Electrochemical water treatment devices are disclosed. The device includes an electrochemical separation module fluidly connectable to the source of water to be treated. The electrochemical separation module includes a first electrode, a second electrode, and a plurality of dilution compartments. Each of the dilution compartments includes a first region of ion exchange media having a first average particle size, a second region of ion exchange media having a second average particle size, and a third region of ion exchange media having a third average particle size. A volume of the second region of ion exchange media being greater than or equal to a total volume of the first and third regions of ion exchange media. Methods of facilitating treatment of water containing weakly ionized species, e.g., dissolved boron containing species and dissolved silica containing species, are disclosed. Electrochemical separation modules are also disclosed.

The article includes a porous scaffold structure comprising a plurality of supports. The article further includes a plurality of metallic or non-metallic nanomaterials disposed on at least one of the supports. Each of the plurality of metallic or non-metallic nanomaterials is directly bound to at least one of the supports.

This disclosure concerns a system for purifying contaminated water and a method for using the system. More specifically, the invention concerns removing contaminants, such as those introduced by fracking, from a contaminated water.

Produced water from a crude oil or natural gas production process is purified using a membrane purification system for petroleum production, agricultural, commercial and domestic uses. The produced water is pretreated to remove, at least, particulates and oil from the produced water. The minimally pretreated water is then purified in a membrane purification system, that is operated at conditions such that membrane scaling is reduced or prevented. In particular, the membrane purification system is operated to maintain the turbidity of clarified water feed to the system or intermediate aqueous streams that are cascading through the membrane purification system. Ensuring that the turbidity of the reject streams generated in the membrane system are useful in achieving long membrane operating life.

An electrodeionization device (EDI device) with improved performance for removing weak acid components such as boron includes a deionization chamber partitioned by a pair of ion exchange membranes between an anode and a cathode. A grain size of 0.1 mm or more and 0.4 mm or less is defined as small grain size, and a grain size of more than 0.4 mm is defined as large grain size. In the deionization chamber, a large grain size layer made of an ion exchange resin of large grain size and a mixed grain size layer in which an ion exchange resin of large grain size and an ion exchange resin of small grain size are mixed are arranged along a flow of water to be treated.

A water remediation and treatment device that includes a process channel having fluid inlet and a fluid outlet; at least one tube unit in fluid communication with the process channel, the tube unit defining an interior chamber defining an interior fluid flow path, at least one anode and at least one cathode contained in the interior chamber and positioned in the interior fluid flow path; and at least one device configured to remove material accumulated on the surface of the cathode and/or the electrode during water treatment.

Water treatment systems including electrically-driven and pressure-driven separation apparatus configured to produce a first treated water suitable for use as irrigation water and a second treated water suitable for use as potable water from one of brackish water and saline water and methods of operation of same.

A method of boron-contained wastewater treatment includes the following steps. Pretreatment: Mix a boron-contained wastewater with hydrogen peroxide for reaction at pH 8-12. Precipitation: Add n moles of barium compound into the pretreated boron-contained wastewater to provide perborate precipitation at pH 8.5-12. The number n is obtained from an equation of n=([B]*a+[NO.sub.3]*0.01+[F]*0.01+[CO.sub.3]*1+[SO.sub.4]*1)*V wherein a is ranged from 0.6-0.9. [B], [NO.sub.3], [F], [CO.sub.3], and [SO.sub.4] are molarities of boron, nitrate ion, fluoride ion, carbonate ion, and sulfate ion of the boron-container wastewater. V is the volume of the boron-container wastewater. A fluidized bed reactor is used.

A concurrent desalination and boron removal (CDBR) process and a system thereof are provided. The system includes: a plurality of single-stage reverse osmosis (SSRO) stages connected in series, and a countercurrent membrane cascade with recycle (CMCR). The process includes the following steps: introducing a retentate from one SSRO stage or a series of SSRO stages optimally as a feed to a CMCR; countercurrent a retentate flow and a permeate flow in the CMCR; permeate recycling to a retentate side in the CMCR; retentate self-recycling in at least one of membrane stages in the CMCR; introducing a permeate from the SSRO stage(s) as a feed to an LPMS; and blending permeate streams from the CMCR and LPMS to achieve concentrations in a water product.

A purification method for an aqueous hydrogen peroxide solution includes subjecting the aqueous hydrogen peroxide solution to a reverse osmosis membrane separation treatment with a high-pressure reverse osmosis membrane separation device. The high-pressure reverse osmosis membrane has a denser skin layer on the membrane surface and is therefore lower in an amount of membrane permeate water per unit operating pressure but higher in the rejection rate of TOC and boron, as compared with a low-pressure or ultralow-pressure reverse osmosis membrane. The high-pressure reverse osmosis membrane permeate water is preferably further subjected to an ion exchange treatment with an ion exchange device including two or more columns packed with gel-type strong ion exchange resins.