共查询到18条相似文献,搜索用时 156 毫秒
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氢-水同位素催化交换速率及过程模拟的研究进展 总被引:1,自引:0,他引:1
氢-水同位素催化交换在处理ITER聚变堆废水以及核裂变反应堆重水升级方面具有应用前景。该交换过程及核心设备催化交换塔的模型化研究,对工艺和工程优化设计具有十分重要的意义。本文重点介绍了氢-水同位素催化交换过程模拟的研究进展,讨论了同位素催化交换速率的计算方式以及吸收塔模型和滴流床模型在同位素催化交换过程模拟中的应用,探讨了氢-水同位素催化交换过程模拟今后的研究方向。通过各类模型的比较,滴流床模型被认为在催化交换过程模拟中有良好应用前景。氢-水同位素催化交换机理及速率计算方法和催化交换塔模型化等方面有待进一步研究。 相似文献
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固体表面吸附的氢同位素具有自发与气相氢同位素交换并达到某种程度平衡的性质,这种交换作用在金属氢化物表面同样存在.由于金属氢化物体系一般具有氢同位素效应,使得交换平衡时气-固相间的同位素丰度发生变化.利用这种性质可以进行金属氢化物柱内氢同位素间的置换,实现工程方面的应用. 相似文献
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氢同位素的交换与置换 总被引:1,自引:0,他引:1
固体表面吸附的氢同位素具有自发与气相氢同位素交换并达到某种程度平衡的性质,这种交换作用在金属氢化物表面同样存在。由于金属氢化物体系一般具有氢同位素效应,使得交换平衡时气-固相间的同位素丰度发生变化。利用这种性质可以进行金属氢化物柱内氢同位素间的置换,实现工程方面的应用。 相似文献
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为了处理高浓氚水,搭建了一台氢-水同位素交换串联水汽变换的两级钯膜反应器装置,可以实现级联处理工艺。以天然水代替氚水为源项,以D2代替H2开展了除氢实验,最高获得了207.4的除氢因子,验证了两级钯膜反应器用于处理氚水的可行性。通常情况下,水汽变换反应的除氢因子大于氢-水同位素交换反应。其中,氢-水同位素交换中D2/H2O体积流量比越大,该反应除氢因子越大;氢-水同位素交换中原料侧压力越大,该反应除氢因子越大;原料水流量越大,两个反应的除氢因子均会下降。由于一级膜反应器采用氢-水同位素交换可将氚水浓度降低1个量级以上,因而可以尽量避免二级膜反应器中CO与高浓氚接触,抑制含氚有机物的生成。由此可见,两级钯膜反应器有望成为一种高效的氚水处理装置。 相似文献
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计算模拟应用于氢同位素分离领域,能够方便、快捷地进行工艺条件分析。本工作采用数值模拟的方法对比研究了水-氢催化交换过程中HD/H_2O、DT/D2O和HT/H_2O三种氢同位素体系的分离性能。研究表明:在一定工艺条件下,三种体系均在操作温度为343K时达到最大的分离效果;随着气液比从1.0增大到3.0,最优操作温度均从343K降低到323K,但是在此过程中,HT/H_2O体系的分离效果受温度的影响较小一些;在达到最大分离效果的目标下,HT/H_2O体系需要的理论塔板数比HD/H_2O和DT/D2O体系少,同时,在优化的工艺条件下,三体系气相中氢同位素浓度在交换柱内分布曲线存在一定的差异。 相似文献
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氢—水液相催化交换法脱氚 总被引:3,自引:0,他引:3
对疏水催化剂的设计与制备方法及氢-水液相交换反应过程进行了讨论,并概要评述了以常温氢-水催化交换法进行重水脱氚的液相催化交换(LPCE)及其联合电解的催化交换(CECE)工艺流程。 相似文献
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《Fusion Engineering and Design》2014,89(9-10):2103-2107
Nuclear waste management has to be taken into account for fusion machine using tritium as fuel. Soft housekeeping waste (e.g. gloves, tissues, protective clothes, etc.) is produced during the whole life as well as during the dismantling of the reactor and is contaminated by tritium under reduced (HT) and oxidized (HTO) forms.In collaboration with ENEA, a lab-scaled facility has been built at CEA Cadarache for soft housekeeping waste detritiation and tritium valorization. The previously milled waste is placed in a reactor to be heated up to a temperature lower than the housekeeping melting point. A carrier gas is then injected in the detritiation reactor to remove tritium, thanks to the combined effects of temperature and carrier gas (type and feed flow). The tritiated gas exhausted from the detritiation reactor is then sent through a catalytic Pd–Ag membrane reactor (CMR) where tritium is recovered via isotopic exchange reaction and permeation phenomenon.Based on previous studies that have allowed defining the most efficient operating conditions for the detritiation process, this work presents the results obtained by the coupling of the detritiation facility with the CMR. Due to safety considerations, restrictions on the nature of the carrier gas were applied, rejecting air as the carrier gas even though air was the best candidate for the detritiation part of the process. The performance of the whole system was estimated by means of a parametric study on the influence of flow rates in the CMR and transmembrane pressure. 相似文献
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In nuclear installations, tritiated water is generally produced in the process of detritiation of air circulating in the glove boxes. The goal of this work concerns enrichment of this tritiated water at low concentration by electrolysis. The choice of this electrolyzer was dictated by the passivity of selected materials to the radiolysis in low-level tritiated water and the selectivity of the method avoiding further elimination of tritiated water and moisture before release in environment. According to the results, it is feasible to treat non-negligible volume of low-level tritiated water using a cathodic palladium membrane coated on an ionic solid polymer membrane. Presence of a palladium black deposit on the palladium membrane improves effectiveness. Enrichment in tritiated water depends on the isotopic separation factor, thereby the current and the permeability values. 相似文献
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采用Pt-SDB疏水催化剂和亲水填料混装进行含氘、氚氢气与水的液相催化交换实验,研究反应温度、气体流量和液体流量对D、T转化率以及H-D、H-T的总传质系数Kya的影响。研究结果表明:在相同操作条件下,T的转化率η(H-T)比D的转化率η(H-T)高,H-T的总传质系数比H-D的高;从D、T转化率随气体流量和液体流量的变化趋势可知,气体流量对D、T转化率的影响较大;选择合适的反应温度即可获得较佳的转化率和总传质系数。在实际工艺中,反应温度选为45℃较适宜。 相似文献