CN1884149A - Method for treating waste water in production of 4,6-dinitro o-sec-butyl phenol - Google Patents
Method for treating waste water in production of 4,6-dinitro o-sec-butyl phenol Download PDFInfo
- Publication number
- CN1884149A CN1884149A CN 200610014584 CN200610014584A CN1884149A CN 1884149 A CN1884149 A CN 1884149A CN 200610014584 CN200610014584 CN 200610014584 CN 200610014584 A CN200610014584 A CN 200610014584A CN 1884149 A CN1884149 A CN 1884149A
- Authority
- CN
- China
- Prior art keywords
- water
- treatment process
- colourity
- cod
- dnbp
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Abstract
The invention discloses a disposing method of 4, 6-dinitrobutylphenol (DNBP) wastewater, which comprises the following steps: 1. diluting DNBP with over 80000mg/L COD value and 50000 colority; diverting high-density acid water (48 percent) and neutralizing water and rinsing water; 2. disposing high-density acid water; 3. disposing low-density acid water to reach drainage standard with COD not more than 150mg/L, colority not more than 80 times, phenols not more than 0.5 mg/L, NH3-N not more than 20mg/L, SS not more than 20mg/L and pH value at 6-9.
Description
Technical field
The present invention relates to a kind of treatment process of 4.6-dinitro o-sec-butyl phenol factory effluent.
Background technology
4.6-dinitro o-sec-butyl phenol (abbreviation DNBP) be a kind of orange to liquid russet, have the singularity smell, dissolve in oil and most of organic solvent, can with mineral alkali or organic bases salify; It is a kind of new and effective stopper, is high temperature high-efficiency polymerization inhibitor required in the phenyl ethylene rectification process, and its polymerization inhibition effect is better than other nitrophenol polymerization inhibitor.Simultaneously can reduce environmental pollution, improve the production of styrene ability.And in producing 4.6-dinitro o-sec-butyl phenol process, have acid-bearing wastewater to discharge, major ingredient in the waste water be the high density sour water (sulfuric acid and nitric acid contain mixing acid, concentration is about 48%), COD up to 80,000 mg/litre about, colourity is up to more than 50000 extension rates.The high acidity waste water of the poisonous and hazardous high COD value and high colour of this class is wanted low operating cost (2-3 unit/ton water), low investment is administered is one of difficult problem of present art technology, also is domestic one of the field that sets foot in of still not having.
Do the colourity and the COD index that how with concentration are 48% waste acid water lower? so that it uses it for anything else in addition, promptly develop derived product; How how with in its product and the high chroma of water and washing water (about 2000-20000 doubly) high COD (5000-20000mg/L) waste water treatment extremely can meet secondary standard among the GB8978-1996 of country's " integrated wastewater discharge standard ", also be to wait the technical barrier that solves at present.
Summary of the invention
For solving the problem that exists in the above-mentioned technology, the treatment process that the purpose of this invention is to provide a kind of 4.6-dinitro o-sec-butyl phenol factory effluent, DNBP in the high acidity COD value high chroma spent acid solution (about 48%) is reclaimed, other uses it for anything else, and another purpose will be hanged down the high COD high chromaticity industrial waste water of acidity (PH1-3) and be handled to qualified discharge.
For achieving the above object, the technical solution used in the present invention provides a kind of treatment process of 4.6-dinitro o-sec-butyl phenol factory effluent, and its method may further comprise the steps:
1., be＞50000 extension rates for＞80000mg/L, colourity at first with the COD value that contains that produces in 4.6-dinitro o-sec-butyl phenol (abbreviation DNBP) production technique, with in producing in high density sour water (concentration ~ 48%) and this production technique and water and washing water, promptly the lower concentration sour water is shunted.To be about 48% concentrated acid water be HNO to concentration among the described DNBP
3+ H
2SO
4Concentration is mixed sour water, wherein HNO
3Account for about 8% H
2SO
4Account for about 40%.
2., to the treatment process of above-mentioned high density sour water:
The high density sour water of a, DNBP (organic phase: water=2: 8) with ethylbenzene extraction, static, layering; Organic phase is advanced production process, recovery, and water takes on a red color, and COD reduces to 10000-20000mg/L from 80000-90000mg/L, and colourity is reduced to about 10000 times from 50000 times;
B, the above-mentioned water that takes on a red color continue extraction with ethylbenzene and tributyl phosphate (ratio is 7: 3), and this organic phase is used repeatedly near saturated (be shallow with water and orange redly show it), recycles after regenerating with the back extraction of 5-10% sodium hydroxide then; Sodium hydroxide waste liquor after the back extraction is through electrolysis treatment, neutralization, qualified discharge;
The water of c, above-mentioned redness becomes and mixes yellowly after ethylbenzene and tributyl phosphate extraction, and water is with carrying a nano level TiO
2Porous silica gel and carbon compositing catalyst, about the logical catalytic ozonation 5h of water, be bright light yellow, COD2000-3000mg/L, colourity 600-800 doubly, the hold-up vessel of can packing into stays and does its and use;
3., to the treatment process of above-mentioned lower concentration sour water:
Lower concentration sour water COD ~ 5000-20000mg/L of a, DNBP, colourity 2000-30000 doubly, PH1-3, turbidity＞100NTU, phenols＞500mg/L extracts, leaves standstill with ethylbenzene and tributyl phosphate (ratio 7: 3), layering, organic phase can be used the back extraction of 5-10% sodium hydroxide, regenerates, recycles, and its water colourity is mixes yellow;
B, with the mixed yellow water of separating after the above-mentioned extraction, logical catalytic ozonation 3-5h to water white transparency, transfers to PH6-7 with NaOH again, adds sodium bisulfite and removes O
3, entering Biochemistry Reaction System, hydraulic detention time 〉=12h gets final product qualified discharge;
Effluent quality pollutent index: COD≤150mg/L, colourity≤80 times, phenols≤0.5mg/L, NH
3-N≤20mg/L; SS≤20mg/L; PH6-9.
Described step 2., the catalyzer of ozone catalytic reactive system in 3. is nano level TiO
2, wherein used carrier is porous silica gel particle or one of porous ceramics or gac, the ability of ozone degradation COD is from general 0.1mgO
3Degraded 0.1mgCOD is to 0.1mgO
3Degraded 2mgCOD.
To the sodium hydroxide waste liquor after the back extraction of step in 2. through catalytic electrolysis reaction, neutralization, qualified discharge.
The interior catalyst system therefor of catalytic electrolysis groove is the plant slag heavy metal oxide in the catalytic electrolysis reaction.
Electrode in the electrolyzer of catalytic electrolysis reaction is a porous graphite electrode.
Effect of the present invention is that this method can be removed 95% or more from the 80000-140000 mg/litre COD value in the DNBP factory effluent middle and high concentration sour water, make the spent acid of its processing can make the exploitation derived product and use (producing various relevant Nitrateses and Sulfates etc.), its colourity from＞50000 times reduce to＜800 times be light yellow spent acid.With lower concentration sour water (PH1-3) high chroma (2000-20000 doubly) high COD value (5000-20000mg/L), the industrial wastewater treatment that contains DNBP is to the secondary standard that reaches the GB8978-1996 of country's " integrated wastewater discharge standard ".The COD removal ability of ozone has been improved about 20 times; Percent of decolourization reaches more than 99%.Present technique wastewater treatment running cost is lower, can reach≤index of 2.5 yuan of/ton water.
Embodiment
Treatment process to 4.6-dinitro o-sec-butyl phenol factory effluent of the present invention is illustrated in conjunction with the embodiments.
1., at first will produce waste water middle and high concentration sour water and the shunting of lower concentration sour water that 4.6-dinitro o-sec-butyl phenol (abbreviation DNBP) produces, the COD value that contains that is about to produce in the DNBP production technique is＞50000 extension rates for＞80000mg/L, colourity, with in producing in high density sour water (concentration ~ 48%) and this production technique and water and washing water, promptly the lower concentration sour water is shunted.
2., to the treatment process of above-mentioned high density sour water:
The high density sour water of a, DNBP (organic phase: water=2: 8) with ethylbenzene extraction, static, layering; The organic phase production art flow process of bringing back to life enters product.Water takes on a red color, and COD reduces to 10000-20000mg/L from 80000-90000mg/L, and colourity is reduced to about 10000 times from 50000 times.
B, the above-mentioned water that takes on a red color continue extraction with ethylbenzene and tributyl phosphate (ratio is 7: 3), and this organic phase is renewable, recycle repeatedly near saturated (be shallow with water and orange redly show it).Then with recycling after the 5-10% sodium hydroxide back extraction regeneration; Sodium hydroxide waste liquor after the back extraction is through electrolysis treatment, neutralization, qualified discharge.
The water of c, above-mentioned redness becomes and mixes yellowly after ethylbenzene and tributyl phosphate extraction, and water is with carrying a nano level TiO
2Porous silica gel and carbon compositing catalyst, about the logical catalytic ozonation 5h of water, be bright light yellow, COD2000-3000mg/L, colourity 600-800 doubly, the hold-up vessel of can packing into stays and does its and use.
3, to the processing of above-mentioned low acidity sour water:
A, DNBP lower concentration sour water COD ~ 5000-20000mg/L, colourity 2000-30000 doubly, PH1-3, turbidity＞100NTU, phenols＞500mg/L, extract, leave standstill with ethylbenzene and tributyl phosphate (ratio 7: 3), layering is divided into organic phase and water, and organic phase can be used the back extraction of 5-10% sodium hydroxide, regenerate, recycle, wherein water colourity is mixed yellow.When not enough, can add the ethylbenzene and the tributyl phosphate of new preparation in the processing.The waste lye that produces is handled the back qualified discharge through slag catalytic electrolysis (800mA, 10-20V Graphite Electrodes method).
B, the mixed yellow water separated after the above-mentioned extraction is being carried a nano level TiO
2The catalyzer of gac exist down, logical catalytic ozonation 3-5h, water outlet transfers to PH6-7 with NaOH more to water white transparency, adds sodium bisulfite and removes O
3, entering Biochemistry Reaction System, hydraulic detention time 〉=12h gets final product qualified discharge.If the still below standard (standard≤150mg/L),, get final product qualified discharge of COD through charcoal absorption.Wherein, described Biochemistry Reaction System is a biological filter process.
Above-mentioned Biochemistry Reaction System is a biological filter process, domestication, the method for spreading cultivation of its microorganism used therefor flora are: conventional method is: the above-mentioned generation waste plant sewage of the abundant amount of fetching is always arranged mouthful contains the same trade effluent of bacterium mud, clear water and nutriment (sanitary sewage or chemical fertilizer, some trade effluent does not need to add nutriment) mix sprinkle biological filter, back by suitable proportion, water outlet enters second pond, and with second pond as circulating water pool, circular flow.After microbial film mark phenomenon obviously appears in filter bed, be reference with the second pond effluent quality, in circulation, progressively adjust the ratio of trade effluent and water outlet, normal up to water outlet.At this moment, domestication-biofilm finishes.
Effluent quality pollutent index: COD≤150mg/L, colourity≤80 times, phenols≤0.5mg/L, NH
3-N≤20mg/L; SS≤20mg/L; PH6-9.
Above-mentioned steps 2., the catalyzer of ozone catalytic reactive system in 3. is nano level TiO
2Gac, wherein used carrier is porous silica gel particle or porous ceramics or gac or molecular sieve etc.The ability of ozone degradation COD is from general 0.1mgO
3Degraded 0.1mgCOD is to 0.1mgO
3Degraded 2mgCOD.
The interior catalyst system therefor of catalytic electrolysis groove is the plant slag heavy metal oxide in the catalytic electrolysis reaction, and the electrode in the electrolyzer is a porous graphite electrode.
The specific embodiment of the invention:
Tianjin Rui Tai Fine Chemical Co., Ltd produces the high-concentration sulfuric acid of 4.6-dinitro o-sec-butyl phenol (DNBP), the mixing sour water of nitric acid, and the quantity discharged of every day is respectively about 6 tons; About 25 tons of lower concentration sour waters; The phenolic wastewater that also has some flushing mill floors in addition.
Concrete treatment process is as follows:
1, at first with high density (48%) sour water and the shunting of lower concentration (PH1-3) sour water, handles respectively.
2, high concentrated acid water technology:
1. DNBP high density sour water (sulfur acid 40%, nitric acid about 8%, COD82000mg/L, 50000 times of colourities, dark brown red), with ethylbenzene extraction (ethylbenzene: water=2: 8), fully stirred 20 minutes, leave standstill 1 hour after, the water (taking on a red color) of lower floor is put into second extractor; The organic phase on upper strata (ethylbenzene and DNBP etc.) is returned DNBP production process neutralizing zone, reclaims.
2. add ethylbenzene and tributyl phosphate (7: 3), water to above-mentioned second extractor: organic phase=8: 2, fully stirred 20 minutes, left standstill 1 hour, the water of lower floor is put into the catalytic ozonation system.Its organic phase recycles, and until with the regeneration of 5-10%NaOH solution, can also recirculation use.
3. activated-carbon catalyst (the TiO that carries Nano titanium dioxide is housed in the ozone oxidation system
2Content be about 3%), water: catalyzer=100: 5 (W/V), square tube ozone (50gO under catalyzer
3/ h) aeration 4-5 hour, waste water is become light yellow, transparent by orange-yellow muddiness, promptly stop, and tinning uses it for anything else fully.
3, the lower concentration sour water is handled and is gone up skill:
DNBP hangs down acidity waste water, and (about COD10000mg/L, colourity is more than 5000 times, PH1-3), with ethylbenzene and tributyl phosphate extraction, fully stirred 20 minutes, left standstill 1 hour, layering, organic phase is continued to employ, and water enters the catalytic ozonation system, reacts 4-5 hour, waste water is regulated PH6-7 after being water white transparency, add the laggard biological filter of sodium bisulfite deozonize and carry out biochemical reaction and handle, degraded COD, take off N, remove P after, the water outlet qualified discharge.
Above-mentioned O
3The catalytic oxidation system is with 3 8m
3Cement pit, 5% year nano level TiO is housed
2Activated-carbon catalyst, its bed thickness are 300 millimeters, O
3Producer is 100gO
3The aerating system of/h is formed.
Biochemistry Reaction System is the secondary reinforcement biochemical system: the anaerobism → aerobic → oxygen of holding concurrently, denitrogenation removes the biological filter process of P.Used biochemical flora is got this factory's discharging and is sucked bacterium mud in its biological filter, gets through taming, spreading cultivation.Hydraulic retention total time 20h, gas-water ratio is 10: 1.
The alkali waste water of above-mentioned regeneration usefulness uses slag catalytic electrolysis reaction treatment to qualified discharge.Electric current 500-800mA, voltage 6-10V, electrode porous graphite plate, the reaction times decides on colourity, COD.
Wherein electrolytic catalyst is used is that the slag of chemical plant, Dagu power plant forms through selected, utilizes the relevant heavy metal oxide in the slag to play katalysis.
Waste water before handling (low acidity waste water): COD5000 ~ 10000mg/L, 2000 ~ 20000 times of colourities, PH1-3, phenols＞500mg/L, red-brown.
Processed waste water: COD≤150mg/L, colourity≤80 times, PH6-9, phenols≤0.5mg/L, SS≤20mg/L, NH
3-N≤20mg/L.
The treatment process of 4.6-dinitro o-sec-butyl phenol factory effluent of the present invention also is applicable to the processing to the 2.4-dinitrophenol(DNP) trade effluent of the mixing acid that contains nitric acid, and through test run, effect also is clearly.
Claims (6)
1, a kind of treatment process of 4.6-dinitro o-sec-butyl phenol factory effluent, its method may further comprise the steps:
1., be＞50000 extension rates for＞80000mg/L, colourity at first with the COD value that contains that produces in 4.6-dinitro o-sec-butyl phenol (abbreviation DNBP) production technique, with in producing in high density sour water (concentration ~ 48%) and this production technique and water and washing water, promptly the lower concentration sour water is shunted;
2., to the treatment process of above-mentioned high density sour water:
The high density sour water of a, DNBP (organic phase: water=2: 8) with ethylbenzene extraction, static, layering; Organic phase is advanced production process, recovery, and water takes on a red color, and COD reduces to 10000-20000mg/L from 80000-90000mg/L, and colourity is reduced to about 10000 times from 50000 times;
B, the above-mentioned water that takes on a red color continue extraction with ethylbenzene and tributyl phosphate (ratio is 7: 3); This organic phase is used repeatedly near saturated (be shallow with water and orange redly show it), recycles after regenerating with the back extraction of 5-10% sodium hydroxide then; Sodium hydroxide waste liquor after the back extraction is through electrolysis treatment, neutralization, qualified discharge;
The water of c, above-mentioned redness becomes and mixes yellowly after ethylbenzene and tributyl phosphate extraction, and water is with carrying a nano level TiO
2Porous silica gel and carbon compositing catalyst, about the logical catalytic ozonation 5h of water, be bright light yellow, COD2000-3000mg/L, colourity 600-800 doubly, the hold-up vessel of can packing into stays and does its and use;
3., to the treatment process of above-mentioned lower concentration sour water:
Lower concentration sour water COD ~ 5000-20000mg/L of a, DNBP, colourity 2000-30000 doubly, PH1-3, turbidity＞100NTU, phenols＞500mg/L extracts, leaves standstill with ethylbenzene and tributyl phosphate (ratio 7: 3), layering, organic phase can be used the back extraction of 5-10% sodium hydroxide, regenerates, recycles, and its water colourity is mixes yellow;
B, with the mixed yellow water of separating after the above-mentioned extraction, logical catalytic ozonation 3-5h to water white transparency, transfers to PH6-7 with NaOH again, adds sodium bisulfite and removes O
3, entering Biochemistry Reaction System, hydraulic detention time 〉=12h gets final product qualified discharge;
Effluent quality pollutent index: COD≤150mg/L, colourity≤80 times, phenols≤0.5mg/L, NH
3-N≤20mg/L; SS≤20mg/L; PH6-9.
2, treatment process according to claim 1 is characterized in that: to be about 48% concentrated acid water be HNO to concentration among the described DNBP
3+ H
2SO
4Concentration is mixed sour water, wherein HNO
3Account for about 8% H
2SO
4Account for about 40%.
3, treatment process according to claim 1 is characterized in that: described step 2., the catalyzer of ozone catalytic reactive system in 3. is nano level TiO
2, wherein used carrier is porous silica gel particle or one of porous ceramics or gac, the ability of ozone degradation COD is from general 0.1mgO
3Degraded 0.1mgCOD is to 0.1mgO
3Degraded 2mgCOD.
4, treatment process according to claim 1 is characterized in that: to the sodium hydroxide waste liquor after the back extraction of step in 2. through catalytic electrolysis reaction, neutralization, qualified discharge.
5, treatment process according to claim 4 is characterized in that: used catalyzer is the plant slag heavy metal oxide in the catalytic electrolysis groove in the catalytic electrolysis reaction.
6, treatment process according to claim 5 is characterized in that: the electrode in the electrolyzer of catalytic electrolysis reaction is a porous graphite electrode.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100145843A CN100486921C (en) | 2006-06-30 | 2006-06-30 | Method for treating waste water in production of 4,6-dinitro o-sec-butyl phenol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2006100145843A CN100486921C (en) | 2006-06-30 | 2006-06-30 | Method for treating waste water in production of 4,6-dinitro o-sec-butyl phenol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1884149A true CN1884149A (en) | 2006-12-27 |
| CN100486921C CN100486921C (en) | 2009-05-13 |
Family
ID=37582472
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2006100145843A Expired - Fee Related CN100486921C (en) | 2006-06-30 | 2006-06-30 | Method for treating waste water in production of 4,6-dinitro o-sec-butyl phenol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100486921C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105036258A (en) * | 2015-09-09 | 2015-11-11 | 陆秀英 | Application method of porous graphite electrode in industrial wastewater treatment |
| CN106145481A (en) * | 2016-08-31 | 2016-11-23 | 格斯瑞科技有限公司 | The apparatus and method of organic industrial sewage are processed based on cavitation technique |
| CN108203183A (en) * | 2018-01-23 | 2018-06-26 | 孙国芳 | A kind of sewage pretreatment device and processing method |
| CN109534546A (en) * | 2018-12-12 | 2019-03-29 | 江苏湖大化工科技有限公司 | A kind of processing method of phenol resin production waste water |
| CN112607962A (en) * | 2020-12-04 | 2021-04-06 | 上海天汉环境资源有限公司 | Emulsion wastewater treatment method and system |
-
2006
- 2006-06-30 CN CNB2006100145843A patent/CN100486921C/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105036258A (en) * | 2015-09-09 | 2015-11-11 | 陆秀英 | Application method of porous graphite electrode in industrial wastewater treatment |
| CN106145481A (en) * | 2016-08-31 | 2016-11-23 | 格斯瑞科技有限公司 | The apparatus and method of organic industrial sewage are processed based on cavitation technique |
| CN108203183A (en) * | 2018-01-23 | 2018-06-26 | 孙国芳 | A kind of sewage pretreatment device and processing method |
| CN109534546A (en) * | 2018-12-12 | 2019-03-29 | 江苏湖大化工科技有限公司 | A kind of processing method of phenol resin production waste water |
| CN112607962A (en) * | 2020-12-04 | 2021-04-06 | 上海天汉环境资源有限公司 | Emulsion wastewater treatment method and system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100486921C (en) | 2009-05-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101781054B (en) | Method for utilizing three-dimensional electrode coagulation combination to carry out advanced treatment on coking wastewater | |
| CN108793540A (en) | A kind of method of organic wastewater with difficult degradation thereby advanced treating | |
| CN1765779A (en) | Printing and dyeing wastewater recovery and disposal method | |
| CN1724420A (en) | Process for combined water treatment of chemical oxidizing-biological biological filtering tank | |
| CN101050044A (en) | Method for carrying out advanced treatment on papermaking sewage | |
| CN105016589B (en) | A kind of method of iron cement recycling | |
| CN107459170A (en) | A kind of method for removing fine chemistry industry biochemical treatment tail water toxicity | |
| CN100486921C (en) | Method for treating waste water in production of 4,6-dinitro o-sec-butyl phenol | |
| CN102583679A (en) | Method for treating petrochemical waste water and biochemical tail water through recycled coagulant | |
| CN210176671U (en) | High-salt high-concentration degradation-resistant organic wastewater treatment equipment | |
| CN103708596A (en) | Method for enhanced removal and recovery of nitrogen and phosphorus in traditional white spirit waste water treatment process | |
| CN101343129B (en) | Pretreatment technique for decolorization of wastewater at middle plate of paper-making pulping | |
| CN110963634A (en) | Advanced treatment method for papermaking wastewater | |
| CN105836968A (en) | Printing and dyeing wastewater treatment process | |
| CN104926033A (en) | Efficient treatment method for printing and dyeing wastewater | |
| CN102070263A (en) | Coking phenol cyanogen sewage treating method | |
| CN1396126A (en) | Process and gas-film air tower for treating hydrazine contained sewage generated in production of azodimethylamide | |
| CN110066044A (en) | A kind of sewage water treatment method of ozone-loaded catalyst concerted reaction | |
| CN102863114B (en) | Deep treatment method for pulping papermaking wastewater | |
| CN115784421A (en) | Method for promoting aerobic sludge granulation by adding Fenton iron mud | |
| CN102765799B (en) | Method of chain scission for high concentration persistent organic pollutants in wastewater | |
| CN107673522A (en) | A kind of coked waste water deep treatment method | |
| CN113582463A (en) | Direct-discharge treatment method for high-salinity fracturing flowback fluid | |
| CN106698860B (en) | Nitrobenzene wastewater treatment process | |
| CN111167453A (en) | Preparation method and application method of catalyst for removing ammonia nitrogen in water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090513 Termination date: 20110630 |