Kinetics of Simultaneous Ammonium and Phosphate Recovery by Natural Zeolite

2021 ◽  
Vol 5 (4) ◽  
pp. 68
Author(s):  
Sandro Pesendorfer ◽  
Markus Ellersdorfer
Keyword(s):  
Ion Exchange ◽  
Natural Zeolite ◽  
Large Scale ◽  
Ph Value ◽  
Exchange Process ◽  
Phosphate Removal ◽  
Synthetic Wastewater ◽  
Nutrient Recovery ◽  
Phosphate Recovery ◽  
Kinetics Of

Nowadays, fertilizers containing nitrogen and phosphorus are indispensable for medium and large-scale industrial agriculture. To meet the growing demand of nutrients and reduce the accompanied ecological footprint of primary fertilizer production, processes and technologies for nutrient recovery are necessary and have to be developed. This study represents the basis of an extension of the ion-exchange-loop-stripping process (ILS), which is a combined stripping and ion exchange process using natural zeolite for nitrogen recovery. In batch experiments with a special zeolite filled stirrer, the mechanism and kinetics of simultaneous ammonium and phosphate recovery by natural zeolite were determined. Zeolite loadings of 6.78 mg PO43− g−1 were reached and after regeneration, phosphate recovery rates up to 75% of the initial concentration were achieved. The speed of phosphate precipitation is mostly controlled by the pH value of synthetic wastewater. Phosphate removal in simultaneous experiments does not affect ammonium sorption onto zeolite. These findings and the different removal mechanisms of ammonium and phosphate lead to versatile applications in wastewater treatment and reveal great potential of natural zeolite in simultaneous nutrient recovery processes.

Removal of Copper-Cyanide Complexes from Electroplating Industry Effluents by Ion-Exchange Fiber

2012 ◽  
Vol 476-478 ◽  
pp. 1847-1850 ◽  
Author(s):  
Zhan Qiang Cao ◽  
Ming Yu Li ◽  
Yao Ran Sun ◽  
Qing Xuan Zeng
Keyword(s):  
Ion Exchange ◽  
Room Temperature ◽  
Ph Value ◽  
Exchange Process ◽  
Packed Beds ◽  
Copper Cyanide ◽  
Ion Exchange Process ◽  
Cyanide Complexes ◽  
Ion Exchange Fiber ◽  
Industry Effluent

Removal of copper-cyanide complexes from electroplating industry effluent were studied by using an ion-exchange process. A kind of polypropylene strong alkaline anion exchange fiber was used to perform packed beds continuous experiments. The conditions of adsorption were wastewater pH value 9.0 and flow rate 90-120 BV•h-1 at room temperature. The packed beds were exhausted at 1300 bed volumes for copper-cyanide complexes The elution of copper-cyanide complexes from ion-exchange fiber was studied. The results showed that copper-cyanide complexes were easily eluted from ion exchange fiber using either 2.0 mol•L-1 NaNO3 or NaCl. With 1.0 mol•L-1 NaNO3 solution at 30 BV•h-1, the regenerating rate of copper-cyanide complexes was more than 95%.

Kinetics of ion exchange process for separation of glutamic acid

1989 ◽  
Vol 4 (6) ◽  
pp. 249-256 ◽  
Author(s):  
T. H. �zdamar ◽  
S. Taka� ◽  
G. �alik ◽  
R. Ballica
Keyword(s):  
Ion Exchange ◽  
Glutamic Acid ◽  
Exchange Process ◽  
Ion Exchange Process ◽  
Kinetics Of ◽  
Kinetics Of Ion Exchange

Zur Kinetik der Ionenaustauscher III. Die Filmdiffusion bei vollständigen Umbeladungen

1969 ◽  
Vol 24 (6) ◽  
pp. 900-902
Author(s):  
Kurt Bunzel
Keyword(s):  
Ion Exchange ◽  
Exchange Reaction ◽  
Exchange Process ◽  
Ionic Composition ◽  
Selectivity Coefficient ◽  
Film Diffusion ◽  
Ion Exchange Process ◽  
Ion Exchange Reaction ◽  
Diffusion Controlled ◽  
Kinetics Of

The selectivity coefficient K21 of an ion-exchange process is in general a function of the ionic composition of the material. As a result, the value of K21 will change continuously during a com­plete conversion of the ion-exchanger. Equations for the kinetics of such a conversion with variable K21 are given for a film diffusion controlled ion-exchange reaction.

Ureolytic phosphate precipitation from anaerobic effluents

2009 ◽  
Vol 59 (10) ◽  
pp. 1983-1988 ◽  
Author(s):  
E. Desmidt ◽  
W. Verstraete ◽  
J. Dick ◽  
B. D. Meesschaert ◽  
M. Carballa
Keyword(s):  
Hydraulic Retention Time ◽  
Ph Value ◽  
Continuous Operation ◽  
Phosphate Concentration ◽  
Phosphate Removal ◽  
Synthetic Wastewater ◽  
Processing Industry ◽  
Operational Conditions ◽  
Constant Ph ◽  
High Concentrations

In this work, the elimination of phosphate from industrial anaerobic effluents was evaluated at lab-scale. For that purpose, the ureolytic method previously developed for the precipitation of Ca2 +  from wastewater as calcite was adapted for the precipitation of phosphate as struvite. In the first part of the study, computer simulations using MAPLE and PHREEQC were performed to model phosphate precipitation from wastewater as struvite. The results obtained showed that relative high concentrations of ammonium and magnesium are needed to precipitate phosphate as struvite. The total molar concentrations ratio of Mg2 + :PO43−-P:NH4+ required to decrease PO43−-P concentrations from 20 to 6 mg PO43−-P/l at pH 8.4-8.5 was estimated on 4.6:1:8. In the second part of the study, lab-scale experiments with either synthetic wastewater or the anaerobic effluent from a vegetable processing industry were carried out in batch and continuous mode. Overall, the continuous operation at a hydraulic retention time (HRT) of 2.4 h and an added molar concentration [Mg2 + ]:[PO43−-P]:[NH4+] ratio of 1.6:1:2.3 resulted in a constant pH value in the reactor (around 8.5) and an efficient phosphate removal (>90%) to residual levels of 1–2 mg PO43−-P/l. Different operational conditions, such as the initial phosphate concentration, HRT and the use of CaCl2 or MgO instead of MgCl2, were analysed and the performance of the reactor was satisfactory under a broad range of them. Yet, overall, optimal results (higher phosphate removal) were obtained with MgCl2.

Synthesis of linear alkylbenzene sulphonate intercalated iron(II) iron(III) hydroxide sulphate (green rust) and adsorption of carbon tetrachloride

Clay Minerals ◽  
2007 ◽  
Vol 42 (3) ◽  
pp. 307-317 ◽  
Author(s):  
K. B. Ayala-Luis ◽  
D. K. Kaldor ◽  
C. Bender Koch ◽  
B. W. Strobel ◽  
H. C. B. Hansen
Keyword(s):  
Carbon Tetrachloride ◽  
Ion Exchange ◽  
Exchange Process ◽  
Green Rust ◽  
Stoichiometric Ratio ◽  
X Ray Diffraction ◽  
Linear Alkylbenzene ◽  
Ion Exchange Process ◽  
Linear Alkylbenzene Sulphonate ◽  
Kinetics Of

AbstractGreen rusts, GRs, can act as both sorbents and reductants towards selected pollutants. Organo-GRs are expected to combine these properties with a high affinity for hydrophobic substances. A novel organo-GR, GRLAS, was synthesized by incorporating a mixture of linear alkylbenzenesulphonates (LAS) into the interlayer space of synthetic sulphate green rust, GRSO4 . Mössbauer analysis of GRLAS indicates that the structure of the organo-GR is very similar to that of the initial GRSO4 with regard to the FeII/FeIII ratio and local coordination of Fe atoms. X-ray diffraction demonstrates that the GRLAS formed was well ordered, although a mixture of surfactant was used for intercalation. The basal spacings of the GRLAS and the kinetics of the ion-exchange process were dependent on the initial surfactant loading; basal spacings of ~2.85 nm were obtained at LAS solution concentrations >10 mM. The ratio LASadsorbed/SO42–desorbed significantly exceeded the stoichiometric ratio of 2 during the initial part of the ion-exchange process (t = 5 h). However, this ratio was reached progressively with time. GRSO4 preferentially sorbed LAS homologues with long alkyl chains over short ones. Carbon tetrachloride was successfully adsorbed into GRLAS. The adsorption isotherm was linear with a distribution coefficient, Kd, of 505±19 litre kg–1.

The Avco continuous moving bed ion exchange process and large scale desalting

Desalination ◽  
1975 ◽  
Vol 17 (1) ◽  
pp. 111-120 ◽  
Author(s):  
H. Gold ◽  
A. Todisco ◽  
A.A. Sonin ◽  
R.F. Probstein
Keyword(s):  
Ion Exchange ◽  
Large Scale ◽  
Exchange Process ◽  
Moving Bed ◽  
Ion Exchange Process

An ion-exchange process with thermal regeneration. III. Properties of weakly acidic ion-exchange resins

1966 ◽  
Vol 19 (4) ◽  
pp. 589 ◽  
Author(s):  
DE Weiss ◽  
BA Bolto ◽  
R McNeill ◽  
AS MacPherson ◽  
R Siudak ◽  
...  
Keyword(s):  
Ion Exchange ◽  
Acrylic Acid ◽  
Methacrylic Acid ◽  
Ph Value ◽  
Exchange Process ◽  
Thermal Regeneration ◽  
Ion Exchange Process ◽  
Titration Curves ◽  
Acid Resin ◽  
Poly Acrylic Acid

A series of cross-linked poly(acrylic acid) and poly(methacrylic acid) resins has been synthesized. Their titration curves, and those of similar commercial resins, show that at c. 20� the pH value at half neutralization may be varied within about one unit by using acrylic or methacrylic acid monomers, or by changing the degree of cross-linking. The titration curves of such resins do not have a pronounced plateau although the acidity is due only to carboxyl groups. Resins with flatter titration curves can be made by copolymerizing acrylic or methacrylic acids with methyl methacrylate. Copolymerization reduces the effective acid strength of carboxylic acid resins but does not always produce a resin with a flatter titration curve. The effects of salt concentration, calcium ions, and temperature on the titration curves of a poly(acry1ic acid) resin have been studied. Heating the resins in a salt solution from c. 20 to 80� decreases their effective acidity slightly. A bigger reduction in acidity with heating is observed with several polymers in which a "snake" polymer, such as a poly(ethy1ene oxide), is incorporated within a cross-linked poly(acrylic acid) resin cage.

scholarly journals Removal of Mercury from Waste Water: Large-Scale Performance of an Ion Exchange Process

1992 ◽  
Vol 25 (3) ◽  
pp. 165-172 ◽  
Author(s):  
J. A. Ritter ◽  
J. P. Bibler
Keyword(s):  
Waste Water ◽  
Ion Exchange ◽  
Large Scale ◽  
Exchange Process ◽  
Ion Exchange Resin ◽  
Mercury Content ◽  
Water Stream ◽  
Ion Exchange Process ◽  
Laboratory Waste ◽  
Pass Through

Duolite™ GT-73 ion exchange resin routinely reduces the mercury content of a waste water stream to less than the permitted level of 10 ppb. Effluent concentrations from the ion exchange facility (IEF) are consistently between 1 to 5 ppb, even though the feed contains a varying concentration of mercury (0.2 to 70 ppm). Two operational problems have been encountered at that facility, however. Firstly, the stated capacity of the resin for mercury was not being achieved. The abnormally low capacity was traced to analytical laboratory waste which was intermittently treated by the resin. That waste contained hydrochloric acid, stannous chloride, and potassium permanganate, among other chemicals, which presumably eluted sorbed mercury from the resin and also oxidized the thiol (SH) functional groups on the resin and rendered them inactive. The net effect was that the resin had to be replaced more frequently than anticipated. Secondly, the IEF was temporarily shut down because the mercury content of the waste water could not be reduced to below the permitted level, even with fresh resin. That problem was caused by slow settling solids composed mainly of iron which apparently adsorbed some of the mercury and allowed it to pass through the resin untreated. The solids were presumably a result of processing waste water abnormally high in iron which may have co-precipitated with mercury and other elements in the feed and caused a residual buildup of solids throughout the IEF. The problem was remedied by installing a 0.2 µm cartridge filter between the feed tank and the columns.

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