CN87106009A - The thallium method of removing of bullion lead and lead bullion - Google Patents
The thallium method of removing of bullion lead and lead bullion Download PDFInfo
- Publication number
- CN87106009A CN87106009A CN87106009.4A CN87106009A CN87106009A CN 87106009 A CN87106009 A CN 87106009A CN 87106009 A CN87106009 A CN 87106009A CN 87106009 A CN87106009 A CN 87106009A
- Authority
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- China
- Prior art keywords
- thallium
- lead
- chloride
- melt
- bullion
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- 229910052716 thallium Inorganic materials 0.000 title claims abstract description 28
- BKVIYDNLLOSFOA-UHFFFAOYSA-N thallium Chemical compound [Tl] BKVIYDNLLOSFOA-UHFFFAOYSA-N 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims abstract description 26
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 12
- 239000000460 chlorine Substances 0.000 claims abstract description 12
- 229910052751 metal Inorganic materials 0.000 claims abstract description 10
- 239000002184 metal Substances 0.000 claims abstract description 10
- 229910001510 metal chloride Inorganic materials 0.000 claims abstract description 10
- GBECUEIQVRDUKB-UHFFFAOYSA-M thallium monochloride Chemical compound [Tl]Cl GBECUEIQVRDUKB-UHFFFAOYSA-M 0.000 claims abstract description 6
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 claims description 74
- 235000005074 zinc chloride Nutrition 0.000 claims description 37
- 239000011592 zinc chloride Substances 0.000 claims description 37
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 238000002844 melting Methods 0.000 claims description 12
- 238000000502 dialysis Methods 0.000 claims description 4
- 239000011701 zinc Substances 0.000 claims description 4
- 239000000155 melt Substances 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 229910052725 zinc Inorganic materials 0.000 claims description 3
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 2
- 229910001338 liquidmetal Inorganic materials 0.000 claims description 2
- 238000002156 mixing Methods 0.000 claims description 2
- 239000000203 mixture Substances 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 2
- 238000001704 evaporation Methods 0.000 claims 1
- 230000008020 evaporation Effects 0.000 claims 1
- 238000003756 stirring Methods 0.000 description 13
- HWSZZLVAJGOAAY-UHFFFAOYSA-L lead(II) chloride Chemical compound Cl[Pb]Cl HWSZZLVAJGOAAY-UHFFFAOYSA-L 0.000 description 11
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 6
- 238000004458 analytical method Methods 0.000 description 5
- 239000003153 chemical reaction reagent Substances 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 239000003500 flue dust Substances 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 239000002904 solvent Substances 0.000 description 4
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical compound ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000000243 solution Substances 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- 229910052718 tin Inorganic materials 0.000 description 2
- 229910000645 Hg alloy Inorganic materials 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- 229910000635 Spelter Inorganic materials 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- KGBXLFKZBHKPEV-UHFFFAOYSA-N boric acid Chemical compound OB(O)O KGBXLFKZBHKPEV-UHFFFAOYSA-N 0.000 description 1
- 239000004327 boric acid Substances 0.000 description 1
- 229910052810 boron oxide Inorganic materials 0.000 description 1
- 244000309464 bull Species 0.000 description 1
- 229910052791 calcium Inorganic materials 0.000 description 1
- 238000004364 calculation method Methods 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- JKWMSGQKBLHBQQ-UHFFFAOYSA-N diboron trioxide Chemical compound O=BOB=O JKWMSGQKBLHBQQ-UHFFFAOYSA-N 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000011777 magnesium Substances 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- WPBNNNQJVZRUHP-UHFFFAOYSA-L manganese(2+);methyl n-[[2-(methoxycarbonylcarbamothioylamino)phenyl]carbamothioyl]carbamate;n-[2-(sulfidocarbothioylamino)ethyl]carbamodithioate Chemical compound [Mn+2].[S-]C(=S)NCCNC([S-])=S.COC(=O)NC(=S)NC1=CC=CC=C1NC(=S)NC(=O)OC WPBNNNQJVZRUHP-UHFFFAOYSA-L 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 229910052752 metalloid Inorganic materials 0.000 description 1
- 150000002738 metalloids Chemical class 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000009853 pyrometallurgy Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 239000012266 salt solution Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B61/00—Obtaining metals not elsewhere provided for in this subclass
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B13/00—Obtaining lead
- C22B13/06—Refining
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
- Electrolytic Production Of Metals (AREA)
Abstract
The present invention is for removing the method for thallium from bullion lead and lead bullion with metal chloride and/or chlorine, wherein adopt excessive a little metal chloride of total amount or chlorine (in thallium content) to divide multistage to remove the thallium operation and after every section metal melt was separated from containing the thallium chloride melt of generation in 350～450 ℃.
Description
Plumbous production process is with the lead ore concentrate roasting oxidation desulfurization of sulfur compound and in vertical heater oxidiferous product of roasting reduction to be melted.
Thallium in the technology (Tl) is enriched in the roasting oxidation flue dust, and the separable processing of flue dust.
Novel improving of lead method is considered the lead that processing treatment is directly extracted under avoiding the situation that adopts independent roasting oxidation equipment from the concentrate of sulfur compound, wherein as product sulfurous gas high-content waste gas, flue dust, slag and the bullion lead of sending to contact arrangement arranged.Flue dust because of its high lead content constantly reused not can be again with this as the ejecta that contains Tl.Tl is enriched in bullion lead and the slag, therefore must remove Tl in independent refining process from the lead that produces.
In the pyrometallurgy refining process, As, Sb, Sn and Zn remove from plumbous molten bath by making the selective oxidation of oxidizing medium with air.Having only under the situation of adding boron oxide at the same time and generating the boric acid thallium just may be equivalent reaction (M.Foex, Bull Soc.Chim.France 5(1941) 8,897 concerning thallium).
But this reaction must be used and remove the necessary expensive reagent of Tl fully, but also can produce the slag of a large amount of pollution lead, causes to carry out expensive ore dressing processing before storing.
Knownly in addition remove Tl with the mercury alloys ionogen from Pb, this method need be added the equipment that reclaims mercury (L.F.Kosin, N.I.Twantschenkow, J.IZV.Acad.Nauk.K.SSR(1980), 28) except that the electric energy of consumes expensive.
Japanese patent application SHO51-606620(1976 delivers) also be to remove thallium with zinc chloride, wherein to add 20～40 times of equivalent zinc chloride (in the zinc chloride stoichiometry) at least.
Secondly, then use lead chloride in Japanese patent application 78/71623, zinc chloride or aluminum chloride are made reagent.By described embodiment, desire to make Tl final value＜10ppm in the lead, then must add the above muriate of 2000 times of equivalents.But this technology has only with the technical grade lead chloride and just can carry out.Add a large amount of muriates and also can produce a large amount of water-soluble salt melts, correspondingly bring a large amount of storages or handling problem.
Task of the present invention is to propose a kind of method, and available its removes Tl and above-mentioned known disadvantage can not occur or obviously overcome these shortcomings from bullion lead and lead bullion.
This task is to solve like this, promptly divides multistage to remove Tl, wherein adopts by slightly excessive metal chloride or the chlorine (in Tl content) of each section total and from containing the Tl muriate melt of generation metal melt is told after every section.
Can adopt the muriate of various divalent metals (as magnesium, manganese, iron, cobalt, nickel etc.) as metal chloride, but the most handy zinc chloride and chlorine generate lead chloride by it then.
Unexpectedly find now, compare with the situation that the equivalent (in thallium) of prior art such as the Japanese patent application 78/71623 described 2000ppm of being higher than is operated, the present invention but only operates with 20～the highest 50 times equivalent, and the Tl final value can be dropped to and be lower than 10ppm.
This is a significant progress, not only show and can save reagent, and the foreign ion that contains in the lead still less.
By multistage of the present invention except that the scheme that PL operates be in addition, used amount of chloride can reduce greatly, and this not only can save reagent dosage, and can be in the salt-melting amount of removing the low generation of thallium rate same case decline.By the simple treatment step that replenishes, and salt-melting is water-soluble and make the thallium dialysis to spelter, just thallium can be changed into the metallographic phase that is easy to preserve, it can be sold in case of necessity, and reagent is partly turned back to the new thallium that removes operate.
In this method, metal chloride sent into plumbous molten bath or lead is sent into proper container by the salt melt flow stream.Removing the Tl operation is to carry out in 350～450 ℃ of scopes basically.Can vaporization losses occur because of muriatic vapour pressure improves when adopting higher temperature, every period operating time is about 30 minutes.Tl presses the following formula reaction in used muriate and the lead:
1）2Tl+MeCl
2＝2TlCl+Me
2）2Tl+MeCl
2+1/2O
2＝2TlCl+MeO
Metal ingredient constantly is dissolved in the lead in the muriate of formula 1 reaction, can remove by independent refinement step in case of necessity.This metalloid that removes has Sn, Cu, Ca and part Zn.The oxide compound that in formula 2 reaction, produces or evaporate, or take away with salt-melting.
When salt-melting exists with liquid form, should remove the thallium reaction carries out the rapidest the most thoroughly, though the reaction between liquid metal phase and the solid chloride also takes place, wherein causes this reaction with pump by muriate because of muriate is dropped in the metal pool or with metallographic phase.But for can the fused muriate in the used temperature territory, preferably by adding the inertia muriate of not participating in reaction or by reducing its fusing point, so that in used temperature territory, make its liquefaction with other muriatic thorough mixing of participating in reaction.
Removing in the thallium operation has only the chlorine component of metal chloride to be only necessary in principle, therefore also can adopt chlorine, but must have a kind of solvent to reach predetermined low thallium value, thallium can be accompanied by active the reduction and be dissolved in the solvent, because can reach equilibrium value in the metallographic phase of coexistence corresponding to this active reduction.Metal chloride constitutes again on the other hand and reduces the active solvent of Tl on the one hand as the chlorine component of participating in chemical reaction.When adopting chlorine, the lead chloride that solvent is formed by self constitutes.
In multiple process of the present invention, all metal melt was separated fully from containing the Tl muriate melt of producing after every section, only to wherein adding small amount of chloride, so just can in lead, reach the Tl value same then with single stage method.
Remove in the Tl operation at each follow-up section, owing to only have a spot of thallium chloride to be dissolved in the previous metal chloride, this melt can draw back follow-up former sections of removing the Tl operation again again.This has reduced again muriatic total burn-off significantly.The addition of metal chloride or chlorine depends on the Tl content in the lead and the concentration value of expection.
For example in multiple process, in the lead that contains about 1000ppm Tl, add 5 times of normal zinc chloride and/or lead chloride or this two kinds of muriates or other muriatic mixture, then handle back Tl content and promptly reach the following final value of satisfactory 10ppm.As Tl content is 200 or 500ppm when beginning, and the muriate (in stoichiometry) that then consumes 8～50 times just can make the Tl final value be lower than 10ppm.This value can also reduce again by drawing of salt solution.
Based on 2～20kg lead bullion or bullion lead, add muriate to wherein stirring then in the test.Operation generally is divided into 2～15 sections, is preferably 2～4 sections.In the commerical test of 100 tons of every stills, adopt 8 sections to remove Tl, wherein only consume 5 times of normal muriates and just can make that Tl content is lower than 10ppm in the lead.
The processing of salt-melting is by the solid of simple treatment process water with 1: 1: liquid fraction is carried out, and wherein Tl has no to be spongy a large amount of dialysis to zine plate at 25 ℃ with hindering.Normal zinc then enters solution with zinc chloride.But Tl sponge melt into Tl ingot is with its storage or sell.Solution can evaporate and send the extremely new Tl that removes of a part of muriate at least back to and operate.
The present invention illustrates in detail with following example
Example 1
The 10000g bullion lead that will contain 1913ppm Tl dissolves in iron crucible and the 64g zinc chloride is stirred by 10 times of Tl equivalents in 400 ℃ and adds in the fluid lead, and stirring velocity is that per minute 400 changes (Upm), and the time is 30 minutes.
With the experiment scraper liquid state being contained Tl zinc chloride melt then tells from the plumbous surface of fluid fully.Analysis revealed Tl content has dropped to 40ppm.
Second section was stirred down behind the adding 9.4g zinc chloride in the bullion lead Tl content at 400 ℃ and reduces to 9ppm in 30 minutes by 1.5 times of Tl equivalents (in initial value).
Total connects 11.5 times of Tl equivalents needs the 73.4g zinc chloride just 1913ppm Tl content in the bullion lead can be reduced to 9ppm.
Example 2
The 1st section was being stirred adding 80g zinc chloride by 3.5 times of Tl equivalents under 400 ℃ in 30 minutes in the 10000g bullion lead that initially contains 7021ppm Tl.After with scraper melt being told from weld pool surface, Tl content is reduced to 631ppm in the bullion lead.In back 3 sections, respectively press 0.86 times of equivalent with uniform temp and churning time for every section and in bath, stir adding 20g zinc chloride.The zinc chloride melt that all will contain Tl between per two sections is told from weld pool surface fully.
Reaching 85ppm behind second section of the Tl content in the bullion lead, is 18ppm after the 3rd section, is 9ppm after the 4th section.
Just initial 7021ppm Tl can be reduced to 9ppm with the 140g zinc chloride in amounting to 4 sections, the zinc chloride consumption is 6.1 times of equivalents (by removing the required stoichiometry of Tl).
Example 3
Fuse into iron crucible at 400 ℃ of 10000g bullion leads that will contain 212ppmTl down, and in 30 minutes, add the 7.1g zinc chloride to wherein stirring by 16 times of equivalents.Analysis revealed, Tl content is 18ppm in the lead thereafter.The zinc chloride melt that will contain Tl with scraper is told from liquid weld pool surface fully.
In lead, add the 3.5g zinc chloride by 5 times of equivalents in the 2nd section.400 ℃ are stirred 30 minutes post analysis down and show that wherein the Tl final value is 9ppm.Total stirs adding 10.6g zinc chloride (every section all 400 ℃ of operations 30 minutes) by 15 times of equivalents in fluid lead just can reduce to 9ppm with initial 212ppmTl.
Example 4
In the 10000g bullion lead that initially contains 1913ppm Tl, stirring adding 32g zinc chloride by 5 times of Tl equivalents under 400 ℃.Stir and with scraper salt-melting is told from the fluid weld pool surface fully after 30 minutes, wherein contain Tl 18.32g, for partial regeneration it is carried out dialysis and handle.
Analysis revealed, after the 1st section in the bullion lead Tl content be 81ppm.The 2nd section at uniform temp, and churning time and speed (as the 1st section 400 Upm) are added the 32g zinc chloride again by 5 times of Tl equivalents.
The zinc chloride salt-melting of telling from plumbous molten bath only contains 0.6gTl.
Tl content is reduced to 21ppm in the bullion lead.The 3rd section adds the 32g zinc chloride by 5 times of Tl equivalents (in initial value) again under the same mechanical operational condition.
Thereafter Tl content is 5ppm in the lead, and the zinc chloride salt-melting of telling from weld pool surface contains Tl0.16g.Again contact with the bullion lead that contains 1913ppm Tl in 400 ℃ altogether with 3 sections salt-melting the 2nd.Stir and to contain the Tl salt-melting after 30 minutes and tell from weld pool surface.Contain 44ppm Tl in the lead, and then down add the 9.4g zinc chloride, stir after 30 minutes that the Tl final value is 9ppm in the lead by 1.5 times of Tl equivalents in 400 ℃.
Amounting to the 105.4g zinc chloride just to make the 2 * 10000g bullion lead that initially contains 1913ppm Tl reach 5 or the Tl final concentration of 9ppm.This is equivalent to adopt 8.3 times of Tl equivalents.
Example 5
In 350～450 ℃ in steam-heated still dry type stir bullion lead so that 100 tons of bullion leads that initially contain 8498ppm take off Tl.
The 1st section in 370 ℃ of stirring velocity stirring adding 150kg zinc chloride and 50kg lead chlorides of pressing 0.58 times of equivalent with 120 Upm.Reaction finishes the back will be by zinc chloride with proper device, and the salt-melting that lead chloride and thallium chloride are formed is told from weld pool surface.Add muriate in the 1st section, stirring reaction, the separation of scoriaceous drying of fluid and reaction product etc. remove the Tl operation and need 2 hours altogether, and wherein stirring is 30 minutes.Tl content is 6553ppm in the analysis revealed lead afterwards.Follow-up the Tl operating process is fallen and every section required time is identical with the 1st section basically.
The the 2nd and the 3rd section is all respectively carried out with 100kg zinc chloride+100kg lead chloride by 9.53 times of equivalents at 370 ℃.Tl is 5336ppm after containing 2 sections of flow controls, is 4072ppm after the 3rd section.
The 4th section makes Tl content reduce to 3366ppm by 0.26 times of equivalent (by removing the required stoichiometric calculation of Tl) with 50kg zinc chloride+lead chloride in 380 ℃.
Each makes with 100kg zinc chloride+100kg lead chloride that Tl content is 2652ppm in the lead after the 5th section down in 370 or 380 ℃ for the 5th section and the 6th section, is 1152ppm after the 6th section.
The 7th section makes in bullion lead Tl content reduce to 80ppm by 1.06 times of Tl equivalents with 200kg zinc chloride+200kg lead chloride in 370 ℃.
Last the 8th section only just can reach satisfactory 8ppm Tl final value by 0.18 times of equivalent with the 50kg zinc chloride.
Amounting in 8 sections only needs 850kg zinc chloride and 700kg lead chloride just 8498ppm Tl content to be reduced to 8ppm, wherein by 4.3 times of equivalent operations.
Claims (13)
1, adopt muriate or chlorine from bullion lead and lead bullion, to remove the method for thallium, it is characterized in that adopting excessive a little metal chloride of total amount or chlorine (in thallium content) to divide multistage to remove the thallium operation, and after every section, metal melt is separated from containing the thallium chloride melt of generation fully in 350～450 ℃.
2, the method for claim 1 is characterized in that the muriate that is used alone or as a mixture nearly all divalent metal removes thallium.
3, claim 1 and 2 method is characterized in that operation divides 2～15 sections and carries out.
4, the method for claim 1～3, it is characterized in that by initial content and to reach＜the 10ppm final value preferably uses 2～4 times of normal muriates (in stoichiometry) to remove thallium and operates.
5, the method for claim 1～4 is characterized in that reacting in 350～450 ℃ warm territory.
6, the method for claim 1～5 is characterized in that each removes in the thallium step to handle 30 minutes.
7, the method for claim 1～6 is characterized in that muriate is stirred the adding liquid metal.
8, the method for claim 1～7 is characterized in that with pump lead being sent into salt or salt-melting.
9, the method for claim 1～8 is characterized in that chlorine is blown into metal melt.
10, the method for claim 1～9 is characterized in that immersing in the water containing thallium chloride melt, and allows the thallium dialysis to zine plate, and wherein normal zinc enters solution as zinc chloride.
11, the method for claim 1～10 is characterized in that thallium is melt into the thallium ingot, and sells or store, and zinc chloride is then reclaimed for the new thallium that removes by solution evaporation and uses.
12, the method for claim 1～11 is characterized in that adopting 350～400 ℃ not during the melt metal muriate, then at its fusing point by adding the muriate of not participating in reaction or muriatic the mixing reducing its fusing point by what participate in reaction with other.
13, the method for claim 1～12, it is characterized in that with from subsequent step, tell contain thallium chloride melt cause follow-up carry out again remove former sections of thallium operation to save muriatic total consumption.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19863631196 DE3631196A1 (en) | 1986-09-13 | 1986-09-13 | Process for removing thallium from crude lead and high-purity lead |
| DEP3631196.0 | 1986-09-13 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN87106009A true CN87106009A (en) | 1988-05-04 |
| CN1007269B CN1007269B (en) | 1990-03-21 |
Family
ID=6309518
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN87106009.4A Expired CN1007269B (en) | 1986-09-13 | 1987-08-29 | The thallium method of removing of bullion lead and lead bullion |
Country Status (4)
| Country | Link |
|---|---|
| CN (1) | CN1007269B (en) |
| CA (1) | CA1337578C (en) |
| DE (1) | DE3631196A1 (en) |
| IT (1) | IT1211763B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101928841A (en) * | 2010-03-24 | 2010-12-29 | 峨嵋半导体材料研究所 | Preparation process of hyperpure lead |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3922073A1 (en) * | 1989-07-05 | 1991-01-17 | Metallgesellschaft Ag | METHOD FOR REMOVING THALLIUM FROM WORK LEAD |
| US5171550A (en) * | 1989-07-05 | 1992-12-15 | Metallgesellschaft Ag | Process for removing thallium from lead bullion |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52143918A (en) * | 1976-05-27 | 1977-11-30 | Nippon Mining Co Ltd | Separation of thallium from lead |
-
1986
- 1986-09-13 DE DE19863631196 patent/DE3631196A1/en active Granted
-
1987
- 1987-08-29 CN CN87106009.4A patent/CN1007269B/en not_active Expired
- 1987-09-08 IT IT8748367A patent/IT1211763B/en active
- 1987-09-11 CA CA000546647A patent/CA1337578C/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101928841A (en) * | 2010-03-24 | 2010-12-29 | 峨嵋半导体材料研究所 | Preparation process of hyperpure lead |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1007269B (en) | 1990-03-21 |
| DE3631196A1 (en) | 1988-03-24 |
| IT1211763B (en) | 1989-11-03 |
| CA1337578C (en) | 1995-11-21 |
| IT8748367A0 (en) | 1987-09-08 |
| DE3631196C2 (en) | 1989-10-19 |
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