CN102259934B - Oxidization process for producing high-density spherical cobaltosic oxide by virtue of low temperature liquid phase precipitation - Google Patents
Oxidization process for producing high-density spherical cobaltosic oxide by virtue of low temperature liquid phase precipitation Download PDFInfo
- Publication number
- CN102259934B CN102259934B CN 201110126672 CN201110126672A CN102259934B CN 102259934 B CN102259934 B CN 102259934B CN 201110126672 CN201110126672 CN 201110126672 CN 201110126672 A CN201110126672 A CN 201110126672A CN 102259934 B CN102259934 B CN 102259934B
- Authority
- CN
- China
- Prior art keywords
- cobalt
- slip
- tank
- pure water
- add
- 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.)
- Expired - Fee Related
Links
Images
Landscapes
- Inorganic Compounds Of Heavy Metals (AREA)
Abstract
The invention relates to a process for producing high-density spherical cobaltosic oxide by virtue of low temperature liquid phase precipitation oxidization. The process comprises the following steps of: firstly preparing a cobalt chloride solution with the cobalt content of 60-75g/l and a sodium hydroxide solution with the concentration of 100-120g/l, adding the two solutions into a reaction tank in a parallel flow mode, introducing the air to carry out a synthetic reaction, controlling the reaction temperature to be 35-50 DEG C and pH value to be 11.3-12.5, and reacting for 10-20 minutes; adding EDTA (ethylene diamine tetraacetic acid) into an ageing tank according to the ratio of cobalt to EDTA being 100: (1-5) while ageing, and then filtering, slurrying and washing after ageing so as to obtain a wet cobaltosic oxide solid, and finally calcining the wet cobaltosic oxide in a calcining furnace for 3-5 hours at the temperature of 300-500 DEG C, taking out the cobaltosic oxide, and sieving to obtain cobaltosic oxide powder. In the invention, the production process is controllable, the product has uniform particle size distribution, good uniformity, spherical appearance and good dispersity and stability, the recovery rate is high, the energy source and resource are saved, the production cost is low, the compaction specific gravity is high, and the reliable safety performance is obtained.
Description
Technical field
The present invention relates to the tricobalt tetroxide production method that the production such as a kind of novel material making method, especially battery material, catalyzer, magneticsubstance, electronic material, Wimet are used.
Background technology
Existing process for producing cobaltic-cobaltous oxide mainly is that cobalt salt is made cobalt oxalate or cobaltous carbonate, cobalt oxalate or cobaltous carbonate after drying again high temperature sintering become tricobalt tetroxide.The technical process of this working method is long, and the rate of recovery is low, tooling cost is high, waste energy and resource.In addition, this technique easily causes the product particle skewness, and consistence is poor, is unfavorable for the large-scale production of product and stablizing of quality.
Another kind of process for producing cobaltic-cobaltous oxide is the mode that adopts the solution pyroreaction, its technical process has pyroreaction, ageing, press filtration, washing, the oven dry of cobalt liquid, Alkali liquid compounding, 60～75 ℃ of temperature, the operation such as calcine, sieve, still there is technical process length, consumes the many defectives of the energy, and the loose density to product in the production process is wayward, easily cause product particle inhomogeneous, product pattern (dendroid, sheet, bar-shaped etc.) of all kinds, both lack of standardization, inhomogeneous again.
Summary of the invention
The purpose of this invention is to provide a kind of high-density spherical cobaltic-cobaltous oxide low temperature liquid phase precipitation oxidizing process, accomplish that technical process is short, save energy, the controllability of improving the quality of products and stability.
Production stage of the present invention is as follows:
1, preparation cobalt chloride liquid liquid
Cobalt contents control index according to cobalt contents, Preparation tank nominal volume and the cobalt liquor to be prepared of cobalt chloride solution raw material, calculate the add-on of cobalt chloride solution raw material, it is added Preparation tank, open agitating vane, add pure water to Preparation tank nominal volume absolute altitude place, stirred 5～10 minutes, solution is fully mixed, the control cobalt contents is 60～75g/l; Add hydrochloric acid, carry out chemical analysis after adjusting pH and be 2.0～3.0, measure cobalt contents.
2, preparation sodium hydroxide solution
In Preparation tank, add half groove pure water, open agitating vane, slowly add sodium hydrate solid, add-on is pressed sodium hydroxide solution control index and is calculated, and opens cap relief valve, regulating temperature is 30～45 ℃, after sodium hydroxide is dissolved fully, add again pure water to Preparation tank nominal volume absolute altitude place, stirred 5～10 minutes, solution is fully mixed, and controlling its concentration is 100～120g/l.
3, building-up reactions
With cobalt chloride solution and sodium hydroxide solution respectively with 1500～2000l/h flow and 1600～2000l/h flow simultaneously and stream flow in the reactive tank, passing into flow in the reaction solution is 10～15m
3The air of/h, the control temperature of reaction is that 35～50 ℃, pH value are 11.3～12.5, reacts after 10～20 minutes in the slip inflow ageing tank; At this moment according to the throughput ratio of ageing tank nominal volume, cobalt chloride solution and sodium hydroxide solution, the cobalt chloride solution cobalt contents that analysis records, calculate the total content of cobalt in the slip, according to cobalt: EDTA=100: 1～5 ratio adds chemical reagent EDTA in ageing tank, digestion time is 20～25 minutes, impel grain growing even, granule-morphology is more complete;
4, once filtration, pulp
Slip in the ageing tank is all pumped into the 1# pressure filter, at first compress filter plate, make slip after press filtration, become filter cake; Unclamp filter plate and unload filter cake, then begin pulp; Add pure water in the first past 1# slurrying tank and flood agitating vane, toward the interior filter cake that slowly adds of 1# slurrying tank, the limit adds the pure water limit stirred 25～30 minutes, and filter cake is broken up fully, namely finished the pulp first time when opening agitating vane; In the 1# medial launder, add 1.5m in advance again
3Temperature is 35～50 ℃ hot pure water, opens 1# medial launder agitating vane, then slip in the 1# slurrying tank is entered in the 1# medial launder; When slip in the 1# medial launder reaches specified molten long-pending absolute altitude place, slip is pumped into the 2# pressure filter, pump limit, limit adds 30～50 ℃ of hot pure water, until slip all is pumped to the 2# pressure filter in the 1# medial launder.
5, secondary filtration, pulp and washing
Dismounting 2# cake of filter-press carries out the pulp second time, and concrete operations are identical with for the first time pulp; After for the second time pulp slip in the 2# slurrying tank is entered the 2# medial launder that is added with in advance hot pure water, when slip reaches rated value in the 2# medial launder, slip is pumped into the 3# pressure filter, pump limit, limit adds 35～50 ℃ of pure hot water, until slip all is pumped to the 3# pressure filter in the 2# medial launder; After the press filtration of 3# pressure filter finishes, with 35～50 ℃ of hot pure water washing leaching cakes 20～30 minutes, until washing should be less than 0.05g/l with the chloride ion content in the silver nitrate titration detection filtrate at this moment to without white precipitate, namely obtain pure wet tricobalt tetroxide solid.
6, calcining
The tricobalt tetroxide that will wet is packed into and is calcined in the boat, and 1～2.5 kilogram in every boat is sent into calcining furnace and calcined, and calcining temperature is 300～500 ℃, calcines and takes out dry tricobalt tetroxide after 3～5 hours, obtains cobaltosic oxide powder after sieving.
Compared with the prior art, the present invention has following characteristics:
1, production process is controlled, constant product quality
Owing to can carry out Effective Regulation by important parameters such as temperature (35～50 ℃), pH value, air flow quantity, EDTA add-ons in the production process, so product particle is evenly distributed, high conformity, pattern are the class sphere, have good dispersiveness and stability.
2, the rate of recovery is high, save energy and resource, and production cost is low
The present invention need not be dry and the tricobalt tetroxide that directly will wet is sent into calcining furnace and calcined, shortened process, improved the rate of recovery, the rate of recovery is higher more than 5% than traditional technology, the preparation of adding cobalt liquid, alkali lye need not high temperature, save energy, so production cost is low, reduces production costs more than 10%.
3, safety performance is good
Because the jolt ramming proportion of product is high, can reach 2.3～2.7g/cm
3(jolt ramming proportion＜the 2.3g/cm of common tricobalt tetroxide
3), therefore have stronger high temperature resistance, anti-flatulence, anti-overshoot ability, thereby have reliable safety performance.Use feedback through battery producer: with the cobalt acid lithium battery of products production of the present invention, chemical property is more superior, has higher mistake to charge and discharge performance, better high-temperature behavior, longer cycle life.That is to say that product of the present invention has been established solid raw material basis for improving battery quality.
Description of drawings
Fig. 1 is powder metallurgy product quality supervision and test center W201011-16 number " four oxidations, two cobalt test checks report ".
Fig. 2 is the tricobalt tetroxide product structure figure that the present invention produces.
Embodiment
Embodiment one
Production stage is the same, repeats no more herein.Adjusting parameter in each step is as follows:
1, the cobalt contents of the cobalt chloride solution of preparation is 65g/l, and the pH value is 2.2.
2, the concentration of sodium hydroxide solution of preparation is 108g/l, and regulating temperature is 38 ℃.
3, in the synthetic reaction process: the cobalt chloride solution flow is 1500l/h, and the sodium hydroxide flow is 1600l/h, and air flow quantity is 12m
3/ h, temperature of reaction is 35 ℃, pH value 11.5,12 minutes reaction times; When the ageing tank nominal volume is 5m
3The time (as follows), the EDTA add-on is 5.6 kilograms, digestion time 22 minutes.
4, in pulp, washing process, use 35 ℃ of pure hot water.
5, in calcination process, wet tricobalt tetroxide loading capacity is 1.5 kilograms/boat, 350 ℃ of calcining temperatures, calcination time 3.5 hours.
Embodiment two
This example is basic identical with embodiment one, is that following adjusting parameter is different:
1, the cobalt contents of the cobalt chloride solution of preparation is 70g/l, pH value 2.5.
2, the preparation concentration of sodium hydroxide solution is 110g/l, regulates 40 ℃ of temperature.
3, in the synthetic reaction process: the flow of cobalt chloride solution and sodium hydroxide solution all is 1700l/h, and air flow quantity is 13m
3/ h, 37 ℃ of temperature of reaction, pH value 12.2, EDTA add-on are 7 kilograms, digestion time 25 minutes.
4, in pulp, washing process, use 37 ° of pure hot water.
5, in calcination process, wet tricobalt tetroxide loading capacity is 1.8 kilograms/boat, 450 ℃ of calcining temperatures, calcination time 4.5 hours.
Embodiment three
This example is basic identical with embodiment one, is that following adjusting parameter is different:
1, the cobalt contents of the cobalt chloride solution of preparation is 75g/l, pH value 3.0.
2, the concentration of sodium hydroxide solution of preparation is 120g/l, regulates temperature 45 C.
3, in the synthetic reaction process, the flow of cobalt chloride solution and sodium hydroxide solution all is 2000l/h, and air flow quantity is 15m
3/ h, 50 ℃ of temperature of reaction, pH value 12.5, EDTA add-on are 1.88 kilograms, digestion time 25 minutes.
4, in pulp, washing process, use 50 ℃ of pure hot water.
5, in calcination process, wet tricobalt tetroxide loading capacity is 2.5 kilograms/boat, calcination time 5 hours.
Embodiment four
This example is basic identical with embodiment one, is that following adjusting parameter is different:
1, the cobalt contents of the cobalt chloride solution of preparation is 60g/l, pH value 2.0.
2, the concentration of sodium hydroxide solution of preparation is 100g/l, and regulating temperature is 30 ℃.
3, in the synthetic reaction process, the flow of cobalt chloride solution and sodium hydroxide solution all is 1800l/h, and air flow quantity is 10m
3/ h, 35 ° of temperature of reaction, pH value 11.3, EDTA add-on are 7.5 kilograms, digestion time 20 minutes.
4, in pulp, washing process, use 35 ℃ of pure hot water.
5, in calcination process, wet tricobalt tetroxide loading capacity is 1 kilogram/boat, calcination time 3 hours.
Claims (1)
1. a high-density spherical cobaltic-cobaltous oxide low temperature liquid phase precipitates the oxidation production technique, it is characterized in that production stage is as follows:
A, preparation cobalt chloride solution
Cobalt contents control index according to cobalt contents, Preparation tank nominal volume and the cobalt liquor to be prepared of cobalt chloride solution raw material, calculate the add-on of cobalt chloride solution raw material, it is added Preparation tank, open agitating vane, add pure water to Preparation tank nominal volume absolute altitude place, stirred 5～10 minutes, solution is fully mixed, the control cobalt contents is 60～75g/l; Adding hydrochloric acid, adjusting pH is to carry out chemical analysis after 2.0～3.0, measure cobalt contents;
B, preparation sodium hydroxide solution
In Preparation tank, add half groove pure water, open agitating vane, slowly add sodium hydrate solid, add-on is pressed sodium hydroxide solution control index and is calculated, and opens cap relief valve, regulating temperature is 30～45 ℃, after sodium hydroxide is dissolved fully, add again pure water to Preparation tank nominal volume absolute altitude place, stirred 5～10 minutes, solution is fully mixed, and controlling its concentration is 100～120g/l;
C, building-up reactions
With cobalt chloride solution and sodium hydroxide solution respectively with 1500～2000l/h flow and 1600～2000l/h flow simultaneously and stream flow in the reactive tank, passing into flow in the reaction solution is 10～15m
3The air of/h, the control temperature of reaction is 35～50 ℃, pH value is 11.3～12.5, reacts after 10～20 minutes in the slip inflow ageing tank; At this moment according to the throughput ratio of ageing tank nominal volume, cobalt chloride solution and sodium hydroxide solution, the cobalt chloride solution cobalt contents that analysis records, calculate the total content of cobalt in the slip, according to cobalt: EDTA=100: 1～5 ratio adds chemical reagent EDTA in ageing tank, digestion time is 20～25 minutes, impel grain growing even, granule-morphology is more complete;
D, once filtration, pulp and washing
Slip in the ageing tank is all pumped into the 1# pressure filter, at first compress filter plate, make slip after press filtration, become filter cake; Follow washing leaching cake, unclamp filter plate and unload filter cake, then begin pulp: flood agitating vane toward the interior pure water that adds of 1# slurrying tank first, in the 1# slurrying tank, slowly add filter cake when opening agitating vane, the limit adds the pure water limit and stirred 25～30 minutes, filter cake is broken up fully, namely finished for the first time pulp; In the 1# medial launder, add 1.5m in advance again
3Temperature is 35～50 ℃ hot pure water, opens 1# medial launder agitating vane, then slip in the 1# slurrying tank is entered in the 1# medial launder; When slip in the 1# medial launder reaches nominal volume absolute altitude place, slip is pumped into the 2# pressure filter, pump limit, limit adds 30～50 ℃ hot pure water, until slip is all pumped into the 2# pressure filter in the 1# medial launder;
E, secondary filtration, pulp and washing
Dismounting 2# cake of filter-press carries out the filtration second time, pulp, and concrete operations are identical with for the first time pulp; After for the second time pulp slip in the 2# slurrying tank is entered the 2# medial launder that is added with in advance hot pure water, when slip reaches nominal volume in the 2# medial launder, slip is pumped into the 3# pressure filter, and pump limit, limit adds 35～50 ℃ of hot pure water, until the slip in the 2# medial launder all is pumped to the 3# pressure filter; After the press filtration of 3# pressure filter finishes, with 35～50 ℃ of hot pure water washing leaching cakes 20～30 minutes, until washing should be less than 0.05g/l with the chloride ion content in the silver nitrate titration detection filtrate at this moment to without white precipitate, namely obtain pure wet tricobalt tetroxide solid;
F, calcining
The tricobalt tetroxide that will wet is packed into and is calcined in the boat, and 1～2.5 kilogram in every boat is sent into calcining furnace and calcined, and calcining temperature is 300～500 ℃, calcines and takes out dry tricobalt tetroxide after 3～5 hours, obtains cobaltosic oxide powder after sieving.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110126672 CN102259934B (en) | 2011-05-17 | 2011-05-17 | Oxidization process for producing high-density spherical cobaltosic oxide by virtue of low temperature liquid phase precipitation |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201110126672 CN102259934B (en) | 2011-05-17 | 2011-05-17 | Oxidization process for producing high-density spherical cobaltosic oxide by virtue of low temperature liquid phase precipitation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102259934A CN102259934A (en) | 2011-11-30 |
| CN102259934B true CN102259934B (en) | 2013-02-06 |
Family
ID=45006809
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201110126672 Expired - Fee Related CN102259934B (en) | 2011-05-17 | 2011-05-17 | Oxidization process for producing high-density spherical cobaltosic oxide by virtue of low temperature liquid phase precipitation |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102259934B (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102689933A (en) * | 2012-03-15 | 2012-09-26 | 湖南红太阳电源新材料股份有限公司 | Method for producing hydroxy cobalt oxide |
| CN103359794B (en) * | 2012-03-30 | 2016-09-14 | 北京当升材料科技股份有限公司 | A kind of spherical cobaltic-cobaltous oxide and preparation method thereof |
| CN103771539B (en) * | 2012-10-19 | 2015-11-18 | 宁波金和锂电材料有限公司 | A kind of method and device preparing Large stone spherical cobaltic-cobaltous oxide |
| CN103964514A (en) * | 2013-01-29 | 2014-08-06 | 宁波科博特钴镍有限公司 | Preparation method of regular octahedron-type cobaltosic oxide |
| CN104058468A (en) * | 2013-03-19 | 2014-09-24 | 南通瑞翔新材料有限公司 | Compact spherical cobalt oxide and preparation method thereof |
| CN106340643A (en) * | 2015-07-10 | 2017-01-18 | 北京当升材料科技股份有限公司 | Method for preparing large-grain spherical cobaltosic oxide |
| CN105129869B (en) * | 2015-08-28 | 2017-03-01 | 上饶市鼎鑫金属化工有限公司 | A kind of spherical big particle diameter hydroxy cobalt oxide no ammonia continuous production technology |
| CN108862405A (en) * | 2017-05-15 | 2018-11-23 | 江苏凯力克钴业股份有限公司 | A kind of preparation method and device of low sodium cobaltosic oxide |
| CN109354075B (en) * | 2018-09-30 | 2020-10-09 | 衢州华友钴新材料有限公司 | Preparation method of small-particle-size uniformly-aluminum-doped spherical cobaltosic oxide |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101269848A (en) * | 2008-03-05 | 2008-09-24 | 广州融捷材料科技有限公司 | High-density spherical cobaltic-cobaltous oxide and method for preparing the same |
| CN101434416A (en) * | 2008-11-28 | 2009-05-20 | 宁波金和新材料有限公司 | Hydroxy spherical cobaltosic oxide and preparation thereof |
| CN101434417A (en) * | 2008-11-28 | 2009-05-20 | 宁波金和新材料有限公司 | Dry preparation of battery grade spherical cobaltosic oxide particle |
| CN101982421A (en) * | 2010-10-21 | 2011-03-02 | 江苏东新能源科技有限公司 | Preparation method of nano cobalt oxide |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20050142058A1 (en) * | 2003-12-30 | 2005-06-30 | Industrial Technology Research Institute | Low temperature process for preparing tricobalt tetraoxide |
-
2011
- 2011-05-17 CN CN 201110126672 patent/CN102259934B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101269848A (en) * | 2008-03-05 | 2008-09-24 | 广州融捷材料科技有限公司 | High-density spherical cobaltic-cobaltous oxide and method for preparing the same |
| CN101434416A (en) * | 2008-11-28 | 2009-05-20 | 宁波金和新材料有限公司 | Hydroxy spherical cobaltosic oxide and preparation thereof |
| CN101434417A (en) * | 2008-11-28 | 2009-05-20 | 宁波金和新材料有限公司 | Dry preparation of battery grade spherical cobaltosic oxide particle |
| CN101982421A (en) * | 2010-10-21 | 2011-03-02 | 江苏东新能源科技有限公司 | Preparation method of nano cobalt oxide |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102259934A (en) | 2011-11-30 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102259934B (en) | Oxidization process for producing high-density spherical cobaltosic oxide by virtue of low temperature liquid phase precipitation | |
| CN102745662B (en) | Preparation method of amorphous iron phosphate | |
| CN102689933A (en) | Method for producing hydroxy cobalt oxide | |
| CN101913659B (en) | Battery-grade cobaltosic oxide preparation method | |
| CN110098406A (en) | A kind of preparation method with high compacted density high capacity LiFePO4 | |
| CN109942030B (en) | Preparation method of high-density small-particle-size spherical cobaltosic oxide | |
| CN106587170A (en) | Preparation method of cobaltosic oxide with rare earth element doped body phase | |
| CN110534719A (en) | A kind of preparation method for mixing magnalium nickel manganese spherical cobaltic-cobaltous oxide | |
| CN101920948A (en) | Method for preparing granularity controllable ferric orthophosphate powder | |
| CN110451587A (en) | A kind of ternary precursor preparation system | |
| CN108539127A (en) | A kind of continuous device and method for preparing ternary material | |
| CN101850955A (en) | Method for preparing spherical iron phosphate grains | |
| CN102790214B (en) | Method for preparing lithium iron phosphate | |
| CN107673415A (en) | Utilize the nickel oxide method that Ore Leaching prepares nickel sulfate at high temperature under high pressure | |
| CN102115214B (en) | Method for preparing small-particle-size cobalt carbonate | |
| CN104843787A (en) | Preparation method of cubic lanthanum zirconate nanometer monocrystal | |
| CN104577100A (en) | Method for preparing lithium ion secondary battery positive electrode material LiNi0.5Co0.2Mn0.3O2 by adding high-polymer saccharides as forming media | |
| CN103172125A (en) | Production method of cobaltosic oxide | |
| CN111892094A (en) | Mass production method of low-impurity and high-solubility basic cobalt carbonate | |
| CN112830526B (en) | Method for regenerating ternary precursor by using nickel-cobalt-manganese slag | |
| CN208385525U (en) | A kind of equipment continuously preparing ternary material | |
| CN102070179B (en) | Method for preparing spherical carbonate ternary precursor | |
| CN110697801B (en) | Preparation method and device of transition metal lithium oxide | |
| CN111029550A (en) | Surface modification method of high-nickel cathode material of lithium ion battery | |
| CN104403373A (en) | Method for preparing pigment-class chrome oxide green by adopting microwave heating |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Owner name: HU NAN REDSUN NEW MATERIALS CO., LTD. Free format text: FORMER OWNER: ZHOU HONGYANG Effective date: 20120522 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20120522 Address after: Loudi City, Hunan Province Wan Bao 417007 Louxing District Xin Zhi Cun Applicant after: Hunan Red Sun Power Supply New Material Co.,Ltd. Address before: 417007 Hunan city of Loudi province Loudi Wanbao town red sun power new material company Applicant before: Zhou Hongyang |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: ZHOU HONGYANG Free format text: FORMER OWNER: HU NAN REDSUN NEW MATERIALS CO., LTD. Effective date: 20150814 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20150814 Address after: 417007 Loudi City, Hunan Province Yue Ping Yin Tong District Six neighborhood offices Patentee after: Zhou Hongyang Address before: Loudi City, Hunan Province Wan Bao 417007 Louxing District Xin Zhi Cun Patentee before: Hunan Red Sun Power Supply New Material Co.,Ltd. |
|
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130206 Termination date: 20150517 |
|
| EXPY | Termination of patent right or utility model |