用循环流化床技术焙烧金矿石

鲁奇冶金公司(自2002年起成为奥托昆普工艺公司的一部分,现已更名为奥托昆普工艺公司)在将近50年大量应用流化床工艺的过程中,以几种不同类型的反应器逐步发展了流化床技术。流化床反应器系统的适用性已在包括固体燃料的矿物处理和黑色及有色冶金工艺中得到了证实。工艺应用包括焙烧、煅烧、燃烧、煤的炭化以及烟气处理。     

流化床处理粉铁矿工艺研究

评述了流化床处理粉铁矿的工艺,根据流化床反应器在工业中的应用实际,分别评述了流化床磁化焙烧生产铁精矿,流化床预热粉铁矿并低预还原度还原后添加到铁浴熔池,流化床生产直接还原铁(DRI)和碳化铁(Fe3C)作电炉炼钢原料,多级流化床生产较高预还原度DRI供熔融气化炉终还原冶炼铁水等工艺中流化床反应器的应用.     

《中国有色冶金》2006年(第35卷)总目次

篇名期次国外工程技术清洁的炼钢工艺l确保弃渣含铜较低的三菱工艺l用循环流化床技术焙烧金矿石2曼托维蒂堆浸一溶剂浸出一电积厂的工艺改进2改进的EcuPrex工艺—处理含黄铜矿铜精矿有前途的湿法冶金工艺3用旋涡熔炼法直接生产白冰铜和粗铜3铜湿法冶金现状及未来发展方向4艾萨熔炼法—不只是昙花一现4采用高电流密度生产优质电积铜5铜冶炼厂现有最佳硫酸生产技术:最新总结5综述与专论在不断创新中开创新的百年—水口山有色金属集团有限公司110年创新发展历程和展望6轻金属大型预焙铝电解槽侧部破损的处理方法l白银160 kA电解槽技术改造实…     

ZEWA--处理钢铁工业废料以获得有价值产品的冶金新工艺

ZEWA冶金新工艺将工业废料转化成铁水或矿物类产品如生产水泥用的水硬性胶结物、脱硫用冶金渣、铺路用材料等。工艺中包括专门设计的电加热反应器,用以进行高温熔融还原处理。一个包括所有必要的辅助设施在内的示范厂已在捷克共和国的Vitkovice钢厂建成,11次试验证实了利用碳钢和不锈钢生产的废料来生产铁水和有价值矿物类产品的技术和经济可行性。     

难处理金精矿加压氧化浸出技术的工业应用

1　前言戴纳泰克 (Dynatec)公司冶金技术工程部是高压湿法冶金领域公认的主导企业。在有色金属湿法冶金技术的开发与商品化方面 ,已具有 50年的历史。其前身是谢里特公司 (Sherritt)。几十年来 ,该公司致力于开发多种处理工艺 ,包括锌与铅锌混合硫化物精矿 ,以及铜、镍、钴、硫化物精矿 ,难处理金精矿、硫化物矿渣等有色金属提取冶金工艺。本文主要介绍戴纳泰克公司加压浸出难处理金精矿提金的工业化实例。戴纳泰克提金技术常用来从难处理硫化物原料中回收金。许多金矿石和精矿含有细粒金 ,它们被包在黄铁矿或砷黄铁矿这样的硫化物中 ,这些…     

转炉出钢口套整体袖砖工艺技术开发

介绍了天津天铁冶金集团有限公司炼钢厂转炉出钢口袖砖工艺的开发过程，主要工艺参数的制定，实践证明，该工艺的应用取得了良好的使用效果。     

振动反应器在锌湿法冶金中的应用及设计研究

本文概述了国外在湿法冶金中应用振动技术研究工作的最新试验成果，着重介绍了国内在锌湿法冶金中振动反应器用于浸出与净化的半工业试验情况，振动反应器的结构及主要参数选择等，供研制和设计振动反应器参考。     

现代锌处理技术的最新经验

自从1969年芬兰的科科拉（kokkola）锌厂投产以来，奥托昆普已在几个扩产阶段中开发并拓展了焙烧、浸出、净液和电积等锌厂工艺，开发出了取代黄钾铁矾工艺的奥托昆普转化浸出工艺、基于砷的奥托昆普净液工艺和奥托昆普精矿直接浸出工艺等新工艺。自收购了挪威锌公司奥达厂和德国ObemrSel的鲁奇冶金公司后，奥托昆普在焙烧、烟气净化、制酸和电积方面扩展了其技术诀窍。鲁奇冶金公司于1962年在印度第一次投入锌焙烧炉开始了其锌方面的商业运作，其后共有70多台鲁奇锌焙烧炉在世界各地投产。由于这些成绩，奥托昆普现在可以将目前的锌处理技术融合在一整套技术内。     

基于CPFD的流化床反应器的数值模拟

流化床反应器已被广泛应用于冶金等领域,其结构设计、优化与放大至关重要。本文利用计算颗粒流体力学(CPFD)商业软件对两种典型的流化床反应器的颗粒-流体流动进行了数值模拟,结果显示该方法能够有效模拟颗粒和流体的真实运动状态,可以为设计人员和使用人员的设计、选型、控制和操作提供相应的理论依据。     

提高炼铜炉渣贫化率的搅拌方法研究

本文突出了强化火法冶金炉渣贫化工艺的可行性。通过试验得到了不同搅拌条件对重金属沉降效果的影响,试验原料为奥路毕斯贫化炉的炉渣。此外,本文还论述了强化渣贫化的新西马格搅拌反应器原理,以及在亚琛建立工业规模反应器、在汉堡建立示范性反应器的条件。     

Iron ore reduction in a continuously operated multistage lab-scale fluidized bed reactor—Mathematical modeling and experimental results

Industrial-scale fluidized bed processes for iron ore reduction (e.g., FIOR and FINMET) are operated by continuous feeding of ore, while laboratory tests are mostly performed under batchwise operation. The reduction behavior under continuous operation is influenced by both the residence time of the iron ore particles and the reduction kinetics, which is obtained by batch tests. In a mathematical model for such a process, the effect of both phenomena has to be considered. The residence time distribution of iron ore particles in a laboratory fluidized bed reactor was obtained by measuring the response of a step input and described by mathematical models similar to a continuously stirred tank reactor. In the same reactor, reduction tests with continuous feeding of iron ore were performed. Based on batch tests in a fluidized bed reactor, a mathematical model was developed to describe the kinetics of iron ore reduction under fluidized bed conditions. This kinetic model was combined with the fluidized bed reactor model to describe continuous iron ore reduction. In this detailed model, the change of gas composition while rising in the fluidized bed was considered. The degree of reduction and the gas conversion for reactors in series were calculated. The results obtained by the mathematical model were compared with experimental data from the laboratory-scale reactor.     

Fluidized Bed Roasting Process for Desulphurization of Scheelite

Studies on roasting of sheelite concentrate have been carried out in fluidized bed to reduce its sulphur content to <5%. Initial investigations have been done using a 10 cm I.D. fluidized bed roaster and the data so generated was used for the design of a fluidized bed roaster of 50 kg/hr capacity. The experiences on roasting of sheelite concentrate with the fluid bed reactor and the methods for scale up to large size reactor are presented.     

流化床反应器的流动模型

在理论分析的基础上,建立了流化床反应器的流动模型,给出了气体流速、床体尺寸、处理能力等参数的计算公式和判断内部流态化流型的依据。在此基础上,给出了1个模型的算例,并与文献给出的计算结果相比较,结果表明二者的符合性较好,根据模型计算得到的参数具有良好的合理性。该模型对使用流化床反应器炼铁有一定的指导意义。     

流化床反应器的流动模型

在理论分析的基础上,建立了流化床反应器的流动模型,给出了气体流速、床体尺寸、处理能力等参数的计算公式和判断内部流态化流型的依据。在此基础上,给出了1个模型的算例,并与文献给出的计算结果相比较,结果表明二者的符合性较好,根据模型计算得到的参数具有良好的合理性。该模型对使用流化床反应器炼铁有一定的指导意义。     

CO2 Capture from Flue Gases Using Three Ca-Based Sorbents in a Fluidized Bed Reactor

Experiments of CO2 capture and sorbent regeneration characteristics of limestone, dolomite, and CaO/Ca12Al14O33 at high temperature were investigated in a thermogravimetric analyzer (TGA) and a fluidized bed reactor. The effect of reactivity decay of limestone, dolomite, and CaO/Ca12Al14O33 sorbents on CO2 capture and sorbent regeneration processes was studied. The experimental results indicated that the operation time of high efficient CO2 capture stage declined continuously with increasing of the cyclic number due to the loss of the sorbent activity, and the final CO2 capture efficiency would remain nearly constant, due to the sorbent already reaching the final residual capture capacity. After the CO2 capture step, the Ca-based sorbents need to be regenerated to be used for a subsequent cycle, and the multiple calcination processes of Ca-based sorbent under different calcination conditions are studied and discussed. Reactivity loss of limestone, dolomite and CaO/Ca12Al14O33 sorbents from a fluidized bed reactor at both mild and severe calcination conditions was compared with the TGA data. At mild calcination conditions, TGA results of sorbent reactivity loss were similar to the experimental results of fluidized bed reactor for three sorbents at 850°C calcination temperature, and this indicated that TGA experimental results can be used as a reference to predict sorbent reactivity loss behavior in fluidized bed reactor. At severe calcination condition, sorbent reactivity loss behavior for limestone and dolomite from TGA compare well with the result from a fluidized bed reactor.     

Use of a tapered fluidized bed as a continuous bioreactor

Reactor systems based on tapered fluidized beds are being developed for aqueous bioprocesses in which adhering microorganisms or immobilized active biological fractions are used. The use of a fluidized bed prevents biomass buildup, accommodates particulates in the feed stream, is compatible with gas sparging, and allows easy removal or addition of the active materials. The tapered reactor tends to stabilize the fluidized bed, thus allowing a much wider range of operating conditions. Preliminary experimental results and an empirical mathematical model of the tapered bed indicate that bed stability is associated with a decreasing velocity and void-fraction profile up the bed and the pressure drop across the bed decreases with increasing flow rates. The tapered fluidized bed bioreactor is being evaluated for use in the enzymatic production of hydrogen, microbiological denitrification, and microbiological degradation of coal conversion aqueous waste streams. The enzyme catalyzed conversion of lactose to glucose and galactose was used in the evaluation of the reactor concept.     

On the Distributors and Design Criteria for Gas-Solid and,Gas-Liquid-Solid Fluidized Beds

Fluidized beds are well known for their versatile applications in chemical, metallurgical, mineral and bio - processing industries. Inspite of their several potential uses, the design and selection of the fluidized bed reactor is still empirical. One of the key parts which influences the reactor performance is the distributor/grid which has been recognized as the heart of the fluidized system. Distributor also called grid in fluidized bed plays a vital role in assessing the hydrodynamics and performance of the reactor. Though the importance of the distributor has long since been recognized, not much seems to have been done on basics of its design aspects. In the context of significant developments that have taken place in the field in the last decade the need exists for a comprehensive review updating the available information on the role of distributors and their design for the fluid bed system. Hence a state-of-the-art review of a wide range of distributors/grids has been attempted in this paper and the need for careful consideration of the design principles is discussed. Prediction of operating flow rates as influenced by distributors, pressure drop criteria pertinent to stability of operation, the choice of grids or distributors and their types from laboratory scale to commrecial size units, design models and the role of plenum chamber and pumping requirements are all critically reviewed and analyzed. Nomographs for the distributor design and the scope for future research stressing the immediate needs are presented.     

The kinetics of nickel oxide reduction by hydrogen; Measurements in a fluidized bed and in a gravimetric apparatus

The suitability of a batch fluidized bed laboratory reactor for measuring the rates of gas-solid reactions was investigated. Experiments were carried out on the reduction of Falconbridge nickel oxide by hydrogen in a batch fluidized bed reactor within the tem-perature range 550 K to 650 K using particles in the range of 60 to 100 mesh. The reactor was operated at approximately atmospheric pressure and gas flow rates were in the range of two to four times the minimum fluidization velocity at temperature. The results showed internal consistency and rough agreement with the results of previous workers. The re-sults were interpreted and correlated by means of a structural model for gas-solid reac-tions. As a check on the fluidized bed measurements, experiments were also carried out using the conventional gravimetric technique to measure the rate of reduction of compac-ted pellets of nickel oxide by hydrogen. When due allowance was made for the change of surface area of the oxide during compaction, the results were in close agreement with the fluidized bed results. Rate measurements using hydrogen-nitrogen mixtures revealed that the reaction is not first order with respect to hydrogen, as usually assumed, but is ap-proximately of order two-thirds at one atmosphere hydrogen partial pressure. Formerly Graduate Student at Berkeley     

Treatment of Landfill Leachate by a Combined Anaerobic Fluidized Bed and Zeolite Column System

The use of a combined anaerobic fluidized bed and zeolite fixed bed system in sanitary landfill leachate treatment was investigated. Anaerobic treatability studies were successfully performed in the anaerobic fluidized bed reactor. The chemical oxygen demand (COD) removal was attained up to 90% with increasing organic loading rates as high as 18?g?COD/L?day after 80?days of operation. Good biogas production yield (Ygas) of 0.53?L biogas per gram removed COD with methane (CH4) content of 75% was obtained. The attached biomass concentration increased along the column height from bottom to top, and its mean value was found 6,065?mg/L after 100?days of operation. The anaerobically treated landfill leachate was further treated by a zeolite fixed bed reactor. While excellent ammonia removal (>90%) was obtained with the untreated zeolite, the regenerated zeolites showed higher performance. Consequently, this combined anaerobic and adsorption system is an effective tool to remove high COD and high ammonia in landfill leachate.