# The Application of Response Surface Methodology in the Study of Photodegraded Industrial Dairy Effluents by the Photo-Fenton Process: Optimization and Economic Viability

Authors: Carla Cristina Almeida Loures; Hélcio José Izário Filho; Ivy dos Santos Oliveira; Gisella Rossana Lamas Samanamud; André Luiz de Souza; Messias Borges Silva
Journal: ISRN Chemical Engineering
 (2014)

---

## Abstract

This study presents results from an application of Photo-Fenton process for organic-load reduction in dairy effluents. Process efficiency was evaluated in terms of percentage dissolved organic carbon, chemical oxygen demand, and biochemical oxygen demand (DOC, COD, and BOD, resp.), whose initial values were1658
±
145 mg O2 L−1, 9500
±
500 mg O2 L−1, and 2400
±
100 mg O2 L−1, respectively. We applied a statistical design represented by Box-Behnken factorial design inclusive of Fenton's reagent, the power of applied radiation (W), and pH factors. The set temperature value was 30°C with a reaction time of 60 min. The maximum efficiency obtained was at p
H
=
3.5, Fenton reagent in the proportion of 35 g H2O2 + 3.6 g Fe2+, and ultraviolet radiation potency of 28 W. The results obtained for DOC, COD, and BOD were 81%, 90.7%, and 78.8%, respectively. Regarding the cost/benefit evaluation, the variables and their levels should be the following: pH 3.5, 35.0 g H2O2/Fe2+ 3.6 g, and 28 W UV, obtaining a reduction in concentration of 79.5% DOC.


---

## Body

## 1. Introduction

Dairy industry effluents are characterized by high volumes of water consumption and elevated organic contents and inhibited recalcitrancy for a conventional treatment [1]. The escape into the aqueous environment of such pollutants, defined as industry-relevant organic components and BOD, COD, pH, fats, and phosphates, among others, demands treatment formulas that minimize the devastating impact of effluent pollution inclusive of degraded waterways, harmed environment, and a general detriment to animal and human health [2, 3].Economically advantageous biological processes are typically used for dairy effluent treatments regardless of a series of practical limitations [4, 5]. A common problem in this methodology is the oscillation of the organic load in the dairy effluent, resulting in expanded sludge volume and compromises to the efficiency of biological processes [5].POAs are defined as processes with considerable capacity for hydroxyl radical (•OH) production [6, 7]. A high standard reduction potential (see (1)) for this radical is capable of oxidizing a wide variety of organic compounds to CO2, H2O, and inorganic ions from heteroatoms:
(1)
•
OH
+
e
-
+
H
+
⟶
H
2
O
E
°
=
2,730
eV
Among the POAs, the use of Fe2+/Fe3+ in the presence of hydrogen peroxide under irradiation, called a Photo-Fenton reaction, is considered the most promising for remediation of effluents containing a variety of toxic nonbiodegradable organic compounds [8, 9].Several industrial effluent treatment studies using this process have been made in recent decades [5, 8–11].Using a process parameter optimization, the experimental design has been widely employed to improve product quality through the application of engineering concepts and statistical models [12]. The Box-Behnken models are a class of models rotational or almost rotational second order based on factorial models incomplete of three levels. The number of experiments (N) required for the model development Box-Behnken is defined as follows:
(2)
N
=
2
k
(
k
-
1
)
+
C
o
,
where k is the number of factors and C
o is the replicate number of the central point.This study focused on the application of the Photo-Fenton reaction to a Box-Behnken matrix in treatment of dairy effluent.


## 2.  Materials and Methods

### 2.1. Sampling and Preservation

The effluent studies were performed at an industrial dairy in the city of Guaratinguetá, Vale do Paraiba Region, in the state of São Paulo. Samples were collected from the production line feeding the treatment plant before the acid pretreatment. 400 L of raw effluent was collected and held in refrigerated storage at 4°C.Due to complex characteristics, some methodologies were adapted to improve accuracy and analytical precision as suggested by Lima et al. [13]. Determinations of COD in dairy effluents required adjustments to 5220 D Closed Reflux colorimetric method of APHA-AWWA [14]. Winkler’s modified method was used to measure BOD. Preliminary tests with diluted deionized water were specific to concentrations for each methodology for COD and BOD determinations. Dissolved organic carbon determination was performed in a TOC-VCPH Total Organic Carbon Analyzer (high sensitivity) from Shimadzu on high temperature catalytic oxidation.


### 2.2. Degradation of Dairy Effluent by Photo-Fenton Process

Photochemical treatment was undertaken in a semibatch reactor with a plug flow reactor model GPJ-463/1 with nominal volume of 1 L. Mercury lamp was used of model GPH-463TJL with UV radiation in 254 nm and intensity of 15 W and 28 W protected by quartz tube. Fenton’s reagent was added at the following concentrations: 0.82 mol L−1 of FeSO4·7H2O, H2O2 at 30% m/m. After thermal conditioning of the effluent, a simultaneous addition of ferrous ions and H2O2 solutions were added into the system. These additions were performed using a dosing pump during 20 or 30 min intervals through 1 h of reaction time. Sulfuric acid and NaOH (both at 5.0 M) were used to maintain a consistent medium acidity. This control was performed by a borosilicate glass-electrode potentiometer. The electrode was kept in the reaction bath. Figure 1 presents a detailed treatment schematic.Figure 1
Test bench control and layout of experimental procedures for AOPs treatment process.The operational stages with Photo-Fenton process were as follows:(1)
3.0 L of dairy effluent was kept at room temperature, homogenized, and placed in a glass container;
(2)
thermostatic bath and centrifugal pump were turned on;
(3)
temperature was adjusted according to experimental design;
(4)
pH was regulated according to experimental records;
(5)
reactor was started to emit UV radiation;
(6)
in parallel, ferrous and peroxide solution were added during 50 min of a 1 h reaction;
(7)
after adjusting all parameters and setting the time control for 1 hour treatment, pH was kept constant;
(8)
aliquots (20 mL) were taken every 10 minutes;
(9)
the pH of both rates was adjusted from 8.0 to 9.0 for ferrous ions precipitation and filtered in quantitative filter paper;
(10)
each sample of dairy effluent was submitted to determine concentrations of COD, H2O2, and DOC. Dilutions owing to pH adjustment (Advanced Oxidation Process—AOP—and precipitation) were taken into account to the concentration calculation in all analytical determinations.


### 2.3. Box-Behnken Matrix Application

The Box-Behnken matrix optimizes the Fenton reagent pH values in relation to the L9 Taguchi array values obtained by Loures et al. [15] at a fixed temperature of 30°C.Table1 illustrates control factors and levels for treatment with AOP according to Box-Behnken matrix (used in response surface).Table 1
Factors and respective levels used for the experiment matrix for the Box-Behnken in the treatment of dairy effluent by Photo-Fenton process.
Factor
Level (−1)
Level 0
Level (1)
pH
3
3.5
4
Fenton reagent (mH2O2 g + mFe
2
+ g)*
30.0 g H2O2 + 2.1 g Fe
2
+
32.5 g H2O2 + 2.6 g Fe2+
35.0 g H2O2 + 3.6 g Fe2+
Ultraviolet
None
15 W
28 W
*Both H2O2 and Iron II were used in solutions whose concentrations were [H2O2] = 30% m/m and [Fe2+] = 0.82 mol L−1 showing values proportional to 3 L of treated effluent.Table2 presents the Box-Behnken matrix operating on three levels for planning experiments with AOP dairy effluent.Table 2
Box-Behnken matrix values in the study of dairy effluent treatment by a Photo-Fenton process, through the factors pH, Fenton reagent, and UV irradiation, operating on 3 levels (low represented by −1, intermediate represented by 0, and high represented by 1).
Exp.
Central point
Block
pH
Fenton
UV
1
2
1
−1
0
−1
2
2
1
−1
0
−1
3
0
1
0
0
0
4
2
1
−1
−1
0
5
2
1
0
1
1
6
0
1
0
0
0
7
2
1
−1
0
1
8
2
1
0
1
1
9
2
1
−1
1
0
10
2
1
0
−1
−1
11
0
1
0
0
0
12
0
1
0
0
0
13
2
1
1
0
−1
14
0
1
0
0
0
15
2
1
−1
−1
0
16
2
1
0
1
−1
17
2
1
1
−1
0
18
2
1
−1
1
0
19
2
1
0
−1
−1
20
2
1
1
−1
0
21
2
1
−1
0
1
22
2
1
1
1
0
23
2
1
0
−1
1
24
2
1
0
−1
1
25
2
1
0
1
−1
26
2
1
1
0
1
27
0
1
0
0
0
28
2
1
1
1
0
29
2
1
1
0
1
30
2
1
1
0
−1


## 2.1. Sampling and Preservation

The effluent studies were performed at an industrial dairy in the city of Guaratinguetá, Vale do Paraiba Region, in the state of São Paulo. Samples were collected from the production line feeding the treatment plant before the acid pretreatment. 400 L of raw effluent was collected and held in refrigerated storage at 4°C.Due to complex characteristics, some methodologies were adapted to improve accuracy and analytical precision as suggested by Lima et al. [13]. Determinations of COD in dairy effluents required adjustments to 5220 D Closed Reflux colorimetric method of APHA-AWWA [14]. Winkler’s modified method was used to measure BOD. Preliminary tests with diluted deionized water were specific to concentrations for each methodology for COD and BOD determinations. Dissolved organic carbon determination was performed in a TOC-VCPH Total Organic Carbon Analyzer (high sensitivity) from Shimadzu on high temperature catalytic oxidation.


## 2.2. Degradation of Dairy Effluent by Photo-Fenton Process

Photochemical treatment was undertaken in a semibatch reactor with a plug flow reactor model GPJ-463/1 with nominal volume of 1 L. Mercury lamp was used of model GPH-463TJL with UV radiation in 254 nm and intensity of 15 W and 28 W protected by quartz tube. Fenton’s reagent was added at the following concentrations: 0.82 mol L−1 of FeSO4·7H2O, H2O2 at 30% m/m. After thermal conditioning of the effluent, a simultaneous addition of ferrous ions and H2O2 solutions were added into the system. These additions were performed using a dosing pump during 20 or 30 min intervals through 1 h of reaction time. Sulfuric acid and NaOH (both at 5.0 M) were used to maintain a consistent medium acidity. This control was performed by a borosilicate glass-electrode potentiometer. The electrode was kept in the reaction bath. Figure 1 presents a detailed treatment schematic.Figure 1
Test bench control and layout of experimental procedures for AOPs treatment process.The operational stages with Photo-Fenton process were as follows:(1)
3.0 L of dairy effluent was kept at room temperature, homogenized, and placed in a glass container;
(2)
thermostatic bath and centrifugal pump were turned on;
(3)
temperature was adjusted according to experimental design;
(4)
pH was regulated according to experimental records;
(5)
reactor was started to emit UV radiation;
(6)
in parallel, ferrous and peroxide solution were added during 50 min of a 1 h reaction;
(7)
after adjusting all parameters and setting the time control for 1 hour treatment, pH was kept constant;
(8)
aliquots (20 mL) were taken every 10 minutes;
(9)
the pH of both rates was adjusted from 8.0 to 9.0 for ferrous ions precipitation and filtered in quantitative filter paper;
(10)
each sample of dairy effluent was submitted to determine concentrations of COD, H2O2, and DOC. Dilutions owing to pH adjustment (Advanced Oxidation Process—AOP—and precipitation) were taken into account to the concentration calculation in all analytical determinations.


## 2.3. Box-Behnken Matrix Application

The Box-Behnken matrix optimizes the Fenton reagent pH values in relation to the L9 Taguchi array values obtained by Loures et al. [15] at a fixed temperature of 30°C.Table1 illustrates control factors and levels for treatment with AOP according to Box-Behnken matrix (used in response surface).Table 1
Factors and respective levels used for the experiment matrix for the Box-Behnken in the treatment of dairy effluent by Photo-Fenton process.
Factor
Level (−1)
Level 0
Level (1)
pH
3
3.5
4
Fenton reagent (mH2O2 g + mFe
2
+ g)*
30.0 g H2O2 + 2.1 g Fe
2
+
32.5 g H2O2 + 2.6 g Fe2+
35.0 g H2O2 + 3.6 g Fe2+
Ultraviolet
None
15 W
28 W
*Both H2O2 and Iron II were used in solutions whose concentrations were [H2O2] = 30% m/m and [Fe2+] = 0.82 mol L−1 showing values proportional to 3 L of treated effluent.Table2 presents the Box-Behnken matrix operating on three levels for planning experiments with AOP dairy effluent.Table 2
Box-Behnken matrix values in the study of dairy effluent treatment by a Photo-Fenton process, through the factors pH, Fenton reagent, and UV irradiation, operating on 3 levels (low represented by −1, intermediate represented by 0, and high represented by 1).
Exp.
Central point
Block
pH
Fenton
UV
1
2
1
−1
0
−1
2
2
1
−1
0
−1
3
0
1
0
0
0
4
2
1
−1
−1
0
5
2
1
0
1
1
6
0
1
0
0
0
7
2
1
−1
0
1
8
2
1
0
1
1
9
2
1
−1
1
0
10
2
1
0
−1
−1
11
0
1
0
0
0
12
0
1
0
0
0
13
2
1
1
0
−1
14
0
1
0
0
0
15
2
1
−1
−1
0
16
2
1
0
1
−1
17
2
1
1
−1
0
18
2
1
−1
1
0
19
2
1
0
−1
−1
20
2
1
1
−1
0
21
2
1
−1
0
1
22
2
1
1
1
0
23
2
1
0
−1
1
24
2
1
0
−1
1
25
2
1
0
1
−1
26
2
1
1
0
1
27
0
1
0
0
0
28
2
1
1
1
0
29
2
1
1
0
1
30
2
1
1
0
−1


## 3.  Results and Discussion

### 3.1. Characterization of Raw Effluent

The characterization of dairy effluent was carried out according to the most relevant physicochemical aspects, such as pH, COD, BOD5, total phosphorus, ammonia-nitrogen and organic nitrogen, DOC, turbidity, color, total dissolved and fixed solids, settled solids, oils and greases, and the ratio of BOD5/COD.Table3 shows physical/chemical data for dairy effluent in natura and after the AOP and chemical treatment (precipitation in pH 8 and 9) standards as per Articles 18 and 34 of Brazilian Statute CETESB CONAMA 357/05 and values from respective references.Table 3
Results of physical/chemical analysesin naturaand posttreatment dairy effluents.
Parameters
Results
Data in the literature
References
Release standards* (mg L−1)
In Natura
After AOPs and precipitation
Aspect
Turbid
Clear
—
—
—
True color (Co Pt)
431.9
27.86
—
—
Absent
Turbidity (NTU)
1033
12.00
—
—
Absent
pH
6.0–6.4
8.0–8.50
5.25–8.0
[17, 19–21]
5–9
Odor
Pungent
Absent
—
—
—
COD (mg L−1 O2)
9000–10000
929.0–935.0
797–8000
[19–21]
—
BOD (mg L−1 O2)
2300–2500
508.5–515.8
1292–60000
[20]
60
BOD/COD
0.25
0.65
—
—
—
DOC (mg L−1)
1513–1800
336.2–356.1
2500–5000
[5, 20]
—
Phosphorus (mg L−1)
108.7
3.0
38.6–227.1
[17, 20]
—
NH3-N (mg L−1)
158.0
0.0027
0.25–57
[19]
20
Organic N (mg L−1)
179.9
0.0047
16.5–1048
[19, 20]
—
aST (mg L−1)
5680
2830.60
545–15720
—
—
bSTF (mg L−1)
986
880
119
—
cSTV (mg L−1)
4800
1746.0
426–10900
[19]
—
Phenol (mg L−1)
>0.005
>0.005
—
0.5
Oil and grease (mg L−1)
2002.5
0.000
4680
[22]
50
Chloride (mg L−1)
1301.75
27.0
—
—
—
Cyanide (mg L−1)
Absent
Absent
—
0.2
Copper (mg L−1)
1.39
7.8
—
1.0
Chromium (mg L−1)
Absent
Absent
—
0.1
Cadmium (mg L−1)
0.246
0.254
—
0.2
Iron (mg L−1)
48.48
0.013
—
—
15.0
Lead (mg L−1)
0.031
0.028
—
0.5
Zinc (mg L−1)
5.00
5.00
—
5.0
Manganese (mg L−1)
3.120
2.940
—
1.0
Nickel (mg L−1)
0.39
0.32
—
2.0
aST: total solids, bSTV: fixed solids, and cSTV: total volatile solids.
*Standards for effluent release in water bodies (Article 18 CETESB CONAMA 357/05). (—): not specified.The actual process of degradation which occurred in the analysis of both DOC (81.0%) and COD (90.7%) is evident since in the marked reduction of the same after the photochemical treatment.The laws of the State of São Paulo and Federal government, in relation to water amd receiving waters, do not have a specific value of COD for effluents in receiving waters. We recommend the value of BOD < 60 mg L−1 or a reduction in the minimum efficiency of treatment processes at least 80%. In general, in both parameters (DOC and COD), treatments by photocatalysis homogeneous were effective.The ratio BOD5/COD parameter is commonly used to verify the biodegradability of the effluent. The effluent in natura, as a crude pollutant, had a BOD5/COD ratio of 0.25. This value indicates that the effluent presents high recalcitrance, making biological treatment impractical without a due pretreatment. The BOD5/COD ratio shows the effectiveness of oxidation in destroying certain organic loads. Biodegradability was evaluated as described by Jardim and Canela [16], noting that a BOD5/COD ratio of >0.4 is characteristic for biodegradable effluent. Hence, Table 3 shows a ratio result from AOP (photonic and Photo-Fenton) of 0.65, asserting that the photochemical treatment increased the biodegradability of the dairy effluent.The results of color and turbidity proved to be quite satisfactory in reducing 93.55% of color and 98.83% of turbidity.Table3 shows copper at concentrations 4 times higher than the allowed (1.0 mg L−1) as well as an increase in concentration after the photochemical treatment. This increase is due, possibly, to the use of cooling system of serpentine pipes made from copper. Leaching of this metal in systems with acid pH, as used in the photochemical process, is common in increasing the concentration of ionic copper.Phosphorus percentages were reduced from their high after photochemical treatment. In the analysis of treated effluent precipitates after alkalinization, phosphorous was at 98.11 mg L−1, possibly attributed to the formation of low-solubility phosphate compounds after oxidation concurrent with alkaline solubility at a lower value [17].Chlorides presented a 98% reduction. Precipitate analysis showed 967.80 mg L−1 of chloride in the effluent sample that can form insoluble chlorides in alkaline medium, in the presence of cations as Cu2+, Cd2+, and Pb2+ that could be present in the effluent.The ammonia-nitrogen and organic nitrogen also showed a reduced percentage with similar values of 99%. A possible gaseous oxidation of ammonia, a very stable form, could be the cause [18].The results of total and volatile solids presented a percentage reduction in the order of 50% and 64%, respectively.Cadmium and manganese showed values close to the allowed standard (2.0 and 0.2, resp.). Carbonate and bicarbonate ions were not analyzed because of a tendency to transform into CO2 and H2O at acidic pH levels. The Photo-Fenton process was used in an acid medium. It is well known that oxidative processes can only oxidize metallic ions to a less soluble form in relation to the reaction pH and consequently lead to a decrease in its respective concentrations.


### 3.2. Box-Behnken Matrix Results for Total Organic Carbon (TOC)

Table4 shows the results of percentile reduction of DOC obtained with the experimental conditions anticipated in the Box-Behnken matrix. Fifteen experiments with replicates were performed using three factors (pH, Fenton reagent, and UV) at a maintained temperature and reaction time.Table 4
Percentage reduction variations of the DOC as per factors and levels to the array of Box-Behnken array for Photo-Fenton-treated dairy effluent.
Exp.
pH
Fenton reagent
UV
Reduction
mH2O2 (g)
mFe2+ (g)
% DOC
1
3.0
32.5
2.6
0
61.6
2
3.0
32.5
2.6
0
58.7
3
3.5
32.5
2.6
15
60.0
4
3.0
30.0
2.1
15
61.1
5
3.5
35.0
3.6
28
80.9
6
3.5
32.5
2.6
15
61.8
7
3.0
32.5
2.6
28
74.0
8
3.5
35.0
3.6
28
78.4
9
3.0
35.0
3.6
15
68.3
10
3.5
30.0
2.1
0
68.2
11
3.5
32.5
2.6
15
63.6
12
3.5
32.5
2.6
15
66.1
13
4.0
32.5
2.6
0
59.7
14
3.5
32.5
2.6
15
61.5
15
3.0
30.0
2.1
15
59.8
16
3.5
35.0
3.6
0
68.3
17
4.0
30.0
2.1
15
57.6
18
3.0
35.0
3.6
15
69.5
19
3.5
30.0
2.1
0
67.6
20
4.0
30.0
2.1
15
60.0
21
3.0
32.5
2.6
28
73.0
22
4.0
35.0
3.6
15
64.0
23
3.5
30.0
2.1
28
75.6
24
3.5
30.0
2.1
28
76.3
25
3.5
35.0
3.6
0
67.9
26
4.0
32.5
2.6
28
62.1
27
3.5
32.5
2.6
15
65.5
28
4.0
35.0
3.6
15
62.3
29
4.0
32.5
2.6
28
61.0
30
4.0
32.5
2.6
0
55.0Generally, the results of Table4 ranged from 55 to 80% on average, depending on factor levels. Experiment 5 showed the highest percentage of DOC reduction at 80%, similarly reflected in the counterpart of experiment 8.The Box-Behnken matrix analysis by graphics of effects (Figure2) indicated that the Fenton reagent factor (m H2O2 + m Fe2+) and ultraviolet radiation strength must operate at maximum levels. Intermediate level (3.5) pH data indicated elevated effluent-degradation performance. These values are consistent with those described in the literature regarding data indicating the potentials in applying an oxidative process for dairy effluent treatment [8].Figure 2
Primary effects in relationship to mean responses (percentage reduction of DOC) of factors used in the treatment of dairy effluent as per the Box-Behnken matrix.As per the discussions of the Box-Behnken matrix effects, a pH in the range of 3.5 favors the Photo-Fenton process. A greater amount of Fenton reagent potentiated with UV radiation may produce improved kinetics for the formation of OH radicals and mineralized organic matter in the effluent and gives the highest percentage of reduced DOC. The adverse effect, which occurred with the intermediate concentration of Fenton reagent in percentile relation to reduction degradation, can be a function of a mass ratio where intermediate reactions of action reducing hydroxyl radicals were predominant, attributed to the antagonistic ratio between the quantity H2O2 and Fe2+. Systematic errors should be disregarded due to the results of the similar percentage reductions of DOC between the experiments and their replicas.Table5 shows the percentage of reduction for DOC, COD, and BOD5 and their relationships in each Photo-Fenton processes sample to the optimum experimental data in the Box-Behnken matrix.Table 5
Average percentage reductions of DOC, BOD5, and COD obtained in the treatment of dairy effluent by Photo-Fenton processes according to the Box-Behnken matrix for optimal experimental results (5).
Duration (min)
% Reduction DOC
% Reduction COD
% Reduction BOD5
Reduction
BOD5/COD
DOC/COD
0
0
0
0
—
—
10
46.20
52.74
49.47
0.938
0.876
20
56.29
61.04
58.36
0.956
0.922
30
72.42
75.46
71.34
0.945
0.959
40
74.12
76.97
75.11
0.976
0.963
50
77.23
80.10
77.60
0.969
0.964
60
80.08
80.55
79.25
0.984
1.020The increases in biodegradability occurring in AOP treatments are clearly seen in the DOC/COD relationship confirming the efficiency of photochemical treatment process.The resultant effects and interactions are obtained for the DOC parameter response under optimal interpretation using photocatalytic variance oxidation process, as shown in Table6.Table 6
Energy consumed in Photo-Fenton reactions data from Box-Behnken experiments at a volume of 3 L of dairy effluent and 60 min of reaction.
Operational steps
Variables levels
Equipment (kW h)
Thermostatic bath
Lamp reactor
pH meter
Centrifugal pump
Metering pump
Temperature control
1.16
Photonic irradiation
1
—
2
0.0138
3
0.0179
Control pH
—
0.00083
Flow reactor
—
0.0138
H2O2 dose
—
0.00292


### 3.3. AOP Degradation Rate

The percentages of DOC, COD, and BOD reduction were verified photochemicaly after the treatment at 81.0, 90.7, and 78.8%, respectively. The values in Table5 show the relations of BOD5/COD and DOC/COD, after AOP and chemical treatments with the reduction of BOD5 at 78.81%. This demonstrates that a majority of the organic load present in the dairy effluent was degraded by the photochemical processes, meaning a significant AOP contribution for the degradation of dairy effluent.Summary analysis of Table4 data shows a greater influence from photochemical pretreatment in the percentages of reduction for both concentrations of DOC proportional to those of COD and BOD5.


### 3.4. Economic Evaluation of Photo-Fenton Process

The economic evaluation (energy consumption and reagents) of the treatment process for dairy effluent, second Box-Behnken, was performed taking into consideration only the chemical process (Photo-Fenton), that is, omission of physical/chemical analyses.As detailed above, the Photo-Fenton process was performed using the energy consuming equipment: tubular photochemical reactor Germetec Model FPG-463/1 (nominal volume of 1 L and Hg lamp low-intensity irradiation GPH- 463T5L, emitting maximum radiation at 253.7 nm and power of 15 W and 28 W, protected by a quartz tube without causing dispersion), the Quimis Thermostatic Bath Model of Q214S (nominal volume of 10 L of H2O, with unit refrigeration with capacity of 3000 BTU/h and power of 2100 W at 220 V), the centrifugal pump of Bomax Model NH-30 PX-T (0.013 HP and 220/380 V), the metering pump from Hanna Instruments Model BL 1.5 (output 1.5 L/h and 13 bar, and 220/240 VAC at 50/60 Hz), and pH meter Hanna Instruments Model HI 2221 (output 500 m, 12 VDC, 220 V, and 50–60 Hz). The estimated value of energy used by this equipment was determined by experimental measuring using power/consumption meter from ICEL, Model ME-2500 (220 V and 60 Hz), with Certificate of Conformity no. 201111011512, as per Table 6. Energy and temperature controls for all experiments were initially calibrated to a water bath thermostat at 20°C, taking into consideration the time to reach working temperature.As per the data in Table6 (60 min duration), the temperature parameter is the highest energy consumption, requiring the highest value among the other variables (>95%). The second highest energy consumption is the low-intensity Hg lamp and centrifugal pump (approximately 1% to 2%). Thus, the process cost is significantly dependent on the value and respective control of temperature.The percentage of degradation was lower in previously performed formularies, that is, 3 L of dairy effluent, 100 g of H2O2, and 11.9 g Fe2+, adding these two reagents added in the course of the reaction, with control of 3 pH and without temperature control (only the effluent cooled to 20°C and in a still water bath). Percentage of degradation observed was lower. Hence, a temperature control is required.Values were also considered for an estimated consumption of the following reagents as Box-Behnken modeled experiments: H2SO4 (98% w/w), H2O2 (30% w/w), NaOH (98% w/w), and FeSO4·7H2O (98% w/w).Table7 shows the amount of reagents in the Box-Behnken model used in the dairy effluent treatment process for Photo-Fenton process.Table 7
Amount of reagents used in Photo-Fenton processes as Box-Behnken modeled experiments, considering the volume of 3 L of dairy effluent and a 60 min reaction duration.
Operational step
Variable levels
Reagents (g)
H2O2
FeSO4·7H2O
H2SO4
NaOH
Solubility of FeSO4·7H2O
1
11.55
2
14.30
3
19.80
Adjusted pH as per model
1
1.0
2
0.8
3
0.5
Photo-Fenton process
1
100.0
10.46
2
108.3
12.95
3
116.7
17.94
Controls/adjustments for pH during reactions
1
2.4
2
1.6
3
1.2To calculate the final consumption of energy and reagents in relation to a cost/benefit ratio (lower is better), each experiment conformed to the Box-Behnken model with optimal time profiles in 3 L of effluent in reduced DOC concentrations as shown above and in Table8.Table 8
Reagent energy consumption in 3 L of dairy effluent treated by the Photo-Fenton process with each experiment optimized for the Box-Behnken model.
Experiments
Energy consumption*US$/3 L
Reagent consumption**US$/3 L
Total value***US$/3 L
Average DOC reduction%
Relationship US$/%****(×1000)
1 and 2
0.157
0.202
0.359
60.10
5.973
3 and 6
0.131
0.188
0.319
60.90
5.231
4 and 15
0.158
0.191
0.543
60.50
8.920
5 and 8
0.159
0.226
0.385
79.50
4.843
7 and 21
0.133
0.200
0.333
73.00
4.562
9 and 18
0.158
0.218
0.376
68.00
5.530
10 and 19
0.104
0.190
0.294
67.60
4.350
11 and 12
0.132
0.204
0.336
65.10
5.160
13 and 30
0.157
0.204
0.361
60.00
6.020
14 and 27
0.106
0.204
0.310
63.00
4.921
16 and 25
0.131
0.226
0.357
68.00
5.250
17 and 20
0.158
0.190
0.348
58.80
5.920
22 and 28
0.105
0.226
0.331
63.00
5.254
23 and 24
0.133
0.190
0.323
76.00
4.250
26 and 29
0.133
0.204
0.337
61.00
5.524
*1 kW h = US$ 0.133; the third most expensive in Brazil—Brazil Business Portal.
**Quotation no. 212712 from Labsynth Products for Laboratories Ltd., October 23, 2011.
***US$ 1.00 = R$1.847; quote from UOL.
****Factors for further evaluation.Evaluation of the results in Table8 concluded that the best qualitative result corresponds to the highest cost/benefit ratio. This is exemplified in experiments 5 and 8 of Box-Behnken model that obtained 79.50% degradation of the concentration of DOC at a cost/benefit ratio of 11.02. Another relevant factor is that the cost of reagents was higher in relation to energy for all experiments.A separate analysis among several variables of the Photo-Fenton process and related cost/benefit provided two specific evaluations depending on the disposal of the treated effluent. According to national regulation, if the effluent is deposited immediately into rivers, the costs will differ from those of experiments 5 and 18, to present a revised cost/benefit ratio among intermediate experiments.Specifically, if the effluent is treated by Photo-Fenton after biological treatment (e.g., hybrid AOP-activated sludge), the UV variable should be evaluated carefully as the most expensive process. Treatment with UV light should be the least significant factor in the process. Thus, the experiments 23 and 24 should be highlighted as the most advantageous cost/benefit ratio (9.10), with the second best value obtained from the experiments of the Box-Behnken model with pH at intermediate level, reagent at a low level, UV radiation at high level, and a reduced concentration at 76% DOC.


## 3.1. Characterization of Raw Effluent

The characterization of dairy effluent was carried out according to the most relevant physicochemical aspects, such as pH, COD, BOD5, total phosphorus, ammonia-nitrogen and organic nitrogen, DOC, turbidity, color, total dissolved and fixed solids, settled solids, oils and greases, and the ratio of BOD5/COD.Table3 shows physical/chemical data for dairy effluent in natura and after the AOP and chemical treatment (precipitation in pH 8 and 9) standards as per Articles 18 and 34 of Brazilian Statute CETESB CONAMA 357/05 and values from respective references.Table 3
Results of physical/chemical analysesin naturaand posttreatment dairy effluents.
Parameters
Results
Data in the literature
References
Release standards* (mg L−1)
In Natura
After AOPs and precipitation
Aspect
Turbid
Clear
—
—
—
True color (Co Pt)
431.9
27.86
—
—
Absent
Turbidity (NTU)
1033
12.00
—
—
Absent
pH
6.0–6.4
8.0–8.50
5.25–8.0
[17, 19–21]
5–9
Odor
Pungent
Absent
—
—
—
COD (mg L−1 O2)
9000–10000
929.0–935.0
797–8000
[19–21]
—
BOD (mg L−1 O2)
2300–2500
508.5–515.8
1292–60000
[20]
60
BOD/COD
0.25
0.65
—
—
—
DOC (mg L−1)
1513–1800
336.2–356.1
2500–5000
[5, 20]
—
Phosphorus (mg L−1)
108.7
3.0
38.6–227.1
[17, 20]
—
NH3-N (mg L−1)
158.0
0.0027
0.25–57
[19]
20
Organic N (mg L−1)
179.9
0.0047
16.5–1048
[19, 20]
—
aST (mg L−1)
5680
2830.60
545–15720
—
—
bSTF (mg L−1)
986
880
119
—
cSTV (mg L−1)
4800
1746.0
426–10900
[19]
—
Phenol (mg L−1)
>0.005
>0.005
—
0.5
Oil and grease (mg L−1)
2002.5
0.000
4680
[22]
50
Chloride (mg L−1)
1301.75
27.0
—
—
—
Cyanide (mg L−1)
Absent
Absent
—
0.2
Copper (mg L−1)
1.39
7.8
—
1.0
Chromium (mg L−1)
Absent
Absent
—
0.1
Cadmium (mg L−1)
0.246
0.254
—
0.2
Iron (mg L−1)
48.48
0.013
—
—
15.0
Lead (mg L−1)
0.031
0.028
—
0.5
Zinc (mg L−1)
5.00
5.00
—
5.0
Manganese (mg L−1)
3.120
2.940
—
1.0
Nickel (mg L−1)
0.39
0.32
—
2.0
aST: total solids, bSTV: fixed solids, and cSTV: total volatile solids.
*Standards for effluent release in water bodies (Article 18 CETESB CONAMA 357/05). (—): not specified.The actual process of degradation which occurred in the analysis of both DOC (81.0%) and COD (90.7%) is evident since in the marked reduction of the same after the photochemical treatment.The laws of the State of São Paulo and Federal government, in relation to water amd receiving waters, do not have a specific value of COD for effluents in receiving waters. We recommend the value of BOD < 60 mg L−1 or a reduction in the minimum efficiency of treatment processes at least 80%. In general, in both parameters (DOC and COD), treatments by photocatalysis homogeneous were effective.The ratio BOD5/COD parameter is commonly used to verify the biodegradability of the effluent. The effluent in natura, as a crude pollutant, had a BOD5/COD ratio of 0.25. This value indicates that the effluent presents high recalcitrance, making biological treatment impractical without a due pretreatment. The BOD5/COD ratio shows the effectiveness of oxidation in destroying certain organic loads. Biodegradability was evaluated as described by Jardim and Canela [16], noting that a BOD5/COD ratio of >0.4 is characteristic for biodegradable effluent. Hence, Table 3 shows a ratio result from AOP (photonic and Photo-Fenton) of 0.65, asserting that the photochemical treatment increased the biodegradability of the dairy effluent.The results of color and turbidity proved to be quite satisfactory in reducing 93.55% of color and 98.83% of turbidity.Table3 shows copper at concentrations 4 times higher than the allowed (1.0 mg L−1) as well as an increase in concentration after the photochemical treatment. This increase is due, possibly, to the use of cooling system of serpentine pipes made from copper. Leaching of this metal in systems with acid pH, as used in the photochemical process, is common in increasing the concentration of ionic copper.Phosphorus percentages were reduced from their high after photochemical treatment. In the analysis of treated effluent precipitates after alkalinization, phosphorous was at 98.11 mg L−1, possibly attributed to the formation of low-solubility phosphate compounds after oxidation concurrent with alkaline solubility at a lower value [17].Chlorides presented a 98% reduction. Precipitate analysis showed 967.80 mg L−1 of chloride in the effluent sample that can form insoluble chlorides in alkaline medium, in the presence of cations as Cu2+, Cd2+, and Pb2+ that could be present in the effluent.The ammonia-nitrogen and organic nitrogen also showed a reduced percentage with similar values of 99%. A possible gaseous oxidation of ammonia, a very stable form, could be the cause [18].The results of total and volatile solids presented a percentage reduction in the order of 50% and 64%, respectively.Cadmium and manganese showed values close to the allowed standard (2.0 and 0.2, resp.). Carbonate and bicarbonate ions were not analyzed because of a tendency to transform into CO2 and H2O at acidic pH levels. The Photo-Fenton process was used in an acid medium. It is well known that oxidative processes can only oxidize metallic ions to a less soluble form in relation to the reaction pH and consequently lead to a decrease in its respective concentrations.


## 3.2. Box-Behnken Matrix Results for Total Organic Carbon (TOC)

Table4 shows the results of percentile reduction of DOC obtained with the experimental conditions anticipated in the Box-Behnken matrix. Fifteen experiments with replicates were performed using three factors (pH, Fenton reagent, and UV) at a maintained temperature and reaction time.Table 4
Percentage reduction variations of the DOC as per factors and levels to the array of Box-Behnken array for Photo-Fenton-treated dairy effluent.
Exp.
pH
Fenton reagent
UV
Reduction
mH2O2 (g)
mFe2+ (g)
% DOC
1
3.0
32.5
2.6
0
61.6
2
3.0
32.5
2.6
0
58.7
3
3.5
32.5
2.6
15
60.0
4
3.0
30.0
2.1
15
61.1
5
3.5
35.0
3.6
28
80.9
6
3.5
32.5
2.6
15
61.8
7
3.0
32.5
2.6
28
74.0
8
3.5
35.0
3.6
28
78.4
9
3.0
35.0
3.6
15
68.3
10
3.5
30.0
2.1
0
68.2
11
3.5
32.5
2.6
15
63.6
12
3.5
32.5
2.6
15
66.1
13
4.0
32.5
2.6
0
59.7
14
3.5
32.5
2.6
15
61.5
15
3.0
30.0
2.1
15
59.8
16
3.5
35.0
3.6
0
68.3
17
4.0
30.0
2.1
15
57.6
18
3.0
35.0
3.6
15
69.5
19
3.5
30.0
2.1
0
67.6
20
4.0
30.0
2.1
15
60.0
21
3.0
32.5
2.6
28
73.0
22
4.0
35.0
3.6
15
64.0
23
3.5
30.0
2.1
28
75.6
24
3.5
30.0
2.1
28
76.3
25
3.5
35.0
3.6
0
67.9
26
4.0
32.5
2.6
28
62.1
27
3.5
32.5
2.6
15
65.5
28
4.0
35.0
3.6
15
62.3
29
4.0
32.5
2.6
28
61.0
30
4.0
32.5
2.6
0
55.0Generally, the results of Table4 ranged from 55 to 80% on average, depending on factor levels. Experiment 5 showed the highest percentage of DOC reduction at 80%, similarly reflected in the counterpart of experiment 8.The Box-Behnken matrix analysis by graphics of effects (Figure2) indicated that the Fenton reagent factor (m H2O2 + m Fe2+) and ultraviolet radiation strength must operate at maximum levels. Intermediate level (3.5) pH data indicated elevated effluent-degradation performance. These values are consistent with those described in the literature regarding data indicating the potentials in applying an oxidative process for dairy effluent treatment [8].Figure 2
Primary effects in relationship to mean responses (percentage reduction of DOC) of factors used in the treatment of dairy effluent as per the Box-Behnken matrix.As per the discussions of the Box-Behnken matrix effects, a pH in the range of 3.5 favors the Photo-Fenton process. A greater amount of Fenton reagent potentiated with UV radiation may produce improved kinetics for the formation of OH radicals and mineralized organic matter in the effluent and gives the highest percentage of reduced DOC. The adverse effect, which occurred with the intermediate concentration of Fenton reagent in percentile relation to reduction degradation, can be a function of a mass ratio where intermediate reactions of action reducing hydroxyl radicals were predominant, attributed to the antagonistic ratio between the quantity H2O2 and Fe2+. Systematic errors should be disregarded due to the results of the similar percentage reductions of DOC between the experiments and their replicas.Table5 shows the percentage of reduction for DOC, COD, and BOD5 and their relationships in each Photo-Fenton processes sample to the optimum experimental data in the Box-Behnken matrix.Table 5
Average percentage reductions of DOC, BOD5, and COD obtained in the treatment of dairy effluent by Photo-Fenton processes according to the Box-Behnken matrix for optimal experimental results (5).
Duration (min)
% Reduction DOC
% Reduction COD
% Reduction BOD5
Reduction
BOD5/COD
DOC/COD
0
0
0
0
—
—
10
46.20
52.74
49.47
0.938
0.876
20
56.29
61.04
58.36
0.956
0.922
30
72.42
75.46
71.34
0.945
0.959
40
74.12
76.97
75.11
0.976
0.963
50
77.23
80.10
77.60
0.969
0.964
60
80.08
80.55
79.25
0.984
1.020The increases in biodegradability occurring in AOP treatments are clearly seen in the DOC/COD relationship confirming the efficiency of photochemical treatment process.The resultant effects and interactions are obtained for the DOC parameter response under optimal interpretation using photocatalytic variance oxidation process, as shown in Table6.Table 6
Energy consumed in Photo-Fenton reactions data from Box-Behnken experiments at a volume of 3 L of dairy effluent and 60 min of reaction.
Operational steps
Variables levels
Equipment (kW h)
Thermostatic bath
Lamp reactor
pH meter
Centrifugal pump
Metering pump
Temperature control
1.16
Photonic irradiation
1
—
2
0.0138
3
0.0179
Control pH
—
0.00083
Flow reactor
—
0.0138
H2O2 dose
—
0.00292


## 3.3. AOP Degradation Rate

The percentages of DOC, COD, and BOD reduction were verified photochemicaly after the treatment at 81.0, 90.7, and 78.8%, respectively. The values in Table5 show the relations of BOD5/COD and DOC/COD, after AOP and chemical treatments with the reduction of BOD5 at 78.81%. This demonstrates that a majority of the organic load present in the dairy effluent was degraded by the photochemical processes, meaning a significant AOP contribution for the degradation of dairy effluent.Summary analysis of Table4 data shows a greater influence from photochemical pretreatment in the percentages of reduction for both concentrations of DOC proportional to those of COD and BOD5.


## 3.4. Economic Evaluation of Photo-Fenton Process

The economic evaluation (energy consumption and reagents) of the treatment process for dairy effluent, second Box-Behnken, was performed taking into consideration only the chemical process (Photo-Fenton), that is, omission of physical/chemical analyses.As detailed above, the Photo-Fenton process was performed using the energy consuming equipment: tubular photochemical reactor Germetec Model FPG-463/1 (nominal volume of 1 L and Hg lamp low-intensity irradiation GPH- 463T5L, emitting maximum radiation at 253.7 nm and power of 15 W and 28 W, protected by a quartz tube without causing dispersion), the Quimis Thermostatic Bath Model of Q214S (nominal volume of 10 L of H2O, with unit refrigeration with capacity of 3000 BTU/h and power of 2100 W at 220 V), the centrifugal pump of Bomax Model NH-30 PX-T (0.013 HP and 220/380 V), the metering pump from Hanna Instruments Model BL 1.5 (output 1.5 L/h and 13 bar, and 220/240 VAC at 50/60 Hz), and pH meter Hanna Instruments Model HI 2221 (output 500 m, 12 VDC, 220 V, and 50–60 Hz). The estimated value of energy used by this equipment was determined by experimental measuring using power/consumption meter from ICEL, Model ME-2500 (220 V and 60 Hz), with Certificate of Conformity no. 201111011512, as per Table 6. Energy and temperature controls for all experiments were initially calibrated to a water bath thermostat at 20°C, taking into consideration the time to reach working temperature.As per the data in Table6 (60 min duration), the temperature parameter is the highest energy consumption, requiring the highest value among the other variables (>95%). The second highest energy consumption is the low-intensity Hg lamp and centrifugal pump (approximately 1% to 2%). Thus, the process cost is significantly dependent on the value and respective control of temperature.The percentage of degradation was lower in previously performed formularies, that is, 3 L of dairy effluent, 100 g of H2O2, and 11.9 g Fe2+, adding these two reagents added in the course of the reaction, with control of 3 pH and without temperature control (only the effluent cooled to 20°C and in a still water bath). Percentage of degradation observed was lower. Hence, a temperature control is required.Values were also considered for an estimated consumption of the following reagents as Box-Behnken modeled experiments: H2SO4 (98% w/w), H2O2 (30% w/w), NaOH (98% w/w), and FeSO4·7H2O (98% w/w).Table7 shows the amount of reagents in the Box-Behnken model used in the dairy effluent treatment process for Photo-Fenton process.Table 7
Amount of reagents used in Photo-Fenton processes as Box-Behnken modeled experiments, considering the volume of 3 L of dairy effluent and a 60 min reaction duration.
Operational step
Variable levels
Reagents (g)
H2O2
FeSO4·7H2O
H2SO4
NaOH
Solubility of FeSO4·7H2O
1
11.55
2
14.30
3
19.80
Adjusted pH as per model
1
1.0
2
0.8
3
0.5
Photo-Fenton process
1
100.0
10.46
2
108.3
12.95
3
116.7
17.94
Controls/adjustments for pH during reactions
1
2.4
2
1.6
3
1.2To calculate the final consumption of energy and reagents in relation to a cost/benefit ratio (lower is better), each experiment conformed to the Box-Behnken model with optimal time profiles in 3 L of effluent in reduced DOC concentrations as shown above and in Table8.Table 8
Reagent energy consumption in 3 L of dairy effluent treated by the Photo-Fenton process with each experiment optimized for the Box-Behnken model.
Experiments
Energy consumption*US$/3 L
Reagent consumption**US$/3 L
Total value***US$/3 L
Average DOC reduction%
Relationship US$/%****(×1000)
1 and 2
0.157
0.202
0.359
60.10
5.973
3 and 6
0.131
0.188
0.319
60.90
5.231
4 and 15
0.158
0.191
0.543
60.50
8.920
5 and 8
0.159
0.226
0.385
79.50
4.843
7 and 21
0.133
0.200
0.333
73.00
4.562
9 and 18
0.158
0.218
0.376
68.00
5.530
10 and 19
0.104
0.190
0.294
67.60
4.350
11 and 12
0.132
0.204
0.336
65.10
5.160
13 and 30
0.157
0.204
0.361
60.00
6.020
14 and 27
0.106
0.204
0.310
63.00
4.921
16 and 25
0.131
0.226
0.357
68.00
5.250
17 and 20
0.158
0.190
0.348
58.80
5.920
22 and 28
0.105
0.226
0.331
63.00
5.254
23 and 24
0.133
0.190
0.323
76.00
4.250
26 and 29
0.133
0.204
0.337
61.00
5.524
*1 kW h = US$ 0.133; the third most expensive in Brazil—Brazil Business Portal.
**Quotation no. 212712 from Labsynth Products for Laboratories Ltd., October 23, 2011.
***US$ 1.00 = R$1.847; quote from UOL.
****Factors for further evaluation.Evaluation of the results in Table8 concluded that the best qualitative result corresponds to the highest cost/benefit ratio. This is exemplified in experiments 5 and 8 of Box-Behnken model that obtained 79.50% degradation of the concentration of DOC at a cost/benefit ratio of 11.02. Another relevant factor is that the cost of reagents was higher in relation to energy for all experiments.A separate analysis among several variables of the Photo-Fenton process and related cost/benefit provided two specific evaluations depending on the disposal of the treated effluent. According to national regulation, if the effluent is deposited immediately into rivers, the costs will differ from those of experiments 5 and 18, to present a revised cost/benefit ratio among intermediate experiments.Specifically, if the effluent is treated by Photo-Fenton after biological treatment (e.g., hybrid AOP-activated sludge), the UV variable should be evaluated carefully as the most expensive process. Treatment with UV light should be the least significant factor in the process. Thus, the experiments 23 and 24 should be highlighted as the most advantageous cost/benefit ratio (9.10), with the second best value obtained from the experiments of the Box-Behnken model with pH at intermediate level, reagent at a low level, UV radiation at high level, and a reduced concentration at 76% DOC.


## 4. Conclusions

It was concluded that physical-chemical characterizations of the raw dairy effluent with the parameters N (158 mg L−1), phosphorus (108.7 mg L−1), BOD5 (2300 to 2500 mg L−1), COD (9000–10000 mg L−1), and DOC (1313 to 1663 mg L−1) with concentrations above legal limits indicated that dairy wastewater must be treated and made suitable for disposal. It was found that the degree of recalcitrant organic matter present in the dairy effluent at BOD5/COD < 0.25 complicates the conventional biological treatment, which may justify the use of AOPs in pretreatment or treatment. An experimental design and response surface Box-Behnken matrix obtained a percentage DOC-reduction index of 81% and COD of the order of 90.7% after the photochemical treatment. In the design, these factors showed significant effects in reducing DOC.Two aspects were addressed regarding the cost/benefit evaluation. First, if the effluent treated by AOP is released directly into surface waters (rivers), the variables and their levels of the process should be as follows: pH 3.5, 35.0 g H2O2/Fe2+ 3.6 g, and 28 W UV, obtaining a reduction in concentration of 79.5% DOC. If the posttreatment effluent undergoing Photo-Fenton process is subsequently treated biologically, optimal experimental data shows that the cost/benefit ratio should include the following variables and levels: pH 3.5, 30 g H2O2/Fe2+ 2.1 g, and UV irradiation at 28 W to achieve a reduction in concentration of 76% DOC.



---

*Source: 967534-2014-02-19.xml*