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1 Indústrias Nucleares do Brasil - INB XXXXXXXXXXXXXXX XXXXXXXXXXXXXXXXXXXXXXXXXX IMPLEMENTATION OF A NEW MILLING PROCESS xxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxxx AT CAETITÉ-BRAZIL xxxxxxxxxxx URANIUM SITE L.A. Gomiero a, H. Rangel Jr. a, C.A. Morais b a Indústrias Nucleares do Brasil S/A- INB, Caetité-BA, Brazil. b Centro de Desenvolvimento da Tecnologia Nuclear CDTN/CNEN, Belo Horizonte-MG, Brazil. NOME CARGO June 26, 2014
2 CAETITÉ - BRAZIL FACILITY Is a mining and milling facility to produce uranium ore concentrate: - Open pit mining (and underground in a near future). - Physical & Chemical ore processing plant
3 CAETITÉ MINE AND MILL FACILITIES LOCATION
4 CURRENT CAETITÉ MILL FACILITY Ore Treatment Capacity (t/y) 200,000 U Concentrate Production (t/y U 3 O 8 ) 400
5 SIMPLIFIED CURRENTE GENERAL PROCESS FLOWSHEET Open Pit Mining ROM Ore Mining Solid Waste Mining and Milling Solid Waste Tailings Crushing Circuit Mixer Drum Heap Leaching Leached Solid Waste Liquor Clarification Process Water Pond Solvent U Extraction U Stripping Solvent Regeneration Tailing Pond Aqueous Effluent Treatment ADU PRODUCTION Aqueous Effluent Solids or Pulp Aqueous Phase Organic Phase
6 MAIN TARGETS FOR THE MILL EXPANDED PRODUCTION DESIGN Increase the UOC production from 400 to 800 t/y as U 3 O 8 ; Increase the U recovery from 78% to at least 95%; Increase the sustainability by avoiding the use of pollutant chemicals; Production of a UOC with higher purity.
7 CHANGES IN THE CURRENT PROCESS To achieve the established targets the following changes have to be carried out in the current milling process: a) Replacement of the heap leaching process by conventional tank agitated leaching ; b) Replacement of the sodium chloride stripping solution by high concentrated sulfuric acid solution (~4 mol/l) and, c) Replacement of ammonia/ammonium hydroxide solution by hydrogen peroxide solution at the uranium precipitation step.
8 INCREASING PRODUCTION AT CAETITÉ SITE The current process and the INB s plans for changing the leaching process and increasing the production at INB/Caetité site were the subject of two presentations : URAM-2009, Vienna, 2009 URANIUM 2010, Saskatoon (Canada), 2010 In both time plans were mentioned to change the heap leach to conventional agitated leaching process taking advantage of the agitated leaching and filtration equipments existing at the old INB facility in Caldas/MG. After economical evaluation INB decided to buy new equipments for the enlargement of the Caetité mill facility.
9 TYPICAL ANALYSIS OF THE CAETITÉ ORE Species Content (wt%) Species Content (wt%) Species Content (wt%) Moisture < 0.01 V 2 O MnO 0.10 L.I. 500ºC 0.12 Al 2 O ZrO (*) L.I. 900ºC 0.52 Fe 2 O MgO 2.75 (*) U 3 O P 2 O Na 2 O 7.5 SiO CaO 5.38 K 2 O 0.92 TiO SO Y 2 O 3 < 0.01 (*) L.I. = Loss on Ignition
10 INVESTIGATION OF THE BEST LEACHING CONDITIONS Ore Particle Size: Temperature: Uranium recovery (%) Uranium recovery (%) Ore size (microns) Temperature ( o C)
11 INVESTIGATION OF THE BEST LEACHING CONDITIONS Acid / Ore ratio: Leaching Time: Will depend on the carbonate content in the ore Uranium recovery (%) H 2 O 2 NaClO 3 Uranium recovery (%) Acid/ore ratio (kg/t) Leaching Time (h)
12 INVESTIGATION OF THE BEST LEACHING CONDITIONS Main conditions for the new plant design: Ore particle size: ~ 400 microns Temperature: 70 to 80 ºC Acid / ore ratio: ~ 60 kg H 2 SO 4 98%/t of ore Oxidant / ore ratio: ~ 0,6 kg NaClO 3 / t of ore Leaching time: 4 hours Slurry density: 60 to 65 solids wt%. Expected U Recovery: > 95%
13 U STRIPPING WITH STRONG SULFURIC ACID SOLUTION H 2 SO 4 conc. = 4.2 mols/l Aqueous continuous phase in the mixers Number of stages: 6 U 3 O 8 conc. in the pregnant strip Solution (PSS): ~100 g/l Stripping (%) O/A = 1 O/A = 3 O/A = H2SO4 Concentration (mol/l) U3O8 in aqueous phase (g/l) U3O8 in solvent (g/l)
14 U STRIPPING WITH STRONG SULFURIC ACID SOLUTION NEUTRALIZATION OF THE EXCESS SULFURIC ACID IN THE PSS: Neutralization agent: limestone Final ph = ~ 2.5 Reaction time: 4 Hours SOLID / LIQUID SEPARATION OF THE NEUTRALIZED PULP: Centrifuge or Vacuum Belt Filter Gypsum washing Recycle of the washed gypsum to the ore leaching step
15 URANIUM PRECIPITATION URANIUM PRECIPITATION FROM THE FILTRATE: Precipitation Agent: H 2 O 2 Final ph = 3 to wt% Reagent for the ph control: MgO / Mg(OH) 2 SOLID / LIQUID SEPARATION: Centrifuge or Vacuum Belt Filter Precipitate washing Precipitate calcination
16 SIMPLIFIED SCHEDULE OF THE PROJECT Preparation of the basic and detailed designs: The choice of the engineering company was completed and the contract will be signed in July The estimated time for completion of work is 12 months.
17 THANKS
18
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