A high gravity non-alcoholic beverage is disclosed having an ABV between about 0.1% to about 0.8% or between about 3% to about 6%, a real extract by weight between about 15% to about 70%, and an ethyl acetate amount between about 1 to about 500 mg/l. A method for producing the high gravity non-alcoholic beverage from a starting liquid includes providing a set of reverse osmosis pressure vessels, each pressure vessel having a feed inlet, a retentate outlet, and a permeate outlet, the set having a first pressure vessel, providing the starting liquid to the feed inlet of the first pressure vessel, adding water at a blend point when ABV content in a selected one of the permeate streams exceeds ABV content of a retentate stream at the blend point, and obtaining the high gravity non-alcoholic beverage from a selected one of the retentate streams.

An apparatus for producing ultrapure water: first ultrafiltration membrane that is connected to point of use and that supplies ultrapure water to point of use; first concentrated water return line that returns concentrated water of first ultrafiltration membrane to an upstream side of first ultrafiltration membrane; pressure gauge that measures pressure at an outlet of first ultrafiltration membrane; and means for adjusting flow rate of the concentrated water (first valve). Means for adjusting the flow rate of the concentrated water can be operated such that when the flow rate of the concentrated water is changed, a change in the pressure at the outlet of first ultrafiltration membrane that is measured by pressure gauge is kept within a predetermined range.

A method for preparing a filtered beverage includes filtering a raw beverage using a cross-flow ultrafiltration device to produce a solids fraction and a liquid fraction; heating the solids fraction to a temperature of 60° C. or greater to produce a pasteurized solids fraction; microfiltering the liquid fraction through a microfilter having a size cut-off of 1 μm or smaller to produce a microfiltered liquid fraction; and combining the pasteurized solids fraction and the microfiltered liquid fraction to result in the filtered beverage.

Liquid solution concentration methods and related systems involving osmosis units and energy recovery are generally described. In some embodiments, an osmotic system has a pump, a first reverse osmosis unit, a second reverse osmosis unit, and one or more energy recovery devices. Various embodiments are directed to features such as balancing streams, recirculation streams, and/or valving that alone or in combination may afford improved energy efficiency and/or system performance. Some embodiments may improve performance of certain types of energy recovery devices in combination with osmosis units, such as isobaric or turbine energy recovery devices.

An induced symbiotic osmosis system and method for treating produced fluids from a hydraulic fracturing process or system for symbiotic fluids fractionation, salinity power generation, brines and salts solution reverse osmosis. The system includes a reverse osmosis membrane assembly to create potable water from produced water. The membrane assembly includes a hollow fiber or flat sheet membrane and headers to transfer desalinated water therefrom. The system can include an electro coagulation system, an ultra or nano filtration system, and a desalter to treat the produced water or brine. A heat exchanger can be positioned between adjacent reverse osmosis membrane assemblies. An osmotic power generation unit can create electrical power by receiving and utilizing produce water and brine water from a brine storage. The system reduces the release of global warming contributing gases associated with hydraulic fracturing, while producing potable water and power.

Algae harvesting and cultivating systems and methods for producing high concentrations of algae product with minimal energy. In an embodiment, a dead-end filtration system and method includes at least one tank and a plurality hollow fiber membranes positioned in the at least one tank. An algae medium is pulled through the hollow fiber membranes such that a retentate and a permeate are produced.

A nutrient concentration and water recovery system includes a first suspended solids settling tank configured to receive a flow stream that includes a waste stream with a sludge stream. A first centrifugal pump is coupled to the first suspended solids settling tank. The first centrifugal pump having corrosion resistant wetted parts and variable speed drives to transfer or pressurize process flow streams. A first level transmitter coupled to the first centrifugal pump that provides output signals in response to a level of a process material within the first suspended solids settling tank. The first level transmitter is mounted in the first suspended solids settling tank. A first flow transmitter coupled to the first level transmitter is configured to measure a specific volume of material transferred out of the first suspended solids settling tank. A first pump is coupled to the first flow meter and configured to transfer a flush water that includes suspended solids and inorganics. A vibrating screen is coupled to the first pump. A process tank is coupled to the submersible pump. A sedimentation removal system and a removal device coupled to the sedimentation removal system are provided and configured to remove inorganizes out of a suspension.

A biologics manufacturing process that connects the drug substance and drug product processes into an integrated, continuous process.

Algae harvesting and cultivating systems and methods for producing high concentrations of algae product with minimal energy. In an embodiment, a dead-end filtration system and method includes at least one tank and a plurality hollow fiber membranes positioned in the at least one tank. An algae medium is pulled through the hollow fiber membranes such that a retentate and a permeate are produced.

Selective removal of non-aromatic hydrocarbons from a xylene isomerization process for para-xylene production is accomplished using a membrane unit positioned within a xylene recovery loop. The membrane unit may include a one-stage or multi-stage (e.g., two-stage) membrane system and may be configured to separate a membrane unit product stream from a non-aromatics rich stream, which can be removed from the xylene recovery loop. The membrane unit may have a xylene permeance of about 60 gm/m2/hr/psi and a xylene to non-aromatic permeance ratio of about 15.