Intensification of Gold Sorption by Anion Exchange Resins

Gold extraction technology based on anion exchange resins with mixed basicity, commonly used in former soviet countries, includes a complicated and expensive process of resin regeneration and gold stripping by thiocarbamide solution. Satisfactory sorption properties of weak base anion exchange resin at pH 6–8 and low cost of metal stripping by sodium hydroxide solution have aroused considerable interest in these resins as perspective means of gold extraction from cyanide pulps on a large scale. However, the possibility of industrial use of weak base anion exchange resins is hindered by their extremely low sorption activity at pH 10.5 and the formation and release of HCN in the pulp at pH 6–8.

The development of weak-based anion exchange resins which permits efficient gold sorption at pH 10.5 has already been described in literature. A special procedure for treating cyanide pulps has been devised in ?Irgiredmet”. It allows a sigificant rise of gold distribution coefficient between anion exchange resins and liquid phase.

Studies including counter-current tests of gold sorption by anion exchange resins of mixed and weak basicity from cyanide solutions and pulps treated accordingly were carried out. It was found that the gold capacity of mixed base resins has risen by 2–3 times, and the resin flowrate and reagent consumption during its regeneration and gold stripping by thiocarbamide solution have decreased proportionally. After special treatment the gold capacity of weak base resins in solutions and pulps is 3–6 times greater than in nontreated solutions and pulps, which indicated that the sorption capacity of resins is used to the full extent. Introduction of special treatment of cyanide pulp into existing technology makes possible an efficient industrial use of commercially available weak base anion exchange resins for gold recovery.     

A Review on Recovery of Copper and Cyanide From Waste Cyanide Solutions

The mainstream technology for leaching gold from gold ore is still leaching in aqueous alkaline cyanide solution. However, when copper minerals are present in the gold ore, high levels of free cyanide must be maintained during leaching because many common copper minerals react with cyanide, forming copper cyanide complexes that deplete the solution of free cyanide. This results in a significant economical penalty through excessive cyanide consumption and loss of valuable copper in tails. Environmental constraints controlling the discharge of cyanide from mining industry are being tightened by local governments worldwide. The solution chemistry of copper in cyanide solution and various technologies for the recovery of copper and cyanide from barren gold cyanide solutions were reviewed in the paper. Direct recovery methods are mainly based on the acidification–volatilization–reneutralization (AVR) process or its modifications. These processes are not very efficient for treating low cyanide solutions and high metal cyanide solutions due to their substantial operational cost. Indirect recovery technologies by activated carbon, ion-exchange resins (IX) and solvent extraction (SX) have been extensively studied. The basic principle of these technologies is to pre-concentrate copper (and part of cyanide) into a small volume of eluant or stripping solution. The copper and cyanide in the resulted solutions can be further recovered by AVR or similar processes or by the electrowinning process. Activated carbon is only suitable for use as a polishing process to remove cyanide to lower levels from those cyanide solutions where the cyanide content is already low. Compared to activated carbon, ion exchange resins are less easily poisoned by organic matter and can usually be eluted at room temperature, and selectivity for particular metals can be achieved by the choice of the functional group incorporated into the bead or by the selective elution process. Solvent extraction process developed base on guanidine and modified quaternary amines exhibit relative fast extraction kinetics and can be operated in a continuous manner. It will be necessary to thicken and wash the solids in order to produce a clarified feed solution while treating the slurry from operations using carbon-in-pulp (CIP) for the recovery of gold. Other copper and cyanide recovery technologies such as biosorption or direct electrowinning were also proposed, but they have still not found their way to practical application.     

C410哌啶树脂吸附和解吸金的性能研究

研究了用C410哌啶树脂从氯水溶液中吸附和解吸金的性能。考察了溶液中含金量、搅拌速度和温度对该树脂吸附金的影响。用3％硫脲溶液能够很好解吸金。实验测得该吸附过程的表观活化能值为17.0kJ/mol。对吸附金前后的树脂分别用红外光谱进行了分析比较。     

D370型树脂在氰化浸出提金工艺中的应用

对D 370型、201×4型和201×7型树脂从氰化贵液中吸附金、银的吸附容量以及选择性吸附能力进行了对比试验,并对载金D 370型树脂进行了解吸试验。其结果表明,D 370型树脂的各项技术指标,明显优于201×4型和201×7型树脂。     

SK-106树脂在氰化提金中的应用研究

研究了SK－106树脂在氰化浸金溶液中对金的吸附速率，吸附容量，吸附等温线，载金树脂的解吸，用SK－GSR试剂从解吸液中提取金。     

D301树脂吸附金的机理研究

本文利用XPS光电子能谱仪对D301树脂吸附金氰络合物前后的研究:确定此种吸附为离子吸附;D301树脂要达到较高的吸附量,必须先质子化;强的酸性环境可提高对Au(CN)_2~-的选择性,这一点在回收镀金废水中的金很有价值。     

树脂矿浆法提金工艺研究及应用

树脂矿浆法提金工艺属于无过滤提金技术,具有吸附速度快、饱和载金量大、解吸和再生容易、耐磨性好、抗污染能力强及适用范围广等优点。自采用树脂矿浆法提金工艺后,氰化浸出率由原来的90.82%提高到96.88%,提高了6.06%;金的选矿总回收率由90.28%提高到95.86%,提高了5.58%;解吸电积的金泥品位由原来的15%左右提高至70%左右。     

SMF—453树脂富集氰化液中微量金银

就酸度曲线、吸附速度、吸附能力和吸附反应的活化能等几个方面分别对采用SMF－453树脂吸附金银的机理进行了论述。结果表明：SMF－453树脂可以很强地吸附氰化物介质中的Au(CN)2^-and Ag(CN)2^-络合离子。吸附在树脂上的金和银均易被0.1mol/L和3％（M／V）的硫脲溶液洗脱，回收率为99％。     

酰基化强碱性离子交换纤维制备及其对金属氰络合物吸附性能研究

氰化提金工艺产生的含氰废水中多含有金属氰络离子,其会消耗额外的氰化物,进而影响生产工艺指标.研究以聚丙烯纤维为基体,制备了酰基化强碱性离子交换纤维(ASA-IEF),并考察了其对废水中金属氰络离子的去除性能.ASA-IEF的最优制备条件为反应时间4 h、反应温度30℃、三氯乙酰氯与苯乙烯摩尔比1:1.2.在此条件下,纤...     

含铜金矿石氨氰体系浸金机理研究

对于金以非包裹形式存在的含铜金矿石,直接氰化虽然能取得较高的金浸出率(92%),但氰耗高(130 kg/t),而且氰化物耗量并不与铜的浸出量成线性关系。氨氰体系浸金可以得到较高金浸出率的同时,降低氰化物耗量。该体系中最佳氨氰比为3∶1,最大的氰化钠用量为14.7 kg/t,继续增大氰化钠用量,金的浸出率并不明显增高,而过量的氨则会导致试样中铜的快速溶解,同样不利于金的浸出。试样中的可溶性铜使浸出液中的Cu2+浓度满足氨氰体系浸金的要求,过量的Cu2+对浸金不利。研究结果表明,氨氰体系浸出金的机理可能是铜氨络离子充当氧化剂,而氰铜络离子(以Cu(CN)32-为主)充当浸金剂,浸出液中铜浓度和金浓度变化的四个阶段支持了此浸金机理。     

载金炭无氰高效解吸工艺及设备在某炼金厂的应用

载金炭解吸工艺是黄金生产中的重要环节，贵州兴义黄金冶炼厂从投产至今先后引进了4套不同特点的载金炭解吸工艺及设备，其中两次引进了我们研制的高效溶剂解吸设备，经历了从有氰解吸到无氰解吸的转变，尝试了常压和加压的解吸过程，实现了金的解吸率从93％到99％的提高，彻底解决了电解时因钢棉混入金泥影响金的成色的问题，避免了因解吸时产生粉炭降低金总回收率的问题，在设备结构上消除了因解吸溶剂燃烧发生火灾的隐患。     

用离子交换树脂从硫脲硫酸溶液中回收金银的研究

本文从树脂选型、吸附和解吸等方面,介绍了用离子交换法从含金量较低的硫脲硫酸溶液中,回收金、银的试验研究结果。结果表明,用D61和732牌号的强酸性阳离子交换树脂,能有效地从料液中吸附金、银;用氰化钠碱性溶液作解吸剂,金的解吸率>99％,银的解吸率>70％。     

浮选金精矿与原矿混合氰化炭浆法提金工艺的研究与实践

银洞坡金矿矿石物质组分复杂,不同矿体、同矿体不同部位氧化程度变化大,矿石品位属很不均匀类型,矿石含泥质较高,属难选型矿石。将浮选获得的金精矿(主要是低品位)与原矿(含泥量高不易浮选)混合配矿后氰化,达到解决低品位金精矿销售难,同时提高成品金生产能力,即避免单一金精矿氰化因贵液品位高,活性炭吸附不完全降低回收率的缺陷,并相应达到了提高氰化原矿品位和金的回收率,充分利用国家资源的目的。     

离子交换法处理含铁氰化提金尾液问题及解决办法

分析含铁氰化提金尾液的来源、特点及其危害,重点对具有离子交换法吸附、解吸含铁氰化提金尾液的原理、存在问题进行了深入分析研究,结果表明,采用化学沉淀法或电吸附处理技术对含铁氰化提金尾液进行预处理是解决离子交换法处理此类废水瓶颈的最佳途径。     

柠檬酸法脱硫中硫酸根的树脂吸附研究

采用静态法研究D301R、D301G、D370和D315四种弱碱性阴离子交换树脂吸附柠檬酸法脱除SO2的解吸贫液中硫酸根的效果,分析吸附时间、柠檬酸浓度、树脂用量、pH等对硫酸根吸附量的影响,解吸时间、解吸碱液浓度对树脂解吸效果的影响,及多次吸附解吸循环再生对树脂吸附活性的影响。结果表明,D315在高浓度柠檬酸钠溶液(1.0 mol/L)中对SO42-有较好的脱除效果,当氢氧化钠浓度为1.5mol/L时,3min即可将SO42-解吸完全,在经过10轮吸附解吸循环再生后其活性下降,吸附能力降低约15%。     

碱浸预处理提高某含砷锑难处理金精矿回收率的试验研究

内蒙古某黄金矿山金精矿中,金主要包裹在黄铁矿及砷黄铁矿中,同时还有锑金属硫化物的存在。氰化浸出生产工艺中金的回收率比较低,只有76.63%。通过常规氰化工艺条件优化试验,金的回收率最高可达到80.15%。对该低品位含砷、锑难处理金精矿进行碱浸预处理,优先除砷、锑,以提高金氰化浸出率。确定了生产操作的最佳工艺条件,金的氰化回收率由原来的76.63%提高到92%,试验获得了较好技术指标和经济效益。     

从浸金溶液中回收金的研究概况

介绍了从溶液中回收金的主要技术,包括:置换沉淀技术、炭吸附技术、树脂吸附技术、溶剂萃取技术等。简要评述了各种方法的应用情况及其各自的优缺点,也对这些技术应用中存在的问题提出了看法。     

高温高压无氰解吸电解工艺在老挝某金矿应用实践

高温高压无氰解吸电解工艺在老挝某金矿应用实践表明,该工艺解吸电解率高,贫炭金品位低,现场载金炭平均金品位5 595.22g/t,贫炭平均金品位38.10g/t,解吸率达到99.32%,电解后贫液金品位平均0.063g/m~3,电解率达到99.99%。直接作业成本低,药剂材料和动力成本仅为每吨原矿0.69元。解吸液使用次数可达33次以上,且对解吸电解时间、解吸电解率影响不大。影响解吸电解时间的主要因素为电解槽中金泥量,载金炭金品位与解吸电解时间关系不大。     

P510树脂从含金氯化溶液中吸附金和解吸金的性能研究

用静态法研究了PS10树脂从酸性含金氯化溶液中吸附金及其解吸金的性能。考察了吸附时间、酸度、初始金浓度、温度等因素对树脂吸附金的影响,同时考察了解吸时间、解吸剂硫脲浓度对金解吸率的影响。在适宜条件下,PS10树脂对金的吸附率和解吸率均达到99％以上。