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为处理埃尔诺帕尔钠矿体,研制了生产工业品位铀浓缩物的综合加工方法。该矿体矿石储量为115 000吨,平均品位为0.283%,相当于325吨 U_3O_8。该法包括:破碎(-12英寸到-1.5英寸)、浸出液返回循环堆浸、逆流洗涤(就在堆中进行)、溶剂萃取、反萃取、氢氧化铵沉淀铀、过滤、煅烧。详细分析影响堆浸的主要因素:矿石堆的几何形状,破矿粒度和粒度分布,基础的设计和结构,堆矿方法,加酸方法,液体通过堆的流量和洗涤方法。该法浸出率在80—85%之间,洗涤效率从96%到近乎100%,总回收率77—85%。酸耗一般低于25公斤/吨矿。浸出和洗涤采用总固液比约3:1,所以可得到 U_3O_8含量约7克/升的浓溶液。将此溶液过滤,滤液直接送阿拉明336-异癸醇-煤油的溶剂萃取系统。由于萃取原液的铀浓度高,可以用高胺浓度的有机溶剂。有机溶剂含有120克/升阿拉明和98克/升异癸醇。用含100克/升 NH_4Cl 和250克/升(NH_4)_2SO_4溶液反萃取,可得到含70—75克/升 U_3O_8的溶液。随后经通常的沉淀、过滤、煅烧等工序,可得到符合工业规格的产品。另一种方法为硝酸盐反萃取,得到浓度约70克/升 U_3O_8的溶液可直接送 TBP 精制工序而越过生产铀浓缩物阶段。
In order to process the El Nopal sodium ore body, a comprehensive processing method for producing industrial grade uranium concentrate has been developed. The ore reserves of 115,000 tons of ore, the average grade of 0.283%, equivalent to 325 tons U_3O_8. The method includes: crushing (-12 inches to -1.5 inches), leaching solution return to heap leaching, countercurrent washing (on the heap), solvent extraction, back extraction, ammonium hydroxide precipitation of uranium, filtration and calcination. The main factors influencing heap leaching are analyzed in detail: the geometry of the ore heap, the particle size and particle size distribution of the oreblast, the basic design and structure, the heap-mining method, the acid-adding method, the flow rate of the liquid through the heap, and the washing method. The law leaching rate of 80-85%, washing efficiency from 96% to almost 100%, the total recovery of 77-85%. Acid consumption is generally below 25 kg / tonne ore. Leaching and washing using a total solid to liquid ratio of about 3: 1, so can get U_3O_8 content of about 7 g / liter of concentrated solution. The solution was filtered and the filtrate was directly sent to a solvent extraction system of Alramine 336-isodecanol-kerosene. Due to the high concentration of uranium in the extract, it is possible to use organic solvents with high amine concentrations. The organic solvent contains 120 grams per liter of Alamin and 98 grams per liter of isodecanol. Stripping back with a solution containing 100 g / L NH 4 Cl and 250 g / L (NH 4) 2 SO 4 gave a solution containing 70-75 g / L U 3 O 8. Followed by the usual precipitation, filtration, calcination and other processes, can be obtained in line with industrial specifications of the product. Another method for the nitrate back-extraction, to give a concentration of about 70 g / L U_3O_8 solution can be sent directly to the TBP refining process over the stage of production of uranium concentrate.