CN101509073A - Solvent extraction of ferronickel powder and waste liquor processing method - Google Patents
Solvent extraction of ferronickel powder and waste liquor processing method Download PDFInfo
- Publication number
- CN101509073A CN101509073A CNA2009100942435A CN200910094243A CN101509073A CN 101509073 A CN101509073 A CN 101509073A CN A2009100942435 A CNA2009100942435 A CN A2009100942435A CN 200910094243 A CN200910094243 A CN 200910094243A CN 101509073 A CN101509073 A CN 101509073A
- Authority
- CN
- China
- Prior art keywords
- nickel
- leaching
- waste liquid
- ferronickel powder
- ferronickel
- 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.)
- Pending
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/20—Recycling
Abstract
The invention relates to a method for leaching nickel/iron powder and treating waste liquor thereof, in particular to a method for acid-leaching nickel/iron powder and treating nickel-precipitating waste liquor, belonging to the field of non-ferrous metallurgy. The method comprises the following steps: adding hydrochloric acid solution to the nickel/iron powder; heating; feeding air or oxygen for leaching; adding a nickel-precipitating agent to the leaching solution to precipitate nickel ions into nickel sulfide and obtaining the nickel-precipitating waste liquor containing chlorides at the same time; returning part of the nickel-precipitating waste liquor to the step of leaching the nickel/iron powder, atomizing the remaining waste liquor and mixing the atomized waste liquor with hot gases containing chlorine hydride; drying to obtain solid chlorides and gases containing chlorine hydride; absorbing and rinsing the gases containing chlorine hydride to output the chlorine hydride solution, and returning the chlorine hydride solution to the step of leaching the nickel/iron powder; and decomposing the solid chlorides into oxides and the hot gases containing chlorine hydride through calcinations. The method has the advantages of simple process, high recovery rate of nickel and cobalt and high production efficiency; chlorine hydride, as the leaching agent of the nickel/iron powder, can be recycled, therefore, the cost is low; and the method realizes zero discharge of the waste water, thereby preventing the environment from being polluted.
Description
Technical field
The invention belongs to the Non-ferrous Metallurgy field, relate to the method for the processing of the acidleach of ferronickel powder and heavy nickel waste water.
Background technology
It is one of main treatment process of red soil nickel ore that fire reduction melting output Rhometal and reduction-mill select the output ferronickel powder, disclosed technological process has: send the dry kiln drying after (1) ore reduction, send calcination rotary kiln again, under 700 ℃ of temperature, drying, preheating and calcining, the output calcining; After calcining adds electric furnace, under the temperature about 1500 ℃, add reductive agent retailoring then, the thick Rhometal of output, (2) red soil nickel ore is through fragmentation, by a certain percentage, adding reductive agent, additive mix with laterite, system ball after drying, in metallurgical furnaces such as rotary kiln or rotary hearth furnace, tunnel furnace 950～1300 ℃ of following reducing roastings, the calcining fragmentation, through magnetic separation, gravity treatment, obtain nickeliferous 7～15% ferronickel powders; (3) red soil nickel ore adds reductive agent and chlorizating agent and mixes with laterite through fragmentation, and 950～1000 ℃ of following chlorination segregation-reducing roastings, the calcining fragmentation through magnetic separation, gravity treatment, obtains nickeliferous 7～15% ferronickel powders after the system ball drying.
The research of the output of red soil nickel ore reduction both at home and abroad ferronickel is a lot, and its emphasis is the production method of ferronickel or ferronickel powder.Ferronickel powder is the primary products that red soil nickel ore is smelted, nickel content low (being generally 3～10%), impurity height, need further refining to improve nickel content, after adding yellow soda ash or lime carbonate desulfurization, going into quartzy flux and impurity such as calcium oxide dephosphorization under oxidizing atmosphere, silicon, obtain refining ferronickel product, or as producing stainless furnace charge.
The acidleach processing aspect of ferronickel, Liu Xi light etc. disclose a kind of method of producing single nickel salt with nickel-clad iron sheet waste material (nickeliferous 15%) in the electronic industry in " hydrometallurgy " 2000 the 4th phases, its process is: nickel plating scrap iron sheet is cleaned back adding sulphuric acid soln and the dissolved ferric iron in the waste material is removed remaining nickel and small amounts of iron H
2SO
4+ HNO
3Mixed-acid dissolution obtains crude nickle sulphate behind filtration, the condensing crystal, after crude nickle sulphate is dissolved in water, adds in the alkali and deironing, filters back condensing crystal output single nickel salt product.This method is a raw material with the nickel-clad iron sheet waste material of electronic industry, and iron removal need repeatedly add sulphuric acid soln, and sulfuric acid consumption is big; The oxynitride that mixed-acid dissolution nickel acid consumption is high, reaction produces needs further to handle; Leaching agent can not be regenerated.
The Chinese patent CN101230422 method of enriching nickel and coproduction iron oxide red " a kind of from red soil nickel ore " has mentioned that a kind of red soil nickel ore selects the treatment process of the thick ferronickel powder of output through rotary hearth furnace reduction-mill, its process is: after thick ferronickel powder adds the sulphuric acid soln pulp, add heating in the autoclave pressure, logical oxygen pressurization leaching, the leached mud washing back that obtains is as the byproduct iron oxide red, leach liquor adds in the sodium hydroxide solution and heavy nickel, obtains the heavy nickel waste liquid of nickel hydroxide solid and contains sodium sulfate.This method nickel direct yield reaches 70～75%, iron oxide red iron content 62～68%, and the iron yield can reach 70～75%, but leaching agent sulfuric acid can not recycle, and there is certain environmental pollution problems in the waste liquid of the heavy a large amount of sulfur-bearing hydrochlorates of nickel process output.
Summary of the invention
The purpose of this invention is to provide a kind of leaching of ferronickel powder and the treatment process of waste liquid, have that technical process is short, leaching agent hydrochloric acid can be recycled, with low cost, non-wastewater discharge, characteristics such as environmentally safe.
Realize that the technical scheme that above-mentioned purpose of the present invention adopted is: add hydrochloric acid soln and heating, bubbling air or oxygen leaching in ferronickel powder, leach liquor adds heavy nickel agent nickel ion is precipitated as nickelous sulfide, and obtains the heavy nickel waste liquid of chloride simultaneously; Heavy nickel waste liquid partly returns the leaching of ferronickel powder, and mix with the hot gas that contains hydrogenchloride its waste liquid atomizing back, obtains chloride solids and the gas that contains hydrogenchloride after the drying; The gas of hydrogenchloride is through the leaching that absorbs, washing output hydrochloric acid soln returns ferronickel powder, and chloride solids is decomposed into oxide compound and described hydrogenchloride hot gas through roasting.
Concrete technical scheme of the present invention also comprises:
(1) is raw material with nickeliferous 5～30%, granularity 200 purpose ferronickel powders, adds 1～6 times hydrochloric acid soln of nickel theoretical amount in the ferronickel powder, under the liquid-solid ratio 3～8:1 of volume and quality condition, leach;
(2) 30%～70% of the heavy nickel waste liquid of the chloride leaching of returning ferronickel powder, the heavy nickel waste liquid atomizing of residue back and temperature are that 400～800 ℃ the hot gas that contains hydrogenchloride directly mixes, and this gas is through absorbing, wash the leaching that the output hydrochloric acid soln returns ferronickel powder;
(3) chloride solids is in rotary kiln internal heating to 600 ℃～1000 ℃ of roastings, obtains temperature and be the chloride waste liquid drying that 400～800 ℃ the hot gas that contains hydrogenchloride returns heavy nickel waste liquid.
Described raw material ferronickel powder is that red soil nickel ore adding reductive agent reduces the ferronickel powder that reduzate fragmentation, magnetic separation and gravity treatment obtain under solid state;
Described ferronickel powder adds the method that hydrochloric acid soln leaches, and feeds pressurized air under the normal pressure in slurry, leaches 6 hours～20 hours under 50 ℃～100 ℃ temperature.
During to the chloride waste liquid of heavy nickel waste liquid dry, behind waste liquid centrifugal atomizing or airflow atomizing, liquid mist is that 400～800 ℃ the hot gas that contains hydrogenchloride mixes with temperature directly.
Ferronickel powder adds hydrochloric acid soln, and after feeding pressurized air leached in slurry under normal pressure, liquid-solid separation obtained leach liquor and leached mud.But the leached mud washing and recycling is as byproduct for treatment; Leach liquor adds the heavy nickel of heavy nickel agent, obtains nickelous sulfide after the liquid-solid separation and contains muriatic waste liquids such as iron protochloride, magnesium chloride.A part is returned the leaching of ferronickel powder in the heavy nickel waste liquid of this chloride, and the oxidation of divalent when feeding the pressurized air leaching in the waste liquid is a ferric iron, discharges the reaction of HCl and ferronickel powder, utilizes the Cl in the iron protochloride
-After remainder adopts centrifugal atomizing or airflow atomizing in the heavy nickel waste liquid of chloride, the hot gas that contains hydrogenchloride with pyritous directly mixes, obtain chloride solids and the gas that contains hydrogenchloride after the drying, the gas containing hydrogen chloride water absorbs the leaching that the output hydrochloric acid soln returns ferronickel powder.Chloride solids is decomposed at the rotary kiln internal heating, iron is oxidized to ferric iron, obtains ferric oxide, magnesium mixed oxide and the above-mentioned hot gas that contains hydrogenchloride, and hot gas returns the drying of chloride waste liquid, thereby no waste discharge in the whole process flow, leaching agent hydrochloric acid can be recycled.
Beneficial effect of the present invention: the nickel leaching yield in the ferronickel powder reaches 95%, and nickel recovery reaches 93%, and the iron leaching yield is less than 30%, leaching agent hydrochloric acid reusable edible; After employing contained muriatic waste water dryings such as iron(ic) chloride, magnesium with part, the method for chloride solids high-temperature roasting was handled, and leaching agent hydrochloric acid recycles, and reagent consumption is little, has solved the improvement and the emission problem that contain iron(ic) chloride, magnesium waste water, environmentally safe; Employing part waste water returns the method for leaching, has improved the solids content of waste water, reduces treatment capacity, has reduced the cost of wastewater treatment; High-temperature gas convection drying centrifugal atomizing that obtains with the solid chloride roasting or the waste liquid behind the airflow atomizing, rate of drying is fast, and the plant factor height improves rate of energy, reduces energy consumption.Nickelous sulfide can be adopted nickel salt or electric nickel, and product is versatile and flexible, effectively promotes the value of the ferronickel powder that red soil nickel ore reduction obtains; The leached mud major ingredient is a ferric oxide, can be used as iron ore concentrate after the washing, the iron in the comprehensive utilization ferronickel powder.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
Specific embodiments
Embodiment 1
Ferronickel powder main component: Ni6.95%, Fe 85.00%, granularity-200 order.
Hydrochloric acid leaches: drop into 150Kg ferronickel powder, 980L water and 254Kg hydrochloric acid (containing HCl31%) in reactor, liquid-solid ratio is that 8:1, hydrochloric acid add-on are 6 times of the theoretical requirement of nickel in the ferronickel powder.Be heated to 50～60 ℃, feed the pressurized air insulated and stirred and leached 18 hours.Obtain leached mud 152Kg, leach liquor 1350L.Leached mud is nickeliferous 0.15%, iron content 60.12%, the nickel leaching yield 97.81% in the raw material, iron leaching yield 28.33%.
Leach liquor sinks nickel output nickelous sulfide 34.40Kg, and nickelous sulfide is nickeliferous 28.73%, and nickel recovery is 94.83%.
Output is sunk nickel waste water 13101, and main component is: FeCl
287.31g/l, NiCl
20.53g/l, pH value 2.5～3.To wherein 400l waste water centrifugal atomizing in the turriform drying, with temperature be 400～500 ℃ hot gas combination drying, the chloride solids that obtains is put into rotary kiln 650～700 ℃ of following roastings, the dry gas water obtains the 180l hydrochloric acid soln after absorbing, and returns the leaching of ferronickel powder after merging with the heavy nickel waste liquid of residue 910l.
Embodiment 2
Ferronickel powder main component: Ni6.95%, Fe 85.00%, granularity-200 order.
Hydrochloric acid leaches: drop into 150Kg ferronickel powder, 600L water and 170Kg hydrochloric acid (containing HCl31%) in reactor, liquid-solid ratio is that 5:1, hydrochloric acid add-on are 4 times of the theoretical requirement of nickel in the ferronickel powder, be heated to 70～80 ℃, feed the pressurized air insulated and stirred and leached 12 hours.Obtain leached mud 163Kg, leach liquor 810L.Leached mud is nickeliferous 0.182%, iron content 64.03%, the nickel leaching yield 97.15% in the raw material, iron leaching yield 18.13%.
Leach liquor sinks nickel output nickelous sulfide 29.80Kg, and nickelous sulfide is nickeliferous 32.53%, and nickel recovery is 93.07%.
Output is sunk nickel waste water 780l, and main component is: FeCl
2105.02g/l, NiCl
21.21g/l, pH value 2.5～3.To wherein 400l waste water centrifugal atomizing in the turriform drying, with temperature be 600～700 ℃ hot gas combination drying, the chloride solids that obtains is put into rotary kiln 780～830 ℃ of following roastings, the dry gas water obtains the 230l hydrochloric acid soln after absorbing, and returns the leaching of ferronickel powder after merging with the heavy nickel waste liquid of residue 380l.
Embodiment 3
Ferronickel powder main component: Ni6.95%, Fe 85.00%, granularity-200 order.
Hydrochloric acid leaches: drop into 150Kg ferronickel powder, 380L water and 85Kg hydrochloric acid (containing HCl31%) in reactor, liquid-solid ratio is that 3:1, hydrochloric acid add-on are 2 times of the theoretical requirement of nickel in the ferronickel powder, be heated to 90～100 ℃, feed the pressurized air insulated and stirred and leached 7 hours.Obtain leached mud 186Kg, leach liquor 520L.Leached mud is nickeliferous 0.28%, iron content 64.22%, the nickel leaching yield 95.02% in the raw material, iron leaching yield 6.32%.
Leach liquor sinks nickel output nickelous sulfide 39.81Kg, and the nickeliferous 24..53% of nickelous sulfide, nickel recovery are 93.67%.
Output is sunk nickel waste water 490l, and main component is: FeCl
288.17g/l, NiCl
20.64g/l, pH value 2.5～3.To wherein 400l waste water centrifugal atomizing in the turriform drying, with temperature be 600～700 ℃ hot gas combination drying, the chloride solids that obtains is put into rotary kiln 780～830 ℃ of following roastings, the dry gas water obtains the 190l hydrochloric acid soln after absorbing, and returns the leaching of ferronickel powder after merging with the heavy nickel waste liquid of residue 380l.
Claims (5)
1, the treatment process of a kind of leaching of ferronickel powder and waste liquid, it is characterized in that: in ferronickel powder, add hydrochloric acid soln and heating, bubbling air or oxygen leaching, leach liquor adds heavy nickel agent nickel ion is precipitated as nickelous sulfide, and obtains the heavy nickel waste liquid of chloride simultaneously; Heavy nickel waste liquid partly returns the leaching of ferronickel powder, and mix with the hot gas that contains hydrogenchloride its waste liquid atomizing back, obtains chloride solids and the gas that contains hydrogenchloride after the drying; The gas of hydrogenchloride is through the leaching that absorbs, washing output hydrochloric acid soln returns ferronickel powder, and chloride solids is decomposed into oxide compound and described hydrogenchloride hot gas through roasting.
2, the treatment process of the leaching of ferronickel powder according to claim 1 and waste liquid is characterized in that:
(1) is raw material with nickeliferous 5～30%, granularity 200 purpose ferronickel powders, adds 1～6 times hydrochloric acid soln of nickel theoretical amount in the ferronickel powder, under liquid-solid ratio 3～8: 1 condition of volume and quality, leach;
(2) 30%～70% of the heavy nickel waste liquid of the chloride leaching of returning ferronickel powder, the heavy nickel waste liquid atomizing of residue back and temperature are that 400～800 ℃ the hot gas that contains hydrogenchloride directly mixes, and this gas is through absorbing, wash the leaching that the output hydrochloric acid soln returns ferronickel powder.
(3) chloride solids is in rotary kiln internal heating to 600 ℃～1000 ℃ of roastings, obtains temperature and be the chloride waste liquid drying that 400～800 ℃ the hot gas that contains hydrogenchloride returns heavy nickel waste liquid.
3, the treatment process of the leaching of ferronickel powder according to claim 2 and waste liquid is characterized in that: described raw material ferronickel powder is that red soil nickel ore adding reductive agent reduces the ferronickel powder that reduzate fragmentation, magnetic separation and gravity treatment obtain under solid state;
4, the treatment process of the leaching of ferronickel powder according to claim 2 and waste liquid is characterized in that: the method that ferronickel powder adds the hydrochloric acid soln leaching is to feed pressurized air under the normal pressure in slurry, leaches 6 hours～20 hours under 50 ℃～100 ℃ temperature.
5, the treatment process of the leaching of ferronickel powder according to claim 2 and waste liquid, it is characterized in that: during the chloride waste liquid of heavy nickel waste liquid dry, behind waste liquid centrifugal atomizing or airflow atomizing, liquid mist is that 400 ℃～800 ℃ the hot gas that contains hydrogenchloride mixes with temperature directly.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100942435A CN101509073A (en) | 2009-03-20 | 2009-03-20 | Solvent extraction of ferronickel powder and waste liquor processing method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009100942435A CN101509073A (en) | 2009-03-20 | 2009-03-20 | Solvent extraction of ferronickel powder and waste liquor processing method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101509073A true CN101509073A (en) | 2009-08-19 |
Family
ID=41001604
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2009100942435A Pending CN101509073A (en) | 2009-03-20 | 2009-03-20 | Solvent extraction of ferronickel powder and waste liquor processing method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101509073A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2011006223A1 (en) * | 2009-07-14 | 2011-01-20 | Vale S.A. | Process of recovery of base metals from oxide ores |
| US8802042B2 (en) | 2002-07-19 | 2014-08-12 | Vale S.A. | Process of recovery of base metals from oxide ores |
| CN106957955A (en) * | 2017-04-27 | 2017-07-18 | 江苏省冶金设计院有限公司 | Handle the method and system of lateritic nickel ore |
| CN106957954A (en) * | 2017-04-27 | 2017-07-18 | 江苏省冶金设计院有限公司 | Handle the method and system of lateritic nickel ore |
| CN109628738A (en) * | 2019-02-26 | 2019-04-16 | 中钢集团南京新材料研究院有限公司 | A kind of method of the sulfuric acid Selectively leaching of ferronickel concentrate |
| CN111498918A (en) * | 2020-06-01 | 2020-08-07 | 中国恩菲工程技术有限公司 | Wet processing technology of ferronickel material |
| CN113355520A (en) * | 2021-06-08 | 2021-09-07 | 金川镍钴研究设计院有限责任公司 | Treatment process of nickel-containing alloy powder in hydrochloric acid system |
-
2009
- 2009-03-20 CN CNA2009100942435A patent/CN101509073A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US8802042B2 (en) | 2002-07-19 | 2014-08-12 | Vale S.A. | Process of recovery of base metals from oxide ores |
| WO2011006223A1 (en) * | 2009-07-14 | 2011-01-20 | Vale S.A. | Process of recovery of base metals from oxide ores |
| EA019801B1 (en) * | 2009-07-14 | 2014-06-30 | Вале С.А. | Process of recovery of base metals from oxide ores |
| CN106957955A (en) * | 2017-04-27 | 2017-07-18 | 江苏省冶金设计院有限公司 | Handle the method and system of lateritic nickel ore |
| CN106957954A (en) * | 2017-04-27 | 2017-07-18 | 江苏省冶金设计院有限公司 | Handle the method and system of lateritic nickel ore |
| CN109628738A (en) * | 2019-02-26 | 2019-04-16 | 中钢集团南京新材料研究院有限公司 | A kind of method of the sulfuric acid Selectively leaching of ferronickel concentrate |
| CN111498918A (en) * | 2020-06-01 | 2020-08-07 | 中国恩菲工程技术有限公司 | Wet processing technology of ferronickel material |
| CN113355520A (en) * | 2021-06-08 | 2021-09-07 | 金川镍钴研究设计院有限责任公司 | Treatment process of nickel-containing alloy powder in hydrochloric acid system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101550491B (en) | Method for extracting nickel or cobalt from nickel ore with chloridizing roasting-leaching method | |
| CN101736151B (en) | Method for removing iron by oxidation and neutralization in cobalt wet smelting process | |
| CN101818250B (en) | Method for processing cobalt-copper-iron alloy | |
| CN106065435A (en) | A kind of method and system processing vanadium slag | |
| CN101509073A (en) | Solvent extraction of ferronickel powder and waste liquor processing method | |
| CN101311281B (en) | Green metallurgical process for integrated utilization of nickel laterite ore | |
| CN102011010A (en) | Method for totally extracting vanadium, gallium and scandium by using titanium dioxide hydrolysis waste acid to leach steel slag containing vanadium | |
| CN106048251B (en) | A kind of process of clean and effective processing setting form | |
| CN101575673B (en) | Method for separating and extracting copper and cobalt-nickel in low-grade complex mixed copper-cobalt ore | |
| CN101407355B (en) | Method for comprehensively utilizing iron vitriol dreg of yellow sodium | |
| CN107090551B (en) | A kind of method of the direct vanadium extraction of vanadium titano-magnetite | |
| CN109234522A (en) | A kind of cobalt iron concentrate synthetical recovery processing method | |
| CN109957657B (en) | Method for simultaneously recycling iron, sodium and aluminum from red mud | |
| CN101643858A (en) | High temperature chlorination processing method of lateritic nickel ore | |
| CN101550483A (en) | Combined flow path processing method of laterite nickel | |
| CN110093502A (en) | A kind of copper smelting slag cooperates with the method utilized with ferrous manganese ore | |
| WO2012171481A1 (en) | Hydrometallurgical process for complete and comprehensive recovery with substantially no wastes and zero emissions | |
| CN101824554A (en) | Liquid alkali roasting decomposition extraction process of mixed rare earth concentrates | |
| CN106065436A (en) | A kind of method and system processing vanadium slag | |
| CN107236871A (en) | A kind of method for mixing vanadium slag and v-bearing steel slag pressurization vanadium extraction | |
| CN102925701A (en) | Method using wet alkaline process of cobalt-nickel (Co-Ni) residue containing arsenic to prepare arsenate | |
| CN104232924A (en) | Copper extraction and iron removal method of copper ore acid leaching liquid | |
| CN102154553A (en) | Method for removing iron and aluminum by autoxidation of iron-based waste material containing high-value elements | |
| CN103205772B (en) | Method for producing electrolytic manganese dioxide | |
| CN101831542A (en) | Method for extracting metallic elements of ferrum, magnesium and calcium from molybdenum milltailings |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20090819 |