Removal Of Acrylic Acid Research Articles

Removal of acrylic acid from aqueous solution utilizing tri-n-octyl amine or tributyl-phosphate in edible oils through reactive extraction

The separation of acrylic acid from its aqueous solutions with edible oils by reactive extraction method was investigated. Walnut oil, hazelnut oil, sesame oil, and safflower oil were used to prepare a relatively environmentally friendly and low-toxic organic phase. Tributyl phosphate (TBP) and tri-n-octyl amine (TOA) were chosen as extractants. In addition, a modifier (octanol, decanol, octyl acetate, methyl isobutyl ketone, 2-octanone, dimethyl phthalate) was added to the organic phase, and its effect on the extraction was investigated. The temperature effect (25, 45, and 65 °C), one of the parameters affecting the extraction process, was investigated. The results were presented as distribution coefficient (D), extraction efficiency (E%), and loading factor (Z). In the physical extraction experiments performed with edible oils, the extraction efficiency ranged between 14 and 21%, while it reached around 70% with TBP and above 90% with TOA in the reactive extraction. It was observed that the highest efficiency among the oils was obtained with safflower oil (71.88% for TBP and 92.68 % for TOA) for both extractants used. Moreover, using octanol as a modifier in the organic phase had a positive effect on the removal of acrylic acid from aqueous media by reactive extraction.

Acrylic Acid Removal Using Membrane Contactors during Acrylate Downstream Processing: A Techno-economic Assessment

Acrylic Acid Removal Using Membrane Contactors during Acrylate Downstream Processing: A Techno-economic Assessment

Comparison of strongly and weakly basic anionic resins as adsorbent for acrylic acid removal

In the current study, the removal of acrylic acid from the aqueous medium was examined by an adsorption technique using different basic anionic adsorbents, including Amberlite resins (IRA-67 and IRA-400). Amberlite IRA-67 and Amberlite IRA-400 were used as weakly and strongly base anionic resins, respectively. Kinetic, isotherm, and thermodynamic studies were exerted to detect the adsorption properties of these Amberlite IRA resins for the acrylic acid removal. In this context, the impacts of contact time (30–210 min), initial acrylic acid concentration (2%–10% (w/w)), temperature (25 °C-55 °C), and resin quantity (0.05–0.25 g) on the adsorption capacity (qe) were evaluated by experimentally. At these different adsorption conditions, the adsorption capacities of Amberlite IRA resins were determined and compared. The optimal adsorption conditions were determined as the contact time of 180 min, initial acrylic acid concentration of 10% (w/w), the temperature of 25 °C, and the resin quantity of 0.05 g. Comparison of Amberlite IRA resins in acrylic acid adsorption indicated that Amberlite IRA-67 with maximum qe = 232.44 mg.g−1 was an effective resin than Amberlite IRA-400 with maximum qe = 120.21 mg.g−1 at the optimal adsorption conditions.

Catalytic peroxidation of acrylic acid from aqueous solution incorporated with highly active La0.5Sr0.5BO3 (B=Cu, Fe and Ni) perovskite-like catalysts.

In the current study, catalytic behaviour of La0.5Sr0.5BO3 (B=Cu, Fe and Ni) perovskite-like catalysts synthesized by sol-gel method were examined in catalytic peroxidation of acrylic acid as a model organic compound and further characterized by X-ray diffraction (XRD), fourier transform infrared spectroscopy (FTIR), scanning electron microscopy (SEM) with energy dispersive X-ray (EDX), X-ray photoelectron spectroscopy (XPS) and transmission electron microscopy (TEM). The effect of various parameters such as catalyst dose, H2O2/acrylic acid molar ratio, temperature, pH and initial acrylic acid concentration on acrylic acid and COD removal was studied. The maximum acrylic acid and COD removal of 86.79% and 71.57% were observed at optimum operating conditions (e.g., La0.5Sr0.5CuO3 catalyst dose = 600mg/L, stoichiometric molar ratio of H2O2/acrylic acid = 1.5, pH = 3, temperature 65°C and reaction time = 3h). The ROS scavenging studies were performed to identify in-situ generated reactive oxidant species, e.g., hydroxyl radicals (•OH), superoxide radicals (O2 •־) and singlet oxygen (1O2) and treated with their respective quencher during catalytic peroxidation of acrylic acid. Acrylic acid removal kinetics was performed by first order and Langmuir-Hinshelwood kinetic models. The plausible degradation mechanism was proposed based on intermediates identified by GC-MS analysis during catalytic peroxidation of acrylic acid.

Acrylic acid and related dimethylated sulfur compounds in the Bohai and Yellow seas during summer and winter

Abstract. Spatiotemporal distributions of dissolved acrylic acid (AAd) and related biogenic sulfur compounds including dimethylsulfide (DMS) and dissolved and total dimethylsulfoniopropionate (DMSPd and DMSPt) were investigated in the Bohai Sea (BS) and Yellow Sea (YS) during summer and winter. AAd and DMS production from DMSPd degradation and AAd degradation were analyzed. Significant seasonal variations in AAd and DMS(P) were observed. AAd exhibited similar distributions during summer and winter; i.e., relatively high values of AAd occurred in the BS and the northern YS, and the concentrations decreased from inshore to offshore areas in the southern YS. Due to strong biological production from DMSP and abundant terrestrial inputs from rivers in summer, the AAd concentrations in the surface seawater during summer (30.01 nmol L−1) were significantly higher than those during winter (14.98 nmol L−1). The average concentration sequence along the transects during summer (AAd > DMSPt > DMS > DMSPd) showed that particulate DMSP (DMSPp) acted as a DMS producer and that terrestrial sources of AAd were present; in contrast, the sequence in winter was AAd > DMSPt > DMSPd > DMS. High values of AAd and DMS(P) were mostly observed in the upper layers, with occasional high values at the bottom. High AAd concentrations in the porewater, which could be transported to the bottom water, might result from the cleavage of intracellular DMSP and reduce bacterial metabolism in sediments. In addition, the production and degradation rates of biogenic sulfur compounds were significantly higher in summer than in winter, and the removal of AAd was primarily attributed to microbial consumption. Other sources of AAd existed aside from the production from DMSPd.

Adsorptive removal of acrylic acid from the aqueous environment using raw and chemically modified alumina: Batch adsorption, kinetic, equilibrium and thermodynamic studies

Herein, raw alumina was chemically modified using strong acid (HCl) and base (NaOH) to constitute alumina adsorbents, which were applied for the removal of an emerging pollutant, acrylic acid from the aqueous environment. The as-synthesized alumina samples were characterized using FT-IR, SEM, EDX, and surface area analyzer. Characterization results revealed that the chemical modification of alumina did not affect its chemical nature. SEM images demonstrated the porous nature of alumina with irregular shape and rough texture. EDX data shows the elemental composition as Al and O in raw alumina while Cl and Na were found as additional elements in acid (HCl) alumina and base (NaOH) modified alumina, respectively. BET specific surface area of alumina samples was in the range from 155.63–158.36 m2/g. The point of zero charges (PZC) was also determined and found to be 5.9, 6.4 and 9.0 for raw, acid (HCl) and base (NaOH) modified alumina, respectively. In the adsorption study, pH 4.5, 25 °C and 72 and 24 h using the raw and chemically modified alumina, respectively, were found to be the best experimental conditions using 0.1 mol/L acrylic acid solution and 1.0 g alumina. During the consecutive desorption experiments, 86.9 ± 2.5–95.5 ± 3.8 % acrylic acid was desorbed at pH 13. The data follows the pseudo-second-order kinetic and Freundlich adsorption models with 4080–4330 μmol/g adsorption capacity. Moreover, the adsorption process was non-spontaneous and exothermic with the lowering of the randomness of the system at the solid-solution boundary. In conclusion, the high uptake capacity and recyclable nature of the alumina adsorbents render them as promising candidates for the remediation of wastewater and industrial effluents containing such toxic pollutants.

Adsorption Process for Acrylic Acid Removal from Wastewater

The objectives of this study were to develop the mathematical model of the adsorption process of the acrylic acid by using the activated carbon and also to validate the simulation of the adsorption process by using the experimental data. Simulation of the adsorption process is necessary to understand the acrylic acid removal using adsorption process. Acrylic acid is removed from the waste water because it can cause serious damage to the environment due to its high toxicity for the aquatic organisms. As a conclusion, the objective is expected to achieve. The new mathematical model of the adsorption process of the acrylic acid by using the activated carbon can be created. The validation of the simulation is carried out to compare the simulation data with the experiment data.

Reactive extraction of acrylic acid using trioctylamine (TOA) in versatile diluents

Herein, since the extraction of organic acids is very important for recovery, acrylic acid was investigated from aqueous solutions by different diluents of trioctylamine (TOA). The extraction of acrylic acid with TOA dissolved in various individual solvents has been worked. Solvents have selected as dimethyl phthalate (DMP), cyclohexyleacetate (CHA), methyl isobutyl ketone, 2-octanone, 1-octanol, and 1-decanol. The experimental results of experiments are reported as distribution coefficients, D, loading factors, Z, and extraction efficiency, E. It is essential to improve extraction by adding extractant. The maximum removal of acrylic acid is 97.32% with DMP 1.15 mol/kg initial concentration of TOA. Here in, the LSER model has been applied to TOA + alcohol systems on extraction of acrylic acid to make predictions of distribution coefficient.

(Liquid + liquid) equilibria in {water + acrylic acid + (1-butanol, or 2-butanol, or 1-pentanol)} systems at T = 293.2 K, T = 303.2 K, and T = 313.2 K and atmospheric pressure

(Liquid + liquid) equilibrium (LLE) data for {water + acrylic acid + (1-butanol, or 2-butanol, or 1-pentanol)} at T = 293.2 K, T = 303.2 K, and T = 313.2 K and atmospheric pressure (≈95 kPa) were determined by Karl Fischer titration and densimetry. All systems present type I binodal curves. The size of immiscibility region changes little with an increase in temperature, but increases according to the solvent, following the order: 2-butanol < 1-butanol < 1-pentanol. Values of solute distribution and solvent selectivities show that 1-pentanol is a better solvent than 1-butanol or 2-butanol for acrylic acid removal from water solutions. Quality of data was ascertain by Hand and Othmer-Tobias equations, giving R 2 > 0.916, mass balance and accordance between tie lines and cloud points. The NRTL model was used to correlate experimental data, by estimating new energy parameters, with root mean square deviations below 0.0053 for all systems.

Investigation of acrylic acid extractability from aqueous solution using tridodecyl amine extractant

2-Propenoic acid (acrylic acid) extraction from aqueous solution using tridodecylamine (TDA) extractant dissolved in fi ve single solvents (isoamyl alcohol, heptanol, hexanol, octanol, decanol) at 298K was studied. Some parameters related extraction, the extent to which the organic phase may be loaded with acrylic acid is expressed as loading ratio, Z, its values extraction efficiencies E and distribution coefficients, KD , were calculated in light of the experimental data. According to Bizek Approach, equilibrium complexation constants for (acid:amine) (1:1), (1:2) have been determined. The maximum removal of acrylic acid accomplished was about 91% with isoamyl alcohol having 1.188 mol.dm−3 initial concentration of TDA. Linear Solvation Energy Relationship (LSER) model was applied experimental data. LSER model results were compared with the experimental results and well agreement between them was observed.

Extraction Equilibria of Acrylic Acid from Aqueous Solutions by Amberlite LA-2 in Various Diluents

Amberlite LA-2 (a secondary amine mixture) has been studied for its ability to extract acrylic acid at different amine concentrations. The extraction of acrylic acid by Amberlite LA-2 dissolved in seven single solvents (cyclohexane, 2-octanone, toluene, methyl isobutyl ketone (MIBK), iso-octane, hexane, and 1-octanol) has been investigated with respect to different amine concentrations at 298.15 K. In the extraction, two acid−amine complexes, (HO):(R2N) and (HO):(R2N)2, have been assumed to exist in the organic phase in the case of proton-donating diluents, while the complexes (HO):(R2N) and (HO)2:(R2N)3 have been suggested in the case of nonproton-donating diluents. Important data for the design and analysis of different separation processes have been obtained as a result of batch experiments. These important data are distribution coefficients (D), loading factors (Z), extraction efficiency (E), and overall extraction constants (K11, K12, K23). The maximum removal of acrylic acid is 98.22 % with MIBK at ...

Acrylic acid removal from synthetic wastewater and industrial wastewater using Ralstonia solanacearum and Acidovorax avenae isolated from a wastewater treatment system manufactured with polyacrylonitrile fiber

Ralstonia solanacearum and Acidovorax avenae were isolated from a wastewater treatment system manufactured with polyacrylonitrile fiber. The investigation goal is to elucidate the effectiveness of Ralstonia solanacearum and Acidovorax avenae in treating acrylic acid from synthetic wastewater and industrial wastewater. The results reveal that Ralstonia solanacearum and Acidovorax avenae could utilize acrylic acid from synthetic wastewater for growth, when the initial acrylic acid concentration was below 1,009.1 mg/l and 1,383.4 mg/l, respectively. When the acrylic acid concentration was below 606.8 mg/l, the acrylic acid removal ability reached 96.7% and 100%, respectively. Both strains could tolerate acrylamide toxicity, but only Ralstonia solanacearum could tolerate acrylonitrile toxicity. Ralstonia solanacearum and Acidovorax avenae could utilize acrylic acid from industrial wastewater for growth, when the initial acrylic acid concentration was below 1,741.1 mg/l and 1,431.2 mg/l, respectively. When the acrylic acid concentration was below 690.8 mg/l, the acrylic acid removal efficiency reached 83.5% and 62.2%, respectively. Whether the acrylic acid existed in synthetic wastewater or in industrial wastewater, the removal efficiency of acrylic acid by Ralstonia solanacearum exceeded that by Acidovorax avena.

Isotherm and kinetics study for acrylic acid removal using powdered activated carbon

The potential of powdered activated carbon (PAC) for the adsorption of acrylic acid (AA) from aqueous solution was studied at the initial concentration ( C 0) in the range of 50–500 mg/l over the temperature range of 303–348 K. The equilibrium adsorption studies were carried out to evaluate the effect of adsorbent dosage and contact time, change in pH by adding adsorbents and the initial concentration. Langmuir, Freundlich and Redlich–Peterson (R–P) equilibrium isotherm models were tested to represent the data. Error functions were used to test their validity to fit of the adsorption data with the isotherm and kinetic models. The Freundlich isotherm equation is found to best represent the equilibrium separation data in the temperature range of 303–348 K. The maximum adsorption capacity of AA onto PAC was obtained as q m = 36.23 mg/g with an optimum PAC dosage w = 20 g / l at 303 K for C 0 = 100 mg/l. The pseudo-second-order kinetics is found to represent the experimental AA–PAC data. The negative value of Δ G a d o (−16.60 to −18.18 kJ/mol K) indicate the feasibility and spontaneity of the adsorption process.

Acrylic acid removal by acrylic acid utilizing bacteria from acrylonitrile–butadiene–styrene resin manufactured wastewater treatment system

The aim of this study is to isolate the acrylic acid utilizing bacteria from the ABS resin manufactured wastewater treatment system. The bacteria should have the ability to remove acrylic acid and tolerate the acrylonitrile and acrylamide toxicity. The aim is also to understand the performance of isolated pure strain for treating different initial acrylic acid concentrations from synthetic wastewater. The results are: twenty strains were isolated from the ABS resin manufactured wastewater treatment system and twelve of them could utilize 600 mg/l acrylic acid for growth. Seven of twelve strains could tolerate the acrylonitrile and acrylamide toxicity, when the concentration was below 300 mg/l. Bacillus thuringiensis was one of the seven strains and the optimum growth temperature was 32 degrees C. Bacillus thuringiensis could utilize acrylic acid for growth, when the initial acrylic acid concentration was below 1,690.4 mg/l. Besides this, when the initial acrylic acid concentration was below 606.8 mg/l, the acrylic acid removal efficiency exceeded 96.3%. Bacillus thuringiensis could tolerate 295.7 mg/l acrylamide and 198.4 mg/l acrylonitrile toxicity but could not tolerate 297.3 mg/l epsilon-caprolactam.

Separation and Recovery of Low Molecular Weight Organic Acids by Emulsion Liquid Membranes

Abstract Emulsion liquid membrane (ELM) extraction of low molecular weight organic acids resulting from whey fermentations was investigated. Rates of removal of lactic, acetic, propionic, and acrylic acids decreased as pH and concentration were increased. An ELM process for selective removal of acrylic acid from acrylic acid-propionic acid mixtures was developed through incorporation of a co-solvent (cyclohexanone) in the membrane phase of the emulsion. Degree of removal for each acid and, hence, selectivity among the acids appears to be determined by the water-membrane phase partition coefficient.