A vapor separation system including a cooler having an inlet configured to receive an air-oil-water mixture, and an outlet configured to discharge separated oil and water in two different phases of matter. A first sensor is at the outlet of the cooler. A controller is communicatively coupled to the cooler, wherein the controller is configured to receive temperature feedback from the first sensor, and increase or reduce the amount of cooling, with the cooler and based on the temperature feedback, the oil-water mixture to a separation temperature configured to liquefy at least a portion of the oil in the air-oil-water mixture, while maintaining at least a portion of the water in the air-oil-water mixture in a vaporized state.

The present invention is a aroma recovery equipment from gases exhausted of fermentation vats comprising a first recovery group (100) comprising a first condenser (110) operating at a first temperature of recovered aromas; one second recovery group (200) comprising a second condenser (210) operating at a second temperature of recovered aromas; a cooling group (300) to provide cold by a cooling fluid (301) to said first recovery group (100) via a first fluid connection (302) and to said second recovery group (200) via a second fluid connection (303); control means (400) configured to coordinately control the temperature of said first recovery group (100) and the temperature of said second recovery group (200); and a mobile housing (500) containing said first recovery group (100), said second recovery group (200), said cooling group (300) and said control means (400).

A flue gas condensation water extraction system includes a flue gas condensation-end system and a flue gas refrigeration source-end system. The flue gas condensation-end system includes a desulfurization absorption tower, a flue gas purification and condensation tower, and a condensed water storage tank. The flue gas purification and condensation tower is arranged above the desulfurization absorption tower. A flue gas outlet, a water inlet, and a water outlet are provided on the flue gas purification and condensation tower. The flue gas refrigeration source-end system includes a cooling tower. The water outlet is connected to the condensed water storage tank via a condensed water downcomer. The water inlet is connected to the cooling tower via a circulating water supply pipe. A condensation circulation water pump is provided on the circulating water supply pipe. The cooling tower is connected to the condensed water storage tank via a circulating water return pipe.

A distillation head of embodiments of the disclosed technology has a vertical tube which extends to and partially through a fraction collector. The vertical tube is mostly filled with a distillation key which is attached to a top side of the fraction collector and extends downwards through the vertical tube without coming into contact with same. A class housing or shell surrounds the vertical tube, which in turn, surrounds the distillation key or, at least a majority of each while the vertical tube extends past an area circumscribed by the shell and the distillation key extends past an area circumscribed by the vertical tube in some embodiments of the disclosed technology.

A method which allows the ejection of non-condensable gases, notably air, from a closed loop power generation process or heat pump system, is disclosed. A vessel in which a working fluid is absorbed or condensed can be separated from the power generation processes by valves. Residual gas comprising C02, non-condensable gas such as air, water and alkaline materials including amines may be compressed by raising the liquid level in said vessel. The concurrent pressure increase leads to the selective absorption of C02 by alkaline materials. In simpler embodiments, mainly air is removed from one- or two-component processes. Following the compression, non-condensable gas may be vented, optionally through a filter. The method is simple and economic as vacuum pumps may be omitted. The method is useful for any power generation and Rankine cycle, and particularly useful for the power generation process known as C3 or Carbon Carrier Cycle.

A method is disclosed for activating or regenerating a Fischer Tropsch catalyst used in a gas-to-liquids process operating in recycle mode. The method permits the use of specific inert gases to adjust the mole weight of the gas so that the recycle compressor designed for normal steady state operation can also be used in the ROR method. Nitrogen and carbon dioxide are specifically excluded for the reduction steps of the ROR method as they have been demonstrated to have a negative effect on the method. Nitrogen is used in the oxidation step with small amounts of oxygen containing gas, preferably air, and may be modified with the addition of argon, helium, or carbon dioxide if the mole weight of the oxidation gas needs to be modified to satisfy the requirements of the compressor.

A multi-stage distillation system includes multiple stages, and each stage Si includes an evaporator Ei and a condenser Ci. Each condenser includes a steam chamber in pressure-connection with a steam chamber of each evaporator of the same stage. Each evaporator has a steam chamber outlet connected to a spray inlet of the next evaporator Ei+1, and the outlet of the last evaporator En connects to the spray inlet of the first evaporator E1 with a respective fluid line to form an evaporator circuit. Each outlet of each condenser Ci connects to the one spray inlet of the previous condenser Ci1, and the outlet of the first condenser C1 connects to the spray inlet of the last condenser Cn with a fluid line to form a condenser circuit. A steam line connects between condensers Ci+1 and Ci or between the evaporators En and E1.

Provided herein are systems, devices and methods for generating water from atmospheric air, making use of a molecular selective processing unit and a vapor exchange unit to efficiently generate pure water from water vapors, selectively separated from air.

A water vapor distillation system. The system includes a water vapor distillation device configured to receive a volume of source water from a fluid source and produce distillate, the device comprising: a concentrate flow path comprising a concentrate output; a distillate flow path comprising a distillate output; at least one source proportioning valve; a first heat exchanger comprising at least a portion of the distillate flow path; a second heat exchanger including at least a portion of the concentrate flow path, wherein the first heat exchanger and the second heat exchanger in fluid flow communication with the fluid source; a distillate sensor assembly in communication with the distillate flow path and located downstream the first heat exchanger, the distillate sensor assembly configured to generate a distillate temperature measurement; and a controller configured to control the source proportioning valves, the controller configured to: receive the distillate temperature measurement; determine the difference between a first target temperature and the distillate temperature measurement; and split the source water from the fluid source between the first heat exchanger and the second heat exchanger based on the difference between the first target temperature and the distillate temperature measurement.

A method for recovering organic carbonates in an electrolytic solution of a waste lithium ion battery is provided. The organic carbonates include a first carbonate and a second carbonate having a higher melting point and a higher boiling point than the first carbonate. The method includes performing a temperature adjustment process in which an internal temperature of a drier in which the waste lithium ion battery is accommodated is kept in a first temperature range, an internal temperature of a pipe extending to below the drier is kept in a second temperature range, and an internal temperature of a condenser connected to the drier via the pipe is kept in a third temperature range, and performing a recovery process of reducing internal pressures of the drier, the pipe, and the condenser from a normal pressure to a first pressure and recovering the first carbonate in the condenser.