目前國內每年約產生10,000 ~ 12,000公噸加氫脫硫廢觸媒。廢觸媒經資源化程序回收釩、鉬後之殘渣即為藍泥。進一步將藍泥資源化時，經酸培燒及浸漬後之溶液中仍含相當濃度的釩、鉬等金屬離子。因此本研究以藍泥浸漬液為處理對象，以離子交換樹脂法分離釩、鉬金屬離子。主要研究內容為利用批次方式進行吸附與脫附試驗，獲得樹脂對釩、鉬分離之參數，再藉由離子交換管柱試驗進行釩、鉬分離及純化試驗。
批此實驗得知螯合型樹脂對釩、鉬皆有優異的吸附效果，並進行批次比較(簡稱為M、I樹脂)。由動力吸附實驗得知，鉬比釩需較長時間才可達吸附平衡，吸附動力行為較符合擬二階動力方程式。經Langmuir等溫吸附模式分析得知，樹脂M對釩飽和吸附量最大，約為38mg/g。樹脂M對釩、鉬的吸附效果皆比IRC748為佳。經Freundlich等溫吸附模式分析得知樹脂I與M對釩的吸附容量不受溶質平衡濃度影響，吸附鉬則皆受溶質平衡濃度影響。樹脂I與M吸附釩、鉬反應之活化能皆為正值，分別為36.92、6.16、38.02、0.75 KJ mole-1。以熱力學方程式可獲得I與M吸附釩、鉬反應之Gibbs自由能變化(△G0)、焓變(△H0)、熵變(△S0)。由脫附批次試驗可知，H2SO4與NaOH可脫附吸附於I與M樹脂之釩離子，NH4OH與NaOH可脫附鉬離子。
以樹脂I進行管柱試驗，可知進料流速越慢吸附效果越好。藍泥浸漬液需在pH＝2時，樹脂I對釩、鉬吸附效果最佳，不同金屬離子之吸附能力大小順序為鉬>釩>>鎳>鋁。管柱吸附約140B.V之進料後進行階段洗脫，可分別富集尖峰濃度約1200ppm、純度87.3%之釩溶液，與1800ppm、純度99.1%之鉬溶液，達到鉬與釩分離純化之效果。

At present, the annual production of wasted hydrodesulfurization catalyst domestically is about 11,000 tonnes. The residues obtained by extracting V and Mo from wasted hydrodesulfurization catalyst is called the blue sludge. In order to further recover V, Mo and Ni, the blue sludge was subjected to acid-roasting and hot-water leaching process. This process yields an leachate rich in Ni and Al and also containing some V and Mol ions. The subject of this research is the leachate from blue sludge. In this study we investigate the recovery and separation of V and Mo ions in leachate by ion exchange process.
Batch experimental results indicated that both chelating resin；referred to as resin M and I；adsorb V and Mo effectively. The effects of contact time, pH and temperature on ion exchange behavior of two metal ions was studied. The adsorption isotherms were described by means of Langmuir and Freundlich models. Langmuir isotherm model showed that resin M adsorbs more V and Mo than I. Freundlich isotherm model indicated that the adsorption capacity of V is insenstive to the change in the equilibrium concentration of solute. However the adsorption capacity of Mo is influenced by the change in the equilibrium concentration of solute. The kinetic data were tested using the Lagergren-first-order and pseudo-second-order kinetic models. Data for Ion exchange of V and Mo correlated well with the pseudo-second-order kinetic model, indicating that the chemical adsorption was the rate-limiting step. The activation energy for the exchange of V and Mo on resin I and M is 36.92、6.16、38.02、0.75 kJ mole-1 respectively. Various thermodynamic parameters for exchange reactions between I、M and V、Mo such as Gibbs free energy change ( G0), enthalpy change( H0) and entropy change( S0) were calculated. A negative G0 indicated that the ion exchange of V and Mo from solution using I was feasible. Results of batch desorption tests show that V ions on resin M and I were succesfully desorbed by using H2SO4 and NaOH respectively. Mo ions on resin M and I were succesfully desorbed by using NH4OH and NaOH respectively.
The results of column tests indicated that the slower the flow rate of feed solution the better the adsorption of V and Mo. Maintaining the pH of leachate at 2, resin I has the highest adsorption capacity for V and Mo. Resin I adsords ions in the following order: Mo> V>> Ni> Al. Having operated for 140B.V in adsorption mode, the loaded resin I can be successfully eluted. Finally, a V concentrate with 1200ppm peak concentration and 87.3 purity and a Mo concentrate with 1800ppm peak concentration and 99.1 purity were obtained.

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