A condensation system for recuperating the energy discharge of a nuclear power plant comprises a nuclear power unit, an air intake means, a compressor, a condenser, a water chamber equipped with a sprinkler, an electrical current generator, a pure water pump station, a cooling water pump station, a secondary condensate pool and a turboexpander. The air intake structure is connected to a compressor, which is connected to the condenser, which is connected to the turboexpander, which is supplied with the electric current generator and is connected to the water chamber, which is connected to the secondary condensate pool, which is connected to the pure water pump station, the condenser being connected to the cooling water pump station, wherein the air intake structure is accommodated in the discharge water channel, which is connected to the nuclear power unit and is equipped with a sealing cover.

A liquid separator and concentrator is disclosed. An example liquid separator and concentrator includes a separator column. A spray chamber has a sprayer nozzle to spray an influent within the spray chamber and create a falling film in the separator column. A heating jacket surrounds the separator column, wherein the heating jacket heats the falling film to evaporate at least one portion of the falling film and leaves a concentrate. A concentrate collection vessel receives the concentrate from the separator column.

Examples of a flexible pyrolysis system are provided that include at least one reaction chamber capable of pyrolyzing a combination of coal in a supercritical carbon dioxide (CO.sub.2) atmosphere. The system includes a recuperating and condensing circuit that removes dissolved pyrolysis products from the supercritical CO.sub.2 atmosphere and then recovers CO.sub.2 for reuse in the reaction chamber. The recuperating and condensing circuit includes multiple stages of recuperators and collectors that can be independently controlled in order to selectively fractionate the pyrolysis products. In addition, the pyrolysis reaction may be controlled to alter the pyrolysis products generated.

A rotary evaporator distillation device is provided that includes a flash vaporization section in which the bulk of solvent is removed. By removing most of the solvent before it enters the evaporating flask, the entire device may be smaller in size but achieve distillation at a pace available only in much larger systems.

A process of purifying acetic acid is provided. The process includes feeding a stream of acetic acid into a distillation column and distilling acetic acid in the presence of an oxidizing agent in the distillation column, to oxidize oxidizable impurities in the acetic acid, wherein the oxidizing agent is an oxidant capable of cleaving CC bonds. The process further includes removing a distilled acetic acid stream from the distillation column. Further processes for purifying acetic acid and systems for purifying acetic acid are also provided.

A continuous distillation process comprises the following steps: putting a material into a multilayer distillation tower to enable the material to sequentially undergo preheating, extrusion pricking, steam distillation, meal roasting, drying and cooling treatment, condensing essential oil-containing steam, and carrying out water separation, so as to obtain an essential oil.

A process of purifying acetic acid is provided. The process includes feeding a feed stream comprising acetic acid into a bottom half of a distillation column and distilling the acetic acid in the presence of a homogeneous oxidizing agent in the distillation column, to oxidize oxidizable impurities in the acetic acid, wherein the homogeneous oxidizing agent is capable of cleaving CC bonds. The process further includes removing a distilled acetic acid stream from the distillation column. Further processes for purifying acetic acid and systems for purifying acetic acid are also provided.

The present invention relates to a process (100) for separatory processing of a starting mixture containing predominantly hydrogen, methane and hydrocarbons having two or two or more carbon atoms, wherein at least a portion of the starting mixture is cooled to form one or more condensates using one or more heat exchangers (101, 103, 105, 107) and at least a portion of the condensate(s) is subjected to a rectification to form a gaseous methane-rich fraction. It is provided that the gaseous methane-rich fraction is used to form a first fluid stream which is at least partly compressed, in an unchanged composition with respect to the gaseous methane-rich fraction, to a liquefaction pressure level of 35 to 45 bar, and at least partly liquefied by cooling, and in that the first fluid stream, or a second fluid stream formed using the first fluid stream, is expanded to a delivery pressure and heated in the or at least one of the heat exchanger(s) (101, 103, 105, 107). A corresponding plant likewise forms part of the subject matter of the invention.

Systems and methods related to desalination systems are described herein. According to some embodiments, the desalination systems are hybrid systems comprising one or more first desalination units and one or more second desalination units. In some embodiments, the one or more second desalination units, which may form a fluidic circuit that is located downstream from the one or more first desalination units, may be configured to desalinate higher salinity liquid streams than the one or more first desalination units. In certain embodiments, the one or more first desalination units are operated under steady-state conditions and/or configured to operate under steady-state conditions. In certain embodiments, the one or more second desalination units are transiently operated and/or configured to facilitate transient operation. In some embodiments, a liquid stream comprising water and at least one dissolved salt is flowed through the one or more first desalination units, which are configured to remove at least a portion of the water from the liquid stream to form a first concentrated brine stream enriched in the dissolved salt. In some embodiments, at least a portion of the first concentrated brine stream is fed to a fluidic circuit comprising the one or more second desalination units. In some embodiments, the one or more second desalination units are configured to remove at least a portion of the water from the first concentrated brine stream to produce a second concentrated brine stream further enriched in the dissolved salt. In certain cases, the second concentrated brine stream is recirculated through at least a portion of the fluidic circuit until the second concentrated brine stream reaches a relatively high density (e.g., at least about 10 pounds per gallon) and/or a relatively high salinity (e.g., a total dissolved salt concentration of at least about 25 wt %).

A system for sustainable generation of energy, comprising at least one device for converting natural power into useful energy, and at least one internal combustion engine or heat engine. The internal combustion engine or heat engine may be connected to a gas cleaning device for fuel or heat supply. A method for sustainable generation of energy, comprising the steps of generating a first amount of useful energy by converting natural power; and generating a second amount of energy by operating at least one internal combustion engine or heat engine, wherein the internal combustion engine or heat engine is driven by fuel or heat derived from cleaning a waste gas.