An apparatus and process for separating a gas mixture is disclosed. The apparatus includes a first membrane stage, a second membrane stage, and a third membrane stage. The first membrane stage includes a first gas separation membrane configured to separate the gas mixture into a first retentate stream and a first permeate stream. The second membrane stage includes a second gas separation membrane configured to separate the first permeate stream into a second retentate stream and a second permeate stream. The second retentate stream of the second membrane stage is recycled back to connect with the first retentate stream to form a mixed fluid stream. The third membrane stage includes a third gas separation membrane configured to separate the mixed fluid stream into a third retentate stream and a third permeate stream, and the third retentate stream is configured to be withdrawn as a product or discarded.

A method and system is provided for treating waste generated from manufacturing operations including at least one of Printed Circuit Boards Fabrication (PCB FAB), General Metal Finishing (GMF), semiconductors manufacturing, chemical milling, and Physical Vapour Deposition (PVD). The method and system are used to create zero liquid discharge recycling.

Systems and methods for filtering materials from biologic fluids are discussed. Embodiments may be used to filter cerebrospinal fluid (CSF) from a human or animal subject. In an example, CSF is separated into a permeate and retentate using a tangential flow filter. The retentate is filtered again and then returned to the subject with the permeate. During operation of the system, various parameters may be modified, such as flow rate and waste rate.

Systems and methods for filtering materials from biologic fluids are discussed. Embodiments may be used to filter cerebrospinal fluid (CSF) from a human or animal subject. In an example, CSF is separated into a permeate and retentate using a tangential flow filter. The retentate is filtered again and then returned to the subject with the permeate. During operation of the system, various parameters may be modified, such as flow rate and waste rate.

A system for processing leachate is provided. The system has an ultrafiltration unit that receives the leachate and produces both an ultrafiltration permeate and an ultrafiltration reject. The system recovers the ultrafiltration reject and recirculates it through the ultrafiltration unit to produce a combined ultrafiltration permeate. The system also has a nanofiltration unit that receives the combined ultrafiltration permeate and produces both a nanofiltration permeate and a nanofiltration reject. The system also has a carbon filtration system that receives the nanofiltration reject and produces a carbon filtration permeate. The system also has a system output that receives the nanofiltration permeate and the carbon filtration permeate and produces a mixture of both permeates as an output mixture.

Zero liquid discharge systems, processes, and techniques for treating a saltwater without evaporative crystallization. The saltwater is treated by a fluidic circuit comprising a high-pressure reverse osmosis (“HPRO”) unit configured to operate at a hydraulic pressure of at least 1,500 psi, a cooling crystallizer, and a solids-liquid separator. The saltwater is first concentrated by the HPRO unit to produce an HPRO brine, which is subsequently cooled to a designated crystallization temperature by the cooling crystallizer. The cooling crystallizer crystallizes salt crystals from the cooled HPRO brine and produces a salt-diminished brine. The solids-liquid separator separates the salt-diminished brine from the salt crystals. The salt-diminished brine from the solids-liquid separator is returned to the HPRO unit for further treatment, which allows additional salts to be crystallized from the returned salt-diminished brine.

Zero liquid discharge systems, processes, and techniques for treating a saltwater without evaporative crystallization. The saltwater is treated by a fluidic circuit comprising a high-pressure reverse osmosis (“HPRO”) unit configured to operate at a hydraulic pressure of at least 1,500 psi, a cooling crystallizer, and a solids-liquid separator. The saltwater is first concentrated by the HPRO unit to produce an HPRO brine, which is subsequently cooled to a designated crystallization temperature by the cooling crystallizer. The cooling crystallizer crystallizes salt crystals from the cooled HPRO brine and produces a salt-diminished brine. The solids-liquid separator separates the salt-diminished brine from the salt crystals. The salt-diminished brine from the solids-liquid separator is returned to the HPRO unit for further treatment, which allows additional salts to be crystallized from the returned salt-diminished brine.

The present disclosure provides systems and methods that can treat feeds with elevated organic levels, e.g., feeds with ≥300 Pascals (Pa) organic osmotic pressure, with one or more enhanced filter membrane modules, which may be referred to herein as membrane modules or simply modules. Preferably, a filter membrane module consistent with the present disclosure include one or more plate and frame modules, one or more spiral format modules, or a combination of plate a frame and spiral format modules. The systems and methods provided herein can provide reliable performance when used to treat feeds with elevated organic levels.

Liquid solution concentration systems, and related methods, are generally described. In some embodiments, the system is an osmotic system comprising a plurality of osmotic modules. For example, the osmotic system can comprise a feed osmotic module configured to produce an osmotic module retentate outlet stream having a higher concentration of solute than the retentate inlet stream transported to the feed osmotic module. The osmotic system can also comprise an isolation osmotic module fluidically connected to the feed osmotic module. The osmotic system can also optionally comprise a purification osmotic module fluidically connected to the feed osmotic module and/or the isolation osmotic module. Certain embodiments are related to altering the degree to which the feed osmotic module retentate outlet stream is recycled back to the retentate-side inlet of the feed osmotic module during operation. Additional embodiments are related to the manner in which the retentate-side effluent from the isolation osmotic module is distributed among the system modules during operation.

Water deionization systems based on electrochemical water desalination or softening using a capacitive or intercalative deionization devices including a stack of electrochemical cells. Each cell includes first and second electrodes and an ion exchange membrane. Each cell includes inlet and outlet channels with control valves that control the separation of the source water into brine (e.g., concentration) and clean water (e.g., purification) streams. The deionization device or module may include multiple electrochemical cells connected electrically in series, parallel or a combination of both. The cells may also be in serial, parallel, or combined fluid communication. The output water of one or more streams from each cell or collection of cells may be recirculated and combined with one or more input water streams to improve the electrochemical energy efficiency of the cells. The electrochemical cells at different rows may have varying electrode thickness, area and loading of the active material.