内蒙某CO2 + O2原地浸出采铀现场试验方案设计.doc

1、 内蒙某CO2 + O2原地浸出采铀现场试验方案设计摘要:内蒙某铀矿是中国的大型铀地浸矿山之一，采用CO2 + O2原地浸出方法开采铀矿。为了获得铀矿地浸工业试验的前期试验参数, 对其进行实验室扩大试验。根据实验室扩大试验的要求，采用“井场设计井型与井距确定过滤吸附淋洗合格液酸化沉淀压滤111产品”的工艺流程。设计“6抽14注”的6组钻孔单元，抽液钻孔开孔直径311 mm，注液钻孔开孔直径215 mm。浸出液中含有一些泥砂和小颗粒不溶物，吸附前需要用袋式过滤机过滤。浸出液中铀浓度为30 mg/L，饱和树脂工作容量为40 kg U/m3 R。采用三塔串联带压吸附，吸附方式为新型固定床上进液，浸出

2、液pH为6.87.5，溶液处理量为50 m3/h，吸附空塔线速度为30 m/h，吸附尾液铀浓度为0.5 mg/L，树脂孔隙度40%。饱和树脂不需要反冲，直接进入淋洗工序，淋洗采用三塔串联上进液方式，淋洗剂为100 g/L NaCl和16 g/L NH4HCO3的混合液，淋洗剂用量为两个树脂床体积，淋洗剂pH值8.59.0，淋洗空塔线流速1 m/h，停留时间120 min。合格液中平均铀浓度19.8 g/L，合格液用盐酸酸化至终点pH值4.55.0，工业盐酸消耗量为2 t/t U。沉淀采用循环老化常温沉淀工艺，沉淀剂为片碱，片碱消耗量为0.38 t/t U，沉淀时间1 h,沉淀老化时间24 h。

3、沉淀母液铀浓度为20.0 mg/L。沉淀过滤压力为0.30.5 MPa。滤饼含水30%，产品铀含量60%，金属铀总水冶回收率96%。关键词：井场设计；地浸采铀；设备选型；药剂选择；ivField Test of Uranium mine in the Inner Mongolia Autonomous Region by in-situ leaching with CO2 and O2Abstract：Uranium mine in the Inner Mongolia Autonomous Region is one of the biggest in-situ leaching urani

4、um producers in China, using a in-situ leaching process in which CO2 and O2 are used to leach the uranium。To obtain the preliminary parameters of in-situ leaching uranium industrial test，The enlarged experiments was done。According to the enlarged experiments，well field designdetermination of well ty

5、pe and well spacingadsorptionresin elutionThe uranium concentration of eluate is acidified with hydrochloric acidprecipitationpressure filtration111 product is selected。The process is as follows：six groups of well unit which include six pumping wells and the fourteen injection wells is designed。pump

6、ing well diameter is 311 mm，and injection well diameter is 215 mm。Leaching solution contains some sediment and small particles of insoluble，so filtered with bag type filters before adsorption。The uranium concentration in the leaching solution is 30 mg/L。The saturated resin work capacity is 40 kg U/m

7、3 R。Leaching solution is adsorbed with three adsorption columns in series ，and they can bear pressure。Leaching solution is adsorbed with innovative adsorption columns ，and flows from the upper part of innovative adsorption columns。The leaching solution pH values range from 6.8 to 7.5。The flow of lea

8、ching solution is 50 m3/h。The linear velocity of leaching solution flowing into the adsorption columns is 30 m/h。The uranium concentration in the adsorption tail liquid is 0.5 mg/L。The resin porosity is 40%。The unsaturated resin does not require backwashing with water，and iseluted directly。The unsat

9、urated resin is eluted with innovative elution columns ，and eluants flow from the upper part of innovative elution columns。100 g/L NaCl and 16 g/L NH4HCO3 are used as eluants. Eluants dosage is 2 times BV（bed volume）。Eluants pH values range from 8.5 to 9.0。The linear velocity of eluants flowing into

10、 the elution columns is 1 m/h。Eluants stay for 2 hours in the elution columns。The meanuranium concentration of eluate is 19.8 g/L。The uranium concentration of eluate is acidified with hydrochloric acid until pH values of 4.5 to 5。One ton of uranium consume two ton of industrial hydrochloric acid。cyc

11、ling aging method is used for precipiting the uranium concentration of eluate 。Solid sodium hydrate is used as precipitant。One ton of uranium consume 0.38 tons of solid sodium hydrate。Precipitation time is 1h， and cycling aging time is 24h。The uranium concentration in the mother solution is 20.0 mg/

12、L。Precipitation is sent by slurry pump to an automatic box type plate and frame filter press ， and the pressure it can bear is from 0.3 MPa to 0.5 MPa。The water content of filter cake could be reduced to 30%。Uranium mass fraction in the product is more than 60%。The recoveries of uranium is more than

13、 93%。Keywords: well field design；in-situ leaching of uranium；equipment selection； reagent selection；目录1. 试验概况11.1 试验简介11.2 试验设计原则11.2.1 确定水冶厂规模原则11.2.2 确定产品方案原则21.2.3 确定工作制度原则21.3 生产规模与产品方案21.3.1 生产规模21.3.2 产品方案21.4 工作制度21.4.1 年有效工作日21.4.2 日工作班次与工作时长22. 工艺原理32.1 CO2 + O2中性浸出采铀工艺32.1.1 CO2 + O2中性浸出基本

14、原理32.1.2 CO2 + O2中性浸出采铀的应用范围32.1.3 CO2 + O2中性浸出采铀的优缺点42.2 井场设计与成井工艺原理52.2.1 井场设计工艺52.2.2 成井设计工艺52.3 新型固定床清液吸附工艺原理62.4 离子交换工艺原理62.4.1 离子交换反应62.4.2 离子交换树脂分类72.4.3 离子交换影响因素73. 井场工艺设计83.1 试验钻孔概况83.2 钻井工作93.2.1 钻机安放93.2.2 钻井施工103.3 钻井部件安装123.3.1 井管各部件的加工方法123.3.2 过滤器安装位置的设计原则143.3.3 井管安装143.4 成井工艺153.4.1

15、 测井153.4.2 冲孔153.4.3 投砾163.4.4 注浆173.5 洗井183.5.1 活塞加注清水联运洗孔183.5.2 空压机洗孔183.5.3 潜水泵洗孔193.6 钻孔验收193.6.1 钻孔验收应提交的资料193.6.2 钻孔的抽注水量验收203.6.3 其它要求203.7 环境保护203.7.1 钻孔施工的环保措施203.7.2 施工现场清理214. 浸出液后处理工艺214.1 浸出液过滤工艺224.2 吸附淋洗工艺224.3 合格液酸化工艺234.4 沉淀老化工艺244.5 压滤工艺244.6 滤液与沉淀母液循环利用工艺255. 试剂选择255.1 离子交换树脂的选择255.2 淋洗剂的选择265.3 沉淀剂的选择266. 工艺参数276.1过滤276.2 浸出液pH值调节276.3 吸附276.4 淋洗286.5 合格液酸化286.6 沉淀286.7过滤296.8 母液酸化作为淋洗剂297. 工艺设备计算与选型307.1 离子交换塔的计算与选型307.1.1 离子交换塔的计算307.1.2 离子交换塔的选型317.2 袋式过滤机计算与