A fluid purification system has cells whose purifying capability can be regenerated. Some of the cells are arranged in series to reach a high level of purification. An automatic valve network is controlled to cycle the cells in a way that levels the loads on each, thereby maximizing the service interval for replacing expired cells, enabling all of the cells to be replaced at the same time after having each contributing approximately equally to the purification load, and operated such that at any one time, at least one cell is regenerated so as to enable continuous up-time.

A fluid purification system has cells whose purifying capability can be regenerated. Some of the cells are arranged in series to reach a high level of purification. An automatic valve network is controlled to cycle the cells in a way that levels the loads on each, thereby maximizing the service interval for replacing expired cells, enabling all of the cells to be replaced at the same time after having each contributing approximately equally to the purification load, and operated such that at any one time, at least one cell is regenerated so as to enable continuous up-time.

The present invention provides a process for recovering glycol from a process stream comprising glycol, water, dissolved salts, and hydrocarbons. The process comprises subjecting the process stream to a salt-enrichment process to obtain a salt-enriched stream having a salt concentration higher than salt concentration of the process stream, and a salt-reduced stream; subjecting the salt-enriched stream to a glycol reclaiming process to separate the salts and at least a portion of the hydrocarbons from the salt enriched stream to obtain a substantially salt-free water-glycol stream; and blending the salt reduced stream from the salt-enrichment process with the substantially salt-free stream to produce a reclaimed water-glycol stream.

A capacitive deionization filter includes a cation exchange membrane, a spacer positioned below the cation exchange membrane, an anion exchange membrane positioned below the spacer, and an electrode disposed above the cation exchange membrane or below the anion exchange membrane. An edge of the cation exchange membrane and an edge of the anion exchange membrane may be joined by a plurality of joints formed at a certain interval.

There is provided a water treatment apparatus. The apparatus comprises a capacitive deionisation apparatus. The apparatus further comprises a water condition element. The water conditioning element comprises a metal alloy configured such that mineral ions within a flow of water, flowing over a surface of the water conditioning element, precipitate to provide a colloidal dispersion.

A mobile dialysis fluid generation system includes a cargo unit configured to be transported by a vehicle; a cleanroom located inside the cargo unit; water purification equipment; at least one dialysis fluid preparation unit located inside the cleanroom; and at least one area provided outside the cleanroom but inside the cargo unit for storing at least one of a raw material or containers filled with dialysis fluid. The at least one dialysis fluid preparation unit includes at least one concentrate, a mixing device configured to receive purified water from the water purification equipment and to mix the purified water with the at least one concentrate to form dialysis fluid, and a tubing set for transfer of the dialysis fluid from the mixing device to a container positioned and arranged to receive the dialysis fluid.

Disclosed are an anion-exchange membrane and a manufacturing method therefor. The anion-exchange membrane may include: a porous polymer support composed of a membrane structure; and an anion-exchange polymer, wherein the anion-exchange polymer may be present on a surface and in pores of the porous polymer support, anion-exchange groups of the anion-exchange polymer may be uniformly distributed on the surface and in the pores of the porous polymer support, and the anion-exchange polymer may be a crosslinked product of a composition including a crosslinkable monomer represented by Formula 1:

##STR00001## wherein X.sup. is as disclosed in the specification.

The present disclosure describes a flow-electrode capacitive deionization (FCDI) desalination system and method of use. An FCDI desalination system is described employing one or more FCDI cells equipped with two coaxially oriented membranes mounted within a column housing capped with two end caps, each end cap comprising two carbon slurry ports and one water port. The column is lined with a chargeable sleeve capable of receiving a positive or negative charge. The annular space between the chargeable sleeve and the outside surface of the outer concentric membrane creates a flow path for a first carbon slurry to pass therethrough. The space between the inside surface of the outer concentric membrane and the outer surface of the inner concentric membrane creates a flow path for the saline water to be treated. The space within the inner annular portion of the inner concentric membrane creates a flow path for a second carbon slurry and contains a chargeable rod or wire capable of receiving an opposite charge. The first and second opposed end caps on the column are outfitted to continue these independent flow paths. As the saline water travels through its flow path, its salt ions are removed through the coaxial membranes via the two carbon slurries.

The invention relates to a method for removing ions from an aqueous fluid in an electrochemical cell, including directing an aqueous fluid through the electrochemical cell, thereby allowing contact between said aqueous fluid and a first electrode and second electrode; applying a current to the electrochemical cell, thereby forming a deionized aqueous fluid in the electrochemical cell; collecting the deionized aqueous fluid from the electrochemical cell; reverting the current, thereby at least partly regenerating said first electrode and said second electrode, and forming an aqueous fluid enriched in ions into the electrochemical cell; wherein the voltage in the electrochemical cell, is between 1.23 V and 1.23 V and wherein the ratio between the electric current divided by the total weight of the first electrode and the second electrode and the conductivity of the aqueous fluid, when entering the electrochemical cell, is at least 1 to 25 mA.Math.cm/S.Math.g.