Various embodiments include an exemplary design of an apparatus and related process to reduce or eliminate de-gassing from a liquid precursor during dispensing of the liquid precursor under vacuum. In one embodiment, the apparatus includes a liquid-flow controller configured to be coupled to a liquid-supply vessel containing the liquid precursor, and at least one valve hydraulically coupled downstream of and to the liquid-flow controller by a liquid line. The at least one valve is to be opened and closed to maintain a minimum pressure that is sufficiently high enough to reduce or prevent degassing of the liquid precursor throughout the liquid line. An atomizer is hydraulically coupled downstream of and to the at least one valve. The atomizer can produce droplets of the liquid precursor and is further to be coupled on a downstream side to a vacuum source. Other methods and apparatuses are disclosed.

The present application pertains to methods for making metal oxides and/or citric acid. In one embodiment, the application pertains to a process for producing calcium oxide, magnesium oxide, or both from a material comprising calcium and magnesium. The process may include reacting a material comprising calcium carbonate and magnesium carbonate. Separating, concentrating, and calcining may lead to the production of oxides such as calcium oxide or magnesium oxide. In other embodiments the application pertains to methods for producing an alkaline-earth oxide and a carboxylic acid from an alkaline earth cation-carboxylic acid anion salt. Such processes may include, for example, reacting an alkaline-earth cation-carboxylic acid anion salt with aqueous sulfur dioxide to produce aqueous alkaline-earth-bisulfite and aqueous carboxylic acid solution. Other useful steps may include desorbing, separating, and/or calcining.

A wastewater evaporation system includes a plurality of tube sections configured to direct compressed air into the wastewater. A portion of the manifold defines an injection head configured to be at least partially submerged below a surface of the wastewater. The wastewater evaporation system also includes an air compressor configured to direct the compressed air to the manifold. The wastewater evaporation system also includes a buoy system coupled to the manifold. The buoy system includes a buoy configured to maintain a portion of the manifold above the surface of the wastewater.

A wastewater evaporation system includes a plurality of tube sections configured to direct compressed air into the wastewater. A portion of the manifold defines an injection head configured to be at least partially submerged below a surface of the wastewater. The wastewater evaporation system also includes an air compressor configured to direct the compressed air to the manifold. The wastewater evaporation system also includes a buoy system coupled to the manifold. The buoy system includes a buoy configured to maintain a portion of the manifold above the surface of the wastewater.

A waste water processing system includes an upflow contacting column having a flue gas input for receiving flue gas having a temperature of at least 500 degrees F., a waste water input, and a flue gas output. The waste water input is coupled to a fluid injector, e.g., atomizing nozzles, positioned in the throat of a Venturi portion of the upflow contacting column or in a sidewall of the throat of the Venturi portion of the upflow contacting column. The flue gas in the upflow contacting column has a high velocity, e.g., a gas velocity exceeding 65 fps in the throat of the Venturi portion of the upflow contacting column at a position where the fluid injector is located. Drying additives such as recycled ash, lime, and/or cement may be, and sometimes are, input into the upflow contacting column downstream of the waste water input.

A waste water processing system includes an upflow contacting column having a flue gas input for receiving flue gas having a temperature of at least 500 degrees F., a waste water input, and a flue gas output. The waste water input is coupled to a fluid injector, e.g., atomizing nozzles, positioned in the throat of a Venturi portion of the upflow contacting column or in a sidewall of the throat of the Venturi portion of the upflow contacting column. The flue gas in the upflow contacting column has a high velocity, e.g., a gas velocity exceeding 65 fps in the throat of the Venturi portion of the upflow contacting column at a position where the fluid injector is located. Drying additives such as recycled ash, lime, and/or cement may be, and sometimes are, input into the upflow contacting column downstream of the waste water input.

A heat transfer process focused for heat transfer with a potentially scaling, fouling, solids laden or otherwise aggressive fluid employing direct thermal contact between said fluid and an immiscible, phase shifting working media wherein said phase shifting proffers the employ of the latent heat of vaporization for protraction of the heat transfer process. Wherein further said phase shifts modify the working media density therein motivating the immiscible, direct contact fluid dynamics.

A heat transfer process focused for heat transfer with a potentially scaling, fouling, solids laden or otherwise aggressive fluid employing direct thermal contact between said fluid and an immiscible, phase shifting working media wherein said phase shifting proffers the employ of the latent heat of vaporization for protraction of the heat transfer process. Wherein further said phase shifts modify the working media density therein motivating the immiscible, direct contact fluid dynamics.

A feed liquid flows into a second-stage humidifier chamber to form a second-stage humidifier bath. A first remnant of the feed liquid from the second-stage humidifier chamber then flows into a first-stage humidifier chamber to form a first-stage humidifier bath having a temperature lower than that of the second-stage bath. A second remnant of the feed liquid is then removed from the first-stage humidifier. Meanwhile, a carrier gas is injected into and bubbled through the first-stage humidifier bath, collecting a vaporizable component in vapor form from the first remnant of the feed liquid to partially humidify the carrier gas. The partially humidified carrier gas is then bubbled through the second-stage humidifier bath, where the carrier gas collects more of the vaporizable component in vapor form from the feed liquid to further humidify the carrier gas before the humidified carrier gas is removed from the second-stage humidifier chamber.

A feed liquid flows into a second-stage humidifier chamber to form a second-stage humidifier bath. A first remnant of the feed liquid from the second-stage humidifier chamber then flows into a first-stage humidifier chamber to form a first-stage humidifier bath having a temperature lower than that of the second-stage bath. A second remnant of the feed liquid is then removed from the first-stage humidifier. Meanwhile, a carrier gas is injected into and bubbled through the first-stage humidifier bath, collecting a vaporizable component in vapor form from the first remnant of the feed liquid to partially humidify the carrier gas. The partially humidified carrier gas is then bubbled through the second-stage humidifier bath, where the carrier gas collects more of the vaporizable component in vapor form from the feed liquid to further humidify the carrier gas before the humidified carrier gas is removed from the second-stage humidifier chamber.