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Chu Yong Cheng - One of the best experts on this subject based on the ideXlab platform.

  • recovery of germanium from synthetic Leach Solution of zinc refinery residues by synergistic solvent extraction using lix 63 and ionquest 801
    Hydrometallurgy, 2015
    Co-Authors: Sankum Nusen, Zhaowu Zhu, Torranin Chairuangsri, Chu Yong Cheng
    Abstract:

    Abstract A synergistic solvent extraction (SSX) system consisting of LIX 63 and Ionquest 801 was identified and developed to recover germanium from a synthetic Leach Solution of zinc refinery cementation residues. A significant synergistic effect was identified with this novel SSX system, which selectively extracted germanium over other metals in the synthetic Leach Solution. The SSX system consisting of 0.13 M anti-oxime from LIX 63 and 0.13 M Ionquest 801 in ShellSol 2046 is an optimised composition for the extraction of germanium from the synthetic Leach Solution containing 1 g/L Ge(IV) and 1.0 M H 2 SO 4 . The germanium(IV) extraction kinetics was slow with the equilibrium reached after 20 min of mixing at 40 °C. The stripping kinetics of germanium(IV) with strip Solution containing 0.5 M NaOH and 1.0 M Na 2 SO 4 was very fast with the equilibrium reached in 1 min of mixing. Slope analysis showed that, most possibly, the extracted Ge(IV)-organic species is 2Ge(SO 4 ) 2 ·(HA)·(HB) 2 ·H 2 SO 4 via a solvating mechanism with the SSX system consisting of Ionquest 801 (HA) and LIX 63 (HB).

  • fe iii removal from a synthetic chloride Leach Solution of nickel laterite by n n diethyldodecanamide
    Minerals Engineering, 2014
    Co-Authors: Zhaowu Zhu, Karol Tulpatowicz, Yoko Pranolo, Chu Yong Cheng
    Abstract:

    Abstract In recent years, Leaching with chloride Solutions has attracted much interest for nickel laterite processing due to its high Leaching rate, fast kinetics and the recycling of lixiviant and HCl. However, the presence of large amounts of Fe(III) in the pregnant Leach Solution becomes a big challenge for the recovery of nickel and cobalt. A solvent extraction (SX) method using N,N-diethyldodecanamide (DEDA) to remove Fe(III) from a synthetic chloride Leach Solution of nickel laterites was investigated. It was found that using an organic system consisting of 30% (v/v) DEDOA and 30% (v/v) isodecanol (as phase modifier), over 90% Fe(III) was extracted from the strong chloride Solution (6 M Cl) in a single contact and high selectivity of Fe(III) over other metals was obtained in the pH range tested. The Fe(III) extraction increased substantially with the increase in chloride concentration. High Fe(III) stripping efficiency was obtained using water. The Fe(III) extraction McCabe–Thiele diagram shows that almost all Fe(III) can be extracted using three stages at an A/O ratio of 1.25:1. The Fe(III) stripping McCabe–Thiele diagram shows that almost all Fe(III) can be stripped using two stages at an O/A ratio of 2:1. Extraction and stripping kinetics were very fast and phase separation was good and fast for practical operation.

  • Recovery of water and acid from Leach Solutions using direct contact membrane distillation
    Water science and technology : a journal of the International Association on Water Pollution Research, 2013
    Co-Authors: Uchenna Kesieme, Chu Yong Cheng, Nicholas Milne, Hal Aral, Mikel Duke
    Abstract:

    This paper describes for the first time the use of direct contact membrane distillation (DCMD) for acid and water recovery from a real Leach Solution generated by a hydrometallurgical plant. The Leach Solutions considered contained H2SO4 or HCl. In all tests the temperature of the feed Solution was kept at 60 °C. The test work showed that fluxes were within the range of 18–33 kg/m2/h and 15–35 kg/m2/h for the H2SO4 and HCl systems, respectively. In the H2SO4 Leach system, the final concentration of free acid in the sample Solution increased on the concentrate side of the DCMD system from 1.04 M up to 4.60 M. The sulfate separation efficiency was over 99.9% and overall water recovery exceeded 80%. In the HCl Leach system, HCl vapour passed through the membrane from the feed side to the permeate. The concentration of HCl captured in the permeate was about 1.10 M leaving behind only 0.41 M in the feed from the initial concentration of 2.13 M. In all the experiments, salt rejection was >99.9%. DCMD is clearly viable for high recovery of high quality water and concentrated H2SO4 from spent sulfuric acid Leach Solution where solvent extraction could then be applied to recover the sulfuric acid and metals. While HCl can be recovered for reuse using only DCMD.

  • Recovery of scandium from synthetic red mud Leach Solutions by solvent extraction with D2EHPA
    Separation and Purification Technology, 2013
    Co-Authors: W. Wang, Yoko Pranolo, Chu Yong Cheng
    Abstract:

    Abstract The extraction of scandium from an Australian red mud by selective acid Leaching was explored and preliminary Leaching tests showed that diluted sulphuric acid can be used to Leach scandium from the red mud. The recovery of scandium from a synthetic Leach Solution of the red mud using solvent extraction was studied. A number of extractants were investigated for the extraction of scandium and its separation from the other metals in the synthetic Leach Solution. It was found that amongst the three acidic organophosphorus extractants studied, D2EHPA performed best. With the organic system consisting of 0.05 M D2EHPA and 0.05 M TBP in Shellsol D70 under an A/O ratio of 5:1 at pH 0.25 and 40 °C, over 99% scandium was extracted and almost no iron and aluminium were co-extracted. The scandium extracted can be stripped from the D2EHPA/TBP system with 5 M NaOH to obtain Sc(OH)3 product. A conceptual flowsheet for the recovery of scandium from red mud is proposed.

  • purification of synthetic laterite Leach Solution by solvent extraction using d2ehpa
    Hydrometallurgy, 2000
    Co-Authors: Chu Yong Cheng
    Abstract:

    Abstract The world mineral industry is experiencing an unprecedented interest in nickel–cobalt extraction from laterite ores through acid pressure Leach and SX-EW processes. The recovery of cobalt and nickel from the Leach Solution through direct solvent extraction is of great interest as this would result in significant capital and operating cost savings. In the direct solvent extraction approach, the separation of zinc, calcium, copper and, in particular, manganese from cobalt and nickel is highly important. A series of shakeout tests was undertaken to investigate the fundamentals of the separation of the above impurities from cobalt and nickel using di-2-ethylhexyl phosphoric acid (D2EHPA) in kerosene. D2EHPA pH-extraction isotherms from Solutions each containing a single element showed that the extraction order for the seven elements of interest as a function of pH 50 was Zn 2+ >Ca 2+ >Mn 2+ >Cu 2+ >Co 2+ >Ni 2+ >Mg 2+ . This confirmed that manganese would be extracted from sulfate Solution ahead of cobalt and nickel. Extraction isotherms from Solutions containing Zn, Ca, Mn, Cu, Co, Ni and Mg showed that the separation of zinc and calcium from the other elements was not difficult and the separation of copper and manganese from cobalt and nickel was possible. The separation of manganese from cobalt and nickel by D2EHPA in kerosene was affected by temperature and pH. At pH 3.0, better separation of manganese from cobalt and nickel was achieved at room temperature (23°C). At pH 3.5, better separation of manganese from cobalt was achieved at room temperature (23°C). However, better separation of manganese from nickel could be obtained at elevated temperatures (40–60°C). The McCabe–Thiele diagram for the system showed that at pH 3.5 and 40°C, two theoretical extraction stages at A/O ratio 1:1 were needed to extract 99.9% manganese from the aqueous Solution and to reduce the manganese concentration from 2.0 g/L to 3 ppm. Multiple stage extraction with fresh aqueous Solution showed that cobalt and nickel were crowded out by zinc and manganese. Multiple stage extraction with fresh organic Solution showed that manganese and copper in the aqueous Solution were eliminated. Multiple stage scrubbing of the loaded organic Solution with manganese Solution indicated that after one stage of contact, only about 3 ppm cobalt and nickel were present in the organic Solution.

Li Zeng - One of the best experts on this subject based on the ideXlab platform.

  • A novel nanofiltration process for the recovery of vanadium from acid Leach Solution
    Hydrometallurgy, 2014
    Co-Authors: Guanghao Shang, Guiqing Zhang, Congjie Gao, Li Zeng
    Abstract:

    Abstract The effects of pH, feed concentration and operation pressure on the recovery of vanadium from acid Leach Solution of stone coal using nanofiltration membrane technology were investigated. The rejection and permeate flux of vanadium with two kinds of membranes in nanofiltration process were also studied. After pre-treatment of Leach Solution to remove calcium by the addition of sodium carbonate, the vanadium in the final concentrated Solution can be up to 30 g/L from 1.429 g/L in the feed under the optimum conditions of pH 6–6.5 and operation pressure of 2069 kPa at room temperature during nanofiltration process with the rejection of vanadium more than 95%. The final concentrated Solution can be directly used to produce the V2O5 by traditional method, and the permeate stream can be recycled to Leaching. The conceptual flow sheet for the extraction of vanadium from acid Leach Solution using nanofiltration membrane has been developed.

  • study on extraction of vanadium from high acid Leach Solution of stone coal using extractant hbl 101
    Advanced Materials Research, 2013
    Co-Authors: Li Zeng
    Abstract:

    A new extractant HBL@101 was used to directly extract vanadium from high acid Leach Solution of stone coal. The effects of acidity and Eh of feed, time, phase ratio and temperature on the extraction of vanadium were investigated. The extraction distribution isotherm was also obtained. The results showed that the extraction of vanadium reached 98% in single stage with A/O ratio of 1:1 at 35~45 °C for 10 min. More than 99.7% of vanadium can be extracted in three-stage counter current extraction. The loaded organic can be easily stripped using NaOH Solution. After pH adjustment, the strip liquor was used to precipitate vanadium by adding NH4Cl. The final product of V2O5 with purity of 98.7% can be obtained.

  • a study of the vanadium species in an acid Leach Solution of stone coal using ion exchange resin
    Hydrometallurgy, 2010
    Co-Authors: Li Zeng, Lianshen Xiao, Qixiu Zhang
    Abstract:

    Abstract The species of vanadium extracted by a weak base anion resin D314 from sulphuric acid Leach Solution of stone coal was investigated. The saturated adsorption capacity of vanadium on the resin was found to be up to 501 mg/mL wet resin with a distribution ratio of 950 at pH = 3–4 and 15 °C using static adsorption method. Vanadium was adsorbed in the form of V10O286 −  and HV10O285 − . The study provides the theory and fundamental basis for the industrial application of weak base resins for extraction of vanadium from acid Leach Solution of stone coal.

  • extraction of vanadium from the Leach Solution of stone coal using ion exchange resin
    Hydrometallurgy, 2009
    Co-Authors: Li Zeng, Liansheng Xiao
    Abstract:

    Abstract The loading of V on weak base resin D314 from sulphuric acid Leach Solutions of stone coal containing 2.06 g/L V (V2O5) was found to be 260 mg/mL with contact time of 60 min at pH = 4, giving a recovery of 99%. Stripping of loaded resin was excellent using 3 mol/L NaOH, with a maximum V concentration of 150 g/L in the eluate. The resin features stable reusability when regenerated using 1 mol/L H2SO4 or 2 mol/L HCl. The loading of V on the resin in the industrial trial was found to be as high as 280 mg/mL with a maximum V concentration of 200 g/L in the eluate. The final product of V2O5 with high purity (> 99%) meeting the standard specification was produced. Application of this process in industry is expected to make an important impact on the extraction of vanadium from the Leach Solution of stone coal and to deliver good economical benefits.

Gang Fan - One of the best experts on this subject based on the ideXlab platform.

  • direct solvent extraction of indium from a zinc residue reductive Leach Solution by d2ehpa
    Hydrometallurgy, 2015
    Co-Authors: Zhigan Deng, Chang Wei, Gang Fan, Hao Rong
    Abstract:

    Abstract A direct solvent-extraction process was developed to selectively recover indium from Solutions generated by reductive Leaching of zinc residues. This approach avoids the traditional steps of intermediate precipitation, solid–liquid separation, and re-Leaching. Copper in the Leach Solution is easily removed by cementation with iron powder and the remaining Fe(III) is reduced to the ferrous state, which avoids the possibility of its co-extraction with indium. Indium is effectively extracted from the zinc sulfate Solution by 20% (v/v) di(2-ethylhexyl)phosphoric acid (D2EHPA) dissolved in kerosene at an initial pH of 0.5 and aqueous-to-organic phase ratio (A:O) of 6:1 using three countercurrent stages. Indium extraction is 96.1%, zinc and iron are barely extracted, and the separation factors of indium with respect to zinc and iron are 3640 and 4809, respectively. The complete stripping of indium from the loaded organic phase is achieved using 4 mol/L HCl at an A:O of 1:6. A scheme for direct solvent extraction of indium in zinc hydrometallurgical processing is suggested, by which indium can be concentrated into a small volume of strip Solution containing 11 g/L of indium, which is 85 times its concentration in the feed Solution.

  • selective solvent extraction of vanadium over iron from a stone coal black shale acid Leach Solution by d2ehpa tbp
    Hydrometallurgy, 2011
    Co-Authors: Chang Wei, Zhigan Deng, Gang Fan
    Abstract:

    Abstract A D2EHPA and TBP mixed solvent system diluted with kerosene were used for the selective extraction of vanadium(IV) from iron(II) from an acidic stone coal Leach Solution that was reduced using sodium sulfite. Extraction studies were carried out under different pH and solvent concentrations, and optimized conditions were determined. The loaded organic was stripped with sulfuric acid. The number of stages required for the extraction and stripping of vanadium were determined from a McCabe-Thiele plot and confirmed by counter-current simulation studies. Results demonstrate that the extraction of vanadium increases as the initial pH and the D2EHPA concentration increases in the organic phase. A six-stage counter-current extraction simulation test was conducted over a period of 40 h at a initial pH of 2.48 with 10% (v/v) D2EHPA and 5% (v/v) TBP mixed extractant and resulted in a vanadium extraction of 97% for the feed Solution containing 5.78 g/L V2O5 and 10.86 g/L total Fe. The loaded organic phase that contained 5.34 g/L V2O5 and 1.0 g/L Fe can be completely stripped by three-stage counter-current stripping with 1.5 mol/L H2SO4 at a phase flow ratio of O/A = 5:1 to give a strip Solution containing 26.3 g/L V2O5 and 0.72 g/L Fe.

  • Recovery of H2SO4 from an acid Leach Solution by diffusion dialysis.
    Journal of hazardous materials, 2009
    Co-Authors: Chang Wei, Zhigan Deng, Gang Fan
    Abstract:

    Diffusion dialysis with a series of anion exchange membranes was used to recover H(2)SO(4) from an acid Leach Solution produced during the vanadium manufacturing process. The effects of sulfuric acid, FeSO(4) and VOSO(4) concentration, flow rate and flow rate ratio on the recovery of H(2)SO(4) were investigated. The results showed that sulfuric acid permeated well through the membranes used, while metal ions were efficiently rejected. The recovery of H(2)SO(4) increased as the sulfate concentration of the feed increased and the flow rate ratio of water to feed increased. More than 80% of the H(2)SO(4) could be recovered from the Leach Solution which contained 61.7 g/L free H(2)SO(4), 11.2 g/L Fe and 4.60 g/L V at a flow rate of 0.19x10(-3) m(3)/h m(2). V and Fe ion rejection were within 93-95 and 92-94%, respectively. A preliminary economic evaluation revealed that an investment in this process could be recovered within 27 months.

Chang Wei - One of the best experts on this subject based on the ideXlab platform.

  • direct solvent extraction of indium from a zinc residue reductive Leach Solution by d2ehpa
    Hydrometallurgy, 2015
    Co-Authors: Zhigan Deng, Chang Wei, Gang Fan, Hao Rong
    Abstract:

    Abstract A direct solvent-extraction process was developed to selectively recover indium from Solutions generated by reductive Leaching of zinc residues. This approach avoids the traditional steps of intermediate precipitation, solid–liquid separation, and re-Leaching. Copper in the Leach Solution is easily removed by cementation with iron powder and the remaining Fe(III) is reduced to the ferrous state, which avoids the possibility of its co-extraction with indium. Indium is effectively extracted from the zinc sulfate Solution by 20% (v/v) di(2-ethylhexyl)phosphoric acid (D2EHPA) dissolved in kerosene at an initial pH of 0.5 and aqueous-to-organic phase ratio (A:O) of 6:1 using three countercurrent stages. Indium extraction is 96.1%, zinc and iron are barely extracted, and the separation factors of indium with respect to zinc and iron are 3640 and 4809, respectively. The complete stripping of indium from the loaded organic phase is achieved using 4 mol/L HCl at an A:O of 1:6. A scheme for direct solvent extraction of indium in zinc hydrometallurgical processing is suggested, by which indium can be concentrated into a small volume of strip Solution containing 11 g/L of indium, which is 85 times its concentration in the feed Solution.

  • selective solvent extraction of vanadium over iron from a stone coal black shale acid Leach Solution by d2ehpa tbp
    Hydrometallurgy, 2011
    Co-Authors: Chang Wei, Zhigan Deng, Gang Fan
    Abstract:

    Abstract A D2EHPA and TBP mixed solvent system diluted with kerosene were used for the selective extraction of vanadium(IV) from iron(II) from an acidic stone coal Leach Solution that was reduced using sodium sulfite. Extraction studies were carried out under different pH and solvent concentrations, and optimized conditions were determined. The loaded organic was stripped with sulfuric acid. The number of stages required for the extraction and stripping of vanadium were determined from a McCabe-Thiele plot and confirmed by counter-current simulation studies. Results demonstrate that the extraction of vanadium increases as the initial pH and the D2EHPA concentration increases in the organic phase. A six-stage counter-current extraction simulation test was conducted over a period of 40 h at a initial pH of 2.48 with 10% (v/v) D2EHPA and 5% (v/v) TBP mixed extractant and resulted in a vanadium extraction of 97% for the feed Solution containing 5.78 g/L V2O5 and 10.86 g/L total Fe. The loaded organic phase that contained 5.34 g/L V2O5 and 1.0 g/L Fe can be completely stripped by three-stage counter-current stripping with 1.5 mol/L H2SO4 at a phase flow ratio of O/A = 5:1 to give a strip Solution containing 26.3 g/L V2O5 and 0.72 g/L Fe.

  • Recovery of H2SO4 from an acid Leach Solution by diffusion dialysis.
    Journal of hazardous materials, 2009
    Co-Authors: Chang Wei, Zhigan Deng, Gang Fan
    Abstract:

    Diffusion dialysis with a series of anion exchange membranes was used to recover H(2)SO(4) from an acid Leach Solution produced during the vanadium manufacturing process. The effects of sulfuric acid, FeSO(4) and VOSO(4) concentration, flow rate and flow rate ratio on the recovery of H(2)SO(4) were investigated. The results showed that sulfuric acid permeated well through the membranes used, while metal ions were efficiently rejected. The recovery of H(2)SO(4) increased as the sulfate concentration of the feed increased and the flow rate ratio of water to feed increased. More than 80% of the H(2)SO(4) could be recovered from the Leach Solution which contained 61.7 g/L free H(2)SO(4), 11.2 g/L Fe and 4.60 g/L V at a flow rate of 0.19x10(-3) m(3)/h m(2). V and Fe ion rejection were within 93-95 and 92-94%, respectively. A preliminary economic evaluation revealed that an investment in this process could be recovered within 27 months.

Xuewen Wang - One of the best experts on this subject based on the ideXlab platform.

  • Basic Sulfate Precipitation of Zirconium from Sulfuric Acid Leach Solution
    Metals, 2020
    Co-Authors: Srecko Stopic, Xuewen Wang, Kerstin Forsberg, Bernd Friedrich
    Abstract:

    H2SO4 was ensured to be the best candidate for Zr Leaching from the eudialyte. The resulting sulfuric Leach Solution consisted of Zr(IV), Nb(V), Hf(IV), Al(III), and Fe(III). It was found that ordi ...

  • separation and recovery of vanadium and chromium from acidic Leach Solution of v cr bearing reducing slag
    Journal of environmental chemical engineering, 2017
    Co-Authors: Bianfang Chen, Sheng Huang, Biao Liu, Mingyu Wang, Xuewen Wang
    Abstract:

    Abstract The separation and recovery of vanadium and chromium from an acidic V-Cr-bearing reducing slag Leach Solution was investigated by selective oxidation of V(IV) using manganese dioxide, followed by precipitation of V(V) and Cr(III), respectively. The potential-pH diagrams for vanadium-manganese-water systems and chromium-manganese-water systems were drawn. E (MnO 2 /Mn 2+ ) is higher than E (VO 2 + /VO 2+ ) but lower than E (Cr 2 O 7 2− /Cr 3+ ), which proves manganese dioxide can be used to selectively oxidize V(IV). The oxidation of V(IV) can reach 99.5% at a temperature of 95 °C for a oxidation duration of 3 h with the addition of 40 g/L manganese dioxide, and Cr(III) cannot be oxidized. The V(V) in the oxidized Solution was precipitated in the form of ammonium polyorthovanadate and Cr(III) was precipitated as chromic hydroxide. The overall recovery of vanadium and chromium from the acidic Leach Solution was 98.7% and 99.4%, respectively.

  • extraction of molybdenum from acidic Leach Solution of ni mo ore by solvent extraction using tertiary amine n235
    Canadian Metallurgical Quarterly, 2017
    Co-Authors: Bianfang Chen, Sheng Huang, Biao Liu, Mingyu Wang, Pengfei Xian, Xuewen Wang
    Abstract:

    ABSTRACTTertiary amine N235 diluted with sulphonated kerosene containing sec-octyl alcohol as a phase modifier was used to directly extract molybdenum from the acidic Leach Solution of Ni–Mo ore. The results indicated that the extraction of molybdenum can reach more than 88% using a solvent extraction system consisting of 10 vol.-% N235 and 10 vol.-% sec-octyl alcohol in sulphonated kerosene with an O/A ratio of 1:2 at room temperature for 20 min. The extracted molybdenum species of Mo7O21(OH)33–, MoO2(SO4)22– and MoO2(HSO4)42– in loaded organic phase were identified, and the predominant species was Mo7O21(OH)33–. Molybdenum in the loaded organic phase can be stripped with ammonia Solution, and the stripping of molybdenum can reach 95.8% at an O/A ratio of 7:1, phase contact time of 10 min, and the ammonia concentration of 6 mol L−1.

  • separation of v iv and fe iii from the acid Leach Solution of stone coal by d2ehpa tbp
    Hydrometallurgy, 2015
    Co-Authors: Xuewen Wang, Mingyu Wang, Changjun Jiang, Xiaoyan Xiang, Xiaolin Zhang
    Abstract:

    Abstract The separation of V(IV) and Fe(III) from the acid Leach Solution of stone coal by D2EHPA/TBP was studied. Experimental results showed that V(IV) and Fe(III) can be effectively separated from the Solution containing 2.87 g/L V(IV), 2.71 g/L Fe(II) and 8.45 g/L Fe(III) at pH 1.22 by fractional extraction with the kerosene Solution of 15%(v/v) D2EHPA and 2%(v/v) TBP at room temperature. After 5 stages of counter-current extraction with the solvent at O/A ratio 1:1 contact for 20 min, Fe(III) extraction was 91.5% with 9.18% V(IV) co-extracted. The loaded organic phase was first scrubbed with dilute H 2 SO 4 Solution to recover the co-extracted vanadium, and then the Fe(III) was stripped with the Solution of NaCl saturated in 1.50 mol/L HCl. The stripping percentage of Fe(III) was 98.7% by 4 stages counter-current stripping at O/A ratio 1:1 contact for 10 min. After the removal of Fe(III), the Solution was used as the feed liquid of V(IV) extraction with the regenerated solvent after adjusting the pH to 2.40 by adding CaCO 3 under stirring. The extraction percentage of vanadium reached 97.4% by 6 counter-current stages at O/A ratio 1:1 contact for 10 min. The vanadium loaded organic phase was stripped with the V(IV) scrubbed Solution after adding H 2 SO 4 to increase [H + ] to about 1 mol/L, and the pure VOSO 4 Solution containing 13.7 g/L V was obtained.

  • solvent extraction of molybdenum from acidic Leach Solution of ni mo ore
    Rare Metals, 2014
    Co-Authors: Mingyu Wang, Xuewen Wang, Changjun Jiang, Chaofan Tao
    Abstract:

    A P204 (D2EHPA) diluted with sulfonated kerosene was used for the selective extraction of molybdenum from an acidic Ni–Mo ore Leach Solution that was reduced using sodium thiosulfate. The results indicate that P204 (D2EHPA) is an effective extractant for the extraction of molybdenum. The extraction of Mo is more than 90 % at pH of 0.5, contact time of 10 min, and organic-to-aqueous phase (O/A) ratio of 1:1 with 10 vol% P204 (D2EHPA). Molybdenum in the loaded organic phase can be effectively stripped with ammonium acid carbonate Solution, and the stripping of molybdenum with 60 g·L−1 ammonium acid carbonate Solution is 94.67 % at O/A ratio of 2:1 and contact time of 10 min.