A novel fluidized-bed-optical-fibers photocatalytic reactor (FBOFPR) and its performance

Article abstract of DOI:10.1016/j.apcata.2013.11.044

The key in designing a photocatalytic reactor lies in resolving the problems of mass transfer, light transmission and light scattering. Especially, the light scattering of catalyst is very acute, which makes the accurate quantification of light irradiation difficult. In this study, a novel fluidized-bed-optical-fibers photocatalytic reactor (FBOFPR) with easy quantification of light irradiation was designed by combining fluidized-bed photocatalytic reactor with optical-fiber light source that its optical fibers were fixed by an aluminum fixed jacket for UV total reflection, and its performance was tested by using trichloroethylene (TCE) as a target pollutant. The results show that, under the condition of water vapor content at 0.25%, oxygen content at 20.8%, initial concentration of TCE at 303.32 ppm, input light amount at 3.07 × 10¹⁷ s^-1 and residence time at 1.6 s, the apparent photon quantum efficiency is 26.31%, the turnover frequency is 12.44 μmol/(g TiO₂ min) and the removal efficiency is 86.66%. Compared with the conventional flat plate fluidized-bed photocatalytic reactor, FBOFPR exhibits many advantages in the aspect of effective use of photon, sufficient exertion of catalyst activity, effective removal of TCE and easy quantification of light irradiation.

Full text of DOI:10.1016/j.apcata.2013.11.044

Applied Catalysis A: General 471 (2014) 136–141
Contents lists available at ScienceDirect
Applied Catalysis A: General
journal homepage: www.elsevier.com/locate/apcata
A novel fluidized-bed-optical-fibers photocatalytic reactor (FBOFPR)
and its performance
Rongshu Zhua,b,c, Sainan Chea,b,c, Xianbo Liua,b,c, Songxue Lina,b,c
,
a,b,c
a,b,c,∗
Guilin Xu
, Feng Ouyang
a
Environmental Science and Engineering Research Center Harbin Institute of Technology Shenzhen Graduate School, Shenzhen 518055, Guangdong,
PR China
b
Shenzhen Key Laboratory of Water Resource Utilization and Environmental Pollution Control, Shenzhen 518055, Guangdong, PR China
c
Public Platform for Technological Service in Urban Waste Reuse and Energy Regeneration, Shenzhen 518055, Guangdong, PR China
a r t i c l e i n f o
a b s t r a c t
Article history:
Received 27 July 2013
Received in revised form
The key in designing a photocatalytic reactor lies in resolving the problems of mass transfer, light trans-
mission and light scattering. Especially, the light scattering of catalyst is very acute, which makes the
accurate quantification of light irradiation difficult. In this study, a novel fluidized-bed-optical-fibers
photocatalytic reactor (FBOFPR) with easy quantification of light irradiation was designed by combining
fluidized-bed photocatalytic reactor with optical-fiber light source that its optical fibers were fixed by an
aluminum fixed jacket for UV total reflection, and its performance was tested by using trichloroethylene
2
4 November 2013
Accepted 30 November 2013
Available online 7 December 2013
(
TCE) as a target pollutant. The results show that, under the condition of water vapor content at 0.25%,
Keywords:
17
−1
oxygen content at 20.8%, initial concentration of TCE at 303.32 ppm, input light amount at 3.07 × 10
s
Fluidized-bed-optical-fibers photocatalytic
reactor
TiO2
TCE
Apparent photon quantum efficiency
Turnover frequency
and residence time at 1.6 s, the apparent photon quantum efficiency is 26.31%, the turnover frequency is
12.44 ␮mol/(g TiO2 min) and the removal efficiency is 86.66%. Compared with the conventional flat plate
fluidized-bed photocatalytic reactor, FBOFPR exhibits many advantages in the aspect of effective use of
photon, sufficient exertion of catalyst activity, effective removal of TCE and easy quantification of light
irradiation.
©
2013 Elsevier B.V. All rights reserved.
1
. Introduction
Optical fiber has a capacity to transmit light. Using the side of
optical fiber to supply the light to the surface of photocatalyst was
first proposed by Ollis and Marinangeli [4,5]. Hofstadler et al. [6]
The photocatalytic reaction occurs on the light irradiated sur-
face of photocatalyst, which means that a reactant must be in
contact with the light irradiated surface of the photocatalyst to
complete a photocatalytic reaction. This feature determines that
the conventional fixed-bed photocatalytic reactor has no high pho-
tocatalytic efficiency due to the limitation of mass transport and
light transmission during the process of reaction. The fluidized-
bed photocatalytic reactor has high photocatalytic efficiency due
to its highly efficient mass transfer and favorable light irradiation.
However, the conventional fluidized-bed photocatalytic reactor
generally exists the problems that interior light source occupies
most of the volume of the reactor [1] or outer light source decreases
light utilization efficiency [2]. In addition, the accurate quantifica-
tion of light irradiation is difficult in these reactors [3].
designed the TiO -coated quartz optical fiber reactor (OFR) and
2
proved the feasibility through photocatalytic degradation of 4-CP.
After that, many groups [7–15] used optical fibers to supply light for
photocatalytic reactor. However, the light intensity from the side of
optical fiber decreases exponentially with the increase of the fibers
length [12] and whether the light can refract to the surface of TiO2
is affected by coating technology [10].
The optical fibers can not only achieve long distance transmis-
sion of the light but also realize arbitrary distribution of the light.
Using the end of optical fibers to supply light for photocatalytic
reactor, it can irradiate the light directly on TiO surface for reaction
2
as well as distribute the light uniformly, which will overcome the
shortage of using the side of optical fiber to supply light. In addition,
the output of light irradiation from the end of optical fiber is easy
to quantify and the aluminum fixed jacket of optical fibers for UV
total reflection can avoid the loss of scattering of light. However, it is
little reported that combining fluidized-bed photocatalytic reactor
with the end of optical fibers to supply light.
∗ Corresponding author at: Environmental Science and Engineering Research Cen-
ter Harbin Institute of Technology Shenzhen Graduate School, Shenzhen 518055,
Guangdong, PR China. Tel.: +86 755 26033472; fax: +86 755 26033472.
E-mail address: ouyangfh@hit.edu.cn (F. Ouyang).
In this study, a fluidized-bed-optical-fibers photocatalytic reac-
tor (FBOFPR) was designed by using the aluminum fixed jacket of
0
926-860X/$ – see front matter © 2013 Elsevier B.V. All rights reserved.
http://dx.doi.org/10.1016/j.apcata.2013.11.044

R. Zhu et al. / Applied Catalysis A: General 471 (2014) 136–141
137
deionized water, added 0.675 mL fuming sulfuric acid, then diluted
to 250 mL, achieved 0.006 mol/L K Fe(C O ) solution. (2) The
3
2
4 3
preparation of buffer solution: dissolved 80 g ammonium acetate
into 100 mL glacial acetic acid, then diluted to 200 mL. (3) The
preparation of chromogenic agent: dissolved 0.5 g phenanthroline
into deionized water, droped muriatic acid as an auxiliary agent,
then diluted to 100 mL. (4) The measurement of the amount
of light emitted from the optical fibers: took 20 mL photolysis
liquid, located at 10 mm away from the end of the optical fibers,
irradiated 1 min, 5 min, 10 min, 20 min, respectively, then got 1 mL
photolysis liquid to colorimetric tube with stopper, added 5 mL
buffer solution, 2 mL chromogenic agent and diluted to 50 mL,
Fig. 1. Schematic diagram of FBOFPR.
2+
maintained 5–10 min, the light absorption of Fe was measured
at 510 nm, where the concentration of Fe2+ in photolysis liquid
could be obtained from the standard curve. Plotting with time as
optical fibers for UV total reflection to avoid the loss of scattering of
light, using the end of optical fibers to supply light and combining
the fluidized-bed photocatalytic technique. And its performances
were studied by using TCE as removal object.
2+
an abscissa and concentration of Fe as an ordinate, the slope
d[Fe2+]/dt obtained. (5) The calculation of the amount of light
emitted from the optical fibers: the light absorption of photolysis
liquid per volume could be calculated through Eq. (1), where I is
the amount of light irradiation, N is Avogadro’s constant and is
2
. FBOFPR
A
23
6
.022 × 10 , Vp is the volume of photolysis liquid and is 0.02 L, ˚ is
luminous flux and is 1.26 at the wavelength of 365 nm. According
to this measurement and calculation method, the total amount of
light irradiation (Itotal) in present reactor is 3.07 × 10
Fig. 1 shows the schematic diagram of FBOFPR. The photocat-
alytic reactor contains fluidized-bed, fixed jacket of optical fibers
and light source to optical fibers. The fluidized-bed is composed
of gas inlet segment, fluidizing segment, separation segment and
gas outlet segment. Each segment is made of quartz glass (Jinda
Quartz Glass Company, Jinzhou China, UV light transmittance is
more than 98%) except that the gas inlet segment is stainless steel.
The parameters of the fluidized-bed are listed in Table 1. The fixed
jacket of optical fibers is columniform and its material is UV total
reflective aluminum plate. The diameter of the columniform fixed
jackets is 34 mm and their thickness is 1 mm. The circumferential
surface of the fixed jackets is fixed 8 optical fibers equidistantly
and the longitudinal space of the fibers is 3.4 mm. In order to con-
trast to the aluminum fixed jacket for UV total reflection, the fixed
jacket was also made by rubber sheet. The light source to optical
fibers is provided by UV spot light source (L8333-01, Hamamatsu,
Japan) and transported through the optical fiber (A4094-01, Hama-
matsu, Japan) to fluidized-bed. The UV lamp (L8251, Hamamatsu,
Japan) can give wavelength range of the light in 280–400 nm after
filtered by optical filter (A7028-03, Hamamatsu, Japan) and its main
wavelength is 365 nm.
1
7
−1
s .
2
+
I = NA × Vp × d[Fe
]/dt
(1)
˚
3.2. Preparation of catalyst
The photocatalyst used in the experiment was prepared through
direct coating method [18]. Weighed a certain amount of TiO2
nanoparticles (Degussa P25, ca. 75% anatase and 25% rutile, aver-
2
−1
age particle size, ca. 21 nm, BET area, ca. 50 ± 15 m g ), added to
a certain amount of deionized water, oscillated for 0.5 h by ultra-
sonic and so as to form uniform TiO2 suspensions, and adjusted its
pH to 5.5 with dilute ammonia. Weighed SiO2 (Qingdao Haiyang
2
−1
Chemical Co., Ltd., 0.125–0.425 mm, 460 m g ) accordance with
the mass ratio at 10% between TiO and TiO /SiO , poured the SiO
2
2
2
2
into the TiO2 suspension and ultrasound for 3 h. After placed for
◦
2
3
4 h at room temperature and dried for 12 h at 110 C, calcined for
◦
h at 200 C using tube furnace. After sieving the catalyst, selected
the desired particles for experiment.
3
. Experimental
3.3. Testing the performance of the reactor
3.1. Measurement of light irradiation
Used glass beads of diameter of 0.250–0.425 mm as gas distri-
The amount of light emitted from the optical fibers was mea-
sured by using the method of potassium ferrioxalate actinometry
16,17]. The process included five steps: (1) The preparation
bution plate. Put quartz wool about 10 mm high under the glass
beads to support the glass beads and the catalysts to prevent them
leaking to the gas line.
[
of photolysis liquid: dissolved 0.7369 g K Fe(C O ) ·3H O into
3
2
4
3
2
The reaction gas was composed of TCE, O , water vapor and N .
2
2
N2 acted as balance gas. N2 and O2 were provided by gas cylin-
der. TCE and water vapor were prepared by bubbling method [19].
After the reaction gas was mixed in mixing tube, the mixture gas
flowed into the photocatalytic reactor at a flow rate of 106 mL/min.
Table 1
Parameters of fluidized-bed.
Parameters
Size (mm)
Weighed 1.0 g catalyst (contained 0.1 g TiO ) and placed in the reac-
Outer diameter of the gas inlet segment
Inner diameter of the fluidizing segment
Height of fluidizing segment
Curvature radius of separating segment (down)
Height of separating segment (down)
Inner diameter of separating segment (middle)
Height of separating segment (middle)
Curvature radius of separating segment (up)
Height of separating segment (up)
2
10
250
1195
100
16
16
18
10
10
2
tion tube, and the height of the fluidized bed was 36 mm after
uniformly fluidizing (the reaction residence time of 1.6 s). After
reached gas–solid adsorption equilibrium (identified as 5 h by equi-
librium experiment), turned on the light and began the degradation
experiments. The concentration of TCE was measured on line by gas
chromatograph (SP-6890, Rainbow Chemical Instrument Co., Ltd.,
China) equipped with capillary column (50 m × 0.25 mm × 0.5 ␮m)
and FID detector. The concentration of CO and CO2 were measured
on line by gas chromatograph (GC-112A, Precision and Scientific
Inner diameter of the gas outlet segment
Height of the gas outlet segment
50

1
38
R. Zhu et al. / Applied Catalysis A: General 471 (2014) 136–141
Instrument Co., Ltd., China) equipped with column (Propark-Q,
8
0–100 mesh, 3 mm × 0.5 mm × 2.5 m) and FID detector.
The performance of the FBOFPR was evaluated by three parame-
ters: apparent photon quantum efficiency Y (%), turnover frequency
f (␮mol/(g TiO min)) and removal efficiency ꢀ (%).
2
3.3.1. Apparent photon quantum efficiency (Y)
Y is used to evaluate the light utilization efficiency of the reac-
tor, which is defined as the percentage between the photons for
the photocatalytic reaction and the total number of input photons,
also called quantum yield [20]. According to the measured irradia-
tion of UV light emitted from the end of the optical fiber to calculate
the total number of input photons unit time into the photocatalytic
reactor, which assumes that the input photons are absorbed com-
pletely. Because the valence state of carbon element in the organic
compound is zero, it requires four photons to generate +4 valence
state of CO2 and two photons to generate +2 valence state of CO.
Therefore, Y can be obtained through the ratio between the photons
absorbed by CO2 and CO generated per unit time and the amount
of the light irradiation, and the formula for Y can be written as Eq.
Fig. 2. The degradation of TCE. Reaction conditions: initial concentration of TCE:
1
51.66 ppm; water vapor content: 0.25%; oxygen content: 20.8%; total amount of
17 −1
; material of fixed jacket: rubber.
the light irradiation: 3.07 × 10
s
(
2) [21–23]. Where VCO2 and VCO are the generated volume fraction
of CO2 and CO, respectively, in the steady process and their units
are ppm, Q is the flow rate of the reaction gas and is 106 mL/min,
Vm is the molar volume of gas and is approximates at 22.4 L/mol.
the photocatalytic degradation of TCE have been done [25,27–30]
and the degradation process includes: TCE → dichloro acetyl chlo-
ride (DCAC) → CO, CO2, H2O, HCl and phosgene. The results that
reported by Fan and Yates [29] and Amama et al. [30] show that
7
(
2VCO + 4V
) × Q × NA × 10−
CO2
the addition of H O can promote DCAC and phosgene be converted
Y =
(2)
2
6
0 × Vm × Itotal
to CO . Thus, it is possible that the organic carbon of TCE can be
2
totally degraded into CO and CO2 in present of water vapor.
3
.3.2. Turnover frequency (f)
f is defined as unit mass of TiO2 within unit time to remove the
amount of contaminants. The formula for f can be written as Eq. (3)
and its unit is ␮mol/(g TiO min), where m is the mass of TiO2 and
2
is calculated at 0.1 g.
(
VCO2 + V ) × Q × 10−
3
CO
f =
(3)
2
× Vm × m
3.3.3. Removal efficiency (ꢀ)
ꢀ
is used to evaluate the degradation efficiency of organic com-
pounds by the photocatalytic reactor. It is calculated through the
ratio between the generation of CO and CO and the corresponding
2
concentration of the initial total organic carbon. The formula for ꢀ
can be written as Eq. (4), where VTCE is the initial volume fraction
of TCE and its unit is ppm.
2
(
VCO2 + VCO) × 10
ꢀ
=
(4)
2
V
TCE
4
. Results and discussion
Fig. 2 shows the curve of direct photolysis of TCE. From Fig. 2, it
can be seen that about 10.76% of the TCE was degraded directly after
turned on the light. This phenomenon is similar to that reported by
many literatures [24–27]. Because the generation of CO and CO2
was not be detected, indicating the direct photolysis of TCE was
not completely degraded into CO2 and CO, the decreasing of TCE
concentration was attributed to the partial oxidation of TCE [25,26].
In this study, the final products of CO and CO were used to calculate
2
the evaluation parameters. Therefore, the direct photolysis almost
has no effect on the results of the evaluation.
Fig. 2 also shows the curve of photocatalytic degradation of
TCE and the generation curves of CO and CO2 on TiO /SiO . Com-
paring the photolysis curve of TCE with the generation curves of
2
2
Fig. 3. The effects of water vapor content on the degradation of TCE: (a) the gen-
eration curves of CO2 and CO; (b) the corresponding results of Y, f and ꢀ. Reaction
conditions: initial concentration of TCE: 151.66 ppm; oxygen content: 20.8%; total
amount of light irradiation: 3.07 × 10
CO and CO , it can be seen that TCE can be almost completely
2
1
7
−1
s ; material of fixed jacket: rubber.
degraded into CO and CO . Many researches on the mechanism of
2

R. Zhu et al. / Applied Catalysis A: General 471 (2014) 136–141
139
Fig. 5. The effects of total amount of light irradiation on the degradation of TCE:
a) the generation curves of CO2 and CO; (b) the corresponding results of Y, f and ꢀ.
Reaction conditions: initial concentration of TCE: 151.66 ppm; water vapor content:
.25%; oxygen content: 20.8%; material of fixed jacket: rubber.
Fig. 4. The effects of oxygen content on the degradation of TCE: (a) the generation
curves of CO2 and CO; (b) the corresponding results of Y, f and ꢀ. Reaction conditions:
initial concentration of TCE: 151.66 ppm; water vapor content: 0.25%; total amount
of light irradiation: 3.07 × 10
(
0
17
−1
s ; material of fixed jacket: rubber.
of DCAC leads to the generation of CO and CO2 not achieving the
expected steady degradation until 240 min (as shown in Fig. 3a).
Fig. 3a shows the generation curves of CO and CO in the process
2
of photocatalytic degradation of TCE under different water vapor
content and the corresponding results of Y, f, ꢀ are shown in Fig. 3b.
As can be seen from the data in Fig. 3b, a small amount of water
vapor can enhance the degradation of TCE and the removal effi-
ciency of TCE decreases with the increase of the water vapor content
when the content of water vapor increases to a certain extent. The
phenomena that lower water vapor content almost does not affect
the degradation activity of TCE and higher water vapor content
inhibits the degradation of TCE are consistent with many litera-
tures [2,31–35], which is because excessive water molecules will
compete active sites of catalyst surface with TCE or intermediate
species. However, the phenomenon that small amount of water
vapor can enhance the degradation of TCE is not consistent with
these literatures [2,31–35]. This discrepancy may arise from our
data processing. From the generation curves of CO and CO2 under
the condition of no water vapor in Fig. 3a, we can see that the curves
first decrease fast with the time of photocatalytic reaction increas-
ing, then start to rise gradually after 25 min and do not achieve the
desired steady degradation until 240 min. In order to facilitate data
comparison, the data under the condition of no water vapor was
analyzed by same processing as other data, which may lead to a
slightly lower result than that obtained in actual degradation. For
the results that the generation of CO and CO2 decreases firstly and
then increase slowly with the time increase (as shown in Fig. 3a),
it is because the degradation rate of DCAC is slower than that of
TCE by approximate one order [27]. That is the slowly degradation
Fig. 4a shows the generation curves of CO and CO in the process
2
of photocatalytic degradation of TCE under different O content and
2
the corresponding results of Y, f, ꢀ are shown in Fig. 4b. As can be
seen from Fig. 4b, it has little effect on the degradation of TCE when
the content of oxygen changes in the range of 10.4–30.2% and the
degradation of the oxygen content at 20.8% is slightly better than
the degradation at other oxygen content, which is consistent with
the results that reported by Wang et al. [34]. Wang et al. [34] studied
the effects of oxygen content on the degradation of TCE in the range
of 0–20% and found the degradation rate of TCE did not change sig-
nificantly when oxygen content was higher than 10%. During the
oxygen content raising from 30.2% to 50.0%, the efficiency of degra-
dation decreases. This phenomenon is similar to that reported by
Ou and Lo [27] and Demeestere et al. [36]. They thought that is
mainly because the excess of oxygen adsorbs on the catalyst sur-
face and competes the active sites with TCE. It is worth noting that
the decrease of TCE degradation is directly related to the produc-
tion of CO (as shown in Fig. 4, the generation of CO2 is the same,
whereas the generation of CO decreases obviously under the oxy-
gen content of 39.4% and 50.0%) and its mechanism needs to be
further researched.
Fig. 5a shows the generation curves of CO and CO in the process
2
of photocatalytic degradation of TCE under different total amount
of light irradiation and the corresponding results of Y, f, ꢀ are shown
in Fig. 5b. From the data in Fig. 5b, it can be clearly seen that ꢀ and
f increases as the total amount of light irradiation increases. This is

1
40
R. Zhu et al. / Applied Catalysis A: General 471 (2014) 136–141
Fig. 7. The effects of material of fixed jacket on the degradation of TCE: (a) the
generation curves of CO2 and CO; (b) the corresponding results of Y, f and ꢀ. Reaction
conditions: initial concentration of TCE: 151.66 ppm; water vapor content: 0.25%;
oxygen content: 20.8%; total amount of light irradiation: 3.07 × 10
Fig. 6. The effects of initial concentration of TCE on the degradation of TCE: (a) the
generation curves of CO2 and CO; (b) the corresponding results of Y, f and ꢀ. Reaction
conditions: water vapor content: 0.25%; oxygen content: 20.8%; total amount of light
irradiation: 3.07 × 10
1
7
−1
s .
17
−1
s ; material of fixed jacket: rubber.
Fig. 3a (the generation curves of CO and CO first decreases sharply
2
then increases slowly with extent of photocatalytic reaction time),
it suggests that the degradation is limited by water vapor content.
because the greater amount of light irradiation can provide more
photons, the more active sites are produced and the better degra-
dation of TCE is achieved [33,34]. These results are similar to that
reported by Dibble and Raupp [2]. It should be noted that Y did
not change significantly with the increasing of the total amount of
light irradiation. Wang et al. [33,34] reported that the quantum effi-
ciency decreased with the increasing of light intensity, which is not
consistent with our results. For the difference from the result that
reported by Wang et al. [33,34], it may be because the performance
of our reactor is limited by the mass transfer of TCE under this condi-
tion. Thus we further researched the effects of initial concentration
of TCE.
Although the addition of H O can promote DCAC and phosgene be
2
converted to CO2 [29,30], the degradation of high concentration
of TCE forms a large accumulation of DCAC and its concentration
exceeds a proportion of H O. The work of optimization of H O
2
2
content at high concentration of TCE will be further carried out.
Fig. 7a shows the generation curves of CO2 and CO in the pro-
cess of photocatalytic degradation of TCE with different materials
of fixed jacket of optical fibers and the corresponding results of Y,
f, ꢀ are shown in Fig. 7b. From Fig. 7, it can clearly be seen that the
degradation of TCE significantly improves with the aluminum fixed
jacket. Compared with the result that using rubber fixed jacket,
ꢀ increases by 31.66%, Y increases by 9.99% and f increases by
Fig. 6a shows the generation curves of CO and CO in the process
2
of photocatalytic degradation of TCE under different initial concen-
tration of TCE and the corresponding results of Y, f, ꢀ are shown in
Fig. 6b. From the data in Fig. 6b, it can be seen that, within the range
of 150–350 ppm, the ꢀ decreases, while Y and f firstly increases and
then decreases with the increasing of initial concentration of TCE.
For ꢀ decreases with the increasing of the initial concentration of
TCE, it is mainly because the quantity of active site is a certain num-
ber, which results in that the degradation of TCE cannot increase
in proportion to the increasing of initial concentration of TCE. For
Y and f increase with the increasing of the initial concentration
of TCE, it is agreement with the prediction under different total
amount of light irradiation, which Y and f can be improved if the
mass transfer is not limited. For the Y and f further decrease with
the initial concentration increasing, based on the similar shape of
the generation curves of CO2 and CO under the concentration of
TCE at 303.32 ppm in Fig. 6a and under anhydrous conditions in
4.55 ␮mol/(g iO min). This is mainly because the aluminum fixed
jacket reflects the ultraviolet light to avoid the loss of scattering of
light and thus improves the utilization of light.
2
Dibble and Raupp [2] obtained the highest turnover frequency of
TCE was 2 ␮mol/(g TiO min) and the highest quantum efficiency
2
was 13% in flat plate fluidized-bed reactor. Furthermore, the cat-
alyst reversibly deactivated once the initial concentration of TCE
was higher than 10 ppm. Compared with the performance of Dib-
ble’s reactor [2], FBOFPR improves the turnover frequency of the
catalyst by about 6 times and the apparent photon quantum effi-
ciency by about 2 times under steady state. In addition, no catalyst
deactivation occurred when initial concentration was higher than
300 ppm.
From all above, combining the fluidized-bed photocatalytic
reactor with the light source from optical fiber that was fixed by
the aluminum fixed jacket for UV total reflection to design an easy

R. Zhu et al. / Applied Catalysis A: General 471 (2014) 136–141
141
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the easy quantification of light irradiation.
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[
[
17
−1
and residence time at 1.6 s, the appar-
irradiation at 3.07 × 10
ent photon quantum efficiency is 26.31%, the turnover frequency is
2.44 ␮mol/(g TiO min) and the removal efficiency is 86.66%. Com-
s
[
[
1
2
pared with the conventional flat plate fluidized-bed photocatalytic
reactor, FBOFPR exhibits many advantages in the aspect of effec-
tive use of photon, sufficient exertion of catalyst activity, effective
removal of TCE and easy quantification of light irradiation.
[
[
[
[
[
[
Acknowledgments
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[
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Research and Development of Science and Technology in Shenzhen
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