evaluated in this research was obtained from Aguas de Levante S.A. (Barcelona, Spain). It was characterized experimentally and the most relevant properties are BET specific area (963 m2/g), external area (105 m2/g), total pore volume (0.715 cm3/g), bed porosity (0.453), particle porosity (0.588), average particle size (0.9-1.1 mm) and bed density (450 kg/m3).
Analysis of Coffee Aroma
A gas chromatograph (model PERKIN ELMER AUTOSYSTEM XL) with an MS detector (model PERKIN ELMER QMASS 910) was used to measure the composition of the aroma compounds. A capillary column (SGL-20, 0.25 mm ´ 60 m) was used for the separation. Oven temperature was raised from 40ºC to 180ºC at 15ºC/min). An aliquot of 0.1 cm3 of aroma gas was sampled with a gas-tight syringe and injected in the gas chromatograph. Each component in the aroma-containing gas was identified by comparison with standards.
Roasted Coffee Beans and Coffee Oil
Commercial coffee beans and coffee oil were employed in this work.
A pilot plant for selective aroma recovery was designed and built in the Chemical Engineering Department at Valladolid University (Spain). It is a two-step integrated plant comprising CO2 supercritical extraction and selective coffee aroma recovery by adsorption on activated carbon. The pilot plant was designed to operate at P<30 MPa, T<80ºC and a CO2 mass flowrate of 1-20 kg/h and has a treatment capacity of 0.2 kgcofffe/load. It consists of three pressurized vessels of 1L (i.d. = 0.04 m, L = 0.50 m) that can operate as extractors or adsorbers depending on needs; a diaphragm pump to supply solvent and to recirculate CO2 during operation (LEWA Herbert Leomberg type EH1); and auxiliary equipment such as heat exchangers, pressure, temperature, and flow meters and valves and fittings suitable for high-pressure processes together with the data acquisition system (Cocero et al., 2000).
The pilot plant flow diagram is schematically presented in Figure 1. It was based on two consecutive integrated steps comprising CO2 supercritical extraction and aroma recovery on the adsorbent. In the extraction, the supercritical CO2 flows through a fixed bed of milled and roasted coffee beans and dissolves the extractable components of the solid. The added solvent is removed from the extractor and fed into the adsorber where activated carbon has been placed. The clean solvent leaving the adsorber is recirculated to column with the pilot plant under quasi-isobaric conditions (neglecting pressure drop). After 15 minutes, the pump is turned off and the adsorbent is regenerated by heating up to 65ºC and the concentrate stream of volatile coffee compounds is recovered by absorption with 15 cm3 of coffee oil. The enriched coffee oil is then analyzed by GC/MS.
RESULTS AND DISCUSSION
(a) Ethyl Acetate and Furfural
The Effect of Pressure
Some supercritical adsorption experiments for ethyl acetate and furfural in the range of 13-17 MPa were performed in order to check the effect of operating pressure. The temperature was fixed at 37ºC with a constant CO2 flowrate of 3.5 kg/h.
The corresponding breakthrough curves were treated mathematically in order to obtain the characteristic adsorption parameters such as breakthrough and saturation time (tb and ts), breakthrough and saturation adsorptive capacity (qb and qs) and fractional bed utilization (FBU). From the results shown in Table 1 for both solutes it can be deduced that at a low pressure (13 MPa) the adsorption cycle is faster (shorter breakthrough time), the capacity of the adsorbent (amount of solute adsorbed per kg of adsorbent) is higher and utilization of the bed improves. This result suggests that at a low pressure the interaction forces between solute and activated carbon surface are higher than the corresponding solute-solvent binding forces (Ryu et al., 2000). Moreover at a low pressure all mass transfer resistances decrease and it is possible to get a higher degree of fractional bed utilization (Lucas et al., 2004b).
The Effect of Temperature
The adsorption results for ethyl acetate and furfural obtained at temperatures of 35-50ºC at a fixed pressure (14 MPa) and a constant CO2 flowrate of 3.5 kg/h are shown in Table 2. Operating at lower temperatures (37ºC) enables the obtainment of shorter adsorption cycles and higher adsorptive capacities; as can be deduced from analysis of Table 2. The fractional bed utilization decreases slightly with temperature. This affirmation is valid for both solutes and can be attributed to the increase in solvent power with temperature due to the increase in a vapor pressure. This means that at a lower temperature the solute-adsorbent interaction forces versus the corresponding solute-solvent attraction forces prevail.
The Effect of CO2 Flowrate
The adsorption results for ethyl acetate and furfural obtained with CO2 flowrates of 3-5 kg/h at fixed pressure (14 MPa) and temperature (37ºC) are shown in Table 3.
Operating at a low CO2 flowrate produces longer adsorption cycles; although higher adsorptive capacities and higher fractional bed utilization are achieved (Table 4). The amount of solute adsorbed increases with the decrease in solvent flowrate because the solute-adsorbent contact time is shorter.
From the adsorption point of view similar adsorption curves with the same values of adsorptive capacities and fractional bed utilization were obtained for both solutes. The compounds have similar molecular weights (MEA = 88.1 g/mol and MFF = 96.1 g/mol) and molecular dimensions; which makes the selective adsorption of furfural (the undesirable component) is more difficult than that of ethyl acetate. Nevertheless the furfural molecule has greater electronic mobility and reactivity associated with the carbonyl group-aromatic ring linkage. This phenomenon explains the stronger bonding forces between furfural and activated carbon and as a consequence, the higher values of the removal ratio for all the experiment. The higher adsorption heat of furfural (20-32 kJ/mol) than of ethyl acetate adsorption heat (8-9 kJ/mol) corroborates this fact (Lucas et al., 2004a).
(b) Commercial Coffee
Some experiments were carried out in order to determine the optimal conditions for the extraction, adsorption and regeneration steps involved in the overall process.
Extraction-Adsorption Pressure (Experiments 1, 2, 3 and 4)
From the results shown in Table 4, it can be seen that at a higher extraction-adsorption pressure (11.4 MPa) the amount of extractable compounds increased significantly in the final coffee oil. This effect of pressure may be due to the increase in density.
Extraction Temperature (Experiments 5, 6 and 7)
When the extraction temperature was higher (56.5ºC) the amount of the compounds extracted increased slightly. This behavior can be attributed to the increase in extraction rate with temperature (Table 4).
Adsorption Temperature (Experiments 3 and 9)
At a lower adsorption temperature (34.0ºC) the amount of extractable compounds fixed in the coffee oil increased meaningfully. This effect may be due to the decrease in density with temperature versus the increase in vapor pressure at this operating pressure (Table 4).
CO2 Flow-Rate (Experiments 1 and 8)
In the selected range no effect of flowrate can be observed in the final coffee oils (Table 4).
In Figure 2 the chromatogram of the final coffee oil obtained under the optimal operating conditions is shown.
Optimization of the operating conditions of the integrated process proposed comprising CO2 supercritical extraction and aroma concentration on activated carbon reveals that an extraction-adsorption pressure of 12 MPa (quasi-isobaric process), an extraction temperature of 56ºC, an adsorption temperature of 35ºC and a CO2 flowrate of 2 kg/h permit to be obtained a delicate balance in the composition of volatiles in the final coffee oil. This general result corroborates the optimization of the adsorption step carried out with ethyl acetate and furfural as key coffee compounds. This analysis revealed that low adsorption pressures (12 MPa), low adsorption temperatures (35ºC) and low CO2 flowrates were suitable for retaining ethyl acetate (desirable compound) and removing furfural (pungent compound).
The financial support received from CICYT PROJECT PPQ 2000-1796 and SEDA SOLUBLES S.A. are acknowledged.
|FBU||Fractional Bed Utilization||(%)|
|qb||Adsorption capacity at breakthrough point||(gSOLUTE/gCARBON)|
|qs||Saturation adsorption capacity||(gSOLUTE/gCARBON)|
|Removal||Removal Ratio Removal ratio efficiency||(%)|
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Received: October 20, 2004
ccepted: January 18, 2006
* To whom correspondence should be addressed