Journal of Water Technology and Treatment Methods

ISSN 2517-7427

Tannery Wastewater Evaluation and Remediation: Adsorption of Trivalent Chromium Using Commercial and Regenerated Adsorbents

AU Itodo1*,ME Khan1,DP Feka2,B Ogoh1

1 Department of Chemistry, Federal University of Agriculture Makurdi, Nigeria

2 Nigerian Institute of Leather and Science Technology, Samaru, Zaria, Nigeria

Corresponding author

AU Itodo
Department of Chemistry
Federal University of Agriculture Makurdi
Tel. No: +2348039503463

  • Received Date:November 01, 2017
  • Accepted Date:December 15, 2017
  • Published Date:January 30, 2018

DOI:   10.31021/jwt.20181105

Article Type:   Short Communication

Manuscript ID:   JWT-1-105

Publisher:   Boffin Access Limited

Volume:   1.1

Journal Type:   Open Access

Copyright:   © 2018 Itodo AU, et al.
Creative Commons Attribution 4.0


AU Itodo, ME Khan, DP Feka, B Ogoh. Tannery Wastewater Evaluation and Remediation: Adsorption of Trivalent Chromium Using Commercial and Regenerated Adsorbents. J Water Technol Treat Methods. 2018 Jan;1(1):104


The objective of this research is focus on pollutants evaluation and remediation of Tannery effluent discharged from Nigerian Institute of Leather and Science Technology (NILEST) Zaria, Nigeria using activated Carbons as adsorbents. The received, spent and Reborn Adsorbents (RGAC) were characterized using both classical (bulk density, ash content and iodine number) and instrumental (AAS, SEM, FTIR and UV-Vis Spectrophotometer) techniques. The role of different operating parameters on Cr uptake was investigated from a batch adsorption mode. Data generated where fitted into four isotherm models viz; Langmuir, Freundlich, Temkin and Dubinin-Radushkevich. The earlier estimated chromium level in the tannery effluent which was above WHO and NESREA permissible limits was considerably reduced via adsorption. On the general, results show good significance in the adsorption behavior of the regenerated adsorbent compared to the commercial sample.


Wastewater; Pollutants; Remediation; Adsorption; Tannery Effluent; Isotherms; NILEST


Industries have been fingered as the major institutions since the last four decades, responsible for diverse environmental and human catastrophes; hence they are a major contributor to environmental degradation and pollution. Environmental pollution due to appreciating industrial activities is unquestionably some of the most important problems of this century (Ladwani et al., 2012).

Tannery wastewater is highly polluted in terms of the content of its Biological Oxygen Demand (BOD), Chemical Oxygen Demand (COD), Suspended Solids (SS), nitrogen, conductivity, sulphate, sulphide and chromium (Mondal et al., 2005) and in most developing countries tannery effluents are discharged directly into sewers or water bodies without treatment [1,2]. High BOD content of an effluent affects the survival of gill breathing animals of the receiving water body and high COD value indicate toxic State of the wastewater, including the presence of biologically resistant organic substances. High level of ammonia (NH3) is toxic to aquatic organisms and excess nitrogen will cause eutrophic condition. The high salinity and Total Dissolved Solids of effluents may result in physiologically stressful conditions affecting some species of aquatic organisms due to alterations in osmotic conditions. Changes in the ionic composition of water can also eliminate some species while promoting population growth of others [3]. Chrome Tan liquor is greenish in color and highly toxic and acidic with pH 3.1 to 6.0.The waste contains a high concentration of trivalent chromium ranging from 100 to 5500 mg/L. Haxavalent chromium is not generally present in the waste chrome liquor because of the reducing agent used and one bath process utilized [4].

The manufacture of leather has evolved into a significant source of livelihood in many industrialized and developing countries, [5] reported an estimated production capacity of 1.8 billion metric tons of leather yearly, with a larger part of the product processed in Africa and Asia, factored by the high labour intensity involved the manufacture of leather. Procedures employed by most developing countries in leather tanning is still at the traditional level and are not technologically compactable or designed for use with chemical and water. As estimated, the total wastewater discharge from tanneries runs to about 400 million m3 each year. The industry has been painted negatively in the society owing to its high pollutant composition, health and environmental implication is a negative to the sitting of the leather industry. The difficulty in treating tannery effluent owes it to the complex nature of the wastewater produced, leading to various environmental regulations and laws in many developing countries being passed especially in the last ten years.

Adsorption is a phenomenon that occurs on the surface or pores of a solid (sorbent),it is characterized by the available surface area and is a function of the partial pressure (or concentration in aqueous solutions) of a chemical species (solute) [6]. Adsorption occurs if the attractive force between the solute and Adsorbent is greater than the cohesive energy of the substance itself. Adsorption isotherms are important for the description of how adsorbates will interact with an Adsorbent and are critical in optimizing their use [7]. Correlation of equilibrium data using a theoretical or empirical equation is useful for adsorption data interpretation and prediction. Several mathematical models are applicable in describing experimental data of adsorption isotherms.

Langmuir adsorption isotherm, originally developed to describe gas–solid-phase adsorption onto activated carbon, has traditionally been used to quantify and contrast the performance of different biosorbents. In its formulation, this empirical model assumes monolayer adsorption (the adsorbed layer is one molecule in thickness), with adsorption can only occur at a finite (fixed) number of definite localized sites, that are identical and equivalent In its derivation, Langmuir isotherm refers to homogeneous adsorption and can be represent as Equation. 1


Where KL (L/mg) and qm are Langmuir isotherm constants [8]. Freundlich isotherm is the earliest known relationship describing the non-ideal and reversible adsorption, not restricted to the formation of monolayer. This empirical model can be applied to multilayer adsorption, with non-uniform distribution of adsorption heat and affinities over the heterogeneous surface. This model has been expressed either as a non-linear (Eq. 2) or linear (Eqn. 3) form of the model:


KF and n F are Freundlich constants obtained from the intercept and slope of the linear plot of log qe vs log Ce . They are empirical constants which are indicators of sorption capacity and adsorption intensity, respectively [8,9].

The Temkin isotherm assumes that the heat of adsorption of all the molecules increases linearly with coverage. The linear form of this isotherm can be given by:


R is universal gas constant (8.314J/molK), T is absolute temperature (K) and bT is Tempkin isotherm constant. The slopes and intercept are obtained from the graphical plot against ln [10,11].

The linear form of the Dubinin- Radushkevich isotherm can be expressed as:


Where qD is the theoretical saturation capacity (mg g-1 ), B is a constant related to mean free energy of adsorption per mole of the adsorbate (mol2 /J 2 ) and ε is the polanyi potential which is related to equilibrium is given by:


Where, R is the Universal gas constant (8.314 J/mol/K) and T is the temperature in Kelvin. E the mean sorption energy is calculated using the following relation in Equation. 7:


Based on this energy of activation one can predict whether an adsorption is physisorption or chemisorptions. It is general applied to express the adsorption process occurring onto both homogeneous and heterogeneous surfaces, the plot of ln (qe ) vs ɛ2 is used to test the suitability of the data to this model [12].

BET isotherm is a theoretical equation, most widely applied in the gas–solid equilibrium systems. This is a more general, multi-layer model. It assumes that a Langmuir isotherm applies to each layer and that no transmigration occurs between layers. It also assumes that there is equal energy of adsorption for each layer except for the first layer. Its extinction model related to liquid–solid interface is exhibited as Equation. 8:

Equation 8

Where CBET, Cs, qs, and qe are the BET adsorption isotherm (mg /L), adsorbate monolayer saturation concentration (mg/L), the theoretical isotherm saturation capacity (mg/g) and equilibrium adsorption capacity (mg/g), respectively. As CBET and CBET (Ce/Cs) are much greater than 1, the equation is simplified as Equation. 9 [13,14].

Equation 9

Among several Authors, [15] worked on Removal of Chromium from Tannery Effluent Using Bio-adsorbents. On a similar quest, [16] investigated the adsorptive removal of chromium ions from tan liquor using. The Neem Sawdust (NS) gave removal efficiency of 84% at contact time of 120 minute [16]. We now consider a reclamation approach by regenerating spent commercially available activated carbon for a possible reuse in Cr uptake from the Nigerian Institute of Leather and Science Technology (NILEST) Zaria, Nigeria. This present work also investigated pollution load of chrome tan- wastewater and arrayed five isotherm models for interpretation of the sorption phenomenon [17].

Materials and methods

Reagents used were of analytical grade and prepared in line with standard methods as described in the Manual for Standard Analytical Procedures (1999) except otherwise Stated. The FTIR spectrum was recorded on a Fourier Transform Infrared Spectrometer (Agilent technologies Cary 630), scanning electron microscope (SEM) images of virgin, effluent loaded and Chemically regenerated activated carbon at selected magnifications was observed using SEM (Phenomenon Prix, MVE016477830). UV-Visible (Agilent 8453E) Spectrophotometer was used to study the absorbance of both treated and untreated effluent. The procedure was carried out at a pre-determined wavelength (λ max) of 353nm. Atomic adsorption Spectrophotometer (Varian AA240FS) was used to estimate the concentrations of Cr present.

Study Area

The study area, Nigerian Institute of Leather and Science Technology (NILEST) is an Institution of higher learning located in Samaru-Zaria. Coordinates are, Latitude 11.16670 , Longitude 7.63330. It is situated in an area dominated by Schools and research Institutes, Majority of the dwellers are civil servants and farmers


Sampling was carried out in accordance with methods described by Kawser et al. as shown in (figure 1) [18]. Effluent samples by lowering a pre-cleaned 4L glass bottle (previously washed with 0.1M HNO3 before rinsed with distilled water) into different depths of the effluent, allowed to overflow, withdrawn, sealed and stored at 4° C till required for further analysis. Temperature, total dissolved solids, pH and conductivity were determined in situ. Effluent sample to be used for Cr analysis was treated with concentrated HNO3 in order to lower the pH of the sample to less than 2 before refrigeration. Method and duration of the preservation adopted was described by APHAFreeman et al., (2009) and Roger (2002) [19].

Figure 2

Figure 1

Map showing Study Area and Sampling Site in Red

Characterization of tannery effluent

The sampled effluent was analyzed for their physicochemical parameters as well as active functional groups and UV-profile following procedures outlined in the standard method for the examination of water and wastewater [19,20,21]. These parameters include Temperature, Electrical conductivity, Total Dissolved Solids, pH, Turbity, Biochemical Oxygen Demand, (BOD), Chemical Oxygen Demand (COD), Chlorides and Sulphides. Two techniques viz; classical (bulk density, ash content and iodine number) and instrumental (AAS, SEM, FTIR and Uv-vis Spectrophotometer) were used. Results were reported as mean values of triplicate analysis.

Batch Adsorption Experiments

Batch experiments were conducted at room temperature (25±2°C) following the approach reported [22] with a slight modification. 200 mL of adsorbate solution of different concentrations was collected in the 250 mL conical flask, and 1g of each adsorbent was separately added and maintained at the optimized pH 6 and contact time for equilibration. The solution was stirred in mechanical shaker at 120 rpm at room temperature. . After that the solution was filtered and the concentration of the filtered solution was determined by Atomic Absorption Spectrophotometer (Varian AA240FS). The effect of various parameters on the rate of adsorption process was observed by varying contact time, Adsorbent concentration, temperature, and pH of the solution. The solution volume was kept constant.

Chemical regeneration of activated carbon

Regeneration of exhausted activated carbon was carried out in the laboratory using method adopted from Abbas and Waleed, (2008). The exhausted activated carbon (50 g) was weighed by electric balance (Mettler AE200) and mixed with 600 mL 20% ethanol in a 1 L pyrex beaker. The mixture was agitated using a magnetic stirrer (IKA Hitachi RT5) at 200 rpm for 4 h at 25±2oC. The washing liquid was replaced three times during this process, then with 0.1 M NaOH and rinsed with distilled water. The pH of the activated carbon solution was adjusted to pH 7 using 0.1 M HCl. Washed adsorbent was dried in the oven (Gallenkamp BS 0V-160) at 200°C for 3 h and stored as Regenerated Granular Activated Carbon (RGAC).

A batch adsorption experiment similar to the one earlier described was carried out using the regenerated granular activated carbon. The efficiency of the regenerant is judged on the adsorption quantity of activated carbon using equation 10:


Where q0 and qr are quantity of Cr (adsorbate) adsorbed per unit weight of commercial activated carbon and quantity of Cr adsorbed per unit weight of regenerated activated carbon, respectively (Martine and Ng, 1984).


SEM Characterization

Surface morphology of adsorbents was studied by scanning electron microscopy (Plate 1). Plate 1 SEM micrograph of virgin GCAC (Top left), spent GCAC (Top right), RGCAC (bottom left) and spent RGCAC (Bottom right)

Plate 1

Plate 1

Physical Inspection

Physical examination of untreated effluent sample revealed high pollution density as evident by brown colouration, foul odour, microbial activities etc. Similar result was reported [23].

Characteristics parameters of adsorbents

Table 1 compares the physicochemical properties of received and derived adsorbents. Properties fell within range with reported slight differences resulting from losses linked to chemical treatment (bulk density and ash contents) and the measure of micro-porosity (iodine adsorption number).

Iodine adsorption number (an affinity of adsorbent for micro size pollutant) measures activity level and its values are reported in mg/g (typical ranges are from 500-1200). From result displayed on Table 1, High IAN values of 353.12 ±0.02 (mg/g) for GCAC and 218.01 ± 0.02 for RGAC, indicates the suitability of the adsorbents under consideration in the removal of micro (small) size contaminants. It is a measure of micro-pores and it is used as an indication of the total surface area. Sorbents with high iodine number performs better in removing small sized contaminants [24]. It is the most fundamental parameter used to characterize the performance of activated carbon.

Bulk Density (g/cm3 )
0.10 ±0.02
0.08 ±0.02
Iodine Adsorption number (mg/g)
353.12 ±0.02
218.01 ±0.02
Ash Content (%)
1.00 ±0.02
2.40 ±0.02
Moisture Content (%)
1.02 ±0.02
1.10 ±0.02
Volatile matter (%)
12.00 ±0.02

Table 1:Physicochemical parameters of adsorbents

High value indicates high degree of activation as documented [24]. The bulk density value of the adsorbents are given in Table 1 above and are in agreement with the values reported in literatures [25,26]. Low ash content of an activated carbon makes it attractive for adsorption studies, high ash content means interference with pore structure development is likely to occur especially during regeneration and thus, adsorption will be less. Result is in agreement standard values for most commercial CAC [26]. This represents the bulk mineral matter after carbon, oxygen, sulphur and water has been driven off during combustion.

Volatile matter is an index of gaseous fuels present in the carbon. The volatile matter for the GCAC stands at 12 %, while that of RGAC is18.21%; the higher value indicate removal of adsorbed volatile matter after using the GCAC for treatment of the effluent. This refers to components of coal other than moisture, which are liberated at high temperature in the absence of air.

Physicochemical properties of Tan Effluent (TEff)

Table 2 shows the physicochemical properties of untreated tan effluent (TEff). Data compared to those of existing legislations [27,28] unveiled an indication of high pollution loading of effluent. Similar to this was the report of similar studies [18,29,30].


Current study
(NESREA, 2009)
Initial Colour
Light permeable
Conductivity (µs/cm)
TDS (mg/L)
BOD (mg/L)
COD (mg/L)
Alkalinity(mg/L CaCO3 )
Acidity (mg/L CaCO3 )
Chloride (mg/L)
Sulphide (mg/L)
Cr (mg/L)

Table 2: Physicochemical properties of TEff and Legislative discharge limit

Figure 2

Figure 2

Effect of pH on RE (%) of Cr by Adsorbents

These higher values for COD and BOD suggest possibility of depletion of natural oxygen present in the effluent [31]. Evaluated pH value for TEff fall within the WHO and NESREA acceptable limits for the discharge of wastewaters into both surface waters and sewers vary, these ranges are from pH 5.5 to pH 10.0. The present study gives the alkalinity value of the effluent at 225 mg/L CaCO3 Alkalinity is a chemical measurement of a water’s ability to neutralize acids, this is a measure of the buffering capacity of water is ability to resist a change in pH when acids or bases are introduced into it [32]. The high acidity will contribute to corrosiveness and influence chemical reaction rates, chemical speciation and biological processes. Acidity of water is it’s quantitative to react with a strong base to a designated pH [33]. Estimated chloride concentration of 579.82 mg/L exceeds the discharge limit set [27,28] (250.00 mg/L). Chloride is introduced into tannery effluents as sodium chloride usually on account of the large quantities of common salt used in hide and skin preservation or the pickling process [32]. Being highly soluble and stable, it is not affected by effluent treatment and nature, thus remaining as a burden on the environment. Sulphide concentration (450.00 mg/L) in the effluent of the present study is on a high side. Sulphide causes depletion of oxygen in water [33,34]. reported that the upper concentration limit of sulphide in water intended for human consumption is 250 mg/L. Nitrite (NO2) concentration (0.450 mg/L) in this study, falls below the WHO (3.00 mg/L) and is at the recommended level for NESREA (0.5 mg/L)[28]. Cr concentration (148.92 mg/L) was determined and found to be highly above the WHO limit (2.00) and NESREA whose values ranges 1.50-2.00 mg/L [29,30,28].

Physicochemical properties of Tan Effluent (TEff)

Table 4 presents results on removal or adsorption or efficiency (%RE). This study indicated the suitability of using both adsorbents for the removal of Cr in aqueous solution through batch adsorption studies. Mean value of less than 61% could be linked to an early report where high IAN values was reported to favour adsorption of micro rather than medium size pollutants [34].

Effect of pH

TEff – GCAC showed highest % removal of Cr at pH 6 for GCAC and at pH 8 for RGAC. The results shown in Figure 2 indicate that maximum uptake of Cr ions takes place at pH 4 and decrease in adsorption capacity on either side of pH 4. The removal of Cr is Ph dependent because the surface of activated carbons are negatively charged at certain pH [35], the decrease in adsorption capacity in the low pH region would be expected as the acidic medium would lead to an increase in hydrogen ion concentration which would then neutralize the negatively charged carbon surface thereby decreasing the adsorption of the positively charged cation.

Effect of adsorbent dose

The removal of Cr was found to be highest with an adsorbent dosage of 2.5g, achieving above 60 % Cr removal for GCAC and 55 % removal for RGAC Figure 3. The increase in removal of Cr with adsorbent dose can be attributed to the introduction of more binding sites for adsorption. Similar results have been reported [36,37,38].

Figure 3

Figure 3

Effect of Adsorbent Dosage on RE(%) of Cr

Effect of initial concentration

The RE (%) of Cr in the sample is influenced by the initial concentration adsorbate. The highest percentage removal by GCAC was 67 % and 96 % with RGAC Figure 4. Thus, at higher initial concentration, the percentage removal decreases. This could be linked to competition for attachment sites.

Figure 4

Figure 4

Effect of Concentration on RE (%) of Cr Activated Carbon

Figure 5 represents the effect of contact time on Cr uptake. Adsorption increases with increase in contact time. Equilibration was achieved at 60 min, after which desorption sets in.

Figure 5

Figure 5

: Effect of Contact Time on RE (%) of Cr

FTIR Study

Table 3 is a summary of spectral characteristic typical of Figures 6 and 7 for FTIR Spectra of unspent, spent and regenerated adsorbents. Distorted peaks of Figure 6a (3246.2 cm-1) compared to Figure 6b, clearly shows surface interaction between the adsorbent and the adsorbate. An aromatic nitro group also appears at 12710.65 cm-1(C-H, C-N), 24113.4 cm,-1, 820.0 cm-1 (C-H) and 1524.5 cm-1(C=C-C) in Figure 6b are all functional groups attached to GCAC after adsorption. This is visible even in the shift of bands and is visible when compared to peaks shown in Figure 6a. Spectrum of TEff - RGAC, displays strong bands adsorptions at 3280.1 cm-1, for O-H, then 1626.1 cm-1 (C=C) to 1528.2 cm-1 (C=C-C), then at 10287.7 cm1 to 1166.7 cm1 (C-O) which appears d istorted when compared to the RGAC and denotes adsorption.

Figure 6

Figure 6

FTIR spectra of (a) GCAC (b) TEff loaded GAC

Figure 7


FTIR spectra of (a) RGCAC (b) TEff loaded RGAC

Vib. Freq (cm-1)

Observed Frequencies (cm-1)
Functional group



1032.5, 752.9
C-O stretch,
C-O stretch; CH3 symmetric deformation; N-O
N-H bend; C≡C stretch; C=C stretch
N=N=N, Anti-symmetric stretch; C≡C
-PH; C≡N
O-H broad; O-H stretch; -NH stretch; ≡CH-H stretch

Table 3:FTIR spectra characteristics of virgin GCAC, spent GCAC and RGAC

SEM Characteristics of Adsorbents

Plate 1 is SEM micrographs of the GCAC at various treatment conditions. Plate 1 (bottom left) is the SEM image for RGAC revealing a more porous morphological structure over the GCAC. This could mean more site of adsorption or vacancies for pollutants occupation. The loaded SEM images show the adsorption of TEff onto the adsorbents depicting the filled-surfaces of particles after adsorption, it is clearly seen that the caves, pores and surfaces of adsorbent were covered by adsorbed TEff and consequently the surface has become smooth. It is notable that the TEff absorbed onto the adsorbent affected the surface structure.

Isotherm Studies

Table 5 represents the constants deduced from modeling generated equilibrium data four isotherm models namely; Langmuir, Freundlich, Temkin and the Dubinin-Radushkevich. Extent of model fitness was based on the coefficient of correlation (determination or applicability) values, R2

Isotherm Model

KF (mg/g)
bT(K J/mol)
KD (mol2 /KJ2 )
4 x 10-4
2 x 10-4
qS (mg g-1)

Table5: Isotherm experimental constants for adsorption of Cr onto Activated carbon

Langmuir Isotherm R2 value of 0.992 (GCAC) and 0.930 (RGAC) shows a good applicability of the model, indicating both monolayeradsorption and heterogeneous surface conditions (Vinodhini and Das, 2010).In Langmuir theory, the basic assumption is that the sorption takes place at specific homogeneous sites within the adsorbent .The essential feature of the Langmuir isotherm is expressed by means of dimensionless constant separation factor (RL ). In this context, lower RL , less than 1.0 reflects that adsorption is favourable. RL value indicates the adsorption nature to be either unfavourable (RL > 1), linear (RL = 1), favourable (0 < RL < 1) or irreversible (RL = 0). Result from this work on favourable adsorption is in agreement [13].

Coefficient of regression recorded for the Temkin Isotherm was 0.993 and 0.879 for GCAC and RGAC respectively. It can be deduced that the isotherm model for GCAC has a better applicability than RGAC [39]. βT is a constant related to the heat of adsorption, where a high value indicate strong interaction between Cr and the adsorbent. From the result, the constant βT was 1.537 KJ/mol for GCAC and 0.137 KJ/mol for RGAC, indicating a weak interaction between Cr and the adsorbent. Temkin isotherm assumes that the heat of adsorption of the molecules increases linearly with coverage [10,40].

The Freundlich isotherm assumes a heterogeneous surface with non-uniform distribution of heat of adsorption over the surface. The R2 values recorded for GCAC and RGAC are 0.938 and 0.958 respectively, indicating a slightly better applicability of this model to RGAC over GCAC, result recorded also gave the value of 1/n and KF which represents Freundlich constants for adsorption intensity and capacity respectively. It is favourable for 1/n value to be less than 1 or an adsorption intensity (n) value greater than 1. 1/n indicate favourable uptake of adsorbate when 0.1< 1/n < 1. For this research, 1/n values for sorption of Cr on GCAC and RGAC gave values that are above 1.0, with n values < 1.0, implying an unfavorable fitness of the model irrespective of the high R2 values. The values are unlike those for good adsorption [41].

For Dubinin-Radushkevich isotherm model, R2 value for GCAC and RGAC are 0.933 and 0.998, generally showing a good fit for this model but a better fit for RGAC. It is generally applied to express the adsorption mechanism with a Gaussian energy distribution onto a heterogeneous surface [13]. This isotherm model is an empirical model initially conceived for the adsorption of subcritical vapors onto micropore solids following a pore filling mechanism.

Generally, all the models adopted for this study provide explanation on a particular sorption phenomenon. Considering the sorption of Cr on regenerated adsorbent RGAC, best fit coefficient of determination (R2 ) values follows the order; Dubinin-Radushkevich (0.998) > Freundlich (0.958) > Langmuir(0.930) > Temkin (0.879) isotherm models. The reverse trend was observed for the virgin GCAC.


Regeneration of Cr- loaded spent granular activated carbon and its adsorption studies was successfully carried out. Removal efficiencies were high for tannery wastewater detoxification and clarification. All the adopted and investigated isotherms gave explanation on certain adsorbent property. The best fit coefficient of regression (R2 ) value for the sorption of Cr on regenerated adsorbents follows the order of Dubinin-Radushkevich > Freundlich > Langmuir > Temkin. AAS analysis shows that the level of Cr in the tannery effluent is above WHO and NESREA permissible limits and could pose potential threat to the populace. However, results from this study unveiled a removal efficiency of up to 56 and 60 % using commercial and regenerated

activated carbons respectively. Results on the adsorption potentials of adsorbents from existing literatures and those of commercial adsorbent utilized in this study are in good agreement with those of our regenerated adsorbent. On the overall, GCAC and RGAC studied in this work established the potentials of chemically regenerated activated carbon for use in the treatment of pollutants (Cr) from tanneries


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