6,6′-二(5,6-二乙基-1,2,4-三嗪-3-基)-2,2′-联吡啶萃取分离镅与镧系元素

在硝酸介质中,研究了6,6′-二(5,6-二乙基-1,2,4-三嗪-3-基)-2,2′-联吡啶(6,6′-bis(5,6-diethyl-1,2,4-triazin-3-yl)-2,2′-bipyridine,C2-BTBP)/CHCl3体系对镅和镧系元素的萃取行为。重点考察了萃取时间、萃取剂浓度、水相硝酸浓度等因素对C2-BTBP萃取Am的影响。结果表明:C2-BTBP萃取镅时,10min达到平衡;D(Am)随酸度增大先增大后减小。在考察的酸度范围内,镧系元素的分配比均较小。提出了C2-BTBP/CHCl3体系分离三价锕系与镧系元素的概念流程,并经串级实验验证。萃取剂(C2-BTBP/CHCl3)浓度为0.04mol/L,料液酸度为1.0mol/L HNO3,洗涤液酸度为1.0mol/L HNO3,流比为AF∶AX∶AS=1∶1∶0.5,经6级萃取、4级洗涤后,镅的萃取率为99.93%,Am中Ln的去污因子大于103,Am中镧系元素的含量小于0.03%,可较好的实现镅和镧系元素的分离。     

硝酸体系中DGA树脂分离镅与锔

三价镅(Am)与锔(Cm)的相互分离对于α能谱和质谱准确测量镅锔同位素具有重要意义,但它们的化学性质相近,相互分离非常困难。本工作研究了硝酸体系中DGA树脂对Am(Ⅲ)和Cm(Ⅲ)的静态吸附性能和柱分离行为,获得了不同酸度和温度条件下的容量因子(k′)及分离因子(SF)数据,以及不同柱高(L)、线速率(v)条件下的峰分辨率(R)、理论塔板高度(H)等参数。根据色谱理论指导柱分离条件的选择和优化,获得了较好的分离效果:Am与Cm回收率在90%以上时,相互间去污因子达1×10²以上。     

超钚元素分离流程的高灵敏度和定量流线监测方法

本文介绍用于超钚元素分离流程的高灵敏度监测装置和定量分析技术。采用NaI(T1)薄晶体双探头相加谱仪测定X射线和低能γ射线。采用Si(Au)面垒半导体流线监测器测定厚源α谱。描述了监测器的结构和电子仪器,厚源α谱特性的研究结果和定量刻度方法。给出了用于离子交换色层法提取~(248)Am和~(244)Cm流程的实验结果。NaI(T1)薄晶体双探头系统对~(243)Am总加入量的灵敏度好于0.1微居。Si(Au)面垒监测器对镅、锔浓度测定精度为±5％。各收集容器内镅、锔含量分析结果的精度为±10％。     

季铵盐萃取分离镅、锔

一、引言镅、锔分离是超钚元素化学中的难题之一。将Am氧化到五价然后分离的方法只能用于工艺粗分离,且操作繁杂。目前常用的α羟基异丁酸阳离子交换法,分离因子仅为1.5。甲醇-硝酸阴离子交换法,分离因子也只有2.4。近年一些文章报道了用胺类萃取法或萃取色层法分离Am、Cm,优点是胺类萃取剂耐辐照、分离因子也高。Horwitz等研究了用季铵盐从含盐析剂的硝酸中萃取三价     

超钚元素分离流程的高灵敏度和定量流线监测方法

本文介绍用于超钚元素分离流程的高灵敏度监测装置和定量分析技术。采用NaI(Tl)薄晶体双探头相加谱仪测定X射线和低能γ射线。采用Si(Au)面垒半导体流线监测器测定厚源α谱。描述了监测器的结构和电子仪器,厚源α谱特性的研究结果和定量刻度方法。给出了用于离子交换色层法提取~(248)Am和~(244)Cm流程的实验结果。NaI(Tl)薄晶体双探头系统对~(243)Am总加入量的灵敏度好于0.1μCi。Si(Au)面垒监测器对镅、锔浓度测定精度为±5％。各收集容器内镅、锔含量分析结果的精度为±10%。     

用P507-磺化煤油溶液从硝酸溶液中萃取分离镅(锔)与稀土元素

测定了镅(锔)和轻稀土元素(La、Ce、Pr、Nd、Sm)在P507-磺化煤油和硝酸溶液中的分配比,确定了它们被萃取能力的顺序为:La相似文献   

1-苯基-3-甲基-4-氰硫基-5-吡唑酮的合成及其对镅和铕的萃取研究

合成了1-苯基-3-甲基-4-氰硫基-5-吡唑酮(PMTCP),研究了该试剂单独萃取及其与2,2’-联吡啶协同萃取镅和铕的行为。实验结果表明,该试剂单独萃取镅和铕的能力都比较低,但优先萃取镅;含氮协萃剂2,2’-联吡啶的加入可以明显提高镅的萃取率,并将镅和铕的分离因数α(Am／Eu)由PMTCP单独萃取时的2.6提高到4．0。     

HDEHP萃淋树脂在~(242)Cm制备中的应用研究

本文在研究硝酸。硝酸盐和氨羧络合剂溶液中HDEHP萃淋树脂萃取Pu(Ⅳ),Am(Ⅲ).Eu(Ⅲ)和其它一些裂片元素性能的基础上,提出了一个从辐照~(241)AmO_2靶中提取~(242)Cm的流程。该流程较为简单并具有足够高的镅、锔回收率和去除钚和裂片元素的能力。     

链状聚醚用作萃取剂的研究——Ⅲ.Am(Ⅲ)与Cm(Ⅲ)的三甘酰双(二苯胺)萃取及萃取色层分离

本文研究了三甘酰双(二苯胺)的硝基苯溶液从苦味酸溶液中萃取Am(Ⅲ)和Cm(Ⅲ)的性能,并与Ce,Nd和Eu的萃取进行了比较。萃合物组成可表示为ML_2Pic_3;分配比随温度上升而下降;在所有情况下,Am的分配比均大于Cm,平均分离因数为3.0;水相中加入DTPA后,分离因数可达5.6。将此体系移植到萃取色层柱上,实现了Am(Ⅲ)与Cm(Ⅲ)的良好分离。     

An（Ⅲ）及Ln（Ⅲ）萃取分离工艺研究进展

<正>为实现真实高放废液的非α化,需要分离出高放废液中以Am、Cm为代表的An(Ⅲ)。根据前期研究,已通过串级实验判断了TODGA+TBP流程符合本课题的需求,并进一步优化了工艺参数;第二步要实现An(Ⅲ)与Ln(Ⅲ)的分离,在反萃取剂PTD的稳定性及单级分离性能研究结果的基础上,前期工作确定了台架实验工艺参数。结合An(Ⅲ)与Ln(Ⅲ)共萃取分离流程,并     

Neutron Cross Sections of Li-6

Calculation procedures have been developed to evaluate the performance of the multistage counter current extraction of transuranics (TRU) from spent molten salt into liquid metal, taking into account stage efficiency and also the scrub stage. The following results, which supplement previous papers, were derived using these procedures. When Cd is used as the liquid metal and the stage efficiency is assumed to be 100%, at least four stages are necessary to recover 99% of TRU from the salt with a decontamination factor (DF) higher than five. A stage efficiency of the extraction better than 80% is desirable for a practical application. The scrub stage is not very effective in improving the DF when the total number of extractions is less than five. The DF slightly increases with higher TRU concentration in the salt since the accompanying lanthanide FP extracted into the Cd in the later stages works as a mild reducing agent in the earlier stages. Although the extraction process has high separation capability, it is very difficult to separate Np, Am, or Cm from Pu due to their similar separation factors. Therefore, the extraction process has inherent proliferation resistance.     

阳离子交换-DTPA-乳酸淋洗色层法从Am,Cm中除Pm

一、前言用阳离子交换-α-HIBA淋洗色层分离Am,Cm时,Pm在Am.Cm之间被洗脱。前文研究了用DTPA-α-HIBA从Am.Cm中除Pm的可能性。本文的目的是研究在阳离子交换树脂-DTPA-乳酸体系中,各种因素对Am,Cm和Pm分离的影响,以寻找从Am,Cm中除Pm的条件。     

镅锔分离研究进展

乏燃料后处理产生的高放废液中Am和Cm是长期释热的主要来源,将它们分离出来并进一步进行分离和处置,对高放废物的长期安全处理处置具有重要意义。另外,超钚元素生产涉及Am和Cm材料的获取以及辐照后靶件中Am和Cm的化学分离。因此Am、Cm的分离一直是锕系元素化学与材料研究的重要领域之一。但是Am、Cm之间的分离相当困难,水溶液中Am、Cm基本均以正三价离子形式存在,化学性质非常相似。早期的离子交换法分离因子低,近年来主要研究将Am(Ⅲ)氧化到高价态实现分离,或通过Am、Cm与配体的亲和力差异、不同配体组合产生"推拉效应"以提高分离因子。本文综述了相关研究现状,概述了主要流程研发情况,并展望了该领域的研究趋势。     

水-醇介质中离子交换分离超钚元素——Ⅰ.CH_3OH-NH_4NO_3-HNO_3-DTPA-阴离子交换树脂体系

本文研究了Am和Cm在CH_3OH-NH_4NO_3-HNO_3-DTPA溶液和阴离子交换树脂之间的分配系数。结果表明,DTPA的存在对Am和Cm的分离有显著的改善,二者的分离系数可达3.5-3.7。 以适当的淋洗液进行柱分离实验,达到了Am,Cm,Cf三个元素的分离。     

DHDECMP-TBP/煤油从模拟高放废液中萃取回收Am-Gd的研究

研究了ＤＨＤＥＣＭＰ－ＴＢＰ／煤油萃取Ａｍ＾３＋、Ｇｄ＾３＋的各影响因素,在单级萃取实验的基础上,用０．６０ｍｏｌ／ＬＤＨＤＥＣＭＰ－１．４０ｍｏｌ／ＬＴＢＰ／煤油为有机相对模拟高放废液进行了逆流串级萃取实验降流串级反萃实验,成功地从模拟高放废液中分离回收了Ａｍ＾３＋和Ｇｄ＾３＋。     

Continuous extraction and separation of Am(III) and Cm(III) using a highly practical diamide amine extractant

A highly practical diamide-type extractant, which is an alkyl diamide amine with 2-ethylhexyl alkyl chains (ADAAM(EH)), was investigated for the mutual separation of Am(III) and Cm(III). ADAAM(EH) is a multidentate ligand with one soft N-donor atom and two hard O-donor atoms as part of its central frame. This tridentate arrangement of donor atoms provides selective binding to Am(III) compared to that with Cm(III) in highly acidic media (1.5 M HNO₃), resulting in separation factors of up to 5.5. A continuous liquid–liquid extraction and stripping test was conducted using a multistage countercurrent mixer-settler extractor with ADAAM(EH) in n-dodecane. In this test, the separation of Am(III) and Cm(III) was achieved with very high yield.     

Characterization of radiation fields and dose assessment from fuels manufacturing for advanced fuel cycles

The purpose of this study was to examine radiological hazards introduced to workers from the fabrication of fuels with minor actinides (MA) and reprocessed uranium (RepU) and determine the feasibility of using shielded gloveboxes instead of remotely controlled operations in hot cells. Of particular concern is the increase in photon source term from the daughter products in RepU and the mixed neutron and photon fields introduced by MA recycle. In the interest of keeping the glovebox worker's radiation dose as low as reasonable achievable (ALARA), dose rates were calculated for various typical and bounding fuel compositions for light water reactors (LWR) and fast reactor (FR) mixed oxide (MOX) fuels with and without MA. The impact of varying the separation efficiency of americium (Am) and curium (Cm) was examined because current separation processes in reprocessing and recycling do not allow for the complete separation of Am from Cm. The additional Cm will cause a significant increase in the neutron source term. The sensitivity of the fuels to aging time was also examined by decaying the recycled feedstocks from 6 months to 3 years to simulate the effect of delays in reuse of recycled materials. The highest photon and neutron sources were used to calculate the additional shielding requirements that would be needed for fuel fabrication. Through insight gained from this study, it can be concluded that a standard glovebox with one quarter inch stainless steel walls can be used to fabricate fuels with Am with little to no additional shielding. The introduction of small amounts of Cm in the fuels will require the fuel fabrication to be preformed remotely in hot cells. Thus, stressing the importance of developing methods to increase the separation efficiency of Am from Cm.     

甲醇-硝酸-阴离子交换树脂体系中用高压离子交换色层法分离镅和锔

在以硝酸作为络合剂的水-醇混合溶液中分离超钚元素,其效果优于纯水溶液。作者在前一工作中介绍了使用甲醇-硝酸-阴离子交换树脂从辐照靶中分离镅和锔的工艺流程,本文采用高压色层技术进行镅、锔分离,并且对此体系的动力学性能进行探讨。 在文献上未见到阴离子树脂分离元素时采用高压技术,直到实验结束后才看到使用类似     

HEHEHP fractional extraction process with three outlets for separation of Am from rare earths

Americium is similar to light rare earths in solvent extraction by HEHEHP.So the fractional extraction process with three outlets,which is widely used on rare earth industrial scale,can be applied to separate Am from La,Ce,Pr,Nd and Sm.The better process parameters can be calculated by the material and distribution balance equations stage by stage with given organic loading.In order to recover 0.99 mole fraction of Am and remove 0.90 mole fraction of light rare earths from the feed solution,in which the mole ratios of La Ce,Am,Pr,Nd,Sm are 0.140,0.199,0.005,0.109,0.487,0.060,the total number of stages needed is 43,that is the extraction sector 18,first scrubbing sector 2 and second scrubbing sector 23.The fractional extraction process with three outlets is simpler and more convenient than two fractional extraction processes with two outltes.