锰球制备条件对氮化反应的影响

利用自制的密闭氮化系统研究不同制备条件的锰球的氮化反应.考察锰粉粒度、成球压力和黏结剂添加量对氮化反应的影响,并测量锰球氮化过程中实时增重和温度曲线.实验结果表明：锰粉粒度由16~40目变成60~80目时,球心温度到达峰值的时间由164 s缩短为101 s,球心最大温升由147℃增至233℃,氮化1 h的转化率由90.81%增至93.64%;成球压力由266 MPa增至443 MPa,球心峰值温度将提前89 s到达,球心最大温升将提高22℃,氮化1 h的转化率由91.59%增至94.92%;黏结剂添加量由1 g增至3 g,氮化1 h的转化率由92.90%降至89.80%;正态对数分布的概率密度函数可用来近似拟合转化速率与时间的关系.     

低温下氢气还原氧化铁的动力学研究

 用热重分析法研究了低温下不同粒度氧化铁的氢还原动力学,得出在同一温度下,铁矿粉粒度从107.5 μm降到2.0 μm后,由于粉体的表面积大幅度增加,提高了粉气接触面积,从而使得化学反应的速度提高了8倍左右,还原反应的表观活化能从78.3 kJ/mol降低到36.9 kJ/mol;当反应速度相同时, 粒度6.5 μm的粉体的反应温度比107.5 μm的降低了80 ℃左右。同时,通过理论推导和实验结果表明,当反应扩散层厚度相同时,铁矿粉粒度越小,反应扩散层厚度越薄,其还原率越高。     

氮化锰球生产工艺优化的技术方向

简要介绍了氮化锰生产的理论依据及工业生产氮化锰的工艺流程。采用热重分析方法研究了氮化锰产品在氩气下的热稳定性。研究结果表明:当温度升至800℃以上时,氮化锰会发生热分解,氮化温度对氮化锰产品的质量有重要影响;对氮化锰球产品的氮质量分数进行了检测分析,初步实验研究表明:产品氮质量分数低、成分偏差较大的原因是在氮化过程中氮化温度制度不合理以及锰氮反应放热引起了金属锰熔化。同时探讨了关于氮化锰球生产工艺优化的技术思路。     

氮化锰氮含量的工艺控制方法

介绍利用金属锰球,采用"固态氮化方法"生产氮化锰的原理和工艺。使用正交法,在氮化锰中试线上,利用纯氮气(≥99.95%),采用三种不同粒径的金属锰粉,分批次进行正交法试验,在恒定高纯氮气气氛(0.25 MPa)压力下,设定氮化温度和氮化时间,生产出不同氮含量的氮化锰产品,从而得出氮含量不同的氮化锰产品的工艺控制方法,有利于根据生产的质量技术要求,优化生产工艺。     

氢气还原氧化铁动力学的非等温热重方法研究

 用非等温热重分析法对氢气还原不同粒度细微氧化铁的动力学进行了研究。研究表明：铁矿粉粒度越小,起始反应温度越低,反应速度越快,反应达到平台期时所对应的还原率越高;平均粒度为3.5 mm的铁矿粉在400 ℃还原反应开始,700 ℃左右开始反应加快,达到平台期时的还原率为77%,而平均粒度为2 μm的铁矿粉在100 ℃已经开始反应,350 ℃反应加快,达到平台期时的还原率为98%,而且在600 ℃时还原率就达到了100%;铁矿粉粒度从3.5 mm降到2 μm后,还原反应的表观活化能从73.3 kJ/mol降低到30.46 kJ/mol;同时通过分析氢气还原氧化铁的反应机理得出,内扩散和界面化学反应均对整个反应过程起限制作用。     

硅粉直接氮化反应热力学分析及动力学机理研究

用TG-DSC热重同步热实验分析的方法,研究不同升温速率下,硅粉氮化机理及化学反应动力学.发现温度在1 000~1 300 ℃时:差示扫描量热曲线各出现一个吸热、一个放热峰,说明氮化机理已发生改变.在1 000~1 100 ℃温度范围内,氮化硅转化率显著增加,即温度是影响其转化率的主要因素.实验表明:氮化反应的限制性环节由反应开始阶段的界面化学反应控制和之后的界面化学反应与内扩散混合控制组成;通过动力学计算得到表观活化能E=404.5 kJ/mol,频率因子A=9.57×1015 m/s,反应级数n=0.95,最终得到反应的速率方程的数学表达式.      

不同形貌升华氧化钼的还原动力学研究

本文以2种不同形貌升华氧化钼为原料,采用TG-DTA法研究了不同升温速率(3℃/min、5℃/min、10℃/min)下氢气还原氧化钼的动力学。结果表明:2种不同形貌的升华氧化钼一段还原反应起止还原温度几乎相同。但失重速率480℃前1~#MoO_3高于2~#MoO_3,480℃后1~#MoO_3失重速率低于2~#MoO_3。二段还原反应1~#MoO_3的反应温度较2~#MoO_3低。再通过用Flynn-Wall-Ozawa和Kissinger动力学分析方法计算2种不同形貌升华氧化钼的一段平均表观活化能为1~#MoO_3为89. 26 kJ/mol,2~#MoO_3为79. 86 kJ/mol,而二段表观活化能1~#MoO_3平均为103. 53 kJ/mol,2~#MoO_3为93. 16 kJ/mol。     

氮气压力对锰球氮化反应的影响(Ⅱ)

利用自制的密闭氮化系统研究了不同压力下的锰球氮化反应。锰球的制备条件为:锰粉重量100 g、锰粉粒度16~20目、粘结剂添加量2 wt%和成球压力354 MPa。氮化炉温为900℃,氮化时间3 600 s。实验记录了在不同的氮气压力下锰球氮化实时增重和温度曲线。实验结果显示,当氮气压力从0.2 MPa升高至0.6 MPa时:(1)反应速率峰值时刻由266 s缩短至86 s,球心温度峰值时刻由324 s缩短至138 s,球心温度恢复至炉温时刻由1310 s缩短至642 s;(2)球心温度峰值由945℃升高至1 049℃,球心最大温升由55℃升高至159℃;(3)氮化3600 s时的增重率由6.46%增至8.09%,转化率由81.34%增至93.62%;(4)增重速率峰值由8.15×10~(-3) s~(-1)增至62.7×10~(-3) s~(-1),转化速率峰值由10~3×10~(-3) s~(-1)增至726×10~(-3) s~(-1);(5)增重率达到6.46%的时间由3 600 s缩短为555s,缩短84.6%。     

氮气压力对锰球氮化反应的影响(Ⅰ)

利用自制的密闭氮化系统研究了不同压力下的锰球氮化反应。锰球的制备条件为:锰粉重量100 g、锰粉粒度16~20目、粘结剂添加量质量分数为2%和成球压力354 MPa。氮化炉温为900℃,氮化时间3 600 s。实验记录了在不同的氮气压力下锰球氮化实时增重和温度曲线。实验结果显示,当氮气压力从0.2 MPa升高至0.6 MPa时:(1)反应速率峰值时刻由266 s缩短至86 s,球心温度峰值时间由324 s缩短至138 s,球心温度恢复至炉温时由1 310 s缩短至642 s;(2)球心温度峰值由945℃升高至1 049℃,球心最大温升由55℃升高至159℃;(3)氮化3 600 s时的增重率由6.46%增至8.09%,转化率由81.34%增至93.62%;(4)增重速率峰值由8.15×10~(-3)s~(-1)增至62.7×10~(-3)s~(-1),转化速率峰值由103×10~(-3)s~(-1)增至726×10~(-3)s~(-1);(5)增重率达到6.46%的时间由3 600 s缩短为555 s,缩短84.6%。     

工业锰粉氮化工艺的试验研究

以氮化锰粉氮含量为目标,采用单因素试验方法考查氮化温度、锰粉粒度以及氮化时间对氮含量的影响;采用XRD对氮化锰粉的结构进行了分析,并在此基础上应用二次回归正交试验设计方法建立二次方程优化氮化锰粉的制备工艺,经过F检验,回归方程显著性好。结果表明,最佳工艺条件是:氮化温度为836℃,氮化时间8h,氮气压力为1.72P°(101.3kPa),可获得含氮量高达8.35%(质量分数)的氮化锰产品。     

Influence of size of hematite powder on its deoxidation kinetics with H2 at low temperature

 The deoxidation kinetics of hematite ore with various particle sizes with hydrogen at low temperature and reduction mechanisms were studied using the thermogravimetric analysis. Under the same temperature, after particle size of powder becomes thinner from 107.5μm to 2μm, the surface area of powder and the contact area between powder and gas increase, which makes the deoxidation process of hematite accelerate about 8 times, and the apparent activation energy of deoxidation reaction drops to 36.9 kJ/mol from 78.3 kJ/mol because of activity of ore powder improved with refining gradually. Under the same reaction rate, the reaction temperature of 6.5μm powder decreases about 80℃ than that of 107.5μm powder. Thinner diffusion layer also helps accelerate the reaction with powder refining. The higher the temperature, the greater peak of deoxidation rate is; under the same temperature, the greater the particle size, the smaller the peak of deoxidation rate is; both inner diffuse and interface chemical reaction play an important role in the whole reaction process.     

Influence of Size of Hematite Powder on Its Reduction Kinetics by H2 at Low Temperature

The reduction kinetics and mechanisms of hematite ore with various particle sizes with hydrogen at low temperature were studied using the thermogravimetric analysis. At the same temperature, after the particle size of powder decreases from 107.5 μm to 2. 0 μm, the surface area of the powder and the contact area between the powder and gas increase, which makes the reduction process of hematite accelerate by about 8 times, and the apparent activation energy of the reduction reaction drops to 36.9 kJ/mol from 78.3 kJ/mol because the activity of ore powder is improved by refining gradually. With the same reaction rate, the reaction temperature of 6. 5 μm powder decreases by about 80 ℃ compared with that of 107.5 μm powder. Thinner diffusion layer can also accelerate the reaction owing to powder refining. The higher the temperature, the greater is the peak of the reduction rates at the same temperature, the greater the particle size, the smaller is the peak value of the reduction rates both inner diffusion and inter-face chemical reaction play an important role in the whole reaction process.     

硫铁矿-木炭湿法浸出高铁氧化锰矿的研究

针对两矿法浸出高铁氧化锰矿存在生成大量单质硫并覆盖在矿物颗粒表面,降低了反应速率的问题,研究采用在浸出过程中添加木炭粉的方法吸附单质硫以改善浸出效果。考察了木炭粉添加量、硫铁矿用量、硫酸浓度、浸出温度和浸出时间对高铁氧化锰矿中锰浸出率的影响。在高铁氧化锰矿用量10.0g、硫铁矿用量5.0g、木炭粉添加量0.1g、硫酸浓度1.36mol/L、浸出温度70℃和浸出时间4h的条件下,锰浸出率达到96.7%。     

Activation Energy of Nitriding Medium Carbon Ferromanganese Alloy

Investigation of some kinetics aspects of the reaction between nitrogen and medium carbon ferromanganese (MC-FeMn) was made. Nitriding process of fine medium carbon ferromanganese was carried out at temperature ranging from 973 to 1 223 K and time up to 480 min. Nitriding was carried out under nitrogen and hydrogen gas pressures. At temperature of 573 K, hydrogen gas was injected with pressure of about 0.2 MPa followed by injection of nitrogen gas up to 1.2 MPa. Sample mass was 35 g, nitrided in cylindrical chamber with 34 mm in inner diameter and 1 200 mm in length. The change in nitrogen pressure was taken as an indication for nitrogen pickup. The mass gain i.e. nitrogen pickup in kilograms per surface area (m2) was determined by time at different temperatures. Nitriding rate constants were calculated and the activation energy of nitriding process was derived from Arrhenius equation. The nitriding rate constant was found to be increased by increasing temperature of the reaction. The activation energy of nitriding process of fine medium carbon ferromanganese at time ranging up to 28 800 s is around 140 kJ/mol. It was found that the rate controlling step of the nitriding process of MC-FeMn is diffusion mechanism.     

石煤与软锰矿焙烧样耦合提取钒锰的动力学

为实现石煤与软锰矿焙烧样中钒锰的共提取,并解决石煤二段硫酸化焙烧过程中酸过量的问题,通过多因素研究探讨石煤与低品位软锰矿焙烧样耦合浸出工艺对钒锰共浸出率的影响,为石煤及低品位软锰矿焙烧样中钒锰资源高效综合利用提供了参考和依据。试验结果表明,当石煤与低品位软锰矿焙烧样的配矿比为1：1、矿浆液固比为5：1及浸出温度为80℃时,耦合浸出体系中钒的浸出率可达98．13％,而锰的浸出率可达99．45％。对耦合浸出体系的钒锰浸出动力学研究表明,钒浸出过程是通过固体产物层的内扩散控制,其表观活化能为22．401kJ／mol;锰浸出过程在低温区25～55℃下是通过化学反应控制,其表观活化能为57．232kJ／mol,高温区65～95℃下锰浸出过程是通过固体产物层的内扩散控制,其表观活化能为14．323kJ／mol。     

Kinetics of manganese reduction leaching from weathered rare-earth mud with sodium sulfite

The kinetics of manganese reduction leaching in an acidic medium from a weathered rare-earth mud (WREM) were investigated. Using sodium sulfite as a reductant, the effect of reaction temperature, mechanical agitation rate, sulfuric acid dosage, and feed particle size on leaching kinetics were examined. The leaching process can be described by the shrinking-core model. An apparent activation energy of 11.5 kJ/mol for manganese reduction leaching is estimated. The diffusion of reactants and leaching products through a porous ore matrix was found to be the rate-limiting step. An empirical equation relating the manganese leaching rate constant with feed-particle size and leaching temperature was established. It was found that the smaller the feed-particle size or the higher the leaching temperature, the faster the leaching proceeds, as anticipated. The kinetic process exhibited a self-catalysis characteristic of Mn²⁺ in the mud. This finding suggests that Mn(III,IV) in the mud was rapidly reduced to Mn²⁺ during the initial stage of leaching.