Abstract: A CO2 recovery system includes an absorption tower and a regeneration tower. CO2 rich solution is produced in the absorption tower by absorbing CO2 from CO2-containing gas. The CO2 rich solution is conveyed to the regeneration tower where lean solution is produced from the rich solution by removing CO2. A reclaimer heats the lean solution that is produced in the regeneration tower to produce a condensed waste-product from the lean solution by condensing a depleted material contained in the lean solution, and removes the condensed waste-product. A cooler cools the condensed waste-product.

Abstract: Produced natural gas containing carbon dioxide is dehydrated and chilled to liquefy the carbon dioxide and then fractionated to produce a waste stream of liquid carbon dioxide and hydrogen sulfide. Natural gas liquids may be first separated and removed before fractionation. After fractionation, the waste stream is pressurized and transmitted to a remote injection well for injection either for disposal of the waste stream and preferably to urge hydrocarbons toward the producing well. A hydrocarbon stream proceeds from fractionation to a methanol absorber system which removes carbon dioxide gas. The hydrocarbon stream is thereafter separated into at least hydrocarbon gas, nitrogen and helium. Some of the nitrogen is reintroduced into a fractionation tower to enhance the recovery of hydrocarbons. A methanol recovery system is provided to recover and reuse the methanol. The hydrocarbons are sold as natural gas and the helium is recovered and sold. Excess nitrogen is vented.

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 solution contained in a regeneration tower is supplied to a filtering unit. The filter unit filters out solid particles contained in the solution. A washing unit washes out with backwash water solid particles filtered out by the filter unit. An evaporating unit receives the backwash water containing the solid particles, and heats received backwash water thereby obtaining solid-particles concentrated backwash water.

Abstract: Process for the dehydration of gases, comprising: absorbing water vapor by means of a hygroscopic liquid consisting essentially of one or more C2-C8 glycols and an additive capable of forming a minimum type azeotrope with water; distilling the glycol/water/additive mixture to obtain a top product consisting mainly of the water/additive azeotropic mixture and a bottom product consisting mainly of glycol and additive (hygroscopic liquid); recycling the regenerated hygroscopic liquid to the absorption stage.

Abstract: The invention relates to the removal of acid compounds from a gaseous effluent in an absorption method using an aqueous solution of N,N,N?,N?-tetramethylhexane-1,6-diamine formulated with a particular primary or secondary amine, allowing to obtain a single-phase absorbent solution under the absorption conditions of acid gases such as CO2. The invention is advantageously applied to the treatment of natural gas and of gas of industrial origin.

Abstract: An apparatus and method for absorbing and recovering carbon dioxide from flue gas using ammonia water as an absorbent, including an absorption column and a circulation cooler connected to the absorption column so that a high-temperature absorbent is recovered from the absorption column, cooled to a preset temperature, and then supplied again into the absorption column, in order to dissipate absorptive heat generated when carbon dioxide is absorbed from the flue gas.

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: A liquid desiccant regenerator system, including a desiccant/air heat exchanger having a first desiccant inlet and a desiccant reservoir. The reservoir has a first desiccant outlet, a second desiccant outlet and a second desiccant inlet. The first desiccant inlet and the first desiccant outlet are connectable to a heat source, the second desiccant inlet conducts diluted desiccant of the reservoir and the second desiccant outlet conducts concentrated desiccant from the reservoir. The second desiccant inlet and the desiccant outlet are connected to a desiccant/desiccant heat exchanger for applying heat to the diluted desiccant flowing into the reservoir. A dehumidification method is also provided.

Abstract: A CO2 recovery system includes an absorption tower that removes CO2 from exhaust gas, a regeneration tower that regenerates a rich solution, and a separation drum that condensates steam in CO2 gas released from the regeneration tower and separates water. The CO2 recovery system further includes a filtration membrane apparatus that filters solid content remaining in the lean solution using a filter, and cleans the filter using condensed water as cleaning water and again return the condensed water into the system. The CO2-absorbing solution attached to the filter is collected and the filter is cleaned without diluting the CO2-absorbing solution upon replacement of the filter.

Abstract: Produced natural gas containing carbon dioxide is dehydrated and chilled to liquefy the carbon dioxide and then fractionated to produce a waste stream of liquid carbon dioxide and hydrogen sulfide. Natural gas liquids may be first separated and removed before fractionation. After fractionation, the waste stream is pressurized and transmitted to a remote injection well for injection either for disposal of the waste stream and preferably to urge hydrocarbons toward the producing well. A hydrocarbon stream proceeds from fractionation to a methanol absorber system which removes carbon dioxide gas. The hydrocarbon stream is thereafter separated into at least hydrocarbon gas, nitrogen and helium. Some of the nitrogen is reintroduced into a fractionation tower to enhance the recovery of hydrocarbons. A methanol recovery system is provided to recover and reuse the methanol. The hydrocarbons are sold as natural gas; and the helium is recovered and sold. Excess nitrogen is vented.

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: A first contaminant selected from oxygen and carbon monoxide is removed from impure liquid carbon dioxide using a mass transfer separation column system which is reboiled by indirect heat exchange against crude carbon dioxide fluid, the impure liquid carbon dioxide having a greater concentration of carbon dioxide than the crude carbon dioxide fluid. The invention has particular application in the recovery of carbon dioxide from flue gas generated in an oxyfuel combustion process or waste gas from a hydrogen PSA process. Advantages include reducing the level of the first contaminant to not more than 1000 ppm.

Abstract: A process for removing carbon dioxide from a gas stream by scrubbing the carbon dioxide from the gas stream with a mixture of ammonium and alkali carbonates such as sodium carbonate and/or potassium carbonate. Using the mixed alkali carbonate solution as the CO2 scrubbing solution offers the opportunity for both low regeneration energy and low ammonia volatility while still maintaining a high rate of CO2 hydration.

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: A method of regenerating liquid desiccant used in the dehydration or sweetening of gases. A first step involves boiling wet liquid desiccant containing water to create lean liquid desiccant. A second step involves introducing the lean liquid desiccant via a liquid seal pot into a water exhausting stripping column. The hot lean liquid desiccant cascades down the stripping column and evolving equilibrium vapors rise up the stripping column. A third step involves directing the rising equilibrium vapor into a condenser in which the vapor undergoes cooling with a resulting phase change back to liquid. The phase change from vapor to liquid reduces pressure in the condenser, which draws more evolving vapor from the lean liquid desiccant cascading down the stripping column upwards into the condenser, thereby further reducing the water content of the lean liquid desiccant to create a very lean liquid desiccant.

Abstract: The natural gas is successively contacted in column CA with a relatively methanol-rich solvent flowing in through line 4, then with a relatively poor solvent flowing in through line 9. The acid gas-containing solvent recovered through line 3 at the bottom of column CA is expanded through valves V1 and V2 to release acid gases through line 6. A fraction of the expanded solvent is distilled in column CR. The regenerated solvent obtained at the bottom of column CR is sent to the top of column CA through line 9. A second fraction of the expanded solvent is mixed with a solvent drawn off from column CR at an intermediate point between the bottom and the top of this column. This mixture of solvents is sent through line 4 into column CA.

Abstract: An improved method and apparatus for oxidizing undesired compounds residing within a liquid glycol based absorbent wherein the compounds are heated within a reboiler chamber to their boiling point to effectuate production of vaporized effluents. The absorbent's vaporized effluents rise upwardly exiting the reboiler chamber and enter a reflux tower wherein they are partially condensed via a condenser embodied within the interior of the tower. The residual uncondensed effluents are then transported to and first heated via a vaporizer/heat exchanger, thus effectuating the vaporization of any ambient condensed liquids contained within the effluents. The revaporized effluents then enter the invention's thermal oxidizer combustion chamber where they are second heated to a temperature necessary to effectuate destruction of undesirable compounds, such as but not limited to benzene, toluene and xylene.

Abstract: In a process for dehydration/fractionation of a wet natural gas containing heavy constituents and light constituents, In the presence of methanol, aqueous liquid phases are combined and the resultant combined aqueous liquid phase contacted with the first part of the gas to be scrubbed, which carries along the major part of the methanol, which allows to collect practically pure water. Before this step, all or part of one or both of the aqueous liquid phases and/or all or part of the aqueous liquid phase from a washing zone is sent to a distillation stage where practically pure methanol is collected at the top and a methanol-depleted aqueous liquid phase is collected at the bottom prior to being sent back to the first stage or used for the washing stage.

Abstract: Process for dehydrating/fractionating a low-pressure wet natural gas containing “heavy” constituents and “light” constituents includes a stage a) in which at least a fraction of the wet gas at temperature T0 is contacted with an aqueous liquid phase L'1 containing methanol, the gas carrying along substantially all of the methanol contained in phase L'1. In a stage b), the gas from stage (a) is cooled to a temperature T1 lower than temperature T0, producing a gas phase G1 at equilibrium with a hydrocarbon-containing liquid phase L1 containing C3+ and an aqueous liquid phase L'1 containing methanol. In stage c), phase L'1 is sent to stage (a), and in stage d), said phase G1 is fractionated by distillation carried out by continuous thermal exchange with a cooling fluid, so as to extract the “light” constituents (gas phase G2) and the “heavy” constituents (condensed phase L2).

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: The gas which is to be dried is fed into an absorber (1) where it is brought into contact with a glycol in countercurrent. The glycol absorbs the moisture from the gas and impurities. The glycol laden with water and impurities is removed from the absorber (1) via a line (5). It is then regenerated in a reboiler (9) where the water is eliminated by heating. The water-free glycol is passed into a storage vessel (10) from which it can then be refed to the absorber (1). The glycol which is withdrawn from the storage vessel (10) is purified by mixing it with at least half the quantity of water. The mixture is brought to a temperature above cloud point where it is maintained for a predetermined length of time so that the impurities flocculate. The flocculated impurities are removed in a filter (18) arid the purified glycol mixed with water is refed to the reboiler (9) via a line (19). The drying process is very economical as it integrates environmentally-friendly and simple purification of the glycol.

Abstract: Apparatus for use with a natural gas dehydrator wherein a portion of the wet glycol in an emissions separator is pumped under pressure as circulating wet glycol which may be used as a coolant for effluent removed from a reboiler and/or a power source for an eductor to form a vacuum in a first chamber of a liquid water removal separator apparatus. The cooled effluent, comprising at least liquid water, liquid hydrocarbons and uncondensed vapors, moves into the first chamber wherein the liquid water and/or the liquid hydrocarbons are separated from the uncondensed vapors. At least, the uncondensed vapors are removed from the first chamber and move into the eductor wherein they are compressed and combined into the circulating wet glycol. The separated liquid water is transferred to a second chamber of the liquid water removal separator apparatus and then removed therefrom. In some instances, the liquid hydrocarbons are transferred to a third chamber and removed therefrom.

Abstract: A process and a device for separating ethane and ethylene from a hydrocarbon steam-cracking effluent is described. Effluent (1) is absorbed in an absorption column (7) by a cooled solvent (9). At the bottom of the column, liquid phase (12) that contains the solvent and the C2+ hydrocarbons is recovered and hydrogenated (15). The hydrogenation effluent that contains the solvent is introduced into a first distillation column (70) where the solvent is regenerated. The solvent is cooled and recycled at the top of absorption column (7). The C2+ hydrocarbons are collected at the top, and a condensed liquid phase is distilled in a second distillation column (77) to recover a C2 fraction that consists of ethane and ethylene.

Abstract: A process for separating ethane and ethylene from a hydrocarbon steam-cracking effluent is described. Effluent (1) is absorbed in an absorption column by a cooled solvent (9). At the bottom of the column, the liquid phase that contains the solvent and the C2+ hydrocarbons is recovered and hydrogenated (15). The hydrogenation effluent that contains the solvent is introduced into a first distillation column (16). Ethane-ethylene mixture (17) is drawn off laterally from the column, and a phase (19) that contains the solvent and hydrocarbons with at least 3 carbon atoms is drawn off at the bottom of the column. This phase (19) is separated in a second distillation column (22), and C3+ hydrocarbons and, at the bottom of the column, regenerated solvent (26) that is cooled and that is recycled (9, 52) in the absorption column are collected.

Abstract: There is described a method for regeneration of triethylene glycol (TEG) that has been used as a drying medium to remove water from a fluid such as natural gas, where a drier TEG is recovered at the bottom fraction in a regeneration column (7), where water vapor together with other gases is removed at the top fraction and where the partially dried TEG from the regeneration column (7) optionally is also supplied to a stripping column (9) for further dehydration, where in the optional stripping column (9) and in the still column (7) there is supplied a stripping gas in countercurrent to the TEG stream, where as stripping gas there is mainly used gas which is recovered from the top fraction from the regeneration column (7). There is also described an apparatus for carrying out the method.

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 of separating water from ambient air involves a liquid desiccant to first withdraw water from air and treatment of the liquid desiccant to produce water and regenerated desiccant. Water lean air is released to the atmosphere. Heat generated in the process is recycled. The drying capacity, or volume of water produced, of the system for a given energy input is favored over the production of dried air.

Abstract: A process for the purification of an aqueous alkanolamine which process involves subjecting the alkanolamine to a distillation process carried out in one or more film-type evaporators and involves at least two steps, wherein in the first step water is removed from the aqueous alkanolamine and in the second step the de-watered alkanolamine is further purified.

Abstract: Contaminated glycol is refined by vacuum distillation. Specifically the evaporator is heated to a temperature below the degradation temperature of the glycol. The vacuum is used to bring the flashpoint down sufficiently so that glycol evaporates or flashes at that temperature. The glycol is condensed and filtered through activated granular carbon. The principal use of refining the glycol is to refine the triethylene glycol used in natural gas dehydration plants. For such purposes the equipment is mounted upon a trailer to be taken to the plant for cleaning glycol. In such instance, in addition to refining the glycol, a cleaning agent (which contains a degreaser) is added to the refined glycol. The glycol is refined while the natural gas dehydration plant is in normal operation and therefore it is not necessary to stop the natural gas dehydration plant for refining the glycol used therein.

Abstract: A process for the dehydration, deacidification and stripping of a gas, characterized in that:(a) at least one fraction of the gas is contacted with an aqueous phase containing methanol, the resultant gas being thus charged with methanol being withdrawn from stage (a);(b) the gas withdrawn from stage (a) is contacted with a mixture of solvents comprising methanol, water, and a solvent heavier than methanol, the gas leaving stage (b) being thus at least in part freed of the acid gases which it contained initially;(c) the mixture of solvent obtained from stage (b) is at least in part generated by special reduction and/or heating while liberating at least part of the acid gases, the mixture of solvent being at least partially regenerated, or being at the outlet of stage (c) recycled through stage (b); and(d) the gas obtained from (stage b) is refrigerated while producing at least an aqueous phase containing methanol which is at least in part recycled through stage (a).

Abstract: A gas drying method is disclosed in which gas streams are dehydrated to low dew points by contacting the wet gas with a dry liquid desiccant, with the liquid desiccant regenerated by heating it in a reboiler containing an internal reboiler vapor condenser and stripping it with a stripping agent that is dried with solid desiccant.

Abstract: An environmentally safe apparatus for reclaiming uncondensed hydrocarbons normally exhausted to the atmosphere from the still column of a glycol dehydrator system, and utilizing the uncondensed hydrocarbons as fuel in the burner of a reboiler fire-tube by natural draft of the fire-tube exhaust stack.

Abstract: A gas drying method is disclosed in which gas streams are dehydrated to low dew points by contacting the wet gas with a dry liquid desiccant, with the liquid desiccant regenerated by heating it and stripping it with a stripping agent that is dried with solid desiccant.

Abstract: A method for removing volatile organics from landfill gas, in which the landfill gas, which consists primarily of methane and contains volatile organic components, is passed through a quantity of liquid tetraglyme to cause the volatile organic components to be absorbed in the tetraglyme.

Abstract: The invention relates to a process for the recovery of low molecular weight C.sub.2+ hydrocarbons, in particular ethylene and ethane from a cracking gas, in particular from a fluid catalytic cracking waste gas. In accordance with the invention the light C.sub.2+ hydrocarbons are scrubbed out of the cracking gas by absorption, using an organic, preferably paraffinic, physically acting scrubbing agent, the scrubbing agent having a molecular weight of between 50 and 75 g/mol, preferably between 60 and 75 g/mol. Particularly suitable as scrubbing agents are pentane, isopentane or mixtures thereof. Prior to the generation of the loaded scrubbing agent, co-extracted methane is advantageously stripped off.

Abstract: A method of separating a mixture of gases by the following stages:a) absorbing a part G2 of a gas mixture G1 by a solvent L1 in an absorption zone C1;b) expanding the solvent L1, leading to partial vaporization of the absorbed gases G2 and cooling of the solvent L1;c) desorbing the gas fraction G2 in a desorption apparatus D1 having a reboiling zone B1 and an internal heat exchange zone Z1, wherein the solvent L1 from stage (b) is circulated in countercurrent contact with the vapor phase, and simultaneously has counter-current heat exchange with the solvent phase from the reboiling zone B1;d) passing the regenerated solvent leaving the reboiling zone B1 into the heat exchange zone Z1, and transferring the regenerated solvent to the top of said internal heat exchange zone; ande) recycling the regenerated solvent to the absorption zone C1.

Abstract: An apparatus for extracting moisture from the ambient air includes a desint pond for absorbing moisture from the air to produce a water rich desiccant, means for vaporizing the moisture in the water rich desiccant, mixing the vaporized moisture with ambient air to increase the dew point of the ambient air, condensing the vaporized moisture to form a potable water condensate and returning the water lean desiccant back to the desiccant pond.