Kinetic Study of Ambient-Temperature Reduction of FeIIIedta by Na2S2O4

Suchecki, Tomasz T.; Mathews, Barbara; Kumazawa, H.

doi:10.1021/ie0493006

Cited by 50 publications

(34 citation statements)

References 36 publications

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“…In the case of Sn, Table 2 and Figure 4 show that k obs decreases with an increase in pH 0 , and at pH 0 9, the pseudo-first-order kinetic law does not fit the data. Such a trend of the reduction rate conforms to eqs 16 The following findings could be obtained:…”

Section: Zn Powdersupporting

confidence: 83%

Applied Kinetics Aspects of Ferric EDTA Complex Reduction with Metal Powder

Suchecki

Mathews

Augustyniak

et al. 2014

Ind. Eng. Chem. Res.

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Nitrogen and sulfur oxides (NO x and SO x ) emitted from fossil-fuel-fired facilities can be simultaneously absorbed into aqueous mixed solutions of sulfite and Fe II L, a ferrous ion coordinated to a ligand L (a chelate compound). Usually, the ligand L represents an anion of ethylenediaminetetraacetic acid (EDTA or edta). Nitrogen oxide (NO) sparingly soluble in water is promptly bound to the [Fe II (edta)(H 2 O)] 2− complex to form the [Fe II (edta)(NO] 2− compound. However, [Fe II (edta)(H 2 O] 2− chelate is oxidized to form [Fe III (edta)(H 2 O)] − by NO, NO 2 , and O 2 , normally coexisting in flue gases.Because the ferric complex does not react with NO, the suppression of these undesired oxidation processes is a very important technological problem to be overcome. Thus, in this work, the reduction kinetics of ferric ion by metal was discussed on the basis of the kinetic data regarding the ferric ion reduction in aqueous solutions of [Fe III (edta)(H 2 O)] − containing such pulverized metals as aluminum, tin, and zinc. The rate expression for the reduction of [Fe III (edta)(H 2 O] − by a metal powder was derived in terms of the rate-determining step approximation method. Laboratory-scale experiments were conducted in a recirculation-type glass reactor filled with 250 cm 3 of solution. The influence of the following parameters on the reduction rate was investigated: (1) [Fe III (edta)(H 2 O)] 0 − = 0.100−0.010 M, (2) [metal] 0 /[Fe III (edta)(H 2 O)] 0 − = 10−100, (3) pH 0 = 3−9, and (4) temperature = 20−80°C. Zinc and aluminum powders were found to be effective reducing agents for ferric ions coordinated to EDTA. Similar experiments were carried out using a working solution in a simultaneous NO and SO 2 removal process as a solvent of [Fe III (edta)(H 2 O)] − solution.

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Section: Zn Powdersupporting

confidence: 83%

Applied Kinetics Aspects of Ferric EDTA Complex Reduction with Metal Powder

Suchecki

Mathews

Augustyniak

et al. 2014

Ind. Eng. Chem. Res.

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“…Presently, there are many different control technologies in various stages of development (Chmielewski et al, 2010;Chu et al, 2001;Ellison, 2003;Hutson et al, 2008;Jin et al, 2006;Lee et al, 2005;Liu et al, 2010;Suchecki et al, 2005) that will allow these goals to be achieved. The most common and effective technology for SO 2 removal is flue gas desulfurization, in which limestone slurry is used as a scrubbing solution.…”

Section: Introductionmentioning

confidence: 99%

The importance of the location of sodium chlorite application in a multipollutant flue gas cleaning system

Krzyżyńska

Hutson

2012

Journal of the Air & Waste Management Association

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In this study, removing sulfur dioxide (SO2), nitrogen oxides (NO(x)), and mercury (Hg) from simulated flue gas was investigated in two laboratory-sized bubbling reactors that simulated an oxidizing reactor (where the NO and Hg(0) oxidation reactions are expected to occur) and a wet limestone scrubber, respectively. A sodium chlorite solution was used as the oxidizing agent. The sodium chlorite solution was an effective additive that enhanced the NO(x), Hg, and SO2 capture from the flue gas. Furthermore, it was discovered that the location of the sodium chlorite application (before, in, or after the wet scrubber) greatly influences which pollutants are removed and the amount removed. This effect is related to the chemical conditions (pH, absence/presence of particular gases) that are present at different positions throughout the flue gas cleaning system profile. The research results indicated that there is a potential to achieve nearly zero SO2, NO(x), and Hg emissions (complete SO2, NO, and Hg removals and -90% of NO(x) absorption from initial values of 1500 ppmv of SO2, 200 ppmv of NO(x), and 206 microg/m3 of Hg(0)) from the flue gas when sodium chlorite was applied before the wet limestone scrubber. However applying the oxidizer after the wet limestone scrubber was the most effective configuration for Hg and NO(x) control for extremely low chlorite concentrations (below 0.002 M) and therefore appears to be the best configuration for Hg control or as an additional step in NO(x) recleaning (after other NO(x) control facilities). The multipollutant scrubber, into which the chlorite was injected simultaneously with the calcium carbonate slurry, appeared to be the least expensive solution (when consider only capital cost), but exhibited the lowest NO(x) absorption at -50%. The bench-scale test results presented can be used to develop performance predictions for a full- or pilot-scale multipollutant flue gas cleaning system equipped with wet flue gas desulfurization scrubber.

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“…It has been agreed that using chemical additives to an aqueous scrubbing solution could have a significant impact on control strategies [1,2]. Several methods have been developed to enhance NO absorption, including the use of oxidants to oxidize NO to the more soluble NO 2 and the addition of various iron(II) chelates to bind and activate NO [3][4][5][6][7][8][9][10][11][12][13][14]. So far, none of these methods have been put into commercial application.…”

Section: Introductionmentioning

confidence: 99%