Limestone selection criteria for EDR water remineralization

Ruggieri, Flavia; Fernández-Turiel, J. L.; Gimeno, D.; Valero, Fernando; García, Javier Contreras; Medina, María Eugenia Amezquita

doi:10.1016/j.desal.2007.07.020

Cited by 16 publications

(10 citation statements)

References 12 publications

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“…The experimental by Yamauchi et al [2] carried out at 40 o C yielded a value of 6 k// = 31.3 Â 10 À3 mm/s for the kinetic coefficient, while the experimental by Hasson and Bendrihem [1] carried out at 30 o C gave the value of 6 k// = 25.0 Â 10 À3 mm/s. The kinetic coefficient is known to depend on the crystal habit of the specific calcite pellets, their inner porosity, and the impurities they contain [3]. The objectives of this research were to measure the kinetic coefficient of certain specific pellets, to extend the scope of available calcite dissolution data and to study the temperature effect.…”

Section: Introductionmentioning

confidence: 99%

Remineralization of desalinated water by limestone dissolution with carbon dioxide

Shemer

Hasson

Semiat

et al. 2013

Desalination and Water Treatment

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A commonly used remineralization process involves bringing CO 2 -acidified desalinated water in contact with a bed of limestone. Dissolution of limestone provides two essential ingredients to the water: bicarbonate alkalinity and calcium content. The kinetics of limestone dissolution with CO 2 was studied as a function of inlet CO 2 concentration, water flow velocity, and temperature. The experimental data conformed very well to the Yamauchi model. Optimal design of a hardening column is discussed.

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Section: Introductionmentioning

confidence: 99%

Remineralization of desalinated water by limestone dissolution with carbon dioxide

Shemer

Hasson

Semiat

et al. 2013

Desalination and Water Treatment

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“…638 without any chemical addition for SO 4 2À scaling in concentrate stream with SO 4 2À 3,000 mg/L [9]. If amount of Ca 2þ and HCO 3 À in the concentrated water is equal and/ or more than 279 and 570 mg/L in mono valent ionselective ACS, CMX-S membrane from Tokuyama Co., with 20 min polar reversing, the scaling inhibitor (e.g., HCl) is required to add in the concentrated stream to avoid precipitation of CaCO 3 in water and scaling in membrane [12]. In case of Prairie, Canada, a scale inhibitor (Flocon 100) 10 mg/L was injected into concentrate stream to prevent CaSO 4 and CaCO 3 scaling in membranes from Ca 2þ 550 mg/L, SO 4 2À 3,333 mg/L, and HCO 3 À 1,382 mg/L in concentrate stream in Ionics aquamite V with reversal every 20 min [18].…”

Section: Literature Review In Preventing Caso 4 Scaling With and Withmentioning

confidence: 99%

“…1. Non-charged particles such as silica (SiO 2 ) [11], silicon (Si), bacteria, and organic contaminants are not removed by EDR [12,5,3]. Boron is also not removed by EDR [13].…”

Section: Literature Review In Pretreatmentmentioning

confidence: 99%

“…The pH in the concentrated stream is used as an indicator to monitor and avoid scaling problems [5]. The rise, in silica-SiO 2 [12] and silicon-Si [19] in dilution stream after the EDR treatment in Table 1, is due to the mass balance of silica in EDR feed and EDR dilute stream with water amount loss in dilution into concentrated stream.…”

Section: Literature Review In Pretreatmentmentioning

confidence: 99%

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Design of ILEDR for brackish groundwater: A literature review approach

Myint¹,

Ghassemi²,

Nirmalakhandan³

2010

Desalination and Water Treatment

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A literature review was done in details in desalination by using electrodialysis reversal (EDR). All available data -source of water entered into pretreatment and/or directly into EDR, physicochemical characteristics of water, targeted pollutants, methods and the reasons for the pretreatments, specifications used of EDRs, developments/improvements in EDR, fouling causing compounds and methods to control fouling, membrane types, membrane assembly, spacer, and concentrate management, method, and recovering of ions were searched and summarized in Tables 1-3. From the tables, the concentrations profiles of the targeted pollutants were observed in different sub-processes (i.e., pretreatment, ERD dilute and concentrate streams). The percentage removals of individual ion from different literatures were compared. The concentrations of fouling causing compounds (for examples, CaSO 4 and MgSO 4 ) in concentrated streams were eliminated by individual separation process with the specific different types of permselective membranes in four different stages. All these summarized data were used as tools, references, and comparisons to design and select the sub-processes in ILEDR project to treat the brackish groundwater into the drinking water. Design includes designs I (using a single type of membrane pair) and II (using four different types of mono-and di-valent permselective membrane). Permselective membrane design shows 7% cost saving while comparing to the single type of membrane design with the same water recovery rate, the same demineralization rate, and the same membrane life. The saving increases up to 15-18% if membrane life is considered in the design.self-cleaning by reversal the chemical reactions, electricity driving force, and the flows. The effectiveness of current-reversal process of EDR are shattering and detaching polarization films four times/hour to prevent polarization scale; contravention up freshly precipitated scale or seeds of scale and flushing them back into waste stream before they can cause scratch to membrane; reducing slime formations on membrane surface; reducing problems associated with the use of chemicals; cleaning electrodes with acid automatically during alternative anodic operation [4] in reversal. There is a period (1-2 min [4]) instantaneously following the polarity reversal, the waters from both dilute and concentrate are required to send back to the feed stream or diverted to waste because these waters are ''off specification''.EDR efficiency depends on method to prevent membrane from fouling; ion's charge and mobility, solution conductivity, relative concentrations, applied voltage, and the characteristics of the ion-exchange membranes, especially its permselectivity [5]; system design [6,1]; materials used in membrane [7].EDR is not cost effective at plant capacity lower the 40 m 3 /h while comparing with R.O; Elyanow and Persechino recommended that high recovery (94%), elevated SDI (6-12), potential for biofouling, hard-totreat, high hardness, lower salinity waters (from 200 to 5,000...

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“…Melián-Martel et al reported that the chemical constituent causing RO membrane fouling [58] and the cleaning of RO membrane would generate large amounts of acidic wastewater [59]. To overcome this problem, the use of the electro-dialysis reversal (EDR) procedure was initiated and promoted since it could reverse the electrode polarity automatically, and thus had the capacity to backwash the membrane and inhibit membrane fouling [59][60][61][62]. Other methods that are still undergoing research and development include forward osmosis (FO), membrane distillation (MD), capacitance deionization (CDI), gas hydrates (GH), humidification-dehumidification (HDH), and solar stills desalination.…”

Section: Seawater Desalination and Environmental Problems Caused By Bmentioning

confidence: 99%

Landscape Changes and a Salt Production Sustainable Approach in the State of Salt Pan Area Decreasing on the Coast of Tianjin, China

Wang

Zhu

2015

Sustainability

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Landsat images from 1979, 1988, 1999, 2008, and 2013 were used to analyze the landscape area change of salt pans lying on the coast of Tianjin. While initially (1979)(1980)(1981)(1982)(1983)(1984)(1985)(1986)(1987)(1988), the area of Tianjin's salt pan increased, later it declined dramatically. In the first phase (1979)(1980)(1981)(1982)(1983)(1984)(1985)(1986)(1987)(1988) of the studied period the primary roll-in landscape of the salt pan wasbarren land with an area of 60.0 km 2 . By 1988, the area of Tianjin's salt pan rose to 457.8 km 2 . The main roll-out landscape of the salt pan during 1988-2013 was urban, barren land, village/town, harbor, and road whose area amounted to 69.8, 35.9, 27.3, 25.5 and 18.4 km 2 respectively. The roll-out barren land will be transformed to construction land ultimately. By 2013, the total loss reached 167.3 km 2 , which was 36.5% of the salt pan area of Tianjin in 1988. With the development of coastal economy, the salterns with a lower economic value were transformed to and replaced by land use types with a higher economic value. This trend would influence the production of sea salt and the development of sodium hydroxide and sodium carbonate industries. Seawater desalination provides an opportunity for the restoration and compensation of salt production capacity. Based on the theory of circular economy and industrial symbiosis, in this article an industrial symbiosis model for sea salt production and sea water desalination is explored: "mariculture-power plant cooling-seawater desalination-Artemia culture-bromide extraction-sea salt production-salt chemical industry". OPEN ACCESSSustainability 2015, 7 10079Through the application of this process sustainable development of the sea salt production in Tianjin could be achieved.

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Limestone selection criteria for EDR water remineralization

Cited by 16 publications

References 12 publications

Remineralization of desalinated water by limestone dissolution with carbon dioxide

Remineralization of desalinated water by limestone dissolution with carbon dioxide

Design of ILEDR for brackish groundwater: A literature review approach

Landscape Changes and a Salt Production Sustainable Approach in the State of Salt Pan Area Decreasing on the Coast of Tianjin, China

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