Phase diagrams of the MgSO4-Al2(SO4)3-(NH4)2SO4-H2O system at 25 and 55 °C and their application in mineral carbonation

Liu, Weizao; Meng, Fanqi; Chu, Guanrun; Wang, Liming; Yue, Hairong; Liang, Bin; Li, Chun

doi:10.1016/j.fluid.2018.06.021

Cited by 16 publications

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References 19 publications

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“…According to the quaternary phase diagram of MgSO 4 –Al 2 (SO 4 ) 3 –(NH 4 ) 2 SO 4 –H 2 O (no five‐element phase diagram of MgSO 4 –TiOSO 4 –Al 2 (SO 4 ) 3 –(NH 4 ) 2 SO 4 –H 2 O is available), a pure crystal of NH 4 Al(SO 4 ) 2 ·12H 2 O can be obtained by cooling the leachate . The crystallization of Al is affected by cooling temperature, molar ratio of NH 4 + to Al 3+ , and concentration of Al 3+ in aqueous solutions, as discussed in the literatures .…”

Section: Resultsmentioning

confidence: 90%

“…The roasting slag under the optimum roasting condition was leached using 3.5% H 2 37 The crystallization of Al is affected by cooling temperature, molar ratio of NH 4 + to Al 3+ , and concentration of Al 3+ in aqueous solutions, as discussed in the literatures. 38,39 Our preliminary experiments demonstrated that, although the extraction ratios of other ions varied slightly, the extraction of Al significantly increased with an increment in the liquid-to-solid ratio during the leaching upon it larger than 1.5, thus changing the concentration of Al 3+ and molar ratio of NH 4 + to Al 3+ .…”

Section: Recovery Of Value-added Al and Ti Productsmentioning

confidence: 99%

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Indirect mineral carbonation of chlorinated tailing derived from Ti‐bearing blast‐furnace slag coupled with simultaneous dechlorination and recovery of multiple value‐added products

et al. 2018

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The chlorinated tailing (CT) generated during titanium extraction from Ti‐bearing blast‐furnace slag contains 3–5 wt% chlorides, which are hazardous to the environment. In this paper, a process for simultaneous CO2 mineralization, dechlorination, and recovery of multiple value‐added products was proposed to fully utilize the CT. In this process, Ti, Al, Mg, and Ca are extracted in the form of their sulfates via roasting with recyclable (NH4)2SO4 followed by leaching with dilute H2SO4. Their extraction ratios are 83.1%, 87.4%, 89.4%, and 92.1%, respectively. The chlorides are simultaneously removed from the CT as gaseous HCl with a dechlorination ratio of 98.5%. Subsequently, 89.5% of the Al and 97.5% of the Ti in the leaching liquor are successively recovered as NH4Al(SO4)2·12H2O with a purity of 99 wt% and titanium‐rich material with TiO2 of 62.5 wt%. The CaSO4‐rich leaching residue and MgSO4‐rich leachate, after complete depletion of the Al and Ti, are separately carbonated with a mixed gas of CO2 and NH3 with total CO2 capacity up to 279.8 kg CO2 per tonne CT. The preliminary economic evaluation shows that income from selling products after the deduction of the cost of primary raw materials reaches 200 $/tonne CT. The proposed route therefore provides a cost‐efficient alternative for comprehensive utilization of the polluting CT. © 2018 Society of Chemical Industry and John Wiley & Sons, Ltd.

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Section: Resultsmentioning

confidence: 90%

Section: Recovery Of Value-added Al and Ti Productsmentioning

confidence: 99%

Indirect mineral carbonation of chlorinated tailing derived from Ti‐bearing blast‐furnace slag coupled with simultaneous dechlorination and recovery of multiple value‐added products

et al. 2018

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“…In the phase diagram, we can see that the crystalline regions of (NH 4 ) 2 Mn(SO 4 ) 2 ·6H 2 O and (NH 4 ) 2 Mg(SO 4 ) 2 ·6H 2 O are relatively large. The common saturation points in MgSO 4 –(NH 4 ) 2 SO 4 –H 2 O, a subsystem of the system, are compared with the literature values, − and the results are shown in Figure .…”

Section: Results and Discussionmentioning

confidence: 99%

Solid–Liquid Phase Equilibrium of MnSO₄–MgSO₄–H₂O and (NH₄)₂SO₄–MnSO₄–MgSO₄–H₂O Systems at T = 303.15 K

2020

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In this study, the stable (solid + liquid) phase equilibrium and physical–chemical properties of the ternary MnSO4–MgSO4–H2O system at T = 303.15 K have been determined by the method of isothermal solution saturation. It is found that there are three crystalline regions, one unsaturated crystallization region, and one invariant point. The density and refractive index of this system were compared with the experimental values, and it is found that there is little difference between the two systems. The experimental solubility data were compared with the literature values, and the invariant points at different temperatures were fitted to provide data for the water-salt system containing manganese sulfate and magnesium sulfate. At the same time, the solubility data of the MnSO4–MgSO4–(NH4)2SO4–H2O system were determined by the same method, and the phase diagram was drawn. Comparing the actual phase diagram measured by the experiment with the predicted phase diagram obtained by means of translation method, it is found that they have the same crystallization regions. In order to see more clearly the relationship between the quaternary MnSO4–MgSO4–(NH4)2SO4–H2O system and its three ternary sub-systems (MnSO4–(NH4)2SO4–H2O, MgSO4–(NH4)2SO4–H2O, and MnSO4–MgSO4–H2O), we have plotted the related stereoscopic phase diagram. The research of this study provides the data basis for the crystallization process of manganese sulfate.

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CO2 mineral carbonation using industrial solid wastes: A review of recent developments

Liu

Teng

Rohani

et al. 2021

Chemical Engineering Journal

276

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Phase diagrams of the MgSO4-Al2(SO4)3-(NH4)2SO4-H2O system at 25 and 55 °C and their application in mineral carbonation

Cited by 16 publications

References 19 publications

Indirect mineral carbonation of chlorinated tailing derived from Ti‐bearing blast‐furnace slag coupled with simultaneous dechlorination and recovery of multiple value‐added products

Indirect mineral carbonation of chlorinated tailing derived from Ti‐bearing blast‐furnace slag coupled with simultaneous dechlorination and recovery of multiple value‐added products

Solid–Liquid Phase Equilibrium of MnSO₄–MgSO₄–H₂O and (NH₄)₂SO₄–MnSO₄–MgSO₄–H₂O Systems at T = 303.15 K

CO2 mineral carbonation using industrial solid wastes: A review of recent developments

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Phase diagrams of the MgSO4-Al2(SO4)3-(NH4)2SO4-H2O system at 25 and 55 °C and their application in mineral carbonation

Cited by 16 publications

References 19 publications

Indirect mineral carbonation of chlorinated tailing derived from Ti‐bearing blast‐furnace slag coupled with simultaneous dechlorination and recovery of multiple value‐added products

Indirect mineral carbonation of chlorinated tailing derived from Ti‐bearing blast‐furnace slag coupled with simultaneous dechlorination and recovery of multiple value‐added products

Solid–Liquid Phase Equilibrium of MnSO4–MgSO4–H2O and (NH4)2SO4–MnSO4–MgSO4–H2O Systems at T = 303.15 K

CO2 mineral carbonation using industrial solid wastes: A review of recent developments

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Product

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Phase diagrams of the MgSO4-Al2(SO4)3-(NH4)2SO4-H2O system at 25 and 55 °C and their application in mineral carbonation

Solid–Liquid Phase Equilibrium of MnSO₄–MgSO₄–H₂O and (NH₄)₂SO₄–MnSO₄–MgSO₄–H₂O Systems at T = 303.15 K