硝酸胺溶液浸提硬硼酸钙的动力学研究

对硬硼酸钙在硝酸铵水溶液的溶解在间歇式反应器中就搅拌速度、粒径大小、反应温度、固液比和溶液的浓度等参数的影响进行了研究。结果表明溶解速度随温度、硝酸铵水溶液的浓度以及粒径和固液比的增加而增加,但搅拌速度对溶解速度无重要影响。硬硼酸钙在硝酸铵水溶液中可以高达100%。硬硼酸钙的溶解动力学根据多相和均相反应模型进行了检验。实验数据表明有高的活化能,说明基于多相反应动力学模型的溶解速度可表达为：1-(1-X)^1/3=3.28 ×10⁴·D^{-0.653 7}·C^{1.295 8}·(S/L)^{-0.490 9}·e^-41.40/(RT)·t。反应过程的活化能为41.40 kJ·mol^-1。     

酸性AlCl3-BMIC离子液体中的铝阳极溶解

采用线性扫描伏安法研究了Lewis 酸性AlCl₃-BMIC (BMIC: 1-butyl-3-methylimidazolium chloride)离子液体中铝电极的溶解. 铝电极在阳极极化时出现了钝化现象, 钝化是由于在铝电极表面形成了固体AlCl₃钝化膜造成的. 铝的电化学溶解过程可以依次分为三个区: 电化学控制区、过渡区和钝化区. 在电化学控制区, 铝的电化学溶解速率随着电位的正移而逐渐增加; 在过渡区, 由于电极表面AlCl₄^-和Al₂Cl₇^-浓度发生改变而析出固体AlCl₃使得铝电化学溶解速率随着电位的正移而逐渐减小; 当钝化膜形成之后, 铝的电化学溶解速率不再随着电位的正移而发生改变, 铝溶解进入钝化区. 增加搅拌、升高温度、降低离子液体AlCl₃摩尔分数都可以增加铝溶解阳极极限电流密度.     

水热条件下坡缕石在NaOH溶液中的行为及结构变化

分别用1,2和3 mol·L^-1的NaOH溶液,在不同的温度条件下对坡缕石进行了侵蚀实验。对反应后的固相产物进行了XRD和SEM分析,对浸出液中的金属阳离子进行了原子吸收光谱分析。讨论了反应温度和碱溶液浓度对碱溶后产物的影响。XRD和SEM结果表明,c_NaOH≤2 mol·L^-1时,坡缕石经碱溶液侵蚀后,可以生成蒙脱石和方沸石,其中反应温度的升高有利于方沸石的形成,碱溶液浓度的升高有利于蒙脱石的形成。当碱溶液浓度达到3 mol·L^-1,反应温度为200 ℃时,最终产物为SiO₂。浸出液的定量分析结果显示,坡缕石与碱溶液的反应过程中,Na⁺对八面体阳离子的置换具有选择性,置换顺序为：Al³⁺＞Fe³⁺(Fe²⁺)＞Mg²⁺。     

中温固体氧化物燃料电池阴极材料LaBiMn2O6的制备与性能

采用固相法合成了中温固体氧化物燃料电池(IT-SOFCs)阴极材料LaBiMn₂O₆,并利用X射线衍射(XRD)和电化学阻抗谱(EIS)进行表征。结果表明该材料与电解质Ce_0.7Bi_0.3O_1.85(CBO)在1000℃烧结12h不发生反应。交流阻抗和直流极化测试结果发现,阴极极化电阻随测试温度的增加而逐渐减小,700℃空气中的极化电阻为0.71Ω·cm²;氧分压测试结果显示,在600~700℃范围内,电极反应的速率控制步骤为电极上发生的电荷转移反应。电极过电位为85mV时,700℃的阴极电流密度达到216mA·cm^-2,表明LaBiMn₂O₆是一种潜在的中温固体氧化物燃料电池(IT-SOFCs)阴极材料。     

中温固体氧化物燃料电池阴极材料LaBiMn2O6的制备与性能研究

采用固相法合成了中温固体氧化物燃料电池(IT-SOFCs)阴极材料LaBiMn₂O₆,并利用X射线衍射(XRD)和电化学阻抗谱(EIS)进行表征.结果表明该材料与电解质Ce_0.7Bi_0.3O_1.85(CBO)在1 000 ℃烧结12 h不发生反应.交流阻抗和直流极化测试结果发现,阴极极化电阻随测试温度的增加而逐渐减小,700 ℃空气中的极化电阻为0.71 Ω·cm²;氧分压测试结果显示,在600~700 ℃范围内,电极反应的速率控制步骤为电极上发生的电荷转移反应.电极过电位为85 mV时,700 ℃的阴极电流密度达到 216 mA·cm^-2 ,表明LaBiMn₂O₆是一种潜在的中温固体氧化物燃料电池(IT-SOFCs)阴极材料.     

MCM-41负载S2O82-/TiO2固体超强酸的制备和酯化性能研究

采用液相沉积法制备了由MCM-41介孔分子筛负载S₂O₈^2-/TiO₂的固体超强酸催化剂。探讨了成酸机理，并以乙酸和异戊醇的酯化反应作为探针反应考察了焙烧温度、浸渍溶液浓度等制备条件对催化剂催化活性的影响，得到了较佳的制备条件。XRD、N₂吸附-脱附和FTIR结果表明，固体超强酸保持了MCM-41的介孔结构，BET表面积高达211 m²·g^-1，且具有强酸性(H_o<-12.70)。     

纳米SO42-/ZrO2的合成及其在酯交换反应中的催化性能

采用两步晶化-后浸渍法合成了纳米SO₄^2-/ZrO₂固体酸催化剂,并考察了其在植物油与甲醇酯交换反应中的催化性能。XRD、N₂吸附-脱附和TEM等结果表明,经过600℃焙烧,催化剂仍保持单一四方相,粒径大小为5~10 nm,比表面积为137 m²·g^-1,孔径为3.6 nm。NH₃-TPD结果表明,随着焙烧温度升高,催化剂表面的酸含量和酸强度逐渐增加,超强酸含量的增加,更有利于反应在温和条件下进行。在酯交换反应中,当醇油物质的量之比为20：1,反应温度为135℃,反应时间为6 h,600℃焙烧后催化剂用量为5%（w/w）时,植物油能够完全转化为脂肪酸甲酯。与传统的SO₄^2-/ZrO₂催化剂相比,该催化剂在低温反应条件下具有更高的催化性能和良好的重复使用性。     

正、反向共沉淀法对Pr2Zr2O7纳米粒子表观活化能的影响

以氨水作为沉淀剂,采用正、反向共沉淀法制备Pr₂Zr₂O₇纳米粒子。利用XRD、SEM、TEM、TG-DTA等测试手段表征了样品物相及形貌;研究其制备过程中合成动力学和晶粒生长动力学,采用Doyle-Ozawa法和Kissinger法分别计算正、反向沉淀粒子在主要反应阶段的表观活化能。结果表明：反向沉淀的滴定速率为2mL·min^-1、母盐溶液初始浓度0.05mol·L^-1、反应体系温度273K、pH值11、煅烧温度为1173K,保温2h的条件下获得的样品形貌近球形、无团聚现象、一次粒径约60nm。Pr₂Zr₂O₇前驱体的分解过程分为3个阶段,正、反向粒子各阶段平均表观活化能分别为：71.2、197.8、183.2kJ·mol^-1和45.37、84.34、152.16kJ·mol^-1;晶粒生长活化能分别为19.02和11.95kJ·mol^-1,后者比前者的晶粒生长活化能降低了7.07kJ·mol^-1;反向共沉淀制备工艺优于正向共沉淀法。     

含两个酰胺基团的卟啉二聚体分子间氢键引起的发光光谱红移

通过5-（4-甲酸基苯基）-10,15,20-三（4-十二烷氧基苯基）卟啉（HAcTPP）与乙二胺,丙二胺和丁二胺反应,制备了一类含2个酰胺基团的卟啉二聚体C₂（AmTPP）₂、C₃（AmTPP）₂和C₄（AmTPP）₂以及相应的配合物Pt2C₂（AmTPP）₂、Pt2C₃（AmTPP）₂和Pt2C₄（AmTPP）₂。采用¹H NMR、¹³C NMR、质谱、元素分析、循环伏安、紫外-可见吸收光谱和荧光发射光谱等对二聚体的化学结构、热稳定性、电化学和光物理性质进行了表征。实验发现,二聚体和相应的铂配合物的光致发光（PL）光谱性质与溶液的浓度有关,在10^-7 mol·L^-1 THF稀溶液中,二聚体与单羧基卟啉的PL光谱基本一致。当浓度增加到10^-3 mol·L^-1 THF溶液时,二聚体的光致发光光谱最大值从657 nm红移到675 nm,比单羧基卟啉红移了18 nm。当与金属铂配位后,这种发射光谱随浓度增加而变化的特性更加明显。二聚体配合物在10^-7 mol·L^-1 THF稀溶液中PL光谱就产生了红移现象,最大发射峰λ_max为673 nm,比单羧基卟啉红移16 nm。在高浓度10^-4 mol·L^-1 THF溶液和升华薄膜中的PL最大发射峰进一步红移到727 nm的近红外区。进一步,为了证实二聚体配合物分子间的π-π和Pt-Pt相互作用,我们以配合物Pt2C₃（AmTPP）₂为例,对二聚体配合物固体在常温和低温77 K的PL光谱进行了测试,发现固体配合物表现出与温度相关的PL性质。当温度降到77 K时,配合物的最大发射峰从658 nm红移到674 nm,红移了16 nm。实验表明,卟啉二聚体和相应的配合物的红移现象与二聚体的分子结构直接相关,卟啉二聚体中的两个酰胺基团能够产生较强的分子间氢键,导致二聚体分子之间产生一定程度的π-π和Pt-Pt相互作用,使得二聚体PL光谱产生红移。     

离子电池正极材料LiNi0.5Mn0.5O2的合成

采用共沉淀法制备锂离子电池正极材料LiNi_0.5Mn_0.5O₂，前驱体制备过程中金属离子氢氧化物的形貌、粒径分布和最终合成材料的性能息息相关。本文讨论了共沉淀反应过程中沉淀体系、pH值、搅拌速度和氨水浓度对沉淀产物形貌的影响。同时还考察了烧结制度对材料电化学性能的影响。结果表明，在优化条件下制备的正极材料LiNi_0.5Mn_0.5O₂首次放电容量高达178 mAh·g^-1，50个循环后放电容量稳定保持在165 mAh·g^-1(电压范围2.8～4.5 V，电流密度30 mA·g^-1)。     

А kinеtiс аnаlysis fоr prоduсtiоn of саlсium bоrоgluсоnаtе frоm colemanite

In this paper, the kinetic model of colemanite dissolution in gluconic acid solutions was carried out in a batch reactor. The effects of the particle size, reaction temperature, stirring speed, gluconic acid concentration, and solid/liquid ratio on colemanite dissolution were experimentally studied. The empirical parameters were the gluconic acid concentration (0.05-0.2 M), the temperature (20-50°C), the solid/liquid ratio (0.05/500-1.5/500 g⋅L⁻¹), particle size (193.5-1000 μm), and stirring speed (400-700 rpm). The kinetic models for heterogeneous solid-liquid reactions were used with the dissolution data in evaluating the kinetic. The dissolution of colemanite in gluconic acid solutions was controlled by diffusion through the product layer. The activation energy was found to be 8.39 kJ⋅mol⁻¹. The rate expression associated with the dissolution rate of colemanite depending on the parameters chosen may be summarized as follows:      

A study of dissolution kinetics of a Nigerian galena ore in hydrochloric acid

The results of experimental investigation on the study of dissolution kinetics of a Nigerian galena ore in hydrochloric acid solution were discussed. The influence of acid concentration, temperature, particle size, stirring speed and solid/liquid ratio on the extent of dissolution was examined. The elemental analysis by XRF showed that the galena ore is composed mainly of PbS with metals such as Sn, Fe and Zn occurring as minor elements and Mn, Rb, Sr and Nb as traces. The XRD analysis indicated galena as the dominant mineral phase, with the presence of associated minerals, such as α-quartz (SiO₂), sphalerite (ZnS), cassiterite (SnO₂), pyrite (FeS₂) and manganese oxide (MnO₂).Results of leaching studies showed that galena dissolution in HCl solution increases with increasing acid concentration and temperature; while it decreases with particle diameter and solid/liquid ratio at a fixed stirring rate of 450 rpm. The study showed that 94.8% of galena was dissolved by 8.06 M HCl at 80 °C within 120 min with initial solid/liquid ratio of 10 g/L. The corresponding activation energy, E_a was calculated to be 38.74 kJ/mol. Other parameters such as reaction order, Arrhenius constants, reaction and dissociation constants were calculated to be 0.28, 73.69 s^?1, 1.73 ± 0.13 × 10³ and 1.37 ± 0.024 × 10⁴ mol L^?1 s^?1, respectively. The mechanism of dissolution of galena was established to follow the shrinking core model for the diffusion controlled mechanism with surface chemical reaction as the rate controlling step for the dissolution process. Finally, the XRD analysis of the post-leaching residue showed the presence of elemental sulphur, lead chloride and α-quartz.     

Reaction kinetics of malachite in ammonium carbamate solution

The dissolution of malachite particles in ammonium carbamate (AC) solutions was investigated in a batch reactor, using the parameters of temperature, AC concentration, particle size, and stirring speed. The shrinking core model was evaluated for the dissolution rate increased by decreasing particle size and increasing the temperature and AC concentration. No important effect was observed for variations in stirring speed. Dissolution curves were evaluated in order to test shrinking core models for fluid-solid systems. The dissolution rate was determined as being controlled by surface chemical reaction. The activation energy of the leaching process was determined as 46.04 kJ mol^?1.     

Leaching of Celestite in Sodium Hydroxide Solutions and Kinetic Modelling

In this study, the dissolution kinetics of celestite in solutions of sodium hydroxide was investigated by batch process. The results showed that the parameters which had the greatest effect on the dissolution of celestite in sodium hydroxide solutions were reaction temperature, the concentration of sodium hydroxide and stirring speed. It was determined that the dissolution rate increased with increased stirring speed, sodium hydroxide concentration, reaction time and temperature and decreased with increasing particle size and solid-liquid ratio. The leaching process fitted the shrinking core model with diffusion through the product layer model as the rate-determining step. The activation energy of the dissolution of celestite was calculated as 62.24?kJ/mol. A semi-empirical kinetic model was obtained for dissolution of celestite in sodium hydroxide solution.     

Dissolution kinetics of copper(II) oxide in water saturated by sulphur dioxide

The dissolution and the kinetics of dissolution of cooper(II) oxide in water saturated by sulphur dioxide has been studied. In the experiments, the particle size, the flow rate of the gas, the solid to liquid ratio, and the reaction temperature have been chosen as parameters, while the stirring rate was held constant. As a result of present experiments, it was observed that the decrease of the particle size, the solid to liquid ratio, and an increase of the reaction temperature increased the dissolution rate. It was also observed that the flow rate of sulphur dioxide in the range of its flow rate values did not affect the dissolution rate. The reaction kinetics of copper(II) oxide according to the heterogeneous reaction models was examined and it was found that the dissolution rate was controlled by chemical reaction. The calculated activation energy is 66.50 kJmol^?1. © 1994 John Wiley & Sons, Inc.     

Leaching of Celestite with Sodium Sulfide

Leaching of celestite mineral, SrSO₄, with sodium sulfide, Na₂S, was investigated from the point of strontium carbonate, SrCO₃, production. Experiments were carried out to explain the conversion mechanism of celestite to strontium disulfide, SrS₂, in Na₂S solution. Effects of stirring speed, particle size, and concentration of Na₂S on conversion were studied at constant temperature and solid‐to‐liquid ratio. The results showed that the rate of conversion mainly depends on Na₂S concentration. It was concluded that leaching of celestite in Na₂S solution for conversion to SrS₂ is possible but slow.     

Effect of organic and inorganic compounds on dissolution kinetics of chalcopyrite in hydrogen peroxide– Hydrochloric acid system

The addition of 2-Propanol as an organic substance and NaCl as an inorganic compound in hydrochloric acid with hydrogen peroxide as a strong leaching agent of chalcopyrite was investigated. The effects of the leaching parameters on copper extraction, such as stirring speed, H₂O₂ concentration, temperature, HCl concentration and solid/liquid ratio were studied. The maximum final copper extraction of 54.55% was obtained with 600 rpm stirring speed, 1.5 M H₂O₂, 0.5 M HCl, 600 rpm, 50 °C, 240 min of the reaction and particle size of ?106 +75 µm. Further experiments were performed when the solid-to-liquid ratio (S/L), stirring speed, temperature, HCl, H₂O₂ and leaching time were kept constant to examine the influence of NaCl and 2-Propanol concentrations in the range of 0–0.5 M and 0–3 M, respectively. The results showed that the copper extraction was increased up to 58.11% with addition of NaCl. While copper extraction yield reached 94.25% in case of addition of 2-propanol with the optimum parameters(0.5 M HCl,50 °C, 1.5 M H₂O₂, 600 rpm, particle size ?106 +75 μm, solid liquid ratio 2g/L, 3 M 2-propanol). The chalcopyrite leaching in hydrogen peroxide– hydrochloric acid system was found to be described by the interface transfer and diffusion across the product layer with activation energy of 77.14 kJ/mol. Addition of 2-propanol suggested that the reaction was under product layer diffusion control and decreased the activation energy of chalcopyrite leaching to 67.98 kJ/mol.     

Beneficiation of zinc from electric arc furnace dust using hydrometallurgical approach

Zinc bearing wastes such as electric arc furnace dust (EAFD) obtained from steel making constitute an important resource for zinc extraction. Inclusion of heavy metals such as Pb, Cd, Cu, Cr, Ni, etc., in these wastes makes them hazardous to use and/or dispose. In the present research work, leaching kinetics of EAFD with sulfuric acid has been investigated and various experimental parameters such as concentration of lixiviant, stirring rate, sample particle size, liquid/solid proportion, and temperature of the reaction have been optimized. It has been found that the dissolution rate of EAFD increases with rise in temperature, acidic strength, rate of stirring, liquid to solid proportion and with reduction in EAFD particle size. From the analysis of leaching kinetic data by means of graphical and statistical methods, it has been evaluated that the leaching kinetics of EAFD is dictated by surface diffusion reaction. Apparent energy of activation for the leaching reaction of EAFD with sulfuric acid is found to be 13.1 kJ mol^–1 within the temperature range of 308 to 358 K.     

Triphase catalysis. II. Alkylation of phenylacetone with 1-bromobutane catalyzed by aqueous NaOH and polystyrene-supported benzyltriethyl ammonium chloride

Insoluble microporous polystyrene-bound benzyltriethyl ammonium chloride has been used as a catalyst in the alkylation of phenylacetone with 1-bromobutane, and the kinetics of this reaction was investigated under phase-transfer catalytic conditions. The observed reaction rates depend on many experimental parameters, viz., stirring speed, substrate amount, basicity of aqueous NaOH, amount of 1-bromobutane, temperature, order of addition of the reactants and particle size, percent active site, and percent crosslinking of the polymer. The rates are nearly 12 times higher at lower concentrations of base than at higher concentrations and do not vary appreciably with a variation in stirring speed from 200 to 700 rpm. The rate of alkylation increases with a decrease in the particle size of the catalyst and crosslinking of the polymer. Based on the results obtained, a suitable mechanism in which a combination of intraparticle diffusion and intrinsic reactivity limit the reaction rates has been proposed. © 1993 John Wiley & Sons, Inc.