Marine Algae Biomass for Removal of Heavy Metal Ions 25.3 Experimental Methodology 617
Part D | 25.3
t b
1
B
A
c/c 0
A
B
Loading-0
0
t s
Time for biosorption step
Fig. 25.2 Schematic representation of the breakthrough
curves for the biosorption processes in dynamic continuous-flow conditions
tration). The saturation time (t s ) and volume (V s ) are
the time and volume at saturation point, and were
selected as the time and volume when the effluent concentration achieved a constant value around 0:95 c 0
(where c 0 is the initial concentration of the heavy
metal ion), although the biosorbent bed was not fully
saturated.
The efficiency in the overall use of the biosorbent
mixture in the column is indicated by the mass transTable 25.3 Some utilizations of marine algae biomass for the removal of heavy metal ions from aqueous solutions, by
dynamic continuous technique
Marine algae
Biosorbent bed
Heavy metal ions
References
Symphoricarpus albus Biomass bed
Pb(II)
[25.67]
Caulerpa lentillifera
Biomass bed
Cu(II), Cd(II), Pb(II)
[25.32]
Sargassum sp.
Biomass bed
Cu(II), Cd(II), Pb(II), Zn(II), Ni(II), Fe(III) [25.66, 68–72]
Gelidium sp.
Biomass bed
Pb(II), Cu(II), Cr(III)
[25.73, 74]
Ulva reticulata
Biomass bed
Cu(II), Co(II), Ni(II), Zn(II)
[25.75, 76]
Posidonia oceanica
Biomass bed
Cu(II)
[25.77]
Sargassum baccularia immobilized onto polyvinyl alcohol (PVA)
gel beads
Cu(II)
[25.78]
Laminaria japonica
Biomass gel
Re(VI)
[25.79]
Gelidium sp.
Algae waste from the agar extraction
process immobilized with polyacrylonitrile
Pb(II), Cu(II), Cr(III)
[25.73, 74]
Ulva lactuca
Agar matrix
Cu(II), Zn(II),Cd(II), Pb(II)
[25.80]
Ulva lactuca
Mixture: algae waste:
Purolite A-100 D 1 W 2
Pb(II)
[25.81]
fer zone (MTZ), which is defined as the length of the
biosorption zone in the column, and can be calculated
by using the following equation:
MTZ D H
.t s t b /
t s
(25.3)
where MTZ is the length of the mass transfer zone
(cm); H is the length of the biosorbent bed (cm); t b
is the time required to reach the breakthrough point
(min); and t s is the time required to reach the saturation
point (min).
The longer the mass transfer zone, the more biosorbent is not fully utilized at the end of the biosorption
process. So, for the process to be economical it is important to minimize the length of the transfer zone and
increase, thus, biosorbent utilization.
Practically, the dynamic continuous-flow biosorption is accomplished by using batteries of multiple columns that work in parallel and/or in series, to optimize the performance of the process.
Some examples of using marine algae biomass in
continuous-flow biosorption systems are presented in
Table 25.3.
Generally, the smaller the biosorbent particles,
the more difficult is the passing of aqueous solution
through the column. However, the small dimension
of biosorbent particles makes the metal uptake process to be more effective and rapid. When, the particles of biosorbent from the packed bed are larger,
aqueous solution of metal ions can pass through
the column easily, but the efficiency of biosorption
Part D | 25.3
t b
1
B
A
c/c 0
A
B
Loading-0
0
t s
Time for biosorption step
Fig. 25.2 Schematic representation of the breakthrough
curves for the biosorption processes in dynamic continuous-flow conditions
tration). The saturation time (t s ) and volume (V s ) are
the time and volume at saturation point, and were
selected as the time and volume when the effluent concentration achieved a constant value around 0:95 c 0
(where c 0 is the initial concentration of the heavy
metal ion), although the biosorbent bed was not fully
saturated.
The efficiency in the overall use of the biosorbent
mixture in the column is indicated by the mass transTable 25.3 Some utilizations of marine algae biomass for the removal of heavy metal ions from aqueous solutions, by
dynamic continuous technique
Marine algae
Biosorbent bed
Heavy metal ions
References
Symphoricarpus albus Biomass bed
Pb(II)
[25.67]
Caulerpa lentillifera
Biomass bed
Cu(II), Cd(II), Pb(II)
[25.32]
Sargassum sp.
Biomass bed
Cu(II), Cd(II), Pb(II), Zn(II), Ni(II), Fe(III) [25.66, 68–72]
Gelidium sp.
Biomass bed
Pb(II), Cu(II), Cr(III)
[25.73, 74]
Ulva reticulata
Biomass bed
Cu(II), Co(II), Ni(II), Zn(II)
[25.75, 76]
Posidonia oceanica
Biomass bed
Cu(II)
[25.77]
Sargassum baccularia immobilized onto polyvinyl alcohol (PVA)
gel beads
Cu(II)
[25.78]
Laminaria japonica
Biomass gel
Re(VI)
[25.79]
Gelidium sp.
Algae waste from the agar extraction
process immobilized with polyacrylonitrile
Pb(II), Cu(II), Cr(III)
[25.73, 74]
Ulva lactuca
Agar matrix
Cu(II), Zn(II),Cd(II), Pb(II)
[25.80]
Ulva lactuca
Mixture: algae waste:
Purolite A-100 D 1 W 2
Pb(II)
[25.81]
fer zone (MTZ), which is defined as the length of the
biosorption zone in the column, and can be calculated
by using the following equation:
MTZ D H
.t s t b /
t s
(25.3)
where MTZ is the length of the mass transfer zone
(cm); H is the length of the biosorbent bed (cm); t b
is the time required to reach the breakthrough point
(min); and t s is the time required to reach the saturation
point (min).
The longer the mass transfer zone, the more biosorbent is not fully utilized at the end of the biosorption
process. So, for the process to be economical it is important to minimize the length of the transfer zone and
increase, thus, biosorbent utilization.
Practically, the dynamic continuous-flow biosorption is accomplished by using batteries of multiple columns that work in parallel and/or in series, to optimize the performance of the process.
Some examples of using marine algae biomass in
continuous-flow biosorption systems are presented in
Table 25.3.
Generally, the smaller the biosorbent particles,
the more difficult is the passing of aqueous solution
through the column. However, the small dimension
of biosorbent particles makes the metal uptake process to be more effective and rapid. When, the particles of biosorbent from the packed bed are larger,
aqueous solution of metal ions can pass through
the column easily, but the efficiency of biosorption