CN1260128C - Bauxite low temperature continuous dissolving out technology - Google Patents
Bauxite low temperature continuous dissolving out technology Download PDFInfo
- Publication number
- CN1260128C CN1260128C CN 200410035426 CN200410035426A CN1260128C CN 1260128 C CN1260128 C CN 1260128C CN 200410035426 CN200410035426 CN 200410035426 CN 200410035426 A CN200410035426 A CN 200410035426A CN 1260128 C CN1260128 C CN 1260128C
- Authority
- CN
- China
- Prior art keywords
- steam
- stripping
- desiliconization
- bauxite
- exhaust steam
- 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.)
- Active
Links
- 229910001570 bauxite Inorganic materials 0.000 title claims abstract description 27
- 238000005516 engineering process Methods 0.000 title abstract description 7
- 238000010438 heat treatment Methods 0.000 claims abstract description 18
- 239000002002 slurry Substances 0.000 claims abstract description 11
- 238000000034 method Methods 0.000 claims description 33
- 238000009413 insulation Methods 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 10
- 239000003518 caustics Substances 0.000 claims description 7
- 239000012530 fluid Substances 0.000 claims description 4
- 238000004090 dissolution Methods 0.000 claims description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 2
- 229910052782 aluminium Inorganic materials 0.000 claims description 2
- 230000003647 oxidation Effects 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 abstract description 19
- 238000004519 manufacturing process Methods 0.000 abstract description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 5
- 238000010924 continuous production Methods 0.000 abstract description 4
- 230000029087 digestion Effects 0.000 abstract 4
- 238000001704 evaporation Methods 0.000 abstract 3
- 230000002349 favourable effect Effects 0.000 abstract 2
- 238000009825 accumulation Methods 0.000 abstract 1
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 14
- TWNQGVIAIRXVLR-UHFFFAOYSA-N oxo(oxoalumanyloxy)alumane Chemical compound O=[Al]O[Al]=O TWNQGVIAIRXVLR-UHFFFAOYSA-N 0.000 description 12
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N iron oxide Inorganic materials [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 5
- NDLPOXTZKUMGOV-UHFFFAOYSA-N oxo(oxoferriooxy)iron hydrate Chemical compound O.O=[Fe]O[Fe]=O NDLPOXTZKUMGOV-UHFFFAOYSA-N 0.000 description 5
- 229910052814 silicon oxide Inorganic materials 0.000 description 5
- 238000002791 soaking Methods 0.000 description 5
- 239000000377 silicon dioxide Substances 0.000 description 4
- 229910001648 diaspore Inorganic materials 0.000 description 3
- 229910001679 gibbsite Inorganic materials 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 235000012239 silicon dioxide Nutrition 0.000 description 2
- 229910001388 sodium aluminate Inorganic materials 0.000 description 2
- 238000004131 Bayer process Methods 0.000 description 1
- 229910001593 boehmite Inorganic materials 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000011067 equilibration Methods 0.000 description 1
- FAHBNUUHRFUEAI-UHFFFAOYSA-M hydroxidooxidoaluminium Chemical compound O[Al]=O FAHBNUUHRFUEAI-UHFFFAOYSA-M 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical compound O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 description 1
- 229910052622 kaolinite Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000010453 quartz Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 229960001866 silicon dioxide Drugs 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
Images
Abstract
The present invention belongs to the technical field of alumina production, more specifically technology for continuously digesting bauxite under low temperatures. The present invention comprises the steps of channelized digestion, heat insulating desiliconization under pressure and self-evaporation temperature decrease. The temperature of slurry digested from a channel is from 135 to 150 DEG C, and exhaust steam of the self-evaporation temperature decrease is used for digestion preheating. The channelized digestion is indirect steam heating digestion, and a steam heating cavity is arranged outside a digesting channel, and the digesting channel wound spirally from bottom to top corresponds a feeding layer and is heated by steam condensed water, by secondary exhaust steam, primary exhaust steam and fresh steam. The technology for continuously digesting bauxite under low temperatures adopts indirect heating, so that the addition and accumulation of condensed water is avoided when slurry is heated directly. The present invention realizes continuous production, effectively utilizes the residual heat of steam condensed water and exhaust steam of the self-evaporation temperature decrease and reduces the steam consumption and the power consumption for production. The present invention has the advantages of simple operation and favorable economical and social benefits and is favorable to practical industrialized production.
Description
Technical field
The present invention relates to the dissolving-out process technology of bauxite in a kind of alumina producing, belong to technical field of alumina production.
Background technology
Bauxite is topmost raw material in the present alumina producing, be divided into gibbsite type, boehmite type, diaspore type and various mixed type, its character and mineral composition are determining the production method of aluminum oxide, and production method of alumina in the world mainly contains bayer's process, sintering process and integrated process now.External most of alumina producing producer adopts bayer's process to produce aluminum oxide owing to have gibbsitic bauxite mostly; China's bauxite resource is abundant, but the bauxite of having found mostly is diaspore type, and gibbsitic bauxite is very few, and therefore, utilizing the import gibbsitic bauxite to adopt bayer process to produce aluminum oxide is a kind of method of domestic production aluminum oxide.
The stripping operation is as one of most important operation of alumina producing, and main purpose is the aluminum oxide in the bauxite fully to be dissolved enter sodium aluminate solution, obtains high-quality dissolution fluid, enters the alumina producing subsequent processing.And the stripping operation has multiple dissolving-out method as the leading operation of alumina producing, and many bayer's process production lines all are to adopt high temperature stripping (the stripping temperature is 250-280 ℃), and facility investment is big, energy consumption is high.And bayer's process does not have special desiliconization process, but quartzy objectionable impurities as alumina producing must be removed to greatest extent, so adopt good technology to remove the silicon-dioxide particularly important that yet seems.
Steam one of consumes as the important energy source of stripping operation, and reducing steam consumption is the very effective approach that reduces the aluminum oxide manufacturing cost, rationally utilizes steam, and making the maximum usefulness of its performance also is simultaneously one of stripping operation problem that need solve.
Summary of the invention
The object of the present invention is to provide a kind of indirect heating, continuous production, energy-saving and cost-reducing, the simple to operate continuous dissolving-out process of bauxite low-temperature.
The continuous dissolving-out process of bauxite low-temperature of the present invention comprises the canalization stripping, is incubated desiliconization and self-evaporatint n. cooling under pressure, and the slurry temperature of pipeline stripping is 135-150 ℃, and the exhaust steam of self-evaporatint n. cooling is used for the stripping preheating.
The canalization stripping is indirect steam heating stripping, avoided adding in the direct heating slurry situation of long-pending water of condensation, realized continuous production again, the stripping pipeline has the heating steam chamber outward, the corresponding charging layer of coiled coil stripping pipe is from bottom to top heated by steam condensate, successively again by secondary exhaust steam heating, one-level exhaust steam heating and live steam heating.The stripping temperature is low, and the exhaust steam residual heat of steam condensate, self-evaporatint n. cooling is utilized effectively again, has reduced steam consumption, has reduced production energy consumption, has saved production cost.
Best design is that one deck of charging is heated by steam condensate, and second, third layer is with secondary exhaust steam heating from bottom to top, the 4th, layer 5 is with one-level exhaust steam heating, and uppermost four layers are heated with live steam.
The heating Steam Pressure Control of Circulated of pipeline stripping is that 0.55-0.75MPa is suitable.
Slurries after the stripping are incubated desiliconization in the pressure heat insulating jar, it is suitable that temperature and pressure is controlled to be 132-148 ℃, 0.3-0.5MPa respectively.
The insulation desiliconization is carried out successively by a 4-6 insulation jar series connection, realizes the continuous desiliconization of 4-6 level, and desiliconization effect is good, and the insulation jar is convenient to make and use control, and production cost is low.The top design that are incubated jar at different levels there is the gas equalizing pipe, each insulation tank top gas (incoagulability gas) is directly introduced next insulation jar, reach level balance at last, the operation of realization canful by equilibration tube.Simple, reliable and stable.
The technology of the present invention gibbsitic bauxite that suits grinds bauxite to become to contain admittedly and is 200-400g/l, fineness+100
#Enter the stripping pipeline after＜48% the qualified ore pulp, stripping rear oxidation aluminum concentration is 180-220g/l, and A/S value (being desiliconization index) is 180-190, and the dissolution fluid caustic ratio is 1.30-1.45.The insulation desiliconization time is controlled to be 45-60 minute, and the A/S value reaches 190-230.
Bauxite dissolving-out process of the present invention can obtain the measured sodium aluminate solution fluid of matter and carry out alumina producing under low consumed prerequisite.The technico-economical comparison that detects is: the stripping steam consumption is 1.45t/t-AO, and solubility rate is more than 98% relatively.With the pressure of each section temperature, live steam and the exhaust steam of the liquid level of pulp tank, canalization digester, the temperature of water of condensation, aperture of various by-pass valve controls etc., realize automatization control easily, can all introduce the watch-keeping cubicle and concentrate control automatically, simplify worker's operation, reduce manipulation strength.
Bauxite low-temperature dissolving-out process indirect heating of the present invention, continuous production, energy-saving and cost-reducing, simple to operate, help actual suitability for industrialized production, economic benefit and social benefit are considerable.
Description of drawings
Fig. 1, the simple and easy FB(flow block) of bauxite low-temperature dissolving-out process of the present invention.
Fig. 2, the simple and easy schema of insulation desilication process.
Embodiment
The present invention is further illustrated below in conjunction with embodiment.
Bauxite type selecting: gibbsite type, main component is: aluminum oxide 32-65%, and ferric oxide 7.0-20%, silicon oxide is less than 12%, alumina silica ratio is greater than 5, and the thing phase composite mainly is: gibbsite, rhombohedral iron ore, alumogoethite, kaolinite, quartz, anatase octahedrite and an a spot of diaspore.
Embodiment 1
The main component of bauxite is: aluminum oxide 52%, and ferric oxide 8.2%, silicon oxide 5.8%, alumina silica ratio 8.96, the treating processes of the continuous dissolving-out process of low temperature is as follows:
At first it is ground to become to contain admittedly and be 300g/l, fineness+100
#Be 45% qualified ore pulp, 65 ℃ of slurry temperatures are then with 150m
3The input speed of/h enters the canalization digester, the stripping pipeline has the heating steam chamber outward, the stripping pipe of coiled coil from bottom to top, one deck of its charging is heated by steam condensate, second, third layer heats with the secondary exhaust steam from bottom to top, four, layer 5 heats with the one-level exhaust steam, uppermost four layers of live steam heating with the 0.65MPa vapour pressure, after ore pulp is the tubular type stripping of 2m/s through flow velocity, 142 ℃ of drop temperatures, alumina concentration is 200g/l, and the A/S value is 183, and the solution caustic ratio is 1.40.Ore pulp enters 42m successively then
3Four insulation jars that are connected in series of the 0.4MPa pressure of size carry out continuous level Four insulation, soaking time 60 minutes, the gas equalizing pipe is arranged at the top of four insulation jars, the operation of realization canful, at this moment desiliconization index is 200, enter two-stage self-evaporatint n. cooling then, exhaust steam is further fully utilized.Amount to into aluminum oxide output 13.3t/h, the live steam consumption is 19t/h, and the steam consumption of stripping is 1.43t/t-AO.
The exsolution red mud composition is: aluminum oxide 23.1%, and ferric oxide 29.1%, silicon oxide 22.43%, alumina silica ratio 1.04, actual solubility rate are 88.39%.Theoretical solubility rate is 88.84%, and solubility rate is 99.49% relatively.
Embodiment 2
The main component of bauxite is: aluminum oxide 55%, and ferric oxide 8.8%, silicon oxide 5.6%, the treating processes of the continuous dissolving-out process of low temperature is as follows:
At first it is ground to become to contain admittedly and be 250g/l, fineness+100
#Be 40% qualified ore pulp, slurry temperature is 63 ℃, then with 150m
3The input speed of/h enters the canalization digester, live steam vapour pressure 0.60MPa, and after the process flow velocity was the tubular type stripping of 1.6m/s, drop temperature was 135 ℃, and alumina concentration is 210g/l, and the A/S value is 189, and the solution caustic ratio is 1.41.Ore pulp enters 42m successively then
3The 0.35MPa pressure heat insulating jar of size carries out continuous level Four insulation, and soaking time is 50 minutes, and at this moment desiliconization index is 210, enters two-stage self-evaporatint n. cooling then.
Other is substantially the same manner as Example 1.
Embodiment 3
The main component of bauxite is: aluminum oxide 58%, and ferric oxide 10.4%, silicon oxide 6.7%, the treating processes of the continuous dissolving-out process of low temperature is as follows:
At first it is ground to become to contain admittedly and be 340g/l, fineness+100
#Be 38% qualified ore pulp, slurry temperature is 65 ℃, then with 148m
3The input speed of/h enters the canalization digester, live steam vapour pressure 0.72MPa, and after the process flow velocity was the tubular type stripping of 1.8m/s, drop temperature was 145 ℃, and alumina concentration is 190g/l, and the A/S value is 185, and the solution caustic ratio is 1.38.Ore pulp enters 42m successively then
3The 0.46MPa pressure heat insulating jar of size carries out continuous level Four insulation, soaking time 55 minutes, and at this moment desiliconization index is 196, enters two-stage self-evaporatint n. cooling then.
Other is substantially the same manner as Example 1.
Embodiment 4
The treating processes of the continuous dissolving-out process of bauxite low-temperature of the present invention is as follows:
At first it is ground to become to contain admittedly and be 260g/l, fineness+100
#Be 30% qualified ore pulp, slurry temperature is 66 ℃, then with 160m
3The input speed of/h enters the canalization digester, live steam vapour pressure 0.70MPa, and after the process flow velocity was the tubular type stripping of 1.7m/s, drop temperature was 145 ℃, and alumina concentration is 200g/l, and the A/S value is 190, and the solution caustic ratio is 1.42.Enter 42m then
3The 0.42MPa pressure heat insulating jar of size carries out continuous Pyatyi insulation, and soaking time is 55 minutes, and at this moment desiliconization index is 220, enters two-stage self-evaporatint n. cooling then.
Other is substantially the same manner as Example 1.
Embodiment 5
The treating processes of the continuous dissolving-out process of bauxite low-temperature of the present invention is as follows:
At first it is ground to become to contain admittedly and be 330g/l, fineness+100
#Be 40% qualified ore pulp, slurry temperature is 62 ℃, then with 155m
3The input speed of/h enters the canalization digester, and after the process flow velocity was the tubular type stripping of 2.2m/s, drop temperature was 144 ℃, and alumina concentration is 210g/l, and the A/S value is 185, and the solution caustic ratio is 1.38.Ore pulp enters 42m successively then
3The 0.37MPa pressure heat insulating jar of size carries out continuous six grades of insulations, and soaking time is 60 minutes, and at this moment desiliconization index is 215, enters two-stage self-evaporatint n. cooling then.
Other is substantially the same manner as Example 1.
Claims (1)
1, the continuous dissolving-out process of a kind of bauxite low-temperature is characterized in that comprising the pipeline stripping, is incubated desiliconization and self-evaporatint n. cooling under pressure, and the slurry temperature of pipeline stripping is 135-150 ℃, and the exhaust steam of self-evaporatint n. cooling is used for the stripping preheating, and technological process is:
Gibbsitic bauxite ground to become to contain admittedly be 200-400g/l, enter the stripping pipeline after the qualified ore pulp of fineness+100#＜48%, the stripping pipeline has the heating steam chamber outward, one deck of the corresponding charging of coiled coil stripping pipe is from bottom to top heated by steam condensate, from bottom to top second, the 3rd layer is heated with the secondary exhaust steam, the 4th, layer 5 heats with the one-level exhaust steam, uppermost four layers are heated with live steam, the heating vapour pressure of pipeline stripping is 0.55-0.75MPa, stripping rear oxidation aluminum concentration is 180-220g/l, the A/S value is 180-190, and the dissolution fluid caustic ratio is 1.30-1.45;
The insulation desiliconization is carried out successively by a 4-6 insulation jar series connection, realize the continuous desiliconization of 4-6 level, the gas equalizing pipe is arranged at the top of insulation jars at different levels, guarantee level balance, the operation of realization canful, temperature, pressure and the time of insulation desiliconization is respectively 132-148 ℃, 0.3-0.5MPa, 45-60 minute, and the A/S value reaches 190-230.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410035426 CN1260128C (en) | 2004-07-23 | 2004-07-23 | Bauxite low temperature continuous dissolving out technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410035426 CN1260128C (en) | 2004-07-23 | 2004-07-23 | Bauxite low temperature continuous dissolving out technology |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1597524A CN1597524A (en) | 2005-03-23 |
| CN1260128C true CN1260128C (en) | 2006-06-21 |
Family
ID=34664204
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200410035426 Active CN1260128C (en) | 2004-07-23 | 2004-07-23 | Bauxite low temperature continuous dissolving out technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1260128C (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1865142B (en) * | 2005-05-18 | 2010-05-12 | 贵阳铝镁设计研究院 | Desilication and titanium removing process in leaching process |
| CN1865145B (en) * | 2005-05-19 | 2010-04-07 | 贵阳铝镁设计研究院 | Mine adding process after leaching in alumina production |
| CN1730393A (en) * | 2005-07-18 | 2006-02-08 | 贵阳铝镁设计研究院 | High ferro trihydrate bauxite dissolving-out technology |
| CN100398444C (en) * | 2006-07-14 | 2008-07-02 | 中国铝业股份有限公司 | Method of retarding leaching scaling of low temperature pipeline |
| CN102234122A (en) * | 2010-04-23 | 2011-11-09 | 贵阳铝镁设计研究院有限公司 | Method for using steam to supply heat for pipeline digestion and apparatus thereof |
| CN103101942B (en) * | 2011-11-15 | 2015-06-03 | 沈阳铝镁设计研究院有限公司 | Process for efficiently utilizing secondary steam in dissolution procedure |
| CN106145166B (en) * | 2015-03-23 | 2018-01-12 | 沈阳铝镁设计研究院有限公司 | A kind of alumina producing mesohigh dissolution heat integration Application way and device |
| CN106542553B (en) * | 2015-09-21 | 2018-05-22 | 沈阳铝镁设计研究院有限公司 | A kind of dissolving-out process method of hydrargillite in alumina producing |
-
2004
- 2004-07-23 CN CN 200410035426 patent/CN1260128C/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN1597524A (en) | 2005-03-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1260128C (en) | Bauxite low temperature continuous dissolving out technology | |
| CN101767806B (en) | Dissolving-out process for large-sized pipeline remaining tank of diasporite bauxite ore | |
| CN102020299B (en) | Method for producing industrial activated aluminum oxide from pulverized fuel ash | |
| CN101475172A (en) | Recycling, purifying and classifying technology for high purity superfine silicon carbide micro powder | |
| CN102249271B (en) | Tube array and remaining tank dissolving-out system and method for gibbsite bauxite | |
| CN102502722A (en) | Preparation method of high-purity magnesium oxide | |
| CN113979457A (en) | Dealkalization method for Bayer process red mud | |
| CN112551658A (en) | High-alumina fly ash defluorination flocculant and preparation method and application thereof | |
| CN101280354A (en) | Environment-friendly alumyte synthesized smelting technical solution | |
| CN102583461B (en) | Device and method for preheating by utilizing steam condensate water for aluminum oxide high-pressure digestion process | |
| CN101209844B (en) | Technique for preparing high quality boric acid from salt lake type boron ore by one-step method | |
| CN1477059A (en) | Preparation method of nano alumina material | |
| CN102009990A (en) | Method for leaching bauxite ore pulp | |
| CN102502701B (en) | Production process and preparation method of ultrapure ammonia | |
| CN101880772B (en) | Method for recycling magnesium from magnesium-containing waste solution | |
| CN1155521C (en) | Directly heating and decomposing plate heat exchanging technology for alumina laterite washing | |
| CN203593633U (en) | Energy-saving salt and nitre co-production device | |
| CN1865145B (en) | Mine adding process after leaching in alumina production | |
| CN103172060B (en) | Continuous industrialized natural graphite purification equipment | |
| CN203513310U (en) | Rectifying separating system of hydrochloric acid wastewater | |
| Zhao et al. | The trends of Chinese alumina production with combined process | |
| CN1775686A (en) | Method for producing alumina by adding ore and concentrating after hydraulic aluminous stone type bauxite stripping | |
| CN1267354C (en) | Desilication method for sodium aluminate solution with high concentration | |
| CN101746794A (en) | Method for preparing high caustic sodium aluminate solution from low caustic sodium aluminate solution | |
| Songqing | Bayer process efficiency improvement |
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 | ||
| ASS | Succession or assignment of patent right |
Owner name: CHINESE ALUMINIUM CO., LTD. Free format text: FORMER OWNER: SHANDONG ALUMINIUM INDUSTRY CO., LTD. Effective date: 20071026 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20071026 Address after: 100082 No. 62 North Main Street, Beijing, Xizhimen Patentee after: Aluminum Corporation of China Limited Address before: 255052 No. 1, five km road, Zhangdian District, Shandong, Zibo Patentee before: Shandong Aluminium Industry Co., Ltd. |