CN100334006C - Three-phase activated carbon fluidized bed electrochemical treatment installation and method for organic wastewater - Google Patents
Three-phase activated carbon fluidized bed electrochemical treatment installation and method for organic wastewater Download PDFInfo
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- CN100334006C CN100334006C CNB2004100735165A CN200410073516A CN100334006C CN 100334006 C CN100334006 C CN 100334006C CN B2004100735165 A CNB2004100735165 A CN B2004100735165A CN 200410073516 A CN200410073516 A CN 200410073516A CN 100334006 C CN100334006 C CN 100334006C
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 55
- 239000002351 wastewater Substances 0.000 title claims abstract description 25
- 238000000034 method Methods 0.000 title claims abstract description 11
- 238000009434 installation Methods 0.000 title claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 33
- 238000003487 electrochemical reaction Methods 0.000 claims abstract description 19
- 238000005273 aeration Methods 0.000 claims abstract description 9
- 239000010815 organic waste Substances 0.000 claims description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 10
- 229910052760 oxygen Inorganic materials 0.000 claims description 10
- 239000001301 oxygen Substances 0.000 claims description 10
- 239000007789 gas Substances 0.000 claims description 9
- 238000004065 wastewater treatment Methods 0.000 claims description 9
- YADSGOSSYOOKMP-UHFFFAOYSA-N lead dioxide Inorganic materials O=[Pb]=O YADSGOSSYOOKMP-UHFFFAOYSA-N 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 5
- 235000019600 saltiness Nutrition 0.000 claims description 5
- 229910000831 Steel Inorganic materials 0.000 claims description 4
- 239000010959 steel Substances 0.000 claims description 4
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 claims description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 3
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical class C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 3
- 229910003460 diamond Inorganic materials 0.000 claims description 2
- 239000010432 diamond Substances 0.000 claims description 2
- 238000012545 processing Methods 0.000 abstract description 11
- 230000000694 effects Effects 0.000 abstract description 7
- 230000015556 catabolic process Effects 0.000 abstract description 6
- 238000006731 degradation reaction Methods 0.000 abstract description 6
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 238000006056 electrooxidation reaction Methods 0.000 abstract description 5
- 230000009471 action Effects 0.000 abstract description 3
- 238000009826 distribution Methods 0.000 abstract description 2
- 239000003792 electrolyte Substances 0.000 abstract description 2
- 230000001105 regulatory effect Effects 0.000 abstract 1
- 238000001179 sorption measurement Methods 0.000 abstract 1
- 238000010521 absorption reaction Methods 0.000 description 11
- 230000008929 regeneration Effects 0.000 description 9
- 238000011069 regeneration method Methods 0.000 description 9
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 8
- -1 hydroxyl radical free radical Chemical class 0.000 description 8
- 239000003610 charcoal Substances 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- 239000002957 persistent organic pollutant Substances 0.000 description 6
- 238000006243 chemical reaction Methods 0.000 description 4
- 238000002474 experimental method Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000011780 sodium chloride Substances 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 238000012546 transfer Methods 0.000 description 4
- 238000003795 desorption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- QWPPOHNGKGFGJK-UHFFFAOYSA-N hypochlorous acid Chemical compound ClO QWPPOHNGKGFGJK-UHFFFAOYSA-N 0.000 description 3
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 3
- 238000013461 design Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 239000007800 oxidant agent Substances 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 239000002574 poison Substances 0.000 description 2
- 231100000614 poison Toxicity 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OEHNVKBOQOXOJN-UHFFFAOYSA-N 2-(4-nitrophenyl)phenol Chemical compound OC1=CC=CC=C1C1=CC=C([N+]([O-])=O)C=C1 OEHNVKBOQOXOJN-UHFFFAOYSA-N 0.000 description 1
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000007772 electrode material Substances 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000011737 fluorine Substances 0.000 description 1
- 229910052731 fluorine Inorganic materials 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 125000002887 hydroxy group Chemical group [H]O* 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000010525 oxidative degradation reaction Methods 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 230000010287 polarization Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 239000012780 transparent material Substances 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
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Abstract
The present invention relates to an electrochemical processing device and a method for organic wastewater by a three-phase activated carbon fluidized bed. Hydraulic distribution plates ae respectively installed at the upper part and the lower part of a shell body of a processing device; the shell body is orderly divided into a water outlet chamber, an electrochemical reaction chamber and a water inlet chamber from top to bottom; the inner wall of the electrochemical reaction chamber surrounding the shell body is provided with a cathode, and the center is provided with an anode; an aeration head connected with an air inlet pipe is distributed in a ring shape in the water inlet chamber; active carbon is filled between the cathode and the anode; electrolyte is added to the organic wastewater, and a pH value is regulated; the wastewater is pumped into a water outlet at the top of the shell body from the bottom of the shell body to flow out, and gas is led in the air inlet pipe; the wastewater processing is carried out at the normal temperature and under the normal pressure; 0.2 to 2.5 A of direct current is additionally added, the water flow is controlled within the range of 1 to 5 L/min, the rate of gas is controlled within the range of 0 to 50 mL/s, and the active carbon is in the fluidized state. The present invention can improve the degradation rate by the combined action of electrochemical oxidation and active carbon adsorption, and the present invention has the advantages of good processing effect and low cost.
Description
Technical field
The present invention relates to a kind of the organic waste water especially three-phase activated carbon fluidized bed electrochemical treatment installation and method of the organic waste water of bio-refractory of being used for.
Background technology
The waste water that contains the bio-refractory organic pollutant, because its Stability Analysis of Structures, biodegradability are poor, conventional treatment method is difficult to cause effect, brings very big pollution to environment, becomes the technical problem that the environmental protection water treatment field is paid close attention to for many years and will be solved.
Gac is because its flourishing pore structure, huge specific surface area and extremely strong adsorptive power are obtaining application widely aspect feedwater, the wastewater treatment.But gac cost height, and easily adsorb saturatedly, also can not cause secondary pollution if do not regenerate to reclaim to environment, therefore, the application of charcoal absorption in wastewater treatment is restricted.
In recent years, electrochemical oxidation technology is because of its processing efficiency height, easy and simple to handle, advantages of environment protection, caused the very big concern of countries in the world field of water treatment, the exploration of electrode materials and the exploitation of electrochemical treatment technology (Rajeshwar et al. have been carried out one after another, J.Appl.Electrochem., 1994,24:1077).Studies show that the electrode of the contour overpotential for oxygen evolution of plumbic oxide can produce the very strong hydroxyl radical free radical of oxidation capacity under polarization condition, thereby obtains contaminant degradation effect preferably.But in the electrochemical reactor of routine, because of often shifted less than going in the solution main body by mass transfer limit, hydroxyl radical free radical, thereby the degraded of pollutent occurs over just anode surface usually, and the solution main body is rare, and this makes that the space-time speed of organic pollutant degradation is lower.And because the intermediate product of degraded is trapped in anode surface, causes anode surface and poison phenomenon, thereby the reaction that has suppressed to produce hydroxyl radical free radical has reduced the Pollutant Treatment effect.
Therefore, press for the design of optimizing electrochemical reactor, strengthen the mass transfer of the hydroxyl free basal orientation solution main body of anode surface generation.And fluidized-bed is to be expected to one of means that reach this purpose, by introducing gac and forming fluidized state, may promote absorption, the degraded of pollutent, thereby improves degradation rate, reduces cost for wastewater treatment.
Summary of the invention
The objective of the invention is to design three-phase activated carbon fluidized bed electrochemical treatment installation and method that a kind of organic waste water is provided.By in the electrochemical system of routine, introduce gac and control is in fluidized state, reach the combined action of electrochemical oxidation and charcoal absorption and accelerate greatly to handle.And gac then can use thereby can reach repeatedly by electrochemical situ regeneration, greatly reduces cost for wastewater treatment.
Three-phase (the gas of organic waste water of the present invention, liquid, Gu) activated carbon fluidized bed electrochemical treatment installation, comprise housing, on housing, the bottom is separately installed with housing is divided into water-supplying chamber from top to bottom successively, the first waterpower grid distributor of electrochemical reaction room and intake chamber and the second waterpower grid distributor, water-supplying chamber and intake chamber are respectively equipped with water outlet and water-in, at the inner wall device negative electrode of electrochemical reaction room around housing, the center is provided with anode, have the cavity of placing gac between negative electrode and the anode, annular spread has the aeration head that links to each other with inlet pipe in intake chamber.
Above-mentioned negative electrode can adopt stainless (steel) wire or activated carbon fiber, and anode can adopt high oxygen separated overpotential electrode, as plumbic oxide, tindioxide or diamond electrode.Comparatively speaking, lead dioxide electrode is with low cost and catalytic activity is high, but stability is not high, electrode surface easily peels off, and through after fluororesin modified, its stability greatly improves, greatly increase electrode life, thereby be easier to industrial application, therefore, anode preferably passes through fluororesin modified plumbic oxide.
The three-phase activated carbon fluidized bed electrochemical of organic waste water is handled and is carried out at normal temperatures and pressures, gac is filled in negative and positive two interpolars, in pending organic waste water, add ionogen, making the waste water saltiness is 1～15g/L, and adjusting pH value is 2～5, waste water is pumped into the intake chamber of flowing through successively from the housing bottom water-in, bottom waterpower grid distributor, electrochemical reactor, top waterpower grid distributor, water-supplying chamber to case top water outlet flows out, inlet pipe feeds gas, external dc electric current 0.2～2.5A, and discharge is controlled at 1～5L/min, gas velocity is controlled at 0～50mL/s, makes gac be in fluidized state.
Among the present invention, said ionogen can be vitriol or hydrochloride, as Na
2SO
4Or common strong salt electrolyte such as NaCl.Said gas can be oxygen or air.The size of external dc electric current and the flow of water and treatment time, can regulate according to the water quality of handling waste water.
Treatment of Organic Wastewater mechanism of the present invention is mainly electrochemical oxidation, charcoal absorption and electrochemical regeneration thereof.The high oxygen separated overpotential electrode that the present invention adopts under the suitable electric potential condition, produce the extremely strong hydroxyl radical free radical of oxidisability (
OH), its reaction is as follows,
H
2O→
·OH+H
+ (1)
When adding hydrochloride (as NaCl etc.) ionogen in the water, following reaction also can take place on anode,
Cl
-→Cl
ads+e
- (2)
Cl
ads+Cl
-→Cl
2+e
- (3)
Cl
2+H
2O→HOCl+H
++Cl
- (4)
Produce hypochlorous acid, it is a kind of strong oxidizer, thereby has promoted organic further degraded.During processing, control by flow, make gac be in fluidized state, the absorption and the desorption rate of gac are accelerated greatly, the rapid mass transfer of strong oxidizers such as hydroxyl radical free radical that results from anode surface is to solution main body and activated carbon surface, thereby make pollutent (R) that following reaction take place and degraded rapidly and efficiently, gac is regenerated like this.
R+
OH → CO
2+ H
2O+ mineral ion (5)
The present invention has following outstanding feature and beneficial effect:
(1) desorption can be degraded efficiently in the pollutent of activated carbon surface.The present invention has adopted new and effective anode, and this electrode is handled organic pollutant mainly based on the hydroxyl radical free radical oxidation mechanism.As everyone knows, hydroxyl radical free radical is the strong oxidizer that is only second to fluorine, and therefore, the Pollutant Treatment effect improves greatly, and test shows can be up to 80% to the current efficiency of phenyl ring class organic pollutant degradation, the capacity usage ratio height.In addition,, can produce hypochlorous acid by electrochemical reaction by the adding of ionogen (as NaCl), common oxidative degradation organic pollutant, thus make wastewater treatment more thorough.
(2) charcoal absorption, recovery time shorten greatly.Under the active carbon fluid state, effect of mass transmitting is strengthened, and organic pollutant desorption, degraded are accelerated greatly.The regeneration of activated carbon experiment shows, handles 1.5hr the regeneration of activated carbon efficient of saturated absorption is reached more than 92%.In addition, because the anode surface mass transfer is fast, the phenomenon that can generating electrodes poison.
(3) electrode system is stable.The anode performance that the present invention adopts is stable, acid corrosion-resistant, and to be example through fluororesin modified lead dioxide electrode, even test shows is at current density 120A dm
-2, 90 ℃ of temperature extreme condition under, the life-span of this electrode, under the conventional industrial application condition, can reach 10.4 electrode life still up to 1000hr, this helps the industrial application of body series.
Description of drawings
Fig. 1 is the three-phase activated carbon fluidized bed electrochemical treatment installation structural representation of organic waste water.
1 is end cap among the figure, and 2 is water-supplying chamber, and 3 is the first waterpower grid distributor; 4 is flange, and 5 is anode, and 6 is the second waterpower grid distributor; 7 is water-in, and 8 is intake chamber, and 9 is granulated active carbon; 10 is electrochemical reaction room; 11 is housing, and 12 is negative electrode, and 13 is water outlet; 14 is the aeration inlet pipe, and 15 is aeration head.
Embodiment
For understanding technical solution of the present invention better, below be further described by drawings and the specific embodiments.
With reference to Fig. 1, the three-phase activated carbon fluidized bed electrochemical treatment installation of organic waste water comprises housing 11, in the legend, housing 11 has the end cap 1 with flange 4 airtight connections, the first waterpower grid distributor 3 is installed in end cap, in lower part of frame the second waterpower grid distributor 6 is installed, here, the waterpower grid distributor is conventional distribution foraminous plate, these two waterpower grid distributors are divided into water-supplying chamber 2 from top to bottom successively with housing, electrochemical reaction room 10 and intake chamber 8, water-supplying chamber 2 and intake chamber 8 are respectively equipped with water outlet 13 and water-in 7, and at the inner wall device negative electrode 12 of electrochemical reaction room around housing, the center is provided with anode 5, negative electrode 12 can be stainless (steel) wire or activated carbon fiber, and anode 5 adopts high oxygen separated overpotential electrode.In the intake chamber 8 below electrochemical reaction room 10, annular spread has aeration head 15, and aeration head 15 links to each other with inlet pipe 14, like this can uniform distribution inlet pipe 14 expose to the sun into gas.For making things convenient for anode to connect power supply, can make anode 5 pass through the first waterpower grid distributor 3 as shown in the figure, fix with end cap.Has the cavity of placing gac 9 between negative electrode 12 and the anode 5.Housing can adopt transparent material, as organic glass, so that observe.
Embodiment 1: three-phase activated carbon fluidized bed electrochemical is handled p-NP waste water
The anode of electrochemical reaction room is that negative electrode is a stainless (steel) wire through fluororesin modified plumbic oxide vitrified pipe electrode.Before the wastewater treatment, in electrochemical reaction room, add the 3g gac, in waste water, add NaCl, making the waste water saltiness is 5g/L, and regulates wastewater pH to 3, is 0.5A by control current, flow rate of liquid is 3.0L/min, and air aeration speed is 20mL/s, makes gac be in fluidized state.
Test shows, is p-NP (PNP) waste water of 150mg/l for starting point concentration, and p-NP is almost completely removed behind the processing 20min, and chemical oxygen demand (COD) (COD) clearance can reach more than 85% in the 2hr.Under the simulated condition, in independent charcoal absorption and electrochemical oxidation, the p-NP clearance is respectively 35% and 53% approximately behind the processing 20min.This shows, this three-phase activated carbon fluidized bed electrochemical reaction unit is handled waste water and is had the obvious synergistic effect, and the treatment effect of p-NP and COD improves 137.8% and 97.8% respectively than electrocatalysis independent under the simulated condition and charcoal absorption as calculated.
Under the similarity condition, for starting point concentration be 300, the PNP waste water of 500mg/L, the clearance in its 60min is respectively 90% and 80%.
The continuous gac that do not change for 6 times is handled the circulation experiment of pollutent continuously and is shown, waste water treatment efficiency does not have obvious decline, show that gac is effectively regenerated, this has shown the applications well prospect of three-phase activated carbon fluidized bed electrochemical reaction unit in the organic wastewater with difficult degradation thereby process field.Because treating processes, wastewater treatment will be accelerated greatly because of the combined action of electrocatalysis and charcoal absorption, and gac can obtain effective regeneration and reuse, so greatly reduce processing cost.
Embodiment 2: three-phase activated carbon fluidized bed electrochemical is handled phenolic waste water
Employing is handled the phenolic waste water that contains 300mg/L with the electrochemical system of example 1.Before the processing, in electrochemical reaction room, add the 3g gac, in waste water, add Na
2SO
4, making the waste water saltiness is 10g/L, and regulates wastewater pH to 3, is 0.8A by control current, and flow rate of liquid is 3.25L/min, and oxygen rates is 15mL/s, makes gac be in fluidized state.Test shows that phenol is almost completely removed behind the processing 30min, and chemical oxygen demand (COD) (COD) clearance reaches 93% in the 2.0hr.
Embodiment 3: the gac electrochemical regeneration
In order directly to confirm the regeneration of gac in above-mentioned three-phase fluidized bed electrochemical appliance, adopt gac 3g in the example 1, drop into starting point concentration in advance and be that absorption reached capacity in 3 days in the p-nitrophenyl phenol solution of 1000mg/L.Then this gac is moved into electrochemical reaction room, feeding contains the electrolytical aqueous solution and carries out electrochemical regeneration.Other experiment conditions such as saltiness, ionogen, pH value of solution, electric current, gas, flow rate of liquid and example 1 are identical.Experiment shows, electrochemical treatment 1.5hr in above-mentioned reactor, and regeneration of activated carbon efficient can reach 90%.
Claims (7)
1. the three-phase activated carbon fluidized bed electrochemical treatment installation of organic waste water, it is characterized in that comprising housing (11), housing (11) has the end cap (1) with the airtight connection of flange (4), on housing, the bottom is separately installed with housing is divided into water-supplying chamber (2) from top to bottom successively, the first waterpower grid distributor (3) of electrochemical reaction room (10) and intake chamber (8) and the second waterpower grid distributor (6), water-supplying chamber (2) and intake chamber (8) are respectively equipped with water outlet (13) and water-in (7), at the inner wall device negative electrode (12) of electrochemical reaction room around housing, the center is provided with anode (5), the cavity that has placement gac (9) between negative electrode (12) and the anode (5), annular spread has the aeration head (15) that links to each other with inlet pipe (14) in intake chamber (8), said anode (5) adopts high oxygen separated overpotential electrode, is plumbic oxide, tindioxide or diamond electrode.
2. the three-phase activated carbon fluidized bed electrochemical treatment installation of organic waste water according to claim 1 is characterized in that said negative electrode (12) is stainless (steel) wire or activated carbon fiber.
3. the three-phase activated carbon fluidized bed electrochemical treatment installation of organic waste water according to claim 1, it is characterized in that the first waterpower grid distributor (3) be installed in the airtight end cap that is connected of housing (11) (1) on.
4. the three-phase activated carbon fluidized bed electrochemical treatment installation of organic waste water according to claim 1 is characterized in that anode (5) passes through the first waterpower grid distributor (3), fixes with end cap.
5. adopt the three-phase activated carbon fluidized bed electrochemical treatment process of the organic waste water of the described device of claim 1, it is characterized in that on the treatment unit housing, the bottom is installed the waterpower grid distributor respectively, housing is divided into water-supplying chamber from top to bottom successively, electrochemical reaction room and intake chamber, at the inner wall device negative electrode of electrochemical reaction room around housing, the center is provided with anode, the aeration head that annular spread links to each other with inlet pipe in intake chamber, gac is filled in negative and positive two interpolars, in pending organic waste water, add ionogen, making the waste water saltiness is 1～15g/L, and to regulate the pH value be 2～5, and waste water is pumped into the intake chamber of flowing through successively from the housing bottom water-in, bottom waterpower grid distributor, electrochemical reactor, top waterpower grid distributor, water-supplying chamber flows out to the case top water outlet, and inlet pipe feeds gas, and wastewater treatment is carried out at normal temperatures and pressures, external dc electric current 0.2～2.5A, discharge is controlled at 1～5L/min, and gas velocity is controlled at 0～50mL/s, makes gac be in fluidized state.
6. the three-phase activated carbon fluidized bed electrochemical treatment process of organic waste water according to claim 5 is characterized in that said ionogen is vitriol or hydrochloride.
7. the three-phase activated carbon fluidized bed electrochemical treatment process of organic waste water according to claim 5 is characterized in that said gas is air or oxygen.
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| Title |
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| PbO2电极氧化有机废水的研究 申哲民，雷阳明，贾金平，陈玉胜，王文华，高校化学工程学报，第18卷第1期 2004 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101544415B (en) * | 2009-03-20 | 2011-08-31 | 浙江工业大学 | Expanded bed electrolysis unit and processing technique using same for decomposing water phase organic matters |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1654340A (en) | 2005-08-17 |
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