Abstract: A chloride salt eliminator system and method for removal of chloride salt from glycol circulated through a reboiler in natural gas dehydration, in a continuous process, close to the wellhead. Hot glycol from the reboiler is pumped into a salt eliminator unit having independently replaceable filter elements which trap chloride salts which are not soluble in hot glycol and pass clean glycol for return to the reboiler.

Abstract: A process and an apparatus for dehumidifying a moist gas mixture are provided. The apparatus for dehumidifying a moist gas mixture can be used and in the process. The absorption medium used in the process and the apparatus is also provided.

Abstract: The present invention relates to a dehydration composition and method of use thereof for drying gas streams, in particular natural gas streams, wherein the dehydration composition comprises (i) a glycol, (ii) an imidazole compound, and optionally (iii) one or more of an alkali metal carboxylate, an additional glycol different than (i), an alkanolamine, a phosphate acid, a salt of a phosphate acid, a borate acid, a salt of a borate acid, a sweetening agent, a low temperature viscosity improver, a corrosion inhibitor, an antifoaming agent, or mixtures thereof.

Abstract: The embodiments described herein are directed a device for conditioning gas comprising an inlet for receiving fuel. The device includes an injector for injecting an oxygen source into the fuel, a heating component for heating the fuel, a conditioner unit, and a cooling component. The device further comprises an outlet for feeding conditioned gas into an engine. The embodiments are also directed to a method for conditioning gas.

Abstract: The invention relates to an apparatus (10) for drying and/or cooling gas (12), in particular air, by means of a hygroscopic solution (14), said apparatus comprising an absorption device (16) which comprises at least one gas flow duct (18) and at least one flow duct (20) carrying the hygroscopic solution, wherein the inner or gas chamber (22) of a respective gas flow duct is at least partly delimited by a vapor-permeable liquid-tight membrane wall (24) and at least one flow duct is provided, which is formed between such a gas flow duct and a further such gas flow duct adjacent to the latter or an adjacent cooling unit (26) and which carries the hygroscopic solution, so that moisture, in particular water vapor, passes from the gas into the hygroscopic solution via the membrane wall and is absorbed in said solution.

Abstract: Methods, systems, and devices are provided for thermal enhancement. Thermal enhancement may include absorbing heat from one or more devices. In some cases, this may improve the efficiency of the one or more devices. In general, a phase transition may be induced in a storage material. The storage material may be combined with a freeze point suppressant in order to reduce its melt point. The mixture may be used to boost the performance of device, such as an electrical generator, a heat engine, a refrigerator, and/or a freezer. The freeze point suppressant and storage material may be separated. By delaying the periods between each stage by prescribed amounts, the methods, systems, and devices may be able to shift the availability of electricity to the user and/or otherwise boost a device at different times in some cases.

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: 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: Impure carbon dioxide (“CO2”) comprising a first contaminant selected from the group consisting of oxygen (“O2”) and carbon monoxide (“CO”) is purified by separating expanded impure carbon dioxide liquid in a mass transfer separation column system. The impure carbon dioxide may be derived from, for example, flue gas from an oxyfuel combustion process or waste gas from a hydrogen (“H2”) PSA system.

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: 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 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 method of generating heat from a gas stream includes providing a first gas stream having a first temperature and a moisture content approximately saturating the gas stream, removing the moisture content from the first gas stream to form a second gas stream having a second temperature greater than the first temperature of the first gas stream, and heat exchanging the second gas stream having the second temperature greater than the first temperature of the first gas stream.

Abstract: A system (10) for regenerating a rich absorbent solution (26), the system including: an absorber (20) facilitating interaction between a process stream (22) and an absorbent solution, wherein the process stream comprises an acidic component, and interaction of the process stream with the absorbent solution produces a reduced acidic component stream (28) and a rich absorbent solution; at least one heat exchanger accepting at least one of said reduced acidic component stream and the process stream to transfer heat to a heat transfer fluid (60); and at least one mechanism (60a) to transfer the heat transfer fluid from said at least one heat exchanger to a regenerator (34) regenerating the rich absorbent solution, wherein each of the at least one mechanisms is fluidly coupled to each of the at least one heat exchangers.

Abstract: In a method for removing acid gases from a fluid stream, the fluid stream, which is in contact with an absorption medium within an absorber, is passed through a first absorption zone in the absorber to remove a majority of acid gases from the fluid stream. The fluid stream is susequently passed through a second absorption zone in the absorber to further remove acid gases from the fluid stream. The loaded absorption medium is passed into a first regeneration zone to obtain a partially regenerated absorption medium, and a part of the partially regenerated absorption medium is passed into the first absorption zone. The other part of the partially regenerated absorption medium is passed into a second regeneration zone to obtain a regenerated absorption medium. A part of the regenerated absorption medium is passed into the first absorption zone and the other part is passed into the second absorption zone.

Abstract: A system and method for removing water from a liquid desiccant such as a glycol used to dry cooled air in order to restore the desiccant to a purity up to around 97% in a closed continuous flow process. Liquid desiccant can be sprayed into cooled air in a conditioner where it gains moisture. The wet or gained desiccant can be optionally preheated in an economizing heat exchanger and then routed into a concentrator. Desiccant pure to around 97% can be removed from the concentrator, passed through an economizing heat exchanger to provide the preheating and returned to the conditioner holding area. The concentrator can be heated by steam or other means such as natural gas to boil the wet desiccant causing mixed vapor to enter a vertical distillation column where most of the glycol condenses out on the column packing or plates and returns to the concentrator.

Abstract: A power plant may include a combustion apparatus (11) producing an exhaust gas (12), an absorber (20) receiving the exhaust gas (12), the absorber (20) including a desiccant and producing a first stream of desiccant solution containing water and a first concentration of desiccant, and an apparatus (29, 70, 94) for dehydrating the first stream of desiccant solution while maintaining the water in a liquid phase. The apparatus (29, 70, 94) may include a heat exchanger (71, 110), a crystallizing heat exchanger (74, 96), a separator (78, 98) and a flash tank (112) for dehydrating the desiccant solution while maintaining water in a liquid phase and subsequently recovering water from the solution.

Abstract: Impure carbon dioxide (“CO2”) comprising a first contaminant selected from the group consisting of oxygen (“O2”) and carbon monoxide (“CO”) is purified by separating expanded impure carbon dioxide liquid in a mass transfer separation column system. The impure carbon dioxide may be derived from, for example, flue gas from an oxyfuel combustion process or waste gas from a hydrogen (“H2”) PSA system.

Abstract: Systems and processes utilize one or more methods of providing overhead waste process heat to increase the feed temperature of the hot solvent stripping regeneration loop in an acid gas removal process. A heated rich solvent stream can be the primary feed for the hot solvent stripping regeneration loop, and one or more slip streams can be heated and then combined with the heated rich solvent stream to form a combined rich solvent stream prior to further processing in downstream units to remove acid gas from the solvent. A first slip stream can be heated in a stripper gas heat exchanger by heat exchange with a stripped gas stream. A second slip stream can be heated in a regenerator exchanger by heat exchange with an acid gas stream. A third slip stream can be heated in a recycle gas exchanger by heat exchange with a compressed recycle gas stream.

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. The absorbent solution laden with acid compounds is then heated in E1 and E3 so as to separate two fractions in BS1: a first absorbent solution fraction depleted in acid compounds and a second absorbent solution fraction enriched in acid compounds. 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. According to the invention, an absorbent solution portion circulating in C1 is cooled in E2 in order to prevent demixing of the solution in column C1.

Abstract: The invention relates to a method for cooling rising vapor (3) in a desorption column (2) by means of a condenser, which is situated at the head of the desorption column, is configured as an indirect heat exchanger and is traversed by a coolant (1). According to said method, the coolant enters at the bottom of the condenser (1) and flows upwards through conduits (8) that are arranged vertically in the condenser. The coolant is enriched with hydrogen sulphide prior to its entry into the condenser (1) and after the absorption of heat, escapes as an overflow (6) from the top of the condenser (1) through upper openings (10) of the conduits (8). The invention also relates to a desorption column (2) for carrying out said method.

Abstract: An improved apparatus and method for use with a natural gas dehydrator. The apparatus and method of the invention provide for recirculation of gaseous or combustible materials so that they are not released into the atmosphere and to provide fuel for the process. Likewise, liquid hydrocarbons are collected. Various components, including separators, an absorber, wet glycol, dry glycol, an effluent condenser, heat exchangers, and a reboiler are utilized in accordance with the present invention.

Abstract: In a process using a hydrophilic liquid desiccant, for dehydrating a gas containing water with regeneration of the steps of: (a) absorbing water by contact between the moist gas and regenerated liquid desiccant from step c), producing a dry gaseous effluent and a stream of liquid desiccant charged with water and absorbed gases; (b) regenerating the liquid desiccant charged with water in a regeneration zone constituting a reboiling zone and a distillation zone, the charged liquid desiccant being sent to said distillation zone, from which a vapor containing water leaves overhead and from which liquid desiccant still containing water leaves from the bottom in the reboiling zone; (c) passing the liquid desiccant from the reboiling zone of step b) and still containing water to an absorption zone, in which the water in the desiccant is vaporized and the water vapor is absorbed by a fraction of regenerated or non regenerated desiccant, passing the resultant desiccant which has absorbed water vapor to the reboiling z

Abstract: A glycol regenerating system wherein a pressurized reboiler is introduced to a typical prior art system, the pressurized reboiler being in the glycol stream upstream from the conventional atmospheric reboiler. The pressurized reboiler heats the rich glycol coming from the glycol contactor from about 300° F. to 400° F. and keeps the glycol under pressure from about 10-25 psig. in order to first distill and condense VOCs (volatile organic compounds) which constitute non-condensable hydrocarbons and condensable hydrocarbons such as BTEX (Benzene, Toluene, Ethylbenzene, Xylene) compounds, the components being conveniently under pressure for transporting the components to a desired location.

Abstract: A process is disclosed for treating the scrubbing water from the gas scrubbing process in an iron ore reduction plant. The scrubbing water is brought into direct contact with the gas in two gas scrubbers arranged in two successive scrubbing stages at the gas-side, is withdrawn from the gas scrubbers and is supplied again to the gas scrubbers after the solids it contains are separated, and after it is treated and cooled. The scrubbing water is separately withdrawn from the two scrubbing stages and only the scrubbing water from the first scrubbing stage is largely freed from solids in a thickener, then led into a warm water container. The scrubbing water from the second scrubbing stage is directly led into a return water container in which it releases carbon dioxide-rich flash gas led into the scrubbing water in the warm water container to enrich it with carbon dioxide.

Abstract: Apparatus for recovering volatile organic compounds (VOC) from VOC/inert gas mixtures leaving tanker holds during crude oil loading includes an absorption column 12 in which incoming VOC is absorbed into cold kerosene, a portion of the VOC rich kerosene leaving the absorption column being cooled in a cooler 88 and returned to the absorption column to contact incoming VOC/inert gas mixture and absorb further VOC. The remainder of the rich kerosene leaving the absorption column 12 passes to a buffer tank 34 where it is held. It is then pumped to an elevated pressure distillation (stripper) column 46, where VOC is separated from the kerosene by conventional rectification. VOC vapor leaving the top of the distillation column is condensed in condenser 72 and held in the VOC reflux tank 76. Liquid VOC from the reflux tank is passed to a crude oil pipeline 82; a portion of the liquid VOC from the reflux tank enters the top of the distillation column to act as reflux.

Abstract: A process for dehydrating a natural gas or refinery gas containing water and BTEX using a liquid desiccant (glycol) and including regeneration provides the following steps:(a) absorption of the water and the BTEX by contacting the gas with the liquid desiccant which has been regenerated in step (c), producing a dry gaseous effluent and the liquid desiccant charged with water and BTEX;(b) separating the charged liquid desiccant into a vapor containing a portion of the BTEX and a liquid phase containing mainly desiccant charged with water and BTEX;(c) regenerating the liquid desiccant in a distillation zone from which a vapor containing water and BTEX and regenerated liquid desiccant are extracted, the latter being sent to absorption step (a);(d) condensing the vapor from the distillation zone and separating it into three phases: a gaseous effluent containing BTEX, a liquid hydrocarbon phase containing BTEX, and an aqueous liquid phase; and(e) washing the gaseous effluent by absorbing the BTEX in a fraction of

Abstract: A vapor recovery system for hydrocarbon storage tanks captures VOCs (volatile organic compounds) which would otherwise escape to the atmosphere, thereby reducing pollutant emissions to the environment. The system includes a wash chamber, where the VOC vapors are sprayed with water at or below ambient temperature to condense the vapors from the air. The liquid hydrocarbons and water then drain downwardly into an accumulator. Due to the immiscibility of water and hydrocarbon fuels, particularly those having high aromatic content such as gasoline, the liquid VOCs are drained off and returned to the storage tank while the water is recycled for further spray cooling of vapors. The spray chamber is also surrounded by a coolant jacket, through which a coolant (water or other suitable liquid) below ambient temperature is circulated. This further reduces the temperature in the spray chamber, to condense additional VOCs and water from the air, as well as cooling the spray water.

Abstract: An apparatus for extracting condensable materials from exhaust gases which are produced by combustion. In a steam injected gas turbine driven powerplant, water is extracted from the exhaust gasses and returned to the cycle for steam raising and injection into the combustor. Exhaust gases pass flow co-currently with a cold water fog, water vapor in the fog condenses on the fog drops, the flow passes through a de-mister coalescing the drops so as to produce a warm rain of condensate, the condensate is cooled with a heat exchanger using a cooling medium such as seawater, and the cooled condensate is returned to the cycle.

Abstract: A method of low temperature regeneration of glycol used for dehydrating natural gas in a glycol dehydration system including the steps of passing natural gas against flowing glycol in an absorber vessel so that the glycol absorbs water from the gas, providing spent glycol and dehydrated gas, conducting the spent glycol into a reboiler vessel, feeding a portion of the dehydrated gas into a burner positioned within the reboiler vessel where the dehydrated gas is combusted to heat the spent glycol, conducting a first portion of dehydrated gas into a gas distributor located within a lower portion of the reboiler vessel, the gas distributor causing small bubbles of gas to move upwardly through the spent glycol within the reboiler to augment separation of water from the heated glycol, conducting a second portion of the dehydrated gas into an upper gas stripper vessel mounted within an upper portion of the reboiler vessel to contact the dehydrated gas with the spent glycol to further augment the separation of water

Abstract: A method and system for reducing emissions from glycol dehydrators which employ a vapor-liquid contactor operated under ambient conditions to treat the organic vapors and liquids exiting from a condenser attached to the vapor vent of the glycol reboiler. A stream of the organic liquids is passed to the top of the contactor and allowed to descend in counter-current relation to the upward moving gas introduced at the bottom portion of the contactor. Liquids containing a relatively high content of hydrocarbons may be recovered from the bottom of the contactor, and vapors having a reduced content of organic emissions can be emitted directly to the atmosphere from the top the contactor.

Abstract: A method and apparatus for powering a fluid pump (P) for circulation of a regenerated liquid absorber from a treating vessel or regenerator (R) to a liquid/gas contacting vessel (T) where the liquid absorber removes a predetermined component from a gas. The fluid pump (P) is driven by a shaft from fluid motor (M) and an auxiliary electric motor (E, E-1) assisting the fluid motor (M). The fluid pump (P) receives the entire output of regenerated liquid absorber from the regenerator (R) for pumping the regenerated liquid absorber to the contacting vessel (T). A bypass fluid conduit (49, 48) is utilized for initial circulation of glycol during the start up operation. A glycol measuring device (42) is effective for removing trapped air in conduits (18, 15) between the reboiler (R) and the contactor (T), and in bypass conduits (48, 49) in addition to measuring the flow rate for the liquid absorber.

Abstract: When a vapor-phase mixture is brought in contact with a liquid absorbent kept at a temperature above the condensation temperature of the vapor-phase mixture, the vapor-phase mixture becomes concentrated for those components which are absorbed by the absorbent in small or negligible amounts. In the method according to the invention, the regeneration of the absorbent essentially utilizes the heat of absorption of the absorbed components. The actual absorption process can be isothermal or adiabatic or a combination of these. The method is particularly suited to the separation of vapor-phase mixtures of minimum boiling point azeotropes.

Abstract: A method of dehydrating natural gas and for reducing emissions of hydrocarbon aromatics including the steps of passing natural gas upwardly in an absorber against downwardly flowing liquid desiccant to provide treated gas, the desiccant absorbing water and hydrocarbon impurities from the gas and forming spent desiccant, passing a portion of the treated gas from the absorber through a desiccant stripper vessel, the balance of the treated gas being passed for distribution, heating the spent desiccant and passing it downwardly through the desiccant stripper vessel to purge the spent desiccant of hydrocarbon aromatics, conducting the spent desiccant from the stripper vessel into a reboiler to again heat the spent desiccant and conveying treated gas from the stripper vessel to a burner in the reboiler where the treated gas is combusted with air, the spent desiccant is being heated in the reboiler to boil off entrained water to provide a regenerated desiccant that is recirculated back to the absorber.

Abstract: In a gas dehydration system utilizing glycol in which a condensate skimming reflux column mounted on a gas fuel burner and heat exchanger unit separates and skims natural gas condensate off glycol in a settling tank-type reservoir, a fluid scrubber and separator interposed in series in a heat exchanger to reflux column wet glycol return line collects and transfers gas to the fuel burner.