Methods for producing a food product that involve use of a cross-flow filtration module are disclosed. The cross-flow filtration module may be used to recycle wastewater effluent and/or to recover antioxidant compounds from the wastewater effluent. In some embodiments, the cross-flow filtration module includes a stainless steel or nickel alloy substrate.

There is described a method of use of a mass exchanger. In the method the mass exchanger comprises: a first channel for accommodating flow of a liquid to be treated; and a second channel for accommodating flow of a treatment agent, the first and second channels have a permeable membrane provided between them, so as to allow transfer of selected species between the first channel and the second channel. The steps of the mass transfer method comprise passing the liquid to be treated along the first channel and introducing a mixture of liquid and gas into the second channel to provide a two-phase treatment agent. It is desirable to provide a means of adjusting the concentration of gas species in a liquid such as blood, while simultaneously controlling the temperature of the liquid and optionally adjusting the concentration of ionic and/or dissolved species in that liquid. By this method and mass exchanger providing a two-phase treatment agent, it is possible to simultaneously deliver gaseous species (e.g. oxygen) into the treated liquid, while making use of the high heat capacity of the liquid phase of the treatment agent to transfer significant heat into or from the treated liquid.

A polyolefin microporous membrane has excellent strength, permeability and heat resistance, which is obtained by using UHMwPE and employing a sequential stretching system, and a production method of the microporous membrane. In producing a microporous membrane by using a primary material A having a molecular weight (Mw) of less than 1.010.sup.6, a secondary material B having a molecular weight of 1.010.sup.6 or more, and a plasticizer, when the endothermic quantity of a mixture of the primary material and the plasticizer and the endothermic quantity of a mixture of the secondary material and the plasticizer are denoted as Q1 and Q2, respectively, respective resins are designed such that the ratio of endothermic quantity Q2 to endothermic quantity Q1 (endothermic quantity Q2/endothermic quantity Q1) becomes 1 or more over a temperature range of 110 to 118 C.

Disclosed herein is a solar thermal osmosis desalination system comprising a forward osmosis subsystem and a reverse osmosis subsystem where the forward osmosis subsystem is configured to receive solar thermal heat and generate power that can be used to operate the reverse osmosis subsystem.

A distillation apparatus having a hot liquid block, a thermoelectric module (TEM), a condensation surface, a feed liquid chamber having a feed chamber inlet, a feed chamber outlet, and a membrane disposed on at least one side of the feed liquid chamber. One side of the membrane faces to the condensation surface. An air gap of 1 mm to 20 cm separates the condensation surface and the membrane. A permeate outlet in fluid communication with the air gap. A heating unit in fluid communication with the feed liquid chamber and the hot liquid block. A cooling unit in fluid communication with the permeate outlet. A multi-stage distillation apparatus with a plurality of distillation apparatuses. A process of distilling water, by feeding a liquid into the distillation apparatus through the hot block inlet and collecting distilled water from the permeate outlet.

A method for controlling a membrane distillation system includes determining whether there is a day time or a night time at a location of a solar collector system associated with the membrane distillation system; applying a first control mode during the day time to a flow velocity of a feed used by the membrane distillation system; and applying a second control mode, different from the first control scheme, during the night time, to the feed. The first control scheme is a model-free mode.

Per- and polyfluoroalkyl substances (PFAS) are destroyed by oxidation in supercritical conditions. PFAS in water is concentrated in a reverse osmosis step and salt from the resulting solution is removed in supercritical conditions prior to destruction of PFAS in supercritical conditions.

A new apparatus, system and method to purified produced water and removed valuable metals and minerals is described. The apparatus comprises a device for flowing produced water wellbore from a wellbore to the produced water purification apparatus; at least one device to remove heavy metals from the produced water; at least one brine removal device to remove brine from the produced water. The method comprises steps to use the apparatus and the system comprises a control panel that operates the at least one device for removing heavy metals and at least one sensor in a coordinated manner.

A process for the recovery of sodium sulfate from water, in particular from water deriving from a silica manufacturing process.

A system for treating high temperature produced water includes an electrocoagulation unit, a membrane distillation unit in communication with the outlet of the electrocoagulation unit having a hydrophobic membrane with a feed side for receiving the produced water stream and a product side for receiving a deionized water stream. A heat recovery heat exchanger is in communication with the membrane distillation unit for receiving two streams, one from each side of the hydrophobic membrane, such that heat is exchanged between the two streams. A line leaving the heat exchanger returns a heated stream from the heat exchanger to a location in a line upstream of the membrane distillation unit. A brine tank in communication with the membrane distillation unit receives a portion of a stream from the membrane product side and contains a concentrated brine solution containing the portion of the stream from the membrane product side and sodium chloride.