Abstract: A process for producing a chalcogen-containing compound semiconductor includes providing at least one substrate coated with a precursor for the chalcogen-containing compound semiconductor in a process chamber; heat treating the at least one coated substrate in the process chamber, wherein during a heat treatment, a gas atmosphere comprising at least one gaseous chalcogen compound is provided in the process chamber; removing the gas atmosphere present after the heat treatment of the at least one coated substrate as a waste gas from the process chamber; cooling the waste gas in a gas processor, wherein a plurality of gaseous chalcogen compounds-present in the waste gas after the heat treatment of the at least one coated substrate are separated in time and space from one another from the waste gas by respective conversion into a liquid or solid form. Further provided is a device designed to carry out the process.

Abstract: A unit for recovering hydrogen chloride from an aqueous liquid which includes hydrogen chloride and is contaminated with compounds of low or no volatility, the unit having an evaporation unit for forming, from the liquid, a vapour which contains hydrogen chloride and a liquid concentrate which is contaminated with the compounds of low or no volatility, a first distillation unit for separating the hydrogen-chloride-containing vapour into a first top product and a first bottom product, and a second distillation unit for separating a hydrogen-chloride-containing aqueous fluid into a second top product and a second bottom product, one of these two distillation units being configured to be able to implement therein a distillation above the ambient pressure, and the other of these two distillation units being configured to be able to implement therein a distillation below the ambient pressure.

Abstract: A system may include an output manifold that may be in fluid communication with a reservoir and that may include multiple discharge ports. Each of the discharge ports may be configured to discharge electrorheological fluid into a housing. A recovery manifold may be in fluid communication with the reservoir and include multiple recovery ports. Each of the recovery ports may be configured to receive the electrorheological fluid from a housing. A gas remover may be positioned to extract gas from the electrorheological fluid received from the recovery ports. A housing may be connected to the system, and electrorheological fluid from the system may be pumped through the housing and the gas remover.

Abstract: A still/stahl column includes a still section, a primary stahl section, the primary stahl section positioned beneath the still section, and a polishing stahl section, the polishing stahl section positioned beneath the primary stahl section. A process also includes feeding a water rich glycol still feed stream to the still section and feeding a stripping gas feed stream to the polishing still section. The process includes withdrawing a reboiler draw stream from the still section and heating the reboiler draw stream in a reboiler to form a reboiler inlet stream. The process includes injecting the reboiler inlet stream into the primary stahl section, stripping water from the water rich glycol with the stripping gas, and withdrawing a still stripping gas stream from a top portion of the still section. A lean glycol polishing discharge stream is withdrawn from a bottom portion of the polishing stahl section.

Abstract: Systems and methods for operating a water recovery system are described and include activating a condenser of the water recovery system. The method includes measuring a temperature associated with the condenser based on data obtained from a condenser temperature sensor. The method includes comparing the temperature associated with the condenser to a maximum threshold temperature. The method includes activating an auxiliary condenser of the water recovery system in response to the temperature associated with the condenser being greater than the maximum threshold temperature.

Abstract: A system and method for efficiently and sustainably producing propylene and acrylonitrile is disclosed which utilizes biodegradable materials, combustible materials that produce carbon dioxide and/or carbon monoxide. According to one embodiment of the invention, a source of carbon dioxide and/or carbon monoxide is utilized and the carbon dioxide and/or carbon monoxide is electrochemically reduced to ethylene. Dimerization is applied to separate the ethylene to produce 1-butene; which is isomerized to produce 2-butene. The 2-butene is metathesized to produce propylene. The propylene may then be subject to ammoxidation as desired in order to produce acrylonitrile.

Abstract: In accordance with an embodiment, a carbon dioxide capturing apparatus includes a first absorbing unit, a regeneration unit, a water washing capturing unit, and a pre-amine capturing unit. The first absorbing unit brings a gas containing carbon dioxide into contact with an absorbing liquid containing an amine compound, and discharges the absorbing liquid which has absorbed carbon dioxide as a rich liquid. The regeneration unit releases a carbon dioxide gas from the rich liquid sent from the first absorbing unit. The water washing capturing unit captures the amine compound entrained in a decarbonated treatment gas sent from the first absorbing unit. The pre-amine capturing unit receives part of the rich liquid from the first absorbing unit, and traps the amine compound entrained in the decarbonated treatment gas by bringing the decarbonated treatment gas from the first absorbing unit into countercurrent contact with the part of the rich liquid.

Abstract: An exhaust gas purification system includes a tank for storing a fluid and a mounting plate coupled to the tank. A baffle is positioned inside the tank below the mounting plate. The baffle has an outer wall defining an interior cavity and an opening. A sensor is positioned in the interior cavity for detecting a condition of the fluid. A supply conduit extends through the mounting plate into the tank. A return conduit extends through the mounting plate into the tank and has an outlet positioned to discharge a return fluid below the opening and exterior to the baffle and the interior cavity.

Abstract: The invention provides a method and a plant for producing urea ammonium nitrate (UAN). The method involves the use of a condensation section, optionally in combination with a medium pressure decomposition section, between the dissociation and neutralization sections. The invention further provides a method of modifying an existing UAN plant. The advantages of the process of the invention are that the emission of CO2 can be reduced, the plant capacity can be increased and the high capital expenditure needed for CO2 compression equipment is reduced.

Abstract: Provided are a reclaimer 51 that introduces, through a branch line L11, and stores a part 17a of an absorbent 17 regenerated in a regenerator of a recovery unit that recovers CO2 or H2S in a gas, a first alkaline agent supply section 53A that supplies an alkaline agent 52 to the reclaimer 51, a heating section 54 that heats the absorbent 17 stored in the reclaimer 51 and to which the alkaline agent 52 has been mixed to obtain recovered vapor 61, a first vapor cooler 55A that cools the recovered vapor 61 discharged from the reclaimer 51 through a vapor line L12, a first gas-liquid separator 56A that separates a coexisting substance 62 entrained in the cooled recovered vapor 61 into a recovered absorption agent vapor (gas) 17b and the liquid coexisting substance 62 by gas-liquid separation, and an introduction line L13 that introduces the recovered absorption agent vapor 17b separated in the first gas-liquid separator 56A into a regenerator 20.

Abstract: The methods apparatuses described herein involve recovering of glycol from an aqueous phase to form a stream of recovered glycol and a glycol recovery system. The aqueous phase is fed to the top of a lower theoretical stage in a distillation column. An overhead vapour stream is drawn from the distillation column overhead of an upper theoretical stage, and a bottom stream comprising a stream of regenerated glycol is drawn from the distillation column via a bottom outlet configured below the lower theoretical stage. The stream of recovered glycol comprises the regenerated glycol. In addition, a first middle theoretical stage is situated within the distillation column gravitationally above the lower theoretical stage and below the upper theoretical stage. A side stream of liquid water is drawn from the bottom of the upper theoretical stage in the distillation column.

Abstract: A CO2 recovery system includes an absorber 2 and a regenerator 3. The absorber 2 includes a CO2 absorbing section 21 and a water-washing section 22. The CO2 absorbing section 21 allows flue gas 101 to come into contact with a basic amine compound absorbent 103 so that the basic amine compound absorbent 103 absorbs CO2 in the flue gas 101. The water-washing section 22 allows the decarbonated flue gas 101A in which the amount of CO2 has been reduced in the CO2 absorbing section 21 to come into contact with circulating wash water 104 and to be washed with the wash water 104 so that the amounts of the basic amine compounds entrained in the decarbonated flue gas 101A are reduced. The regenerator 3 releases CO2 from the basic amine compound absorbent 103 the CO2 absorbed therein.

Abstract: The present invention relates to a feed distribution device in separation columns and a method of operation. In particular it relates to distillation columns in which the feed stream is substantially liquid phase, or a mixture of gas and liquid upstream of the column, but where the feed vaporizes or vaporizes more when it enters the column. More specifically, the feed distribution device contains a plurality of opening which allow the feed to vaporize inside the column and where the openings are maintained in critical condition during operation. Significant advantage is achieved through the implementation and use of the present feed distribution device.

Abstract: An apparatus that separates and recovers CO2 from a CO2 absorbent that has absorbed CO2 includes a regeneration tower configured to apply heat to the CO2 absorbent that has absorbed CO2, configured to separate and remove CO2 from the CO2 absorbent, configured to exhaust CO2 gas, and configured to regenerate the CO2 absorbent, a plurality of compressors configured to compress the CO2 gas exhausted from the regeneration tower, a dehydration device provided between the plurality of compressors and configured to remove moisture from the compressed CO2, and a line configured to supply air or N2 gas into the dehydration device to preliminarily operate the dehydration device until a stable state is achieved before starting the compressor.

Abstract: A carbon dioxide recovery unit is provided with: an absorption tower for bringing an exhaust gas into contact with a CO2 absorbing liquid to thereby absorb and recover CO2 from the exhaust gas; a regeneration tower for taking out the CO2 from the CO2 absorbing liquid; a CO2 delivery line L3 for delivering the taken-out CO2 to a storage process; and a CO2 return line L5 for returning the taken-out CO2 to the absorption tower. When a CO2 recovery unit and a CO2 compressing device are activated, if a storage process side has some kind of trouble and cannot receive the CO2, a destination part to which the CO2 is delivered from the regeneration tower is switched from the CO2 delivery line L3 to the CO2 return line L5, whereby the CO2 gas is mixed with the exhaust gas in the absorption tower.

Abstract: There is provided an exhaust gas treatment system including a CO2 recovery unit with further enhanced energy efficiency. The exhaust gas treatment system (1) includes: a CO2 recovery unit (10) including a CO2 absorption column (11), an absorbing solution regeneration column (16), a condensate supply pipeline (15) for supplying condensate, which contains CO2 absorbing solution discharged from the CO2 absorption column (11) to a bottom portion of the absorbing solution regeneration column (16), and a CO2 separation section (22) for performing heat exchange, via a heat exchanger (23), between the CO2 discharged from the absorbing solution regeneration column (16) and the condensate; and an exhaust gas heat exchanger (5) provided on a gas upstream side of the CO2 recovery unit (10) for performing heat exchange between exhaust gas before flowing into the CO2 recovery unit (10) and the condensate.

Abstract: A feed distribution device in separation columns and a method of operation for such a device. In particular, distillation columns in which the feed stream is substantially liquid phase, or a mixture of gas and liquid upstream of the column, but where the feed vaporizes or partially vaporizes prior to or as it enters the column. More specifically, the feed distribution device contains a plurality of opening which allow the feed to vaporize prior to or as it enters the column and where the openings are maintained in critical condition during operation. Significant advantage is achieved through the implementation and use of the present feed distribution devices.

Abstract: The present application relates to a system for removal of gaseous contaminants from a gas stream. The system includes an absorber for contacting the gas stream with a wash solution to form a used wash stream, a regenerator for regenerating the used wash solution, a reboiler and at least two heat exchangers in fluid communication with the absorber, regenerator and reboiler.

Abstract: An apparatus for separating and recovering CO2 from a CO2 absorbent, includes: a regeneration tower for regenerating the absorbent that has absorbed CO2 by heating it to separate and remove CO2 therefrom and to exhaust CO2 gas; a compressor for compressing the CO2 gas exhausted from the tower; and a heat exchanger for heating the absorbent in the tower by exchanging heat with a part of the compressed CO2 by the compressor which is introduced into the tower. The apparatus may include a plurality of the compressors and a plurality of the heat exchangers. The plurality of compressors is arranged in series to sequentially compress the CO2 gas exhausted from the tower. The plurality of heat exchangers is configured so that each part of the CO2 compressed by the plurality of compressors is introduced to the tower in parallel to exchange heat with the absorbent in the tower.

Abstract: A slug-containing vapor recovery system wherein pressure and/or fluid level sensors are provided which monitor for conditions caused by the entry of a slug of hydrocarbon liquid, including that caused by a plunger-lift system. The system can be configured to accommodate virtually any anticipated slug-events.

Abstract: The present application relates to systems and processes for removal of gaseous contaminants from gas streams. In particular, the application relates to a process for removal of gaseous contaminants from a gas stream comprising contacting the gas stream with a wash solution to remove gaseous contaminants from the gas stream by absorption into the wash solution; and regenerating the used wash solution to remove gaseous contaminants from the used wash solution, to provide a regenerated wash solution and a gas comprising removed contaminants, wherein in a first regeneration stage the gas comprising removed contaminants is cooled to minimize loss of water vapor from the regeneration step.

Abstract: A method and system for removing gaseous contaminants from a gas stream by contacting the gas stream with a wash solution and regenerating the wash solution in a regeneration system for future use in removing gaseous contaminants from the gas stream.

Abstract: A method for separating carbon dioxide from a flue gas of a fossil fuel-operated power plant is provided. In the method, a fossil fuel is initially burned in a combustion process, wherein a hot waste gas containing carbon dioxide is produced. In a next process step, waste gas containing carbon dioxide is brought into contact with an absorption medium in an absorption process, wherein carbon dioxide is absorbed by the absorption medium, thus forming a charged absorption medium. Next, gaseous carbon dioxide is thermally expelled from the charged absorption medium in a desorption process. For this purpose, a vapor is supplied to the desorption process, the vapor is injected into the charged absorption medium, wherein the condensation heat released by the condensation of the vapor is transferred to the charged absorption medium, and the partial pressure of the carbon dioxide is simultaneously reduced in the desorption unit.

Abstract: The disclosure relates to a process for treating a gas mixture containing carbon dioxide and hydrogen sulphide, including the following steps: deacidificating the gas mixture by bringing the gas mixture into contact with a first lean absorbent solution stream, delivering a deacidified gas mixture, and a first rich absorbent solution stream; regenerating the first rich absorbent solution stream, delivering the first lean absorbent solution stream and a sour gas stream; distillating the sour gas stream, delivering a first carbon-dioxide-rich stream and a hydrogen-sulphide-rich stream; purifying the first carbon-dioxide-rich stream by bringing the first carbon-dioxide-rich stream into contact with a second lean absorbent solution stream, delivering a second carbon-dioxide-rich stream and a second rich absorbent solution stream, the molar concentration of carbon dioxide in the second carbon-dioxide-rich stream being greater than the molar concentration of carbon dioxide in the first carbon-dioxide-rich stream.

Abstract: The present invention relates to a process for the recovery of ammonia contained in a gaseous stream, said process comprising the following phases: (a) subjecting the gaseous stream containing ammonia to a washing with an aqueous washing solution having a pH lower than 7.0, with the formation of a purified gaseous stream and an aqueous solution containing an ammonium salt; (b) treating the aqueous solution containing the ammonium salt coming from phase (a) in a vertical falling film heat exchanger at a temperature from 50 to 250° C. and an absolute pressure ranging from 50 KPa to 4 MPa with the formation of a regenerated washing solution and a gaseous stream comprising NH3 and H2O; (c) recycling said regenerated washing solution to phase (a). The present invention also relates to equipment for effecting the above process.

Abstract: A method for reclaiming CO2 absorbing chemical(s) from a lean aqueous CO2 absorbent leaving a regeneration column (8), where lean absorbent (30) is withdrawn and flashed (31) to generate a vapor that is compressed (34) and returned into the regeneration column as stripper gas (37), where a part of the lean absorbent (20) is withdrawn and introduced into a reclaimer (21) in which the lean absorbent is boiled to generate a gas phase (23) that is withdrawn and returned into the regeneration column as reclaimed absorbent, and a liquid phase containing impurities (24), wherein the gaseous phase that is withdrawn from the reclaimer is compressed (34) together with the vapor part (33) from the flashing of the lean absorbent, to generate a pressure in the reclaimer that is lower than the pressure in the regeneration column, and a reboiler (11) for carrying out the method, are described.

Abstract: In some implementations, a method for dehydrating carbon dioxide includes identifying a stream including at least carbon dioxide and water. At least a portion of the stream is dehydrated using an initial lean sorbent including glycerol and a polyhydric alcohol to generate dry carbon dioxide stream and rich sorbent including water. The polyhydric alcohol reduces an amount of glycerol lost to the dry carbon dioxide stream during dehydration. This process may result in the beneficial reduction in the amount of glycerol that leaves the system with the dry carbon dioxide. The dry carbon dioxide and the rich sorbent are separated. The glycerol is recycled by dehydrating the rich sorbent to produce recycled lean sorbent.

Abstract: The present invention relates to a method for recovery of carbon dioxide from a gas (G3), in particular the present invention relates to a method for recovery of carbon dioxide using a process gas (G1) heated reboiler (A1) for carbon dioxide removal in a stripper (A3).

Abstract: A process for removing carbon dioxide from a fluid comprises the steps of: (a) treating the fluid by bringing it into countercurrent contact with a liquid absorbent in a first absorption zone and thereafter in a second absorption zone to absorb at least part of the carbon dioxide contained in the fluid into the absorbent; (b) depressurizing the loaded absorbent to release a first stream of carbon dioxide and yield a partially regenerated absorbent; (c) recycling a first stream of the partially regenerated absorbent into the first absorption zone; (d) heating a second stream of the partially regenerated absorbent to release a second stream of carbon dioxide and yield a regenerated absorbent; (e) recycling the regenerated absorbent into the second absorption zone; (f) condensing water vapor entrained in the second stream of carbon dioxide by cooling the second stream of carbon dioxide and transferring at least part of the heat recovered to the partially regenerated absorbent by indirect heat exchange.

Abstract: A process for removing carbon dioxide from a fluid comprises the steps of: (a) treating the fluid by bringing it into countercurrent contact with a liquid absorbent in a first absorption zone and thereafter in a second absorption zone to absorb at least part of the carbon dioxide contained in the fluid into the absorbent; (b) depressurizing the loaded absorbent to release a first stream of carbon dioxide and yield a partially regenerated absorbent; (c) recycling a first stream of the partially regenerated absorbent into the first absorption zone; (d) heating a second stream of the partially regenerated absorbent to release a second stream of carbon dioxide and yield a regenerated absorbent; (e) recycling the regenerated absorbent into the second absorption zone; (f) condensing water vapor entrained in the second stream of carbon dioxide by cooling the second stream of carbon dioxide and transferring at least part of the heat recovered to the partially regenerated absorbent by indirect heat exchange.

Abstract: An object of the present invention is to provide an exhaust gas treatment system that effectively use heat recovered from an exhaust gas without any limitation in a CO2 chemical absorption equipment that requires enormous heat energy, and thus enabling reduction in running cost of the CO2 chemical absorption equipment.

Abstract: A method for reducing energy requirements of a CO2 capture system comprises: contacting a flue gas stream with a CO2 lean absorbent stream in an absorber, thereby removing CO2 from the flue gas and providing a CO2 rich absorbent stream; heating a first portion of the CO2 rich absorbent stream using heat from the CO2 lean absorbent stream, and providing the heated first portion of the CO2 rich absorbent stream to a regenerator; providing a second portion of the CO2 rich absorbent stream to the regenerator, wherein the heated first portion is hotter than the second portion and the heated first portion is provided to the regenerator at a lower elevation in the regenerator relative to that of the second portion.

Abstract: A system for recycling a work gas used in a thermal reactor for treating sample materials includes a thermal reactor using a work gas from a first source mixed with carrier gases. The work gas has a boiling point higher than the carrier gases. The system includes a pump, a condenser which converts the work gas into a liquid, and a scrubber.

Abstract: Provided are a CO2 absorber that reduces CO2 contained in flue gas; a regenerator that reduces CO2 contained in rich solvent absorbing CO2 to regenerate the rich solvent, so that lean solvent having the CO2 reduced in the regenerator is reused in the CO2 absorber; a heat exchanger that allows the rich solvent to exchange heat with the lean solvent; and a controller that controls to extract rich solvent portion that is part of the rich solvent, to allow the rich solvent portion to bypass the heat exchanger, and to be supplied into the top of the regenerator without exchanging heat so as to minimize a sum of an enthalpy that is taken out of the regenerator as CO2 gas accompanying steam and an enthalpy of the lean solvent after heat exchange with the rich solvent in the heat exchanger.

Abstract: Processes for operating an ammonia stripper at a low pressure in a gas purification system include providing a first side-draw stream from the ammonia stripper; heating the first side-draw stream with a second side-draw stream from a regenerator; providing a stripper offgas stream from the ammonia stripper to a stripper overhead condenser; and utilizing the stripper offgas stream as a heat source for a regenerating system fluidly coupled to the stripper overhead condenser. Also disclosed are systems for implementing the processes.

Abstract: A method of removing acid gases from raw gas is disclosed in which the raw gas is supplied to an absorption column where it is contacted with a physical absorption agent, having a boiling point lower than 100° C. at atmospheric pressure, under elevated operating pressure to load, the physical absorption agent with acid gases and usable gases and then the physical absorption agent loaded with acid gases and usable gases is driven from the absorption column at its sump while drawing off at the head of the absorption column a purified top gas containing up to a few ppm of acid-gas components. Following the absorption, the physical absorption agent undergoes stripping to remove usable gases, and regeneration to remove the acid gases as well as to provide a regenerated physical absorbent which may be used to treat additional raw gas.

Abstract: A system and process are disclosed for selective removal and recovery of H2S from a gaseous volume, e.g., from natural gas. Anhydrous organic, sorbents chemically capture H2S gas to form hydrosulfide salts. Regeneration of the capture solvent involves addition of an anti-solvent that releases the captured H2S gas from the capture sorbent. The capture sorbent and anti-solvent are reactivated for reuse, e.g., by simple distillation.

Abstract: [Problem] To provide a system for recovering carbon dioxide from flue gas, in which a reboiler in a regenerator can be compactly installed, and a method therefor, in facilities where CO2 or the like contained in flue gas is recovered. [Solving Means] To include an absorber 1006 that absorbs CO2 contained in flue gas 1002, a regenerator 1008 that strips CO2 from CO2 absorbent (rich solution) 1007 to regenerate absorbent, internal shells 101 provided at a bottom of the regenerator 1008 with a predetermined interval therebetween, into which regenerated CO2 absorbent is introduced by a feeding unit 102 from a bottom side thereof so that the CO2 absorbent overflows from an upper end of the internal shell thereof toward the bottom of the regenerator, and a reboiler that is inserted into the internal shells 101 in a direction orthogonal to a vertical axis and includes a heat-transfer tube 103 that reboils absorbent.

Abstract: A CO2 recovery apparatus according to the present invention includes: an absorber (1003) that brings CO2-containing flue gas (1001A) into counter-current contact with CO2 absorbent (1002) to reduce CO2, and a regenerator (1005) that regenerates rich solution (1004) that has absorbed CO2, in which lean solution (1006) having CO2 reduced in the regenerator (1005) is reused in the absorber (1003). The absorber (1003) further includes a CO2 absorbing unit (1010) that recovers CO2 contained in the flue gas (1001A), and the CO2 absorbent (1002) that has absorbed CO2 is extracted from a rich side of the CO2 absorbing unit (1010) to exterior, cooled, and then supplied to a position nearer to a lean side of the absorber (1003) with respect to the position at which the CO2 absorbent (1002) is extracted.

Abstract: A method and apparatus for drying a natural gas or an industrial gas that contains acidic gas components, wherein gas drying is followed by the removal of the acidic gas components from the dried gas. The same physical solvent is used for both of the process steps of gas drying and of acidic gas removal. The gas to be dried is brought into contact with the physical solvent, which absorbs most of the water contained in the gas. The physical solvent, loaded with water, is transferred into a solvent regenerating device to be heated where the water contained in the solvent is stripped from the solvent in the countercurrent by acidic gas that is removed from the dried useful gas during the acidic gas absorption. The acidic gas being released again in the acidic gas solvent regenerating device, stripped from the solvent, and discharged from the solvent regenerating device.

Abstract: To include an absorber (1006) that brings CO2 absorbent that absorbs CO2 contained in flue gas (1002) into contact with the flue gas to remove CO2 from the flue gas, a regenerator (1008) that strips CO2 from CO2 absorbent (rich solution), which is fed from the absorber through a first feed line L1 and has absorbed CO2, to regenerate CO2 absorbent, thereby acquiring regenerated CO2 absorbent (lean solution) (1009), falling film reboilers (1101-1 and 1101-2) that draw off CO2 absorbent (amine solution) (1033) from near the bottom of the regenerator and reheats regenerated CO2 absorbent via steam (1031), a first liquid-vapor separator (1103) that separates the CO2 absorbent reheated by the falling film reboilers into regenerated CO2 absorbent in which CO2 has been removed and vapor containing CO2, and a second feed line L2 for supplying the separated regenerated CO2 absorbent to the absorber.

Abstract: A modular amine plant having a front-end module and a back-end module in fluid communication with each other. The front-end module having pre-fabricated connections for the association of various equipment including: a filter, an absorption tower, and a flash tank. The back-end module having pre-fabricated connections for the association of other various equipment including: a heat exchanger, a distillation tower, and a reboiler. The modular amine plant capable of being installed at a site in less than about 5 days. The modular amine plant further having moment forces sufficient to withstand wind speeds of about 100 miles per hour.

Abstract: A process for removing acid gases from a fluid stream in which a) the fluid stream is treated with an absorption liquid which comprises at least one amine, a stripping aid, and water, wherein the stripping aid is selected from water-miscible liquids, the boiling temperature of which at atmospheric pressure is lower than that of water, b) the treated fluid stream is treated with a liquid aqueous phase in order to convert entrained stripping aid at least in part to the aqueous phase, c) the loaded aqueous phase is heated in order to expel the stripping aid at least in part, and d) the regenerated aqueous phase is cooled and at least in part recycled to step b). The stripping aid promotes the regeneration of the absorbent by stripping. Emissions of the stripping aid via the treated fluid stream are avoided by the treated fluid stream being scrubbed with a liquid aqueous phase.

Abstract: A method of deacidizing a gaseous effluent comprising acid compounds where the gaseous effluent is contacted in C1 with an adsorbent solution so as to obtain a gaseous effluent depleted in acid compounds and an absorbent solution laden with acid compounds, the absorbent solution being selected for its property of forming two separable phases when it has absorbed an amount of acid compounds and when it is heated. The absorbent solution laden with acid compounds is then heated in E1 and E3 so as to separate two fractions: a first absorbent solution fraction depleted in acid compounds and a second absorbent solution fraction enriched in acid compounds. These two fractions are then separated in BS1. The second fraction is regenerated in C2 so as to release part of the acid compounds, and the first absorbent solution fraction and the regenerated absorbent solution are recycled as absorbent solution.

Abstract: A process and system (100) for removing contaminants from a solution to regenerate the solution within the system. The process includes providing a solution (165) from a wash vessel (160) to a stripping column (181), the solution (165) including contaminants removed from a flue gas stream (150) present in the wash vessel (160) and contacting the solution with steam (185) inside the stripping column (181) thereby removing the contaminants from the solution and regenerating the solution. The stripping column (181) is operated at a pressure less than about 700 kilopascal.

Abstract: The gaseous effluent to be treated is contacted in C1 with an absorbent solution selected for its property of forming two separable phases when it has absorbed an amount of acid compounds and when it is heated. According to the invention, the absorbent solution is regenerated in at least two stages in regeneration zones Z1 and Z2. At the end of the first regeneration stage in Z1, at least part of the partly regenerated absorbent solution is separated into two fractions in B1: a fraction rich in acid compounds and a fraction depleted in acid compounds. Fraction 10 rich in acid compounds is sent to the second regeneration stage in Z2. The fraction depleted in acid compounds and regenerated absorbent solution 6 from the second regeneration stage are recycled to absorption column C1. The method can be applied to combustion fumes decarbonation and to natural gas or synthesis gas deacidizing.

Abstract: The present invention relates to a method for recovery of carbon dioxide from a gas stream. The method is a two-step method in which carbon dioxide is compressed in the first step, while the residual carbon dioxide is recovered by an absorption process in a subsequent step. The present invention also relates to the use of the method for the recovery of carbon dioxide and a plant for recovery of carbon dioxide.

Abstract: The present invention relates to a process for separating off CO2 from a gas stream, wherein in a second step the CO2 is removed from the CO2-absorbing agent by means of phase separation.

Abstract: Processes for operating an ammonia stripper at a low pressure in a gas purification system include providing a first side-draw stream from the ammonia stripper; heating the first side-draw stream with a second side-draw stream from a regenerator; providing a stripper offgas stream from the ammonia stripper to a stripper overhead condenser; and utilizing the stripper offgas stream as a heat source for a regenerating system fluidly coupled to the stripper overhead condenser. Also disclosed are systems for implementing the processes.

Abstract: Provided are a CO2 absorber that reduces CO2 contained in flue gas; a regenerator that reduces CO2 contained in rich solvent absorbing CO2 to regenerate the rich solvent, so that lean solvent having the CO2 reduced in the regenerator is reused in the CO2 absorber; a heat exchanger that allows the rich solvent to exchange heat with the lean solvent; and a controller that controls to extract rich solvent portion that is part of the rich solvent, to allow the rich solvent portion to by pass the heat exchanger, and to be supplied into the top of the regenerator without exchanging heat so as to minimize a sum of an enthalpy that is taken out of the regenerator as CO2 gas accompanying steam and an enthalpy of the lean solvent after heat exchange with the rich solvent in the heat exchanger.