An apparatus, system and method to remove purified vapor from a contaminated fluid using energy. The apparatus comprises an inlet wherein contaminated fluid flows in the apparatus through the inlet; at least two outlets wherein a first outlet exits purified vapor and a second outlet wherein contaminated fluid with a portion removed as purified vapor exits the apparatus; an energy source that causes the contaminated fluid to heat to a temperature wherein at least a portion of the contaminated fluid is converted to purified vapor; at least two different flow paths from at least one inlet to the first outlet and second outlet, the first and second flow paths flow through at least a portion of the apparatus.

Disclosed herein are processes for recovering paraxylene in which a first simulated moving bed adsorption unit is used to produce a paraxylene-rich extract stream that also contains a significant amount of the ethylbenzene and a paraxylene-depleted raffinate stream. Because a significant amount of the ethylbenzene is removed in the paraxylene-rich extract stream (at least enough to limit buildup in the isomerization loop), the paraxylene-depleted raffinate stream may be isomerized in the liquid phase. Avoiding vapor phase isomerization saves energy and capital, as liquid phase isomerization requires less energy and capital than the vapor phase isomerization process due to the requirement of vaporizing the paraxylene-depleted stream and the use of hydrogen, which requires an energy- and capital-intensive hydrogen recycle loop.

Processes and systems suitable for purifying or otherwise treating liquids to remove contaminants therein, including but not limited to contaminated water, to permit reclaiming, recycling, and reuse of the liquids. Such a process and system entails the use of a cascading distillation system that evaporates a liquid from the feedstock and then condenses and collects a more purified form of the liquid. The cascading distillation system can be operated to selectively process the feedstock through any of a series of vessels at which different amounts and/or contaminants may be removed from the feedstock.

The separation method separates a polyalcohol compound from water, so as to obtain a purified product stream comprising the polyalcohol compound in an output concentration of at least 90 wt %. Thereto, a mixture of the polyalcohol compound and water is provided, said mixture having a polyalcohol concentration. The polyalcohol concentration of the mixture is increased in an evaporation stage. Subsequently, the mixture is treated in a distillation stage to deliver the purified product stream comprising the polyalcohol compound in the output concentration of at least 90 wt %. Herein, the distillation stage is operated to produce steam output, that is optionally compressed to a steam pressure, and is coupled to the evaporation stage. The maximum distillation pressure and/or said compressed steam pressure is not less than the maximum evaporation pressure. The reactor system is configured for performing the separation method.

Multi-chamber Compressor (6, 206, 506) of Mechanical Vapor re-Compression (MVC) and water treatment methods, the compressor bearing independent compression chambers of positive displacement, for heat-pumps, of two main variants: a) reciprocating-rotary motion (6, 206) wherein the compression chambers (7V) are radially arranged cylindrical sectors based on concentric circular sectors of the same angle, with, pistons of radially arranged vanes (20, 220) of respective surface and with the plane of the vanes passing through the axis of the common rotor (14) and the shaft (16) and b) reciprocating-linear motion (506) wherein the compression chambers (52v) are in series arranged cylinders with pistons/vanes (50v) of corresponding circular surfaces and with the plane of the vanes perpendicular to the common shaft (51). In both cases, the shaft (16, 51) and the motor are common to all the vanes (20v, 50v), which follow identical strokes. The surfaces of the vanes (20v, 50v), as well as of the compression chambers (7V, 52v), differ from each other, since each compression chamber (7V, 52v) has its own and independent pair of evaporation (ev, dv, Lv, by) and heat-exchanger chambers/areas (Cv/eCv, 32v/33v, 132v, 54v/53v), said compression chamber exclusively sucks from, compresses and discharges to, and the fluids/vapors being dispensed, are under different thermodynamic state conditions. The stages are independent from each other, the medium-vapor providing the energy of evaporation is produced in the stage itself, and flow rate and compression ratio CR are independently controlled and adjusted in each stage.

A direct-contact, spray-assisted, evaporation and condensation, DCSEC system includes a heating block configured to receive and heat up seawater; plural evaporation and condensation stages, wherein n is a natural number, each stage being configured to generate water vapors through flash evaporation; an evaporation only stage connected to a last stage of the plural evaporation and condensation stages, the evaporation only stage configured to receive a brine from the last stage n of the plural evaporation and condensation stages; an input/output block configured to receive the brine from the evaporation only stage and to discharge it outside the system, and also to receive cooling water; and a pressure-swing regeneration block fluidly connected to the evaporation only stage to receive the water vapors and to generate a hot vapor, which is provided to the heating block for heating the seawater.

Disclosed is a purified dialkyl furan dicarboxylate (DAFD) vapor composition containing at least 99.5 wt. % DAFD; 5-(alkoxycarbonyl) furan-2-carboxylic acid (ACFC) that, if present, is present in an amount of not more than 1000 ppm, alkyl-5-formylfuran-2-carboxylate (AFFC) that, if present, is present in an amount of not more than 1000 ppm, 5-(dialkoxymethyl)furan-2-carboxylic acid (DAFCA) that if present, is present in an amount of not more than 1000 ppm, and alkyl 5-(dialkoxymethyl)furan-2-carboxylate (ADAFC) that if present, is present in an amount of not more than 1000 ppm, in each case based on the weight of the DAFD vapor composition.

A method for storing solar energy and generating electric power comprising the steps of utilizing a solar powered water treatment device (2) to convert non-potable water (3) into distillate (4) and concentrate (5), storing the distillate and the concentrate in a distillate storage tank (104) and a concentrate storage tank (105) respectively and feeding the distillate from the distillate storage tank and the concentrate from the concentrate storage tank to a salient gradient power device (106) to generate electric power.

A multi-stage flash reversal unit includes a housing; plural stages located inside the housing; an evaporation port that receives a water feed having a first temperature; a condensation port that outputs a concentrated water feed having a second temperature, which is lower than the first temperature; and a cooling unit that cools down the concentrated water feed.

A system for treating a produced water stream to separate the water into a final concentrated brine stream and a final distillate stream includes a first flash vessel for separating the produced water stream into a first distillate stream and a first concentrated brine stream, a second flash vessel connected to the first flash vessel separates the first concentrated brine stream into a second distillate stream and a second concentrated brine stream, a third flash vessel connected to the second flash vessel separates the second concentrated brine stream into a third distillate stream and a final concentrated brine stream, a first pre-heater heat exchanger for heating the produced water stream by the final distillate stream of combination of the first distillate stream from the first flash vessel, the second distillate stream from the second flash vessel and the third distillate stream from the third flash vessel, a second pre-heater heat exchanger connected to the first pre-heater heat exchanger, for heating the produced water stream from the first pre-heater heat exchanger by the concentrated brine stream from the third flash vessel, a third pre-heater heat exchanger connected to the second pre-heater heat exchanger, for heating the produced water stream from the second pre-heater heat exchanger by the third distillate stream from the third flash vessel, a pump connected to the third pre-heater heat exchanger for pumping the produced water stream at positive pressure, an electrical heater connected to the pump for heating the produced water stream, and a waste heat exchanger connected to the first electrical heater for heating the produced water stream.