NO126852B - - Google Patents
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- Publication number
- NO126852B NO126852B NO02898/70A NO289870A NO126852B NO 126852 B NO126852 B NO 126852B NO 02898/70 A NO02898/70 A NO 02898/70A NO 289870 A NO289870 A NO 289870A NO 126852 B NO126852 B NO 126852B
- Authority
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- Norway
- Prior art keywords
- chloride
- zinc
- sulfuric acid
- organic phase
- solution
- Prior art date
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 40
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 claims description 33
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 29
- 239000011701 zinc Substances 0.000 claims description 29
- 229910052725 zinc Inorganic materials 0.000 claims description 29
- 239000000243 solution Substances 0.000 claims description 22
- NWONKYPBYAMBJT-UHFFFAOYSA-L zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 claims description 21
- 238000000034 method Methods 0.000 claims description 19
- 235000009529 zinc sulphate Nutrition 0.000 claims description 18
- 239000011686 zinc sulphate Substances 0.000 claims description 18
- 238000000605 extraction Methods 0.000 claims description 12
- 239000012074 organic phase Substances 0.000 claims description 12
- 239000002699 waste material Substances 0.000 claims description 12
- 239000007788 liquid Substances 0.000 claims description 8
- YKGBNAGNNUEZQC-UHFFFAOYSA-N 6-methyl-n,n-bis(6-methylheptyl)heptan-1-amine Chemical compound CC(C)CCCCCN(CCCCCC(C)C)CCCCCC(C)C YKGBNAGNNUEZQC-UHFFFAOYSA-N 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 6
- 238000005868 electrolysis reaction Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 claims description 5
- 239000002253 acid Substances 0.000 claims description 3
- 239000007864 aqueous solution Substances 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 229960001763 zinc sulfate Drugs 0.000 claims description 3
- 229910000368 zinc sulfate Inorganic materials 0.000 claims description 3
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 2
- 239000003849 aromatic solvent Substances 0.000 claims description 2
- 238000000746 purification Methods 0.000 claims description 2
- 229910021653 sulphate ion Inorganic materials 0.000 claims description 2
- 150000003512 tertiary amines Chemical class 0.000 claims description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims 2
- 229910021529 ammonia Inorganic materials 0.000 claims 1
- 235000011121 sodium hydroxide Nutrition 0.000 claims 1
- FYSNRJHAOHDILO-UHFFFAOYSA-N thionyl chloride Chemical compound ClS(Cl)=O FYSNRJHAOHDILO-UHFFFAOYSA-N 0.000 claims 1
- JIAARYAFYJHUJI-UHFFFAOYSA-L zinc dichloride Chemical compound [Cl-].[Cl-].[Zn+2] JIAARYAFYJHUJI-UHFFFAOYSA-L 0.000 description 10
- 239000012071 phase Substances 0.000 description 9
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 8
- 239000003208 petroleum Substances 0.000 description 6
- 239000002904 solvent Substances 0.000 description 6
- 150000001412 amines Chemical class 0.000 description 5
- 239000008346 aqueous phase Substances 0.000 description 5
- 235000005074 zinc chloride Nutrition 0.000 description 5
- 239000011592 zinc chloride Substances 0.000 description 5
- 125000001931 aliphatic group Chemical group 0.000 description 4
- 239000000460 chlorine Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000004061 bleaching Methods 0.000 description 2
- 150000001805 chlorine compounds Chemical class 0.000 description 2
- 230000009931 harmful effect Effects 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- JPVYNHNXODAKFH-UHFFFAOYSA-N Cu2+ Chemical compound [Cu+2] JPVYNHNXODAKFH-UHFFFAOYSA-N 0.000 description 1
- 229910001297 Zn alloy Inorganic materials 0.000 description 1
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- XEPNJJFNSJKTSO-UHFFFAOYSA-N azanium;zinc;chloride Chemical compound [NH4+].[Cl-].[Zn] XEPNJJFNSJKTSO-UHFFFAOYSA-N 0.000 description 1
- 125000004432 carbon atom Chemical group C* 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 229910001431 copper ion Inorganic materials 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- ZBCBWPMODOFKDW-UHFFFAOYSA-N diethanolamine Chemical compound OCCNCCO ZBCBWPMODOFKDW-UHFFFAOYSA-N 0.000 description 1
- 239000003792 electrolyte Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 238000009854 hydrometallurgy Methods 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 230000000135 prohibitive effect Effects 0.000 description 1
- 229910052709 silver Inorganic materials 0.000 description 1
- 239000004332 silver Substances 0.000 description 1
- -1 silver ions Chemical class 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- YBBRCQOCSYXUOC-UHFFFAOYSA-N sulfuryl dichloride Chemical compound ClS(Cl)(=O)=O YBBRCQOCSYXUOC-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G9/00—Compounds of zinc
- C01G9/003—Preparation involving a liquid-liquid extraction, an adsorption or an ion-exchange
-
- 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/28—Amines
- C22B3/282—Aliphatic amines
-
- 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
- C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
- C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
- C22B3/26—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds
- C22B3/38—Treatment or purification of solutions, e.g. obtained by leaching by liquid-liquid extraction using organic compounds containing phosphorus
- C22B3/384—Pentavalent phosphorus oxyacids, esters thereof
- C22B3/3846—Phosphoric acid, e.g. (O)P(OH)3
-
- 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
Description
Fremgangsmåte til behandling av klorholdig sinkavfall for å gjøre det egnet til bruk som råstoff Procedure for treating chlorine-containing zinc waste to make it suitable for use as raw material
ved fremstilling av sink fra sinksulfatoppløsninger. in the production of zinc from zinc sulphate solutions.
Ved nedsmeltning av sink, sinklegeringer, skrotsink m.m. i den hensikt å skulle støpe ut sink som blokker, barrer eller profiler eller for å utføre en forsinkning for korrosjonsbeskyttelse, er det oftest nødvendig å anvende en klbridholdig flux. Dette kan eksempelvis være ammoniumklorid, sinkklorid eller sinkammoniumklorid. When melting down zinc, zinc alloys, scrap zinc etc. in order to cast zinc as blocks, ingots or profiles or to carry out a zinc coating for corrosion protection, it is most often necessary to use a chloride-containing flux. This can be, for example, ammonium chloride, zinc chloride or zinc ammonium chloride.
Man får ved nedsmeltningen en større eller mindre del avbrann som skummes av i form av et kloridholdig avfall, oftest også delvis iblandet metallisk sink. During the meltdown, a larger or smaller part of the slag is skimmed off in the form of a chloride-containing waste, often also partially mixed with metallic zinc.
Dette avfallsprodukt som er høyverdig med hensyn til sink-innholdet, er oftest så mye forurenset av klorid at det etter kjent teknikk ikke uten videre kan anvendes som råstoff for hydrometallur-gisk/elektrolytisk fremstilling av sink. Det er kjent at selv meget små mengder klorid i elektrolytten er høyst skadelig for elektrolysen. This waste product, which is of high value with respect to the zinc content, is often so contaminated by chloride that, according to known techniques, it cannot be used without further ado as a raw material for the hydrometallurgical/electrolytic production of zinc. It is known that even very small amounts of chloride in the electrolyte are highly harmful to electrolysis.
Dette kloridholdige avfall har derfor etter tidligere kjent teknikk hovedsakelig funnet sin anvendelse i termiske sinkpro-sesser, hvor kloridet har mindre skadelige virkninger. Alternativt kan man også ved en pyrometallurgisk behandling av råstoffet avdrive større eller mindre mengder klorid, og siden anvende det i hydro-metallurgiske prosesser. According to prior art, this chloride-containing waste has therefore mainly found its use in thermal zinc processes, where the chloride has less harmful effects. Alternatively, a pyrometallurgical treatment of the raw material can remove larger or smaller amounts of chloride, and then use it in hydro-metallurgical processes.
Det er tidligere kjent at man til en viss grad kan foreta en kjemisk rensing av sinksulfatoppløsninger for klorid ved en ut-felling av kloridet med sølvioner, med kobberioner eller lignende, dog gjelder dette bare mindre mengder klorid, f.eks. 100-500 mg/l Cl . It is previously known that to a certain extent zinc sulphate solutions can be chemically purified for chloride by precipitation of the chloride with silver ions, with copper ions or the like, but this only applies to smaller amounts of chloride, e.g. 100-500 mg/l Cl .
Fra norsk patent nr. 116.322 er det kjent en fremgangsmåte for rensing av sinksulfatoppløsning for klorid ved en væske/ væske ekstraksjonsprosess basert på en ekstrahering med et.alifatisk amin som inneholder fra 7 til 10 karbonatomer og som enten er oppløst i petroleum med et blandingsforhold amin/petroleum = 1-3'-9-7 eller oppløst i en blanding av petroleum og alkohol. Ifølge dette patent vil altså det organiske oppløsningsmiddel, som også virker som opp-løsningsmiddel for det ekstraherbare kloridkompleks, bestå av alifatiske hydrokarboner med eller uten tilsetning av alkohol. From Norwegian patent no. 116,322, a method is known for purifying zinc sulfate solution for chloride by a liquid/liquid extraction process based on an extraction with an aliphatic amine containing from 7 to 10 carbon atoms and which is either dissolved in petroleum with a mixture ratio of amine /petroleum = 1-3'-9-7 or dissolved in a mixture of petroleum and alcohol. According to this patent, the organic solvent, which also acts as a solvent for the extractable chloride complex, will consist of aliphatic hydrocarbons with or without the addition of alcohol.
Ifølge foreliggende oppfinnelse skal det kloridholdige sinkavfall tjene som råmateriale for fremstilling av sink på hydro-metallurgisk/elektrolytisk måte. According to the present invention, the chloride-containing zinc waste is to serve as raw material for the production of zinc in a hydro-metallurgical/electrolytic way.
Dette er muliggjort ved at sinkavfallet først underkastes en utlutning i svovelsyre, fortrinnsvis retursyre fra elektrolyseprosessen med 100-200 g H2S01| pr. liter. This is made possible by first subjecting the zinc waste to leaching in sulfuric acid, preferably return acid from the electrolysis process with 100-200 g H2S01| per litres.
Ved å utføre denne lutning slik at man har f.eks. 10-40 g/l fri svovelsyre som sluttkonsentrasjon, får man oppløst sinkav-fallets innhold av sink samtidig med at også kloridet bringes i opp-løsning og man får en uren sinksulfatoppløsning med vanligvis 1-10 g/l Cl. By performing this slope so that you have e.g. 10-40 g/l free sulfuric acid as a final concentration, the zinc content of the zinc waste is dissolved at the same time that the chloride is also brought into solution and an impure zinc sulphate solution is obtained with usually 1-10 g/l Cl.
I overnevnte norske-patent hr. 116.322 er det ikke omtalt rensning av sinksulfatoppløsninger for klorid ved tilstedeværelse av fri svovelsyre. Det utførelseseksempel som er anført i det nevnte patent, angir pH=5, hvilket viser at eventuell tilstedeværende fri svovelsyre er ubetydelig. In the above-mentioned Norwegian patent Mr. 116,322, the purification of zinc sulphate solutions for chloride in the presence of free sulfuric acid is not mentioned. The design example listed in the aforementioned patent indicates pH=5, which shows that any free sulfuric acid present is negligible.
Hvis imidlertid fremgangsmåten ifølge norsk patent nr. 116.322 legges til grunn for anvendelse også ved tilstedeværelse av fri svovelsyre i en kloridholdig sinksulfatoppløsning, viser det seg at med amin oppløst i et alifatisk oppløsningsmiddel (petroleum), uten tilsetning av alkohol, vil det dannes en seig og klebrig tredje fase som umuliggjør en praktisk gjennomføring av ekstraheringspro-sessen. Denne tredje fase vil oppstå allerede ved en fri svovelsyre-konsentrasjon på under 1 g/l og blir mer alvorlig med økende mengde fri syre og økende kloridkonsentrasjon i sinksulfatoppløsningen. If, however, the method according to Norwegian patent no. 116,322 is used as a basis for application also in the presence of free sulfuric acid in a chloride-containing zinc sulphate solution, it turns out that with amine dissolved in an aliphatic solvent (petroleum), without the addition of alcohol, a tough and sticky third phase which makes a practical implementation of the extraction process impossible. This third phase will already occur at a free sulfuric acid concentration of less than 1 g/l and becomes more serious with increasing amounts of free acid and increasing chloride concentration in the zinc sulphate solution.
For å unngå dannelsen av en tredje fase ville det derfor være en di-rekte nødvendighet å tilsette alkohol til den organiske fase. In order to avoid the formation of a third phase, it would therefore be a direct necessity to add alcohol to the organic phase.
Under en praktisk gjennomføring av ekstraksjonsprosessen med en slik blanding av petroleum og alkohol, vil forholdet mellom det alifatiske oppløsningsmiddel (petroleum) og alkohol endre seg med mindre man tar spesielle forholdsregler mot dette. Dette skyldes at de to komponenter vil ha forskjellig oppløselighet i sinksulfat-oppløsningen og vaskes ut i forskjellig grad. During a practical implementation of the extraction process with such a mixture of petroleum and alcohol, the ratio between the aliphatic solvent (petroleum) and alcohol will change unless special precautions are taken against this. This is because the two components will have different solubility in the zinc sulphate solution and are washed out to different extents.
Det viser seg også at faseoperasjonen påvirkes og blir vesentlig tregere når fri svovelsyre er tilstede i systemet. En tiltagende tendens til blakning av vannfasen er også observert. It also turns out that the phase operation is affected and becomes significantly slower when free sulfuric acid is present in the system. An increasing tendency towards bleaching of the water phase has also been observed.
Ifølge foreliggende oppfinnelse benyttes det også her According to the present invention, it is also used here
en væske/væske ekstraheringsprosess for å fjerne klorid fra den oven-for angitte oppløsning av sinksulfat i svovelsyre. a liquid/liquid extraction process to remove chloride from the above solution of zinc sulfate in sulfuric acid.
Den organiske fase er imidlertid vesensforskjellig fra den som benyttes ifølge norsk patent nr. 116.322. Ifølge oppfinnelsen benyttes et amin, f.eks. tri-iso-oktylamin, oppløst i et oppløsnings-middel av aromatiske hydrokarboner som f.eks. Solvesso 100. Videre er volumforholdet amin : oppløsningsmiddel vesentlig lavere, f.eks. 1:24, enn i det overnevnte patent hvor det angis 1-3:9-7. The organic phase is, however, fundamentally different from that used according to Norwegian patent no. 116,322. According to the invention, an amine is used, e.g. tri-iso-octylamine, dissolved in a solvent of aromatic hydrocarbons such as e.g. Solvesso 100. Furthermore, the volume ratio of amine : solvent is significantly lower, e.g. 1:24, than in the above-mentioned patent where 1-3:9-7 is stated.
Ved å benytte aromatiske hydrokarboner fremfor alifatiske i kombinasjon med et amin, unngås dannelsen av en tredje fase, som er prohibitiv for prosessen, og det er ikke nødvendig å tilsette alkohol for å unngå dette problem. Det er derfor et vesentlig mer teknisk anvendelig system som benyttes ved foreliggende oppfinnelse. By using aromatic hydrocarbons rather than aliphatic ones in combination with an amine, the formation of a third phase, which is prohibitive to the process, is avoided, and it is not necessary to add alcohol to avoid this problem. It is therefore a substantially more technically applicable system that is used in the present invention.
Videre kan det påpekes at den tilstedeværende fri svovelsyre ved den foreliggende oppfinnelse er prosessteknisk fordelaktig for faseseparasjonen. Uten fri svovelsyre i sinksulfatoppløsningen har denne en tendens til å forbli blakket etter kontakt med den organiske fase. Ved tilstedeværelse av fri svovelsyre blir imidlertid sinksulfatoppløsningen helt klar etter kort henstand. Ved bruk av et alifatisk oppløsningsmiddel med tilsetning av alkohol, er det som tidligere nevnt iakttatt en motsatt tendens, idet blakning av vannfasen Furthermore, it can be pointed out that the free sulfuric acid present in the present invention is technologically advantageous for the phase separation. Without free sulfuric acid in the zinc sulphate solution, this tends to remain cloudy after contact with the organic phase. In the presence of free sulfuric acid, however, the zinc sulphate solution becomes completely clear after a short delay. When using an aliphatic solvent with the addition of alcohol, as previously mentioned, an opposite tendency has been observed, as bleaching of the water phase
tiltar med fri svovelsyre i sinksulfatoppløsninger!. increases with free sulfuric acid in zinc sulphate solutions!.
Oppfinnelsen vedrører altså en fremgangsmåte til behandling av kloridholdig sinkavfall for å gjøre det egnet til bruk som råstoff ved fremstilling av sink fra sulfatoppløsninger, idet fremgangsmåten er karakterisert ved at sinkavfallet oppløses i svovelsyre for å danne ensvovelsur kloridholdig sinksulfatoppløsning som renses for kloridioner ved en væske/væske ekstraksjonsprosess, idet oppløsningen bringes i kontakt med et aromatisk oppløsningsmiddel, The invention thus relates to a method for treating chloride-containing zinc waste to make it suitable for use as a raw material in the production of zinc from sulphate solutions, the method being characterized in that the zinc waste is dissolved in sulfuric acid to form a monosulphuric chloride-containing zinc sulphate solution which is purified from chloride ions by a liquid/ liquid extraction process, in which the solution is brought into contact with an aromatic solvent,
hvori det er oppløst et tertiært amin som f. eks. tri-iso-oktylamin, som danner et kloridkompleks, som er oppløselig i den organiske fase, idet den organiske fase deretter renses for klorid og returneres i prosessen. in which a tertiary amine is dissolved, e.g. tri-iso-octylamine, which forms a chloride complex, which is soluble in the organic phase, the organic phase being then purified of chloride and returned to the process.
Derved fremstilles en kloridrenset sinksulfatoppløsning som er egnet til å blandes med sinkprosessens hovedkretsløp' og inngå som utgangspunkt for en konvensjonell sinkelektrolyse. Thereby, a chloride-purified zinc sulphate solution is produced which is suitable to be mixed with the main circuit of the zinc process and used as a starting point for a conventional zinc electrolysis.
Oppfinnelsen skal forklares nærmere ved hjelp av eksempler. The invention shall be explained in more detail by means of examples.
Eksempel I. Example I.
Vandige oppløsninger inneholdende 0,25 mol svovelsyre Aqueous solutions containing 0.25 mol sulfuric acid
pr. liter med varierende mengder sinkklorid, samt sinksulfat tilsatt i en mengde slik at total sinkkonsentrasjon var konstant 200 g/l, ble rystet til likevekt med en organisk fase inneholdende 0,15 mol/l tri-iso-oktylamin (Adogen 38l) oppløst i Solvesso 100. Kloridet ble tilsatt de vandige oppløsninger som sinkklorid og den resterende sink-tilsetning som sinksulfat. per liters with varying amounts of zinc chloride, as well as zinc sulphate added in an amount so that the total zinc concentration was a constant 200 g/l, were shaken to equilibrium with an organic phase containing 0.15 mol/l tri-iso-octylamine (Adogen 38l) dissolved in Solvesso 100. The chloride was added to the aqueous solutions as zinc chloride and the remaining zinc addition as zinc sulphate.
Volumforholdet mellom de to faser var: organisk/vandig= 3/1. The volume ratio between the two phases was: organic/aqueous = 3/1.
De to faser ble adskilt og likevektsfordelingen for klorid ble bestemt ved analyse av den vandige fase. Likevektsdata er angitt i følgende tabell 1. The two phases were separated and the equilibrium distribution for chloride was determined by analysis of the aqueous phase. Equilibrium data are given in the following Table 1.
Eksempel II. Example II.
Klorid ble ekstrahert fra en vandig fase bestående av 0,133 mol/l svovelsyre, 0,168 mol/l sinkklorid, samt sinksulfat tilsatt i en mengde slik at total sinkkonsentrasjon var 200 g/l. Chloride was extracted from an aqueous phase consisting of 0.133 mol/l sulfuric acid, 0.168 mol/l zinc chloride, and zinc sulphate added in an amount such that the total zinc concentration was 200 g/l.
Ekstraheringen ble foretatt ved motstrøm i fem trinn med en organisk fase bestående av 0,095 mol/l tri-iso-oktylamin (Adogen 38l) oppløst i Solvesso 100. Relativ strømningshastighet: Organisk/vandig = 1,85 : 1. The extraction was carried out by countercurrent flow in five steps with an organic phase consisting of 0.095 mol/l tri-iso-octylamine (Adogen 38l) dissolved in Solvesso 100. Relative flow rate: Organic/aqueous = 1.85 : 1.
Kloridkonsentrasjonen i den vandige fase ble totalt re-dusert fra 11,8 g/l til 0,035 g/l. The chloride concentration in the aqueous phase was totally reduced from 11.8 g/l to 0.035 g/l.
Ekstraheringsforløpet over de enkelte trinn er vist på figur 1. The extraction process over the individual steps is shown in figure 1.
Eksempel III. Example III.
Klorid ble ekstrahert fra en vandig fase bestående av 0,153 mol/l svovelsyre, 0,1 mol/l sinkklorid samt sinksulfat tilsatt en mengde slik at total sinkkonsentrasjon var 167 g/l. Chloride was extracted from an aqueous phase consisting of 0.153 mol/l sulfuric acid, 0.1 mol/l zinc chloride and zinc sulphate added in an amount such that the total zinc concentration was 167 g/l.
Ekstraheringen ble foretatt ved motstrøm i seks trinn med en organisk fase bestående av 0,095 mol/l tri-iso-oktylamin (Adogen 38l) oppløst i Solvesso 100. The extraction was carried out by countercurrent in six stages with an organic phase consisting of 0.095 mol/l tri-iso-octylamine (Adogen 38l) dissolved in Solvesso 100.
Relativ strømningshastighet: Organisk/vandig = 2,2 : 1. Relative flow rate: Organic/aqueous = 2.2 : 1.
Kloridkonsentrasjonen i den vandige fase ble totalt re-dusert fra 7,1 g/l til 0,018 g/l. The chloride concentration in the aqueous phase was totally reduced from 7.1 g/l to 0.018 g/l.
Ekstraheringsforløpet over de enkelte trinn er vist på figur 2. The extraction process over the individual steps is shown in Figure 2.
Claims (4)
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
NO02898/70A NO126852B (en) | 1970-07-24 | 1970-07-24 | |
DE19712136557 DE2136557A1 (en) | 1970-07-24 | 1971-07-22 | Chloride removal - from zinc waste, with recovery of zinc |
NL7110220A NL7110220A (en) | 1970-07-24 | 1971-07-23 |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
NO02898/70A NO126852B (en) | 1970-07-24 | 1970-07-24 |
Publications (1)
Publication Number | Publication Date |
---|---|
NO126852B true NO126852B (en) | 1973-04-02 |
Family
ID=19879232
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
NO02898/70A NO126852B (en) | 1970-07-24 | 1970-07-24 |
Country Status (3)
Country | Link |
---|---|
DE (1) | DE2136557A1 (en) |
NL (1) | NL7110220A (en) |
NO (1) | NO126852B (en) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA1258654A (en) * | 1986-04-22 | 1989-08-22 | Donald L. Ball | Method for the removal of monovalent ions from znso.sub.4 electrolyte by electrodialysis |
DE19640869B4 (en) * | 1996-10-04 | 2010-08-12 | Ruhr-Zink Gmbh | Process for the recovery of valuable metals, in particular zinc, from raw materials containing chlorine or fluorine |
US7037482B2 (en) | 2003-03-10 | 2006-05-02 | Teck Cominco Metals Ltd. | Solvent extraction of a halide from a aqueous sulphate solution |
-
1970
- 1970-07-24 NO NO02898/70A patent/NO126852B/no unknown
-
1971
- 1971-07-22 DE DE19712136557 patent/DE2136557A1/en active Pending
- 1971-07-23 NL NL7110220A patent/NL7110220A/xx not_active Application Discontinuation
Also Published As
Publication number | Publication date |
---|---|
DE2136557A1 (en) | 1972-02-03 |
NL7110220A (en) | 1972-01-26 |
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