Association Mechanism Between Propionic Acid and Trioctylamine

IntroductionIn recent years,solvent extraction has receivedmore and more attention for recovery of carboxylicacids from dilute aqueous solutions,especiallywith the hydrophobic tertiary amines dissolved invarious organic diluents[18] . Studies on theextrac…     

冕宁稀土矿浸出液萃取转型工艺研究

对四川冕宁稀土矿硫酸焙烧后的浸出液萃取转型工艺进行了研究，确定了萃取转型有机相为ＨＡＣ－煤油体系，转型条件为：水相酸度为ｐＨ＝４．０；稀土离子水相初始浓度为０．１Ｍ；萃取时间大于５ｍｉｎ，用３ＭＨＣｌ溶液作反萃液，制得了稀土氯化物和氧化物产品。     

溶剂萃取法分离Sn,Zn

研究了以TBP从盐酸溶液中萃取分离锡与锌,发现如用煤油作稀释剂,则萃取过程会出现第三相。选用MIBK或癸醇作调相剂来消除第三相。作者解释了当用MIBK作调相剂,盐酸浓度大于7mol/L时,又会出现第三相的原因。萃取的最佳条件为:25%TBP-10%MIBK(或癸醇)-65%煤油;室温;6mol/L HCl;负载有机相中的杂质离子Zn~(2+)用6mol/L HCl洗涤,一次洗涤率达95%左右;负载有机相中的锡用0.24mol/L HCl反萃。实验比较了TBP萃取Sn~(4+)与Sn~(2+)的性能,解释了Sn~(4+)比Sn~(2+)略易萃取的原因。由于Sn~(4+),Zn~(2+)的竞争萃取,D_(Zn~(2+))随初始水相中[Sn~(4+)]的增加而减小,但当[Sn~(2+)]小于18g/L时,D_(Zn~(2+))几乎不变。     

络合萃取法处理环氧树脂生产废水

以三辛胺为萃取剂、白煤油为稀释剂络合萃取处理环氧树脂废水。结果表明,在pH=1.0、油水体积比0.35、萃取剂与稀释剂体积比为2时,废水经三级错流萃取COD和C l-的去除率分别达到97.6%和92.0%;萃取相用5%的N aOH、油碱体积比为2反萃10 m in后,可多次反复使用;红外光谱结果证明用三辛胺萃取环氧氯丙烷的反应机理主要为离子缔合反应。     

胺类萃取剂液-液体系界面性质研究——水相酸度、盐浓度和温度对TOA界面吸附性能的影响

研究了平衡水相酸度、水相盐浓度和温度对三辛胺ＴＯＡ－正庚烷／Ｈ２Ｏ液－液体系界面性质的影响,计算了界面吸附特性参数ｃｍｉｎ和ＡＩ,发现ＴＯＡ界面活性随水相ｐＨ及温度升高而降低,随水相盐浓度增加而增加,对有关结果及其与萃取性能的关系做了分析和讨论     

Extraction of Aminobenzoic Acid with TOA and TBP

IntroductionThe separation technique of solvent extractionbased on reversible chemicalcomplexation can havehigh capacity and high selectivity for separatingpolar organic solutes from dilute solutions[1,2 ] .Many researchers have investigated the extractio…     

紫外分光光度法测定200～260℃加氢精制无味煤油中芳烃含量

用一待测200～260℃加氢精制无味煤油试样,利用硅胶吸附、甲醇顶替脱附的办法制取其中的混合芳烃.以异辛烷作为稀释溶剂,求出该混合芳烃在272 nm处的平均吸光系数,然后利用此吸光系数测定与其属同一批原料所生产的其它无味煤油中芳烃含量.在波长272 nm处,本方法的检测下线可达0.57 ug/g,灵敏度指数0.45μg.cm-2,回收率为94%～101%.     

Solvent extraction and recovery of Y(III) and Yb(III) from fluorspar mineral

Yttrium and ytterbium were extracted from sulfuric acid medium using triphenylarsine (TPAs) dissolved in kerosene. The influence of different factors, such as shaking time, extractants, metal ions, sulfate ion concentrations, as well as temperature, was studied in detail. From the slope analysis method and IR measurements, the structure of the extracted species was suggested as MSO₄(HSO₄)·TPAs, where M refers to Y(III) or Yb(III). The equilibrium constants (K_ex) and thermodynamic parameters, such as the change in enthalpy (ΔH), free energy (ΔG), and entropy (ΔS), were calculated. The method of extraction and stripping was applied to obtain the aforementioned metals from a sample of fluorspar mineral giving a recovery yield of 88.2% and 83.5% for yttrium and ytterbium, respectively.     

用萃取第三相形成法处理1－萘胺－8－磺酸生产废水

用萃取第三相形成法，以Ｎ_（２３５）为萃取剂，煤油为稀释剂处理化学需氧量（ＣＯＤ）初始值高达５０ｇ／Ｌ以上的１－萘胺－８－磺酸生产废水。在萃取剂的浓度　为０．２０，相比１：１，萃取时间１０ｍｉｎ和室温条件下，二级错流萃取的ＣＯＤ去除率可达到９７％。     

Comparative analysis of the dissolution kinetics of galena in binary solutions of HCl/FeCl<Subscript>3</Subscript> and HCl/H<Subscript>2</Subscript>O<Subscript>2</Subscript>

A comparative study of the dissolution kinetics of galena ore in binary solutions of FeCl₃/HCl and H₂O₂/HCl has been undertaken. The dissolution kinetics of the galena was found to depend on leachant concentration, reaction temperature, stirring speed, solid-to-liquid ratio, and particle diameter. The dissolution rate of galena ore increases with the increase of leachant concentration, reaction temperature, and stirring speed, while it decreases with the increase of solid-to-liquid ratio and particle diameter. The activation energy (E _a) of 26.5 kJ/mol was obtained for galena ore dissolution in 0.3 M FeCl₃/8.06 M HCl, and it suggests the surface diffusion model for the leaching reaction, while the E _a value of 40.6 kJ/mol was obtained for its dissolution in 8.06 M H₂O₂/8.06 M HCl, which suggests the surface chemical reaction model for the leaching reaction. Furthermore, the linear relationship between rate constants and the reciprocal of particle radius supports the fact that dissolution is controlled by the surface reaction in the two cases. Finally, the rate of reaction based on the reaction-controlled process has been described by a semiempirical mathematical model. The Arrhenius and reaction constants of 11.023 s⁻¹, 1.25×10⁴ and 3.65×10² s⁻¹, 8.02×10⁶ were calculated for the 0.3 M FeCl₃/8.06 M HCl and 8.06 M H₂O₂/8.06 M HCl binary solutions, respectively.     

离子液体作为绿色介质从盐湖卤水中萃取硼酸

制备了1-辛烷基-3-甲基咪唑六氟磷酸盐离子液体,再以离子液体(IL)为萃取介质、异辛醇为萃取剂及煤油为稀释剂建立盐湖卤水硼萃取研究模型,考察了离子液体用量和萃取条件对硼萃取的影响。异辛醇从卤水中萃取提硼的最佳实验条件:离子液体体积分数为10%,萃取剂体积分数为50%,相比(O/A)为1∶1,萃取时间10 min,pH 2.4,Mg2+浓度为4.268 mol/L。在此条件下,当萃取级数为3级时,萃取率为99.54%,卤水中的硼可被完全萃取到有机相中。     

低浓度含铬废水萃取分离的研究

采用磷酸三丁脂（TBP）为萃取剂,煤油为稀释剂,研究了萃取时间、TBP初始浓度、废水中H⁺浓度以及盐析剂（NaCl）对萃取过程的影响。结果表明,TBP对Cr(VI)萃取速率较快,15min后基本达萃取平衡;TBP初始浓度及废水中H⁺浓度在较低范围内对萃取效果影响较大;加入盐析剂可促进反应平衡,提高萃取效果。     

褐藻海带生物质残渣对水中Pd（Ⅱ）的吸附研究

用乙醇处理褐藻海带得到其生物质残渣（Residue of Laminaria japonica,简称ROLJ）,探讨了ROLJ对水溶液中Pd(Ⅱ)的吸附性能.实验考察了溶液pH、接触时间、温度和初始Pd(Ⅱ)浓度等因素对吸附效果的影响,并探讨了ROLJ对Pd(Ⅱ)的吸附动力学及等温吸附特性.结果表明:在pH为3～4范围内,吸附效果最好;吸附平衡时间为80min;吸附动力学符合伪二级动力学模型;Langmuir等温吸附方程能较好地描述Pd(Ⅱ)在ROLJ上的吸附特性,303 K 时ROLJ对Pd(Ⅱ)静态饱和吸附容量为294.12mg/g.热力学分析结果表明,实验条件下ROLJ对Pd(Ⅱ)的吸附反应是自发、吸热和熵值增加的过程.用0.1M HCl+5%硫脲溶液可洗脱回收Pd(Ⅱ),ROLJ是一种有应用前景的钯吸附回收材料.     

全萃法从锗烟尘浸出液中分离锗的研究

选用某胺类萃取剂 ,络合剂 ,改质剂 ,煤油稀释剂 ,NaOH反萃剂 ,系统研究了从某锗烟法浸出液分离提取锗的工艺流程和最佳工作条件。     

酯与离子液体[bmim]BF_4二元双水相体系金属镉(Ⅱ)的萃取分离及测定

Cd(Ⅱ)与碘化钾形成离子化合物CdI_42-,与罗丹明B结合形成离子缔合物(RhB)2(CdI_4),此缔合物在一定条件下,可采用酯与离子液体[bmim]BF4二元双水相体系从目标混合物中实现高效萃取分离,方法用于测定天然水中重金属Cd(Ⅱ)的含量,检测限3.16×10-7mol/L.研究了试剂用量对三元缔合物形成的影响以及温度和酸度对离子液体-双水相萃取体系的影响,得到了Cd(Ⅱ)、KI、RhB三元缔合物(RhB)2(CdI_4)的最佳生成条件以及二元双水相体系的最佳萃取条件.     

十二烷基磷酸钠盐的制备及其在水溶液中CMC的测定

本文报道了十二烷基磷酸二钠和一钠盐的合成,并用一种毋需测定溶液表面张力绝对值的毛细管升高法测定了每种表面活性剂水溶液的临界胶束浓度(C.M.C),此外,还对十二烷基磷酸二钠与盐酸的混合水溶液的C.M.C值也作了测定。     

P204在不同稀释剂中萃取钙（II）的微量量热法研究

用滴定微量热计测定了P204在氯仿和煤油稀释剂中从硫酸盐水溶液中萃取钙（II）的过程的反应热,结果文献的工作,计算出了不同温度下的萃取平衡常数及有关的热力学函数。     

以三正辛胺为载体的微乳液分离钼(Ⅵ)的研究

研究了以三正辛胺(TOA)为载体,由OP-10、异戊醇、环己烷和NaOH水溶液组成的微乳液分离钼(Ⅵ)的行为及机理.当膜相中三正辛胺浓度为0.03 mol/L,内相NaOH的浓度为0.03 mol/L,外相HCl的浓度为0.01 mol/L,可使钼(Ⅵ)的萃取率达98%以上.在该条件下,可使钼(Ⅵ)与Fe(Ⅲ)、Co(Ⅱ)、Ni(Ⅱ)、Zn(Ⅱ)、Mn(Ⅱ)、Cd(Ⅱ)、Cu(Ⅱ)、Pb(Ⅱ)完全分离.     

A thermodynamic model of calculating mass action concentrations for structural units or ion couples in NaClO4-H2O and NaF-H2O binary solutions and NaClO4-NaF-H2O ternary solution

A thermodynamic model of calculating mass action concentrations for structural units or ion couples in NaClO₄-H₂O and NaF-H₂O binary solutions and NaClO₄-NaF-H₂O ternary strong electrolyte aqueous solutions was developed based on the ion and molecule coexistence theory (IMCT). A transformation coefficient was needed to compare the calculated mass action concentration and the reported activity, because they were usually obtained at different standard states and concentration units. The results show that transformation coefficients between the calculated mass action concentrations and the reported activities of the same components change in a very narrow range. The transformed mass action concentrations of structural units or ion couples in NaClO₄-H₂O and NaF-H₂O binary solutions agree well with the reported activities. The transformed mass action concentrations of structural units or ion couples in NaClO₄-NaF-H₂O ternary solution are also in good agreement with the reported activities in a total ionic strength range from 0.1 to 0.9 mol/kg H₂O by the 0.1 mol/kg step with different ionic strength fractions of 0, 0.2, 0.4, 0.5, 0.6, 0.8, and 1, respectively. The results indicate that the developed thermodynamic model can reveal the structural characteristics of binary and ternary strong electrolyte aqueous solutions, and the calculated mass action concentrations of structural units or ion couples also strictly follow the mass action law.     

Process development for the direct solvent extraction of nickel and cobalt from nitrate solution: aluminum,cobalt, and nickel separation using Cyanex 272

A direct solvent extraction (DSX) process for purifying nickel and cobalt from the nitric acid leach solution of nickel laterite ores was conceived and experimentally probed. The proposed process consists of two solvent extraction (SX) steps but with only one extractant-bis(2,4,4-trimethylpentyl)phosphinic acid (Cyanex® 272)-used in both steps. The first extraction step involved the removal of aluminum and zinc, whereas the second extraction step involved the separation of cobalt along with manganese from nickel. The experimental results showed essentially quantitative removal of aluminum (>97%) and zinc (>99%) in a single extraction stage using 20vol% Cyanex 272 at pH 2.1. Some cobalt (32%) and manganese (55%) were co-extracted but were easily scrubbed out completely from the loaded organic phase using dilute sulfuric acid at pH ≤ 1.38. Cobalt and manganese in the first extraction raffinate were extracted completely in four extraction stages at staggered pH values of 4.0, 4.4, 4.5, and 4.0 in the first, second, third, and fourth stages, respectively, using also 20vol% Cyanex 272. A small amount of nickel (up to 6.6%) was co-extracted but was easily scrubbed out completely with dilute sulfuric acid at pH 2.0. A flow diagram showing the input and output conditions and the metals separated under the deduced optimum conditions is presented.