Waste to Wealth approach in sustainable waste management.

1. POTENTIAL USE OF PLANTAIN (MUSA
PARADISIACA) WASTES IN THE REMOVAL OF
LEAD AND CHROMIUM IN EFFLUENT FROM
BATTERY RECYCLING PLANT
ADEOLU ADEDOTUN T.

2. INTRODUCTION
•Heavy metals are pollutants of very high priority
concern in the scientific community because apart
from being non-biodegradable, they are toxic to the
entire ecosystem.
•The presence of heavy metals and other waste
pollutants can be traced majorly to urbanization
and industrialization.
•A variety of industries are responsible for the
discharge of heavy metals into the environment
through their waste water (Sridhar, 2005).

3. INTRODUCTION CONT’D
•Various methods have been applied in the
removal of heavy metals from water and waste
water such as precipitation, coagulation and
filtration, ionexchange, adsorption,
biomineralisation and phytoremediation.
•Adsorption technology is being used
extensively for the removal of heavy metals
from aqueous solutions because it is a cleaner,
more efficient and cheap technology.

4. INTRODUCTION CONT’D
•Some of the low cost agricultural wastes which
are generated in large quantities and difficult to
dispose, have proved very effective in the
adsorption of heavy metals in water/polluted
water
•Plantain (Musa paradisiaca) wastes, which are
easily available, could be used to produce
resource materials such as activated carbon that
are of public health importance.

5. PROBLEM STATEMENT
 Water pollution is a major problem in the global
context. It is the leading worldwide cause of deaths
and diseases, and that it accounts for the deaths of
more than 14,000 people daily (Singleton, 1999).
 Industrial effluent often contains heavy metals
which bio-accumulate and persist in the
environment and thereby constitutes serious health
problems.
 Plantain wastes also constitute nuisance to the
environment particularly in the market. They
produced pungent odour when rotten which are
harmful to the health of the society.
27/09/16
5

6. OBJECTIVES OF THE STUDY
•To assess the use of plantain wastes for the
removal of lead and chromium in effluent from
battery recycling plant.
27/09/16
6

7. METHODOLOGY
 Study Area
• The study was carried out at Acid-Lead battery
recycling plant in Ogunpa in Ibadan North-West
Local Government, Oyo State. The plant deals
with recycling of acid-lead battery from vehicles.
 Study Design
• This study was experimental and laboratory
based.
27/09/16
7

8. SAMPLES COLLECTION
 Effluent
• Effluent was collected from the point of
discharge into Ogunpa river into a 5 litre plastic
bottle from Acid-Lead battery recycling plant,
Ogunpa, Ibadan North-West Local Government,
Oyo State.
• Material used for sample collection was pre-
treated by washing with dilute hydrochloric acid
and later rinsed with distilled water.
• At the collection point, container was rinsed,
and then filled with sample and taken to the
laboratory for treatment and analysis.
27/09/16
8

9. SAMPLES COLLECTION CONTD
 Plantain Wastes
 Ripe peel and plantain stalk were collected in
market within Ibadan in Oyo State.
 The plantain wastes were washed with distilled
water and sun dried for 168 hours and then oven
dried at 450
C to constant weight.
 The samples were ground, sieved and, stored in
polythene container for analysis and treatment
of effluents.
27/09/16
9

10. METHODOLOGY CONT’D
 Effluent
• Physico-chemical characteristics of the effluent
were determined according to standard methods
described by the American Public Health
Association (1998).
• pH, Temperature, Conductivity, Turbidity, Total
Dissolved Solids,
• heavy metals (Lead and Chromium)
27/09/16
10

11. METHODOLOGY CONT’D
 Procedure for Carbonization and Activation
• The plantain wastes were carbonized and activated by
two steps method according to Salami and Adekola,
(2002).
• 50.00g of raw ground each plantain waste sample was
weighed into pre-weighed crucibles and placed in an
Muffle furnace at 400o
C for 1hr under a closed system
and then cooled to room temperature.
• The charcoal was subjected to H3PO4 activation. The
charcoal was agitated in H3PO4. After the agitation, the
pre-carbonized charcoal slurry was left overnight at
room temperature and, then, dried at 110o
C for 24hr.
27/09/16
11

12. METHODOLOGY CONT’D
 The samples were activated in a closed system.
Consequently, the samples were heated to
optimize temperatures of 400o
C and maintained at
a constant temperature for 1hr before cooling.
 After cooling down, the activated charcoal was
washed successively several times with distilled
water to remove the excess activating agents and
other impurities.
27/09/16
12

13. METHODOLOGY CONT’D
400°C, 1hr
Raw ground plantain wastes C (s) + CO2
Δ
AA, 400°C, 1hr
Carbonized plantain wastes AC + CO2
Δ
Where AA represent Activating agents and AC
represent Activated Carbon

14. TREATMENT DETAILS
Treatment Details
PAC Ripe Peel Activated Carbon
SAC Fruit Stalk Activated
Carbon
CAC Commercial Activated
Carbon (Control)
27/09/16
14

15. PLATE: SHOWING THE PREPARED
ACTIVATED CARBON
15

16. ADSORPTION ISOTHERMS
 Effect of pH
• 50cm3
of effluent was measured into each 250cm3
conical
flask at adjusted pH of 2, 4, 6, 8, 10 and 12. The
desired pH was maintained using conc. NaOH to
adjust the pH.
• 1.0g of each activated carbon was added into each
flask and agitated intermittently for the desired time
periods. The mixture was shaken thoroughly at
200rpm with an electric shaker for 90 minutes.
• The suspension adsorbent was filtered through
Whatman No 1 filter paper. Initial and final
concentrations of tested heavy metals were determined
by atomic absorption spectroscopy (AAS).
27/09/16
16

17. ADSORPTION ISOTHERMS
Effect of adsorbent doses
• 50cm3
of effluent was measured into each 250cm3
conical flask at pH of 2 (Unadjusted pH).
•A known amount of activated carbon 0.1, 0.5, 1.0,
1.5 and 2.0g each activated carbon was added into
each flask and agitated intermittently for the
desired time periods.
• The mixture was shaken thoroughly at 200rpm
with an electric shaker for optimum contact time.
27/09/16
17

18. ADSORPTION ISOTHERMS
 Effect of initial ion concentration
• The stock solution of 1000mg/l each of the
standardized Pb2+
and Cd2+
were prepared from their
chlorides using effluent sample. The solutions were
adjusted to pH 10 with 0.1M NaOH.
• Batch sorption experiments were performed in which
50cm3
of effluent was measured into each 250cm3
conical flask and 1.0g of the adsorbent was added into
each flask and agitated intermittently for the desired
time periods.
• The mixture was shaken thoroughly at 200rpm with
an electric shaker for 150minutes.
27/09/16
18

19. ADSORPTION ISOTHERMS
• The amount of metal ion adsorbed during the
series of batch investigations was determined
using a mass balance equation:
Qe = (Cv – Cf) x V
M
• The definition of removal efficiency is as follows:
Removal efficiency (%) = (Cv x Cf) x 100
Cv
• Where Q is the metal uptake (mg/g); Cv and Cf are
the initial and final metal equilibrium
concentration in the effluent sample (mg/l)
respectively, M is the mass of the adsorbent (g)
and V is the volume of the effluent sample (l).
27/09/16
19

20. DATA MANAGEMENT
 Data Analysis
 Data were inputed and analysed using SPSS
software version 16.
 Descriptive, paired t-test and analysis of variance
(ANOVA) was used.
27/09/16
20

21. RESULTS
PARAMETERS UNIT VALUE NESREA
pH 2.0 ± 0.15 6-9
Tempt 0
C 30.0 ± 1.53 <40
Total Dissolved Solid mg/l 895.0 ± 0.00 2000
Conductivity μScm-3
2164.7 ± 0.58 1000
Lead (Pb) mg/l 31.25 ± 0.00 0.01
Chromium (Cr) mg/l 13.06 ± 0.00 0.01
27/09/16
21
The physico-chemical characteristic of the effluent

22. RESULTS
Parameter Unit PAC SAC CAC
Ash % 5.0 ± 0.01 6.2 ± 0.01 5.4 ± 0.01
Porosity kg/m3 0.6 ± 0.01 0.7 ± 0.01 0.8 ± 0.01
Bulk density kg/m3
0.8 ± 0.01 0.8 ± 0.01 0.8 ± 0.01
Surface area m2
/g 524.7 ± 0.01 530.7 ± 0.01 200.4 ± 0.01
Carboxylic 0.1 ± 0.01 0.1 ± 0.01 0.1 ± 0.01
Phenolic 0.3 ± 0.01 0.3 ± 0.01 0.3 ± 0.01
Lactones 0.5 ± 0.01 0.6 ± 0.01 0.6 ± 0.01
Basic 0.6± 0.02 0.6± 0.01 0.5± 0.01
27/09/16
22
Characteristics of prepared activated carbon

23. PERCENTAGE REMOVAL OF
LEAD
27/09/16
23

24. THE AMOUNT ADSORBED OF LEAD
BY PH
27/09/16
24

25. PERCENTAGE REMOVAL OF
CHROMIUM
27/09/16
25

26. THE AMOUNT ADSORBED OF
CHROMIUM BY PH
27/09/16
26

27. PERCENTAGE REMOVAL OF LEAD
FOR ADSORBENT DOSE
27/09/16
27

28. THE AMOUNT ADSORBED OF LEAD BY
ADSORBENT DOSE
27/09/16
28

29. PERCENTAGE REMOVAL OF CHROMIUM FOR
ADSORBENT DOSE
27/09/16
29

30. THE AMOUNT ADSORBED OF CHROMIUM
BY ADSORBENT DOSE
27/09/16
30

31. DISCUSSION
• The mean pH value of the effluent indicated that the
effluent was highly acidic than pH 6-9 of NESREA
recommended limits for battery factory effluents. Low
pH value impaired recreational uses of water and
affect aquatic life.
• The mean conductivity value of the effluent is very
high. It increase the salinity of the receiving river,
which may result in adverse ecological effects on the
aquatic biota. High salt concentrations hold potential
health hazards (Fried, 1991).
• Lead is a suspected pollutant in a battery recycling
effluent because is a major raw material in the
manufacture of lead acid accumulated batteries. Lead
at very low concentration is toxic and hazardous to
most forms of life (USEPA, 1986).
27/09/16
31

32. DISCUSSION
•Ash content affected activated carbon by reducing the
overall activity of activated carbon. The lower the ash
value therefore the better the activated carbon for use as
adsorbent.
•pH is an important parameter for adsorption of metal
ions because it affects the solubility of the metal ions,
concentration of the counter ions on the functional
groups of the adsorbent and the degree of ionisation of
the adsorbate during reaction (Badmus et al, 2007).
•Increasing pH from 2 to 10, there was a corresponding
increase in deprotonation of the adsorbent surface,
leading to a decrease in H+
ion on the adsorbent surface.
This creates more negative charges on the adsorbent
surface, which favours adsorption of positively charge
species and the positive sites on the adsorbent surface .
27/09/16
32

33. DISCUSSION
• The increased percentage adsorption by
adsorbent was as a result of increased surface
area and increased adsorption site occasioned
by increased adsorbent dose.
• The observed decrease in adsorption capacity
is due to change in the solid-liquid ratio which
resulted in this trend since amount adsorbed,
qe, has an inverse proportionality function to
weight of biosorbent.
27/09/16
33

34. CONCLUSION
• Treatment of industrial effluent with plantain
wastes activated carbon should be encouraged in
battery recycling plant so as to reduce its menace in
the environment and enhance effective waste
management.
•Converting the plantain wastes into resource
materials which is useful to the communities and
industries are affordable, available and accessible.
27/09/16
34

35. THANK YOU FOR
LISTENING