用LIX84-I从含硫酸铵的溶液中回收镍

Chinmaypanija等通过试验,确定了从含硫酸铵的溶液中溶剂苹取镍的工艺参数。溶液中,p（NH4）2SO4）=24kg／m3,p（Ni）＝20kg／m3,不含钴;萃取剂为LIX84-I,稀释剂为煤油,（LIX84－1）＝40％。在相比为1时,通过一级萃取,可将水相中大于99％的镍萃入到有机相中,同时有少量氨也被萃入到有机相中。试图从负载有机相中选择性除去氨没能成功,但因为氨的含量很少,所以也就允许它转入到反革取液中。对含镍的负载有机相,用100kg／m3的H2SO4溶液在Va：Vo＝1：3．5条件下,以4级逆流方式进行反萃取,镍的反萃取率大于99％。这种再…     

二氧化硫氨浸及溶剂萃取钴壳

钴壳用二氧化硫气体作还原剂进行了氨浸,研究了浸出时间,浸出温度和碳酸铵浓度对镍、钴、铜、铁和锰浸出的影响,二氧化硫作还原剂,用碳酸铵溶液可实现从钴壳中选择性浸出镍,钴 和铜,在适当的浸出条件下,金属元素的浸出率分别为Ni90%,Co97%,Cu93%,Fe1.8%和Mn6.0%。使用溶剂萃取从碳酸铵溶液中分离镍、钴和铜,萃取试验用LIX－84作萃取剂,铜和镍的萃取率在99％以上,钴则在1．0％以下,钴的萃取被亚硫酸盐离子遮蔽,含有镍和铜的有机相用稀硫酸或盐酸在pH=1.7时反萃镍,pH=0时反萃铜。     

从大洋多金属结核氨浸液中萃取分离铜,镍,钴

用ＬＩＸ８４的煤油溶液作萃取剂，从大洋多金属结核的催化还原氨浸溶液中选择性共萃铜和镍，而钴等留在萃余液中，然后选择反萃镍和铜，再生有机相循环使用，铜和镍溶液可用电积回收铜和镍。本工艺只需一种萃取剂便可有效地将铜、镍、钴三者彼此分离，操作简便，可用于处理大洋多金属结核或其它含铜、镍、钴的复杂矿     

用LIX84从富钴结壳硫酸浸出液中选择性萃取铜

采用LIX84作萃取剂、硫酸作反萃剂 ,从大洋富钴结壳常温常压活化硫酸浸出除铁后液中萃取铜。试验考察了相比、平衡水相pH值、时间等因素对LIX84萃铜的影响。结果表明 ,相比、平衡水相 pH值、混合时间都对铜的萃取率有一定影响。最后优化出的萃取工艺条件为 (体积百分数 )有机相 12 %LIX84+ 88%煤油 ,室温 ,相比 (O/A)=1/ 2 0 ,出口水相pH2 60± 0 0 5 ,萃取级数为 2级 ,每级混合时间 5min。经过 2级萃取、1级洗涤、3级反萃后 ,可以得到完全符合电解沉积要求的硫酸铜溶液 ,从而使浸出液中的铜与其它金属彻底分离     

二氧化硫氨浸及溶剂萃取钴壳

钴壳用二氧化硫气体作还原剂进行了氨浸,研究了浸出时间、浸出温度和碳酸铵浓度对镍、钴、铜、铁和锰浸出的影响.二氧化硫作还原剂,用碳酸铵溶液可实现从钴壳中选择性浸出镍、钴和铜.在适当的浸出条件下,金属元素的浸出率分别为Ni90%,Co97%,Cu93%,Fe1.8%和Mn6.0%.采用溶剂萃取从碳酸铵溶液中分离镍、钴、和铜.萃取试验用LIX-84作萃取剂,铜和镍的萃取率在99%以上,钴则在1.0%以下.钴的萃取被亚硫酸盐离子遮蔽.含有镍和铜的有机相用稀硫酸或盐酸在pH=1.7时反萃镍,pH=0时反萃铜.     

LIX54/Cyanex923从含锂硫酸钠溶液中协同萃取分离锂钠的研究

针对目前废旧电池正极材料湿法回收工艺中锂回收率低和锂钠分离困难等问题，提出了一种可从含锂硫酸钠溶液中选择性提取锂的协同萃取体系LIX54/Cyanex923。实验结果表明，对于含锂0.5 g/L、钠50 g/L的模拟料液，采用0.4 mol/L LIX54+0.2 mol/L Cyanex923+磺化煤油的有机相，在O/A相比1∶1、平衡pH值12.5、温度30℃和时间10 min的条件下锂的单级萃取率达98.72%,β_Li/Na可达1 578。在相比O/A=1∶5、平衡pH值12.5条件下经三级模拟逆流萃取，99%以上的锂被萃取，萃余液中锂的含量小于0.01 g/L。采用1 mol/L HCl在O/A相比8∶1条件下经过两级逆流洗涤，近98%的钠被洗脱，有机相中仅留下0.05 g/L钠。洗后负载有机相用3 mol/L HCl在相比O/A=6∶1下进行两级逆流反萃，锂的反萃率达99%以上，反萃液中锂的浓度被富集到16.93 g/L。LIX54/Cyanex923协同萃取体系能有效地从含锂硫酸钠溶液中选择性回收锂，实现锂与钠的深度分离及锂的高倍富集回收。     

攀枝花硫钴精矿浸出净化液镍钴分离及钴产品制备的试验研究

本文介绍了攀枝花硫钴精矿浸出净化液镍钴分离及钴产品制备的试验研究。钴镍分离采用P507萃取,钴的萃取率大于99．5％,镍的萃取率在0．01％以下。有机相用硫酸反萃得到硫酸钴溶液,用盐酸反萃得到氯化钴溶液。由氯化钴溶液可制取纯氧化钴粉;由硫酸钴溶液可制备结晶硫酸钴;由萃余液可沉淀出碳酸镍粗产品。     

从含氨溶液中分离铜、镍和钴

从含氨溶液中分离铜、镍和钴印度处理含铜、镍和钻的氨－硫酸铵溶液以分离有价金属。用ＬＩＸ６４Ｎ煤油溶液处理溶液使铜与镍共萃取，而钴留在萃余液中。用５％ＬＩＸ６４Ｎ煤油液研究了ｐＨ和硫酸铵浓度对铜和镍萃取效率的影响。确定了从含１．７６Ｋｇ／ｍ￣３铜，１７...     

D2EHPA萃取分离锌和镍试验研究

采用D2EHPA溶剂对含锌镍酸性溶液进行萃取分离锌、镍试验研究,在最佳萃取、反萃分离条件下,锌的萃取、反萃率分别为99．34％、99．79％,镍的萃取、反萃率分别为99．16％、99．58％,锌镍分离系数达25000以上,得到的含锌、含镍反萃液分别符合电解锌、电解镍的技术要求。     

使用LIX87QN共同萃取和选择性反萃铜和镍

以煤油(主要是脂肪簇)作稀释剂，采用萃取剂LIX87QN可从碳酸铵溶液中共同萃取铜和镍。本文研究了平衡PH和萃取剂浓度(有机相)对共同萃取的影响。研究表明，镍的萃取对PH相当敏感，超过平衡PH(约9)的范围，萃取率迅速降低。对于一种典型的浸出液，含铜和镍约3kg／m^3，碳铵60kg／m^3，确定了共同萃取、除NH^3以及选择性反萃镍和铜的工艺条件。铜和镍的萃取率都约为100％，镍的反萃率是99．2％，铜的反萃率接近100％。     

镍精矿加压酸浸新工艺研究

研究了金川镍精矿加压一步全浸镍、钴、铜新工艺,浸出液中和除铜后萃取分离镍钴,镍、钴、铜的浸出率可分别达到99.5%、98%和98%以上。该工艺与硫酸选择性浸出相比具有金属浸出率高、分离彻底、易分别回收等优点。     

Extraction of nickel,cobalt and other metals [Cu,Zn, Fe(III)] with a commercial β-diketone extractant

The extraction of nickel, cobalt, copper and zinc from ammoniacal solutions of ammonium carbonate or ammonium sulphate by solutions of Hostarex DK-16 in kerosene has been investigated as a function of phase contact time, aqueous-phase pH and organicphase reagent concentration. Besides copper, Hostarex DK-16 also partially extracts iron (III) from moderately acidic solutions whereas nickel, cobalt(II), copper and zinc are extracted from neutral or ammoniacal ammonium sulphate and ammonium carbonate solutions. Extraction decreases in the following order of metals: Cu > Co > Ni > Zn. Cobalt(III) is not extracted, but the complex of cobalt(II) with Hostarex DK-16 is slowly oxidized to a cobalt(III) complex which cannot be stripped even when 10 N sulphuric acid is used. Absorption spectra for cobalt complexes with Hostarex DK-16 (purified by preparative thin-layer chromatography) in benzene also suggest oxidation of cobalt(II) to cobalt(III) in the organic phase. Nickel, cobalt(II), zinc and copper can be stripped easily from organic solution with dilute solutions of sulphuric acid. Hostarex DK-16 extracts iron very slowly, nickel moderately rapidly and copper, cobalt(II) and zinc rapidly. Slope analysis and extraction isotherms suggest that the complexes CuR₂, NiR₂ ·HR and CoR₂·HR are present in the organic phase. Nickel can easily be separated from cobalt by extraction with Hosterex DK-16 after oxidation of cobalt in aqueous ammoniacal solution by hydrogen peroxide; however, LIX 64N seems to be a more promising extractant owing to the higher extraction of nickel under analogous conditions and the poorer extraction of zinc in comparison with Hostarex DK-16.     

Selective separation of copper and nickel by solvent extraction using LIX 984N

Selective separation of copper and nickel from ammoniacal/ammonium carbonate medium was carried out by using LIX 984N diluted with deodourised kerosene. The study of the influence of equilibration time, equilibrium pH, extractant concentration and selective stripping of copper and nickel has been optimized. It was found that both the metal extractions were unaffected by the changes in pH. Nickel extraction equilibrium was reached at a longer contact time than that for copper and nickel extraction depends greatly on the extractant concentration in the organic phase. Co-extraction, ammonia scrubbing and selective stripping of copper and nickel were performed for a solution containing 3 g dm^− 3 each of copper and nickel and 60 g dm^− 3 ammonium carbonate. The extraction and the percentage of stripping for nickel and copper were almost quantitative.     

Hydrometallurgical Process for Copper Recovery from Waste Printed Circuit Boards (PCBs)

Present paper focuses on the selective recovery of copper from the enriched ground printed circuit boards (PCBs) using leaching and solvent extraction. The metal-enriched ground sample obtained from the beneficiation of the sized PCBs in a laboratory scale column type air separator contained mainly 49.3% Cu, 3.83% Fe, 1.51% Ni, 5.45% Sn, 4.71% Pb, and 1.85% Zn. The leaching of the enriched sample with 3.5 mol/L nitric acid dissolved 99% copper along with other metals at 323 K temperature and 120 g/L pulp density in 1 h time. The composition of the leach liquor with wash solution was found to be 42.11 g/L Cu, 2.12 g/L Fe, 4.02 g/L Pb, 1.58 g/L Zn, and 0.4 g/L Ni. The McCabe–Thiele plot indicated the requirements of three counter-current stages for maximum extraction of copper from the leach liquor at pH 1.5 using 30, 40, and 50% (v/v) LIX 984 N at the phase ratios (A/O) of 1:3, 1:2, and 1:1.5, respectively. The counter-current simulation studies show the selective extraction of 99.7% copper from the leach liquor feed of 1.5 pH in three stages with 50% LIX 984 N at A/O phase ratio of 1:1.5. The stripping of copper from the loaded organic with sulfuric acid produced copper sulfate solution from which copper metal/powder could be recovered by electrolysis/ hydrogen reduction.     

Recovery of nickel and cobalt from laterite leach solutions using direct solvent extraction: Part 1 — selection of a synergistic SX system

The separation of nickel and cobalt from impurities such as manganese, magnesium and calcium using solvent extraction with Versatic 10 was largely improved by the addition of a synergistic reagent LIX63 (an α-hydroxyoxime) or 4PC (a pyridine carboxylate ester). With the organic systems containing Versatic 10 alone, the separation factors of nickel and cobalt over manganese were 6 and 15 respectively. When 4PC was added to the system, these increased to 147 and 1870 respectively, and with LIX63, they were even higher at 534 and 7720 respectively. This indicates that the synergistic solvent extraction (SSX) system with Versatic 10 and LIX63 performed very well and better than that with Versatic 10 and 4PC.The SSX system consisting of 0.5 M Versatic 10, 0.45 M LIX63 and 1.0 M TBP in Shellsol D70 performed the best among the systems tested containing LIX63. After a single contact, the extraction of Ni and Co was 99.6% and 96.9%, respectively. Only 6 mg/L Mn, 8 mg/L Mg and 1 mg/L Ca were found in the loaded organic solution. The manganese scrub efficiency was 97.7% at pH 5.3, resulting in a scrubbed organic solution containing only 0.8 mg/L Mn. Over 99% nickel, cobalt and manganese were stripped at pH 2.0, indicating easy stripping of these metals.The SSX system consisting of 0.5 M Versatic 10 and 1.0 M 4PC in Shellsol D70 performed the best among the systems tested containing 4PC. After a single contact, the extraction of Ni and Co was 99.4% and 89.4%, respectively. Some 200 mg/L Mn, 10 mg/L Mg and 48 mg/L Ca were found in the loaded organic solution. The manganese could not be scrubbed at the tested pH range of 5.4-6.0. Very fast Ni and fast Co stripping kinetics were observed, however, the Mn stripping kinetics were very slow. After 2 min of stripping, only 1.22% Mn was stripped.It is concluded that the SSX system containing 0.5 M Versatic 10, 0.45 M LIX63 and 1.0 M TBP performed much better than the SSX system containing 0.5 M Versatic 10 and 1.0 M 4PC in terms of both manganese and calcium behaviour in extraction, scrubbing and stripping.     

Separation of the isomers of the commercial α-hydroxyoxime LIX 63

LIX 63, a commercial extractant containing 5,8-diethyl-7-hydroxy-6-dodecanone oxime marketed by General Mills Inc., has been purified and the isomers isolated. One way of achieving this is by extracting Cu(II) into an ethereal solution of the reagent prepared by distilling the LIX 63 as supplied to remove its petroleum spirit content. The anti isomer is then precipitated as a copper complex by gradually replacing the ether with acetone. The syn isomer is isolated from the filtrate by evaporating the acetone. In another method, Ni(II) is extracted by LIX 63 as received whereafter the anti isomer is precipitated as a nickel sulphate complex by contacting the loaded organic phase with a dilute sulphuric acid solution containing NiSO₄. The syn isomer may be isolated from the filtrate.IR, n.m.r. and mass spectra data are reported together with aggregation data in isooctane for the purified isomers.     

Extraction of ammonia by commercial copper chelating extractants

The extraction of ammonia by commercially available hydroxyoxime, β-diketone and quinoline sulphonamide extractants in the absence and presence of copper and nickel has been studied as a function of pH, diluent type and metal loading. Ammonia appears to be extracted by hydroxyoximes directly as the species RH·NH₃ and the data suggest that only the monomeric oxime is involved. Nonylphenol, used in the synthesis of the hydroxyoximes, was found to extract ammonia quite strongly and variation in uptake by various hydroxyoximes may be due to a combination of different nonylphenol contents and degree of oxime dimerisation. Metal loading of the organic phases with copper or nickel reduces the ammonia content. While neither the β-diketone reagent LIX 54 nor the sulphonamide reagent LIX 34 extracted ammonia in appreciable quantities in the absence of copper and nickel, copper loading caused a small increase in ammonia content and nickel loading caused a considerable increase in ammonia content with nickel: ammonia ratios suggesting the extraction of a nickel ammine complex.     

Recovery of nickel and cobalt from laterite leach solutions using direct solvent extraction: Part 2: Semi- and fully-continuous tests

In Part 1 of this paper, two synergistic solvent extraction systems consisting of Versatic 10/LIX63/TBP and Versatic 10/4PC were assessed in batch tests for the separation and purification of nickel and cobalt from synthetic laterite leach solution after iron removal. In Part 2, semi- and fully-continuous tests are reported for the Versatic 10/LIX63/TBP system, with conditions optimised for separating nickel and cobalt from manganese, magnesium and calcium.Semi-continuous extraction tests were conducted using the synergistic organic system consisting of 0.50 M Versatic 10, 0.45 M LIX63 and 1.0 M TBP in Shellsol D70. With a pH profile of 5.5/6.1/6.5 for the three stages EX1/EX2/EX3 at 40 °C, the nickel and cobalt extractions were 99.9% with only 5 mg/L nickel and < 1 mg/L cobalt left in the raffinate. With two stages of scrubbing and a pH profile of 5.4/5.0 at 40 °C, about 2 mg/L manganese and less than 1 mg/L magnesium and calcium were left in the scrubbed organic solution. With two stripping stages and an O/A ratio of 10 at 40 °C using 50 g/L H₂SO₄ as strip solution, the stripping efficiencies of nickel and cobalt were over 95%.A fully-continuous pilot plant was operated for 280 h. With an O/A ratio of about 2 and a pH profile of 5.5/5.8/6.0/6.3 for the four stages EX1/EX2/EX3/EX4 at 40 °C, both nickel and cobalt were almost completely extracted. The nickel and cobalt concentration in the raffinate was lower than detection limit of 0.2 mg/L. The manganese, magnesium and calcium concentrations in the loaded organic solution were 34, 8 and 1 mg/L, respectively. Using a pH profile of 5.4/5.0 for SC1/SC2 at an O/A ratio of 10 and 40 °C, the manganese scrubbing efficiency was over 96% and the concentrations of manganese and magnesium in the scrubbed organic solution were < 5 mg/L and that of calcium 1 mg/L. Using three strip stages and a strip solution containing 50 g/L H₂SO₄ and 55 g/L Ni at an O/A ratio of 10 and 40 °C, over 98% Ni and 99% Co were stripped with only 64 mg/L Ni in the stripped organic solution. The nickel concentration in the loaded strip liquor was 86 g/L, giving a ΔNi of 31 g/L. The loaded strip liquor contained less than 1 g/L acid.     

含Ni~(2+),Fe~(3+),Mg~(2+)的硫酸盐溶液萃取分离Cu~(2+)

采用Lix984作萃取剂,煤油作稀释剂混合而成溶液萃取的有机相,从含Ni~(2+),Fe~(3+),Mg~(2+)离子的硫酸盐溶液中萃取分离Cu~(2+).实验结果表明,在一定范围内,铜萃取率随萃取剂浓度的升高、相比的增加、萃取时间的延长、初始水相pH值的增加、萃取温度的升高以及搅拌时间的延长而增加.本实验的优化条件为萃取剂体积分数达60%,相比为O∶A=2∶1,萃取时间为16 min,萃取初始水相pH值为2.5,萃取温度在25~45℃之间,搅拌速度为240 r/min.在最佳条件下,铜萃取率高达95.55%.Fe~(3+)萃取率为8.82%,Ni~(2+)的萃取率为5.47%,Mg~(2+)的萃取率为2.36%.从而达到Cu~(2+)与其它金属离子有效分离的效果.