Pillar free C-frame fuselage, barrier free for long line and towing products.
The horizontal type can seat in front and back, up and down the lifting table, and the use of molds is extensive.
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Araxa niobium mine located巴西阿拉沙(Araxa) City of Laså—米纳斯å‰(Minas Gerais) territory. A carbonate rock composite deposit. Ore mainly composed of goethite, limonite, magnetite, barite, monazite, titanium, iron, gorceixite, quartz and barium strontium pyrochlore water (i.e., barium pyrochlore containing Nb 2 O 5 63.42%, Mineral composition such as Ta 2 O 5 0.15%, BaO 16.51%). The ore contains Nb 2 O 5 2.5% to 3%, Re 2 O 3 4.44%, ThO 2 0.13%, TiO 2 3.6%, and ZrO 2 0.2%. The leeches of the chlorite are finer and generally do not exceed 1 mm. The reserves of the mine (Nb 2 O 5 ) account for more than 70% of the world's resources, and are the world's largest resource base. The current cut-off grade (Nb 2 O 5 ) is controlled at around 2%. What is being mined is an enriched ore body located in the central part of the structure, which is formed by deep weathering of carbonate bedrock and strong residual enrichment. Beneficiation plant feed grade (Nb 2 O 5) was 3%, using selected from - smelting joint interline, niobium oxide and niobium iron outputs. The whole process consists of three parts: mineral processing, leaching and smelting.
Dressing
The size of the ore dressing plant is 3,500 tons/day, and the annual output of the glauconite concentrate is 42,000 tons. The process of mineral processing equipment is shown in Figure 1. The ore is first passed through a 50 mm 2.1 x 4.2 m Faco (AC) vibrating screen, and the material on the screen (greater than 50 mm, the yield is less than 10% of the ore) is given to the Hazemag impact crusher . Broken to -50 mm, combined with vibrating screen material (less than 50 mm) into the ball mill , grinding to 95%-150 mesh (0.104 mm), ball mill and φ508 mm cyclone constitute closed circuit. The cyclone overflow is selected by a double cylinder weak magnetic separator. Non-magnetic products are sent to the de-sludge section. Because the slime has a great influence on the flotation of the chlorite, and most of the strontium is enriched in the 37-5 micron size, effectively removing the -5 micron fine mud is very important for the flotation operation. Therefore, the three-stage cyclone is used for de-sludge, and each de-sludge section has a de-sludge operation. The first stage of desilting uses a set of φ381 mm cyclones, the underflow of the cyclone is fed into the scrubber and scrubbed, and another set of φ102 mm cyclones is used for the second stage of de-sludge, the second stage of de-sludge and the first stage Scoured and de-sludged as well as mud. The φ381 mm de-drip cyclone underflow and the φ102 mm cyclone underflow are the ore feeding of the main flotation circuit rough selection tank. The φ102 mm cyclone overflows into the third-stage cyclone (φ25 mm) for de-sludge and de-sludge, but no need to scrub again. The φ25 mm cyclone underflow is the fine-grain flotation circuit rough selection tank. Give the mine.
Figure 1 Equipment flow of Araksa é’¡ Chlorite concentrator
Chlorophyll float is selected from amine cation collector , a wetting agent and sodium fluorosilicate for 15 minutes. Sodium fluorosilicate is used as actin activator. Hydrochloric acid is added to control pH 2.5-3.5. The main flotation circuit is thick. The tank is selected for rough selection and four times for selection. The coarse-grain flotation coarse selection tank is subjected to rough selection and one selection. Obtained flotation total concentrate Nb 2 O 5 55%～60%, P0.3%～0.8%, S0.02%～0.2%, Pb0.1%～0.2%, Fe 2 O 3 2%～8%, SiO 2 0.1% to 0.5%, ThO 2 2% to 3%, U 3 O 8 0.05% to 0.1%, BaO 15% to 18%, CaO0% to 0.2%, and the ore recovery rate is about 70%. Due to the high content of phosphorus, sulfur and lead , it needs to be sent to the factory for further processing.
Leaching
The leaching process uses high-temperature calcination of calcium chloride to volatilize lead chloride. Calcium replaces the ruthenium in the crystal lattice of the leeches, forming ruthenium chloride, and then washing with hydrochloric acid to dissolve phosphorus and sulfur. The leaching process is shown in Figure 2. The flotation concentrate is first filtered, and the filter cake is mixed with 25% calcium chloride and 5% lime, and calcined at a temperature of 800 to 900 ° C in a rotary kiln. After the calcined material was cooled, it was leached and filtered with 5% hydrochloric acid at a solid concentration of 50%. This step was carried out in two stages. The leaching residue is washed with water at a concentration of 50%. After filtration and drying, the obtained leached concentrate contains Nb 2 O 5 59%-65%, P0.05%-0.1%, S0.01%-0.05%, Pb0.01 %～0.05%, Fe 2 O 3 2%～8%, SiO 2 0.1%～0.5%, ThO 2 2%～3%, U 3 O 8 0.05%～0.1%, BaO1%～3%, CaO15%～ 20%.
Figure 2 Alasha mink yellow earth leaching process
The PbCl 2 and HCl discharged in the calcination are recovered through a cooling tower, a venturi, and a recovery tower. All the collected gas dust is sent to a 13.72m thickener, the concentrator is sanded into the filter, and the filter cake is returned to the starting point of the process; and the overflow containing the hydrochloric acid and lead chloride and all the waste water from the factory are passed through the milk. After processing, it is sent to the tailings pond.
Smelting
Smelting and smelting is divided into two parts: ferroniobium production and bismuth oxide production.
Niobium iron production: intermittent aluminum thermal reduction process. According to the pyrochlore leaching concentrate, the charge ratio accounted for 61.54%, iron oxide accounted for 13.68%, aluminum powder 20.51%, fluorite 2.56%, and stone 1.71%. Batch charge first mixed in a rotary mixer for 90 minutes and then a steel cylinder lined reactor was charged with magnesium sand, the reactor diameter of 3.7 meters, 1.8 meters high, is placed above the circular pits, with the pits Lime and fluorite are lined and prepared in advance in a silica sand bed. The bottom of the outer layer of the reactor is sealed with sand embankment. After the reaction material is installed, potassium chlorate and aluminum powder are placed on the top, and the mixture is ignited by fire. The reaction is automatically carried out for 15 minutes, the reaction temperature is up to 2400 ° C, and the reaction is cooled for 16 hours. The slag was removed, and the bottom ferroniobium was cooled for a few hours, taken out, placed in the air for 12 hours, and then crushed to less than 100 mm with a jaw crusher and stored in a 1000 kg steel vessel. The slag composition after reduction was: Al 2 O 3 48%, CaO 25%, TiO 2 4%, BaO 2 %, Re 2 O 3 4%, Nb 2 O 5 trace, ThO 2 2%, and U 3 O 8 0.05%.
Production of cerium oxide: In 1979, a factory for the production of cerium oxide was built. In 1981, the company researched a method (the method was not reported) to build a high-purity cerium oxide plant for optical and electronic applications. A pilot plant for the construction of ultrapure crystalline cerium oxide, while producing high-purity ferroniobium and nickel bismuth using industrial cerium oxide.