Abstract: A process for the removal and recovery of carbon dioxide from a gaseous stream, in particular the removal and recovery of carbon dioxide, and optionally hydrogen sulphide, from a natural and/or synthesis gas stream. Furthermore, the present invention provides for the release of the removed and recovered carbon dioxide, and optionally hydrogen sulphide, at an elevated pressure, thereby reducing the high carbon dioxide compression costs associated with further chemical processing e.g. for under-ground carbon sequestration and/or for subsurface enhanced hydrocarbon recovery and/or for the manufacture of urea.

Abstract: The present invention relates to a pressure swing adsorption process, also known as PSA process, which is modified with a view to utilizing the heat from the post-adsorption stream coming from the molecular sieves to heat/vaporize the pre-adsorption stream containing the hydrated product or the mixture component(s) to be adsorbed in said sieves. The present invention provides alternative arrangements for the heat exchanger system in order to use the thermal potential of the post-adsorption stream with the elimination or minimization of the risk of a slug flow regime in the exchangers, the so-called “gush,” which would be a natural result from the periodic oscillation characteristic of PSA processes. With this, the vapor consumption with the modified process according to the present invention is considerably reduced.

Abstract: A method for treating a gas mixture containing acid gases is provided, comprising: contacting the gas mixture with an absorbing solution, by means of which a de-acidified gas mixture and an absorbing solution loaded with acid gases may be obtained; and regenerating the absorbing solution loaded with acid gases; wherein the regeneration comprises the following steps: passing the absorbing solution into a first regenerator at a first pressure; and then passing the absorbing solution into a second regenerator at a second pressure, less than the first pressure; and compressing the gases from the second regenerator and recycling the thereby compressed gases to the first regenerator, subsequent to passing into the second regenerator, passing the absorbing solution into a third regenerator at a third pressure less than the second pressure; and compressing the gases from the third regenerator and recycling the thereby compressed gases to the second regenerator; and wherein at least a portion of the gases from the

Abstract: A method for removing CO2 from a pressurized gas stream with the effluent CO2 remaining at system pressure or higher is disclosed. Specifically, the removal method provides near isothermal absorption of CO2 from a gas stream in a suitable solvent at an elevated pressure and relatively low temperature. The solvent is then removed from contact with the gas stream, and the temperature is increased to such an extent that the CO2 will flash from the solvent.

Abstract: With the help of a method of selective removal of hydrogen sulphides, organic sulphur components and CO2 from crude gases, by using a first and second absorption stage (41 or 49) for separating almost pure CO2, a solution has to be found, with which, among other things, hydrogen sulphides and organic sulphur compounds can be removed in as selective a manner as possible. This is achieved as follows: the absorption agent coming out of the first absorption stage (41) and enriched with hydrogen sulphide and CO2 a.o.

Abstract: The present invention relates to a method of removing acid gases, notably carbonyl sulfide, contained in gaseous effluents, comprising: an acid gas absorption stage by contacting the gaseous effluent with an aqueous solution comprising 2-[2-amino-1-(aminomethyl)ethoxy]ethanol, and possibly another alkanolamine and an organic compound, and at least one aqueous solution regeneration stage. The method can comprise a second aqueous solution regeneration stage. The regeneration stages are carried out by expansion and/or thermal regeneration.

Abstract: Contemplated configurations and methods include a solvent regenerator (58) that has an upper (93) and a lower stripping section (94). Cooled rich solve is used as reflux while heated rich solvent (11) is used as a source of stripping agent in the upper section (91). A reboiler (62) in the lower section provides further stripping agent, hi especially preferred configurations, a portion of lean solved from the regenerator (58) is further stripped in a separate or integrated regenerator (62) to form an ultra-lean solvent. Both lean and ultra-lean solvents are preferably used in a two-stage absorber (52) to thereby from the rich solvent and an offgas that is very low in acid gas.

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 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: A process for pretreating a very acid natural gas containing a substantial amount of hydrogen sulfide (H2S), possibly combined with carbon dioxide (CO2), includes at least a stage wherein the initial natural gas is contacted in a distillation column with a liquid condensate itself resulting from cooling of the gaseous fraction obtained during the contacting stage. This solution allows to eventually recover at a lower cost a gas enriched in methane, depleted in hydrogen sulfide and freed from substantially all of the water it contains, and a liquid phase containing most of the hydrogen sulfide, substantially all of the water and depleted in hydrocarbon. Control of the thermodynamic conditions during the stages that characterize the process, according to the water content of the gas during treatment, allows progressive exhaustion of the water contained in the gas while preventing hydrates formation.

Abstract: An improved methane wash cycle is disclosed wherein a reduced amount of methane wash is required, thereby allowing for savings in energy costs in operation of the cycle and capital costs in constructing the cycle. Further embodiments allow for an energy recovery and an enhanced recovery of a carbon monoxide and/or hydrogen product.

Abstract: A system for removing water from natural gas which comprises: bringing the natural gas into contact with a liquid including an absorbent for the water; subjecting the natural gas and liquid to turbulent mixing conditions thereby causing the water to be absorbed by the absorbent; and separating a natural gas phase with reduced water content and a liquid phase including the absorbent and absorbed water. The mixing is conducted in a turbulent contactor (11) including a gas inlet (15), a liquid inlet (16), an outlet (104) leading to a venturi passage (105) and a tube (106) extending from the outlet (104) back upstream. The tube (106) may be perforated and/or spaced from the periphery of the outlet (104).

Abstract: In a process for treating a gas containing acid gases, the gas is contacted with a methanol-containing aqueous phase and is then contacted in an absorption column with a mixture of solvents including mehtanol, water and a solvent heavier than methanol. Then, the mixture of solvents is at least partly regenerated through pressure reduction and/or heating. The treated gas is cooled by producing at least a methanol-containing aqueous phase that is at least partly recycled. The mixture of solvents flowing out at the bottom of the absorption column is cooled, then re-introduced at a higher level of the absorption column so as to control the temperature in the absorption column.

Abstract: Scrubber liquid from an ethylene oxide process rich in bicarbonate and dissolved ethylene is flashed in two stages to separate ethylene containing vapor from bicarbonate rich solution reduced in ethylene content.

Abstract: In a process intended for dehydration/fractionation of a wet natural gas containing <<heavy>> constituents and <<light>> constituents, in the presence of methanol, which comprises at least the following stages

Abstract: Process for the removal of metal cabonyls before regeneration of a desulfurization wash liquid, which includes removing a part of the carbon monoxide from the wash liquid, conversion of the metal carbonyls to metal sulfides, passing the wash liquid through a reaction and settling zone, removing metal sulfide-containing sludge from the reaction and settling zone, and regenerating the wash liquid.

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: 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: Process for pretreating a very acid natural gas containing a substantial amount of hydrogen sulfide (H2S), possibly combined with carbon dioxide (CO2), comprising at least a stage wherein the initial natural gas is contacted in a distillation column with a liquid condensate itself resulting from cooling of the gaseous fraction obtained during said contacting stage. This solution allows to eventually recover at a lower cost a gas enriched in methane, depleted in hydrogen sulfide and freed from substantially all of the water it contains, and a liquid phase containing most of the hydrogen sulfide, substantially all of the water and depleted in hydrocarbon. Control of the thermodynamic conditions during the stages that characterize the process, according to the water content of the gas during treatment, allows progressive exhaustion of the water contained in said gas while preventing hydrates formation.

Abstract: Process for treating a gas containing acid gases, wherein:

Abstract: A regenerative process for deacidification of a gas containing CO2 and liquid hydrocarbons including contacting the gas to be treated, in an absorption zone, with an absorbent liquid including methyldiethanolamine (MDEA) and an accelerator of absorption of CO2 by the amine, thereby producing a treated gas with reduced CO2 content and an absorbent liquid loaded with CO2, subjecting the loaded absorbent liquid to a regeneration treatment to release CO2 which it has bound, to produce 1) at least one acid gas fraction rich in CO2 and 2) at least one regenerated absorbent liquid; and recycling into the absorption zone the at least one regenerated absorbent liquid, wherein the overall liquid hydrocarbon content in the gas to be deacidified containing CO2 is greater than 14 liters of liquid hydrocarbons per million standard cubic meters of gas, and the activator combined with methyldiethanolamine in the absorbent liquid brought into contact with the gas containing CO2 and liquid hydrocarbons consists of at least one

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: The need to filter gas emanating from a containment vessel is reduced or eliminated by maintaining, within the vessel, a gradient that concentrates most of the gaseous contaminants away from the vessel exits. This is achieved by reducing the density of gas drawn from the region near its source and discharging the reduced-density gas to another region of the vessel. Owing to its reduced density, the discharged gas already has a lower contaminant concentration than the source gas. The concentration decreases further as convection draws the discharged gas back to its source. So long as the gas flows within the containment vessel are non-turbulent, the concentration gradient remains substantially static, and the vents remain exposed only to low concentrations of contaminants. The gas density may be reduced by heating and humidification, catalytic reaction, or reaction among constituents of the gas.

Abstract: A system for cleaning a carbon dioxide gas stream of water soluble contaminants with improved recovery of carbon dioxide wherein the water soluble contaminants are removed into countercurrently flowing water which undergoes at least one pressure reduction step releasing absorbed carbon dioxide for recapture and recycle into the carbon dioxide gas stream.

Abstract: A method is provided for the extraction of aromatic hydrocarbons, including benzene, toluene, ethylbenzene, and xylene, collectively known as “BTEX,” in a continuous process utilizing a glycol contactor to cause absorption of the BTEX upstream of an amine-based gas sweetening process. The preferred glycol for BTEX absorption is triethylene glycol. The glycol used in the glycol contactor for BTEX extraction may either be fully regenerated (dry), or wet glycol from a downstream gas dehydration system. The method may be achieved with the use of a number of separate absorber/contactor vessels, or the method may be achieved within one combination vessel.

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 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 method is disclosed by which vapour is cleaned of gaseous impurities during evaporation of polluted liquids. Vapour is conducted via a boiler, a compressor to a heat exchanger (12) in which condensation takes place. In order to clean the vapour, a scrubber (14) is arranged between the boiler (3) and the heat exchanger (12), in which the vapour is scrubbed in several steps (17, 18) at different pH values. Thus, the step (17) is an acid step, whereas the step (18) is an alkaline step. In this manner, the vapour for condensation may be conducted into the heat exchanger and be condensed in order to remove a clean condensate without pollution of acid or alkaline substances.

Abstract: A treatment method for removing acid gases by contacting a sour gas stream with a solvent (e.g. an organic amine) which absorbs H.sub.2 S in preference to CO.sub.2 and hydrocarbons. The rich solvent is then regenerated by selectively separating the absorbed hydrocarbons in a first flash, a large portion of the CO.sub.2 in a high-temperature, low-pressure second flash tank, and the substantially all of the remaining acid gases in a high-temperature, low-pressure stripper. The regenerated solvent is recycled and the recovered acid gases are processed to recover sulphur from the H.sub.2 S. The CO.sub.2 recovered from the second tank is contacted with a second solvent to provide high-quality CO.sub.2.

Abstract: A method of treating a gas, for example, natural gas containing at least one hydrocarbon and at least one acid gas to remove the acid gas from the natural gas and to produce at least one concentrated acid gas, wherein the gas is subjected to at least two stages of absorption using polar solvents having different properties.

Abstract: The process comprises a cold absorption step 2 for removing acid gas from natural gas using a solvent phase at a pressure P.sub.2 which delivers a purified gas 5; a step for depressurizing and separating resultant acidic solvent phase containing hydrocarbons (lines 4, 11), at a pressure P.sub.12 which is lower than pressure P.sub.2 in a column-heat exchanger 12 which delivers a purified gaseous effluent 13 overhead and a further solvent phase at the bottom (line 17) which is enriched in hydrogen sulphide; and a solvent phase regeneration step carried out in a distillation column 18 at a pressure P.sub.18 and no higher than pressure P.sub.12. A gas 29 containing essentially hydrogen sulphide which is depleted in hydrocarbons is recovered from column 18 and is a suitable feed for a Claus plant for eliminating H.sub.2 S. The regenerated hot solvent phase 20 indirectly exchanges heat with the cold acidic solvent phase from absorber 2 or separator 6. It is then recycled to the absorbent after cooling.

Abstract: A method and an apparatus for cleaning a gas containing pollutants, such as hydrogen chloride and heavy metals, are described. The polluted gas (2) is contacted with an aqueous washing liquid (3) in a scrubber (1), whereupon part of the washing liquid is preevaporated in a preevaporation unit (7) to form a hydrochloric-acid-containing top fraction, which is essentially free from heavy metals, and a bottom fraction containing hydrochloric acid and heavy metals. Part of the bottom fraction is recirculated (15) for renewed preevaporation, while the remainder of the bottom fraction is treated (16) to remove any heavy metals present. The top fraction from the preevaporation is distilled in a rectification unit (22) to form a top fraction (31) and a bottom fraction (35).

Abstract: An improved process for the glycol dehydration of water-containing natural gas comprises contacting the natural gas and glycol in a contacting zone to produce a dried natural gas and a water-rich glycol, and heating the water-rich glycol in a regeneration zone to produce a water-lean glycol for reintroduction into the contacting zone and a water-containing gaseous overhead. The gaseous overhead is partially condensed and the resulting gaseous components are returned to the contacting zone. In a preferred embodiment, the glycol is further purified by contact in a separate stripping column with dry stripping gas under a pressure lower than that of the regeneration zone.