亭南选煤厂降低介耗的实践

针对选煤厂介耗高的问题,亭南选煤厂通过对现场设备及工艺流程进行分析,提出对加介池位置、旋流器溢流箱、脱介筛来料溜槽、筛上喷水、磁选机喷水及脱泥筛等进行改造,使选煤厂的介质消耗由原来的0.75 kg/t降至0.52 kg/t,每年可节约成本96.6万元。     

平朔二号井选煤厂降低介耗探讨

分析了平朔二号井选煤厂影响介耗的主要因素,提出从工艺技术和生产管理两方面来降低介耗是有效的方法。结合生产实践,采取保证重介浅槽分选过程稳定性、改善弧形筛与脱介筛的脱介效果、提高磁选机磁选效率和加强管理等措施降低了介耗。     

降低圆筒重介旋流器末煤精选系统介耗的途径探讨

介绍了末煤重介分选介耗形成的几种主要原因，探讨了筒重介旋流器精选末煤工艺中，改变常规的脱介筛分级粒度，增加重介系统内部循环水、改善喷水效果等途径，可以有效降低介质消耗。     

范各庄矿选煤厂末煤旋流器车间的工艺改进

介绍了范各庄矿选煤厂通过采取增加固定筛和过滤器、改变筛缝和喷水方式等措施,对末煤重介旋流器车间进行工艺改进,提高了筛机的脱介能力,降低了介质消耗.     

范各庄矿选煤厂未煤旋流器车间的工艺改进

介绍了范各庄矿选煤厂通过采取增加固定筛和过滤器、改变筛缝和喷水方式等措施，对末煤重介旋流器车间进行工艺改进，提高了筛机的脱介能力，降低了介质消耗。     

古汉山矿选煤厂末煤重介选降低介耗的实践

介绍了古汉山矿选煤厂针对末煤重介系统介耗所采取的一系列有效措施,主要包括对脱介筛入料点和筛板的改进,喷水量、喷水位置、喷水角度的优化以及分流量和磁选机的合理调节,从而使介质消耗大幅下降,并使磁选效果得以优化。     

末煤重介精选系统的降介及精煤泥回收

介绍了末煤重介选工艺中脱介筛分级粒度对介耗的影响,分析了改变常规的脱介筛分级粒度、强化粗煤泥回收、增加重介系统内部循环水对有效降低系统介耗、降低生产成本的技术支持及优越性.     

改善SLO系列香蕉筛脱介效果的试验研究

介绍了SLO系列香蕉筛的特点,分析了屯兰矿选煤厂SLO系列香蕉脱介筛应用中存在的问题,通过技术改造,改善了脱介筛的脱介效果,减少了产品带介量,降低了重介介耗损失,对使用SLO系列香蕉筛的选煤厂有一定的参考价值。     

末煤重介精选系统的降介及粗煤泥回收

介绍了末煤重介选工艺中脱介筛分级粒度对介耗的影响，分析了改变常规的脱介筛分级粒度、强化粗煤泥回收、增加重介系统内部循环水对有效降低系统介耗、降低生产成本的技术支持及优越性。     

降低圆筒重介旋流器末煤精选系统介耗的途径探讨

介绍了末煤重介分选介耗形成的几种主要原因,探讨了圆筒重介旋流器精选末煤工艺中,改变常规的脱介筛分级粒度、增加重介系统内部循环水、改善喷水效果等途径,可以有效降低介质消耗.     

废镁砖中贵金属综合回收技术创新与实践

针对金银转炉拆迁废镁砖中金银含量较高、脉石主要为氧化镁等特点,在生产实践中综合考虑投资成本、可操作性等情况,在小型选矿试验基础上,经技术研究与论证,提出干磨—筛分分选—细粒浮选工艺,即干磨后试样采用高频振筛,将粗粒金银颗粒预先筛分回收,再采用浮选对细粒金银进一步回收,实现了废镁砖中金银的梯级回收。工业生产获得了金银精矿含金674.91 g/t,含银9.14%,金回收率为90.37%,银回收率为88.02%的较好指标,且具有较好的经济效益。     

含银氧化锰矿高温氯化过程研究

对高温下Mn-Cl-O系及Ag/ASCl平衡图进行分析,找出了理论上银、锰的存在形态。以内蒙呼盟含银氧化锰矿石为原料,在实验室对高温氯化过程中影响银挥发率的因素进行了研究。得出了氯化剂用量,氯化温度、球团直径及氯化时间与银挥发率的定量关系。95％～98％的锰残留在球团中,主要以Mn_2O_3和MnSiO_3形态存在。在最佳条件下银挥发率为98.8％,球团残银12.1g/t。     

Refinement of methods of beneficiation of finely disperse minerals

Conclusions  The prospect of switch-over of the industry to processing lean materials raises the problem of beneficiation of finely disperse placers of noble metals, the profitability of realization of which lies in raising the efficiency of separation processes by reducing frictional forces in the course of implementation of the technological processes and by employing modern technologies for beneficiation. The engineering—technological solutions worked out are distinguished by ecological safety during implementation of the beneficiation processes. The proposed schemes of beneficiation and primary processing of finely disperse minerals may be used:

Mathematical modeling of thermophilic bioleaching of chalcopyrite

Previous studies have shown that the different preferences of thermophiles to oxidize S⁰ or Fe²⁺ is reflected by different [Fe³⁺]/[Fe²⁺] levels in solution. In those studies it was concluded that [Fe³⁺]/[Fe²⁺] governs the thermophilic bioleaching of chalcopyrite rather than temperature or pH. Therefore, the proposed model is mainly based on the finding that thermophilic bioleaching of chalcopyrite is governed by [Fe³⁺]/[Fe²⁺] that result from the activity of thermophiles. A direct interaction between chalcopyrite and thermophiles is neglected because it has been reported that this is not a general behavior for all thermophiles. The case of constant temperature, initial pH 1.5–2.5, and chalcopyrite concentrates is considered. The main assumption is that chalcopyrite can be anodically oxidized or cathodically reduced depending on [Fe³⁺]/[Fe²⁺] in solution. When chalcopyrite is oxidized at high [Fe³⁺]/[Fe²⁺] levels, Cu²⁺ is formed directly at low rates: CuFeS₂ + 4Fe³⁺ → Cu²⁺ + 5Fe²⁺ + S⁰. Whereas, when chalcopyrite is reduced at low [Fe³⁺]/[Fe²⁺] levels, an intermediate (Cu₂S) is formed at higher rates: CuFeS₂ + Fe²⁺ + Cu²⁺ + 2H⁺ → Cu₂S + 2Fe³⁺ + H₂S. Because the oxidation of Cu₂S is relatively fast: Cu₂S + 4Fe³⁺ → 2Cu²⁺ + S⁰ + 4Fe²⁺, its accumulation is assumed to be negligible. To take into account the possibility of chalcopyrite being oxidized or reduced depending on [Fe³⁺]/[Fe²⁺] in solution, the principle of mixed potentials is used. The model is validated by comparing the calculated and measured values of copper extraction, total iron in solution, and pH.     

Specifics of the sulfuric-acid processing of galena concentrates in the presence of nitrous acid

Conclusions  

The performance of nano multicomponent cocatalyst in the improvement of catalytic sensor of methane

Based on the deficiency of catalytic elements in methane sensors such as sintering, activity decrease and surface area reduction at high temperature, three different nano vectors Ce-Zr-Al₂O₃, Ce-Al₂O₃, and Zr-Al₂O₃ were prepared via sol-gel technique in the experiment. BET surface area, catalytic activity and thermal stability were tested and compared. It is found from the experiment that the Ce-doped Al₂O₃ vector possesses higher catalytic activity than pure Al₂O₃ vector. Zr-doped Al₂O₃ vector can enhance the thermal stability of methane sensors. Ce-Zr-Al solid solution can be obtained by the presence of Ce and Zr doped with Al₂O₃. The reaction activity and thermal stability of catalytic sensors were improved because of the unique synergy effect from Ce-Zr-O. Among the mixed cocatalysts, Ce-Zr-O was reported to be an excellent cocatalyst material. The performance of methane sensors can be improved significantly via the modification of Ce-Zr-Al₂O₃ vector.     

Modelling of high voltage pulse breakage of ores

A high voltage pulse (HVP) breakage model was developed as a general modelling structure to represent the three HVP breakage indices: body breakage probability (the D₁-model), body breakage product fineness (the D₂-model), and body breakage product pre-weakening degree (the D₃-model). Relations between the HVP breakage indices and HVP pre-concentration characterisation curves were established. The preliminary result indicated that the HVP breakage model has the potential to predict the recovery of valuable metals from the calibrated model parameters. A t_n-family of curves (t_n is defined as cumulative percentage of product passing 1/n of the initial size) was used to describe the HVP breakage product size distribution. The t_n-family of curves can be employed to estimate the product size distribution from the predicted t₁₀ values by the D₂-model.