Abstract: A natural gas dehydrator wherein a portion of the wet glycol from the absorber is pumped under pressure as circulating wet glycol which is used as a coolant for effluents removed from a reboiler and a power source for an educator to form a vacuum in a first chamber of a liquid water removal separator apparatus. The cooled effluents, comprising liquid water, liquid hydrocarbons and uncondensed vapors, move in to the first chamber wherein the liquid water is separated therefrom. The liquid hydrocarbons and the uncondensed vapors are removed from the first chamber and move into the eductor wherein they are 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. Also, gases from gas emitting level control apparatus in the natural gas dehydrator are collected and fed into the first chamber.

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 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: A process for the removal of CO.sub.2 and sulfur compounds from natural gas and raw synthesis gas wherein N-formylmorpholine and N-acetylmorpholine mixtures are used as the desorbent at temperatures between -20.degree. C. and +40.degree. C. at pressures of 10 to 150 bar in a scrubbing operation. The acid gases are removed from the absorbent by flashing and the regenerated absorbent is recycled to the absorbent.

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 system for controlling organic contaminants released from a regenerator during the process of liquid dehydration of natural gas where contaminants are vaporized into a gaseous mixture. The system includes conducting the vaporized mixture from the regenerator to a heater, heating the vaporized mixture in the heater, conducting the vaporized mixture from the heater to a liquid collection chamber where suspended liquid particles are separated out from the vaporized mixture, drawing the vaporized mixture from the liquid chamber using fuel gas as an aspirator, mixing atmospheric air with the vaporized mixture, and combusting the vaporized mixture in order to incinerate the vaporized mixture.

Abstract: A method of treating a fluid containing at least methane and at least one acid gas and producing the acid gas or gases in liquid form. The method includes a step of regenerating the solvent, operated at a pressure whose value is at least equal to the bubble pressure of the mixture of acid gases produced in liquid form, a step in which the gaseous fraction from the regeneration step is rectified in a contact zone by separating at least some of the solvent from the gaseous fraction, a step in which the gaseous fraction from the modification step is cooled to a given temperature to cause at least some of the gaseous faction to condense forming at least one liquid fraction enriched with liquid acid gases and a step during which the liquid fraction of gases is separated from the remaining gaseous fraction.

Abstract: A Vertical Combined Production Facility, or gas-well production system, in which the separation of each phase (hydrocarbon gas, hydrocarbon liquids, and produced water), dehydration of natural gas, removal of minute traces of water from the hydrocarbon liquids, and polishing of produced water, are performed in a single pressure vessel. Additionally, the pressure vessel is installed in a vertical configuration such that the pressure vessel shell also serves as the structural support for a small deck and helideck. Additionally, the inlet heating of the well flow-stream is accomplished by a heat exchanger installed in the dehydration/regeneration heater (reboiler).

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: A process for separating chlorine of high purity from a chlorine-containing feed gas by absorption of the chlorine using an inert absorbent and downstream desorption of the chlorine from the absorbent/chlorine mixture drawn off from the absorption stage by the supply of mixture to a desorption distillation column which is coupled to a chlorine separation column in such a way that the top of the chlorine separation column and an upper section of the desorption distillation column and a lower section of the desorption distillation column and the bottom of the chlorine separation column are connected to one another on both the gas and the liquid side, the absorbent/chlorine mixture being supplied exclusively to the desorption distillation column, and high-purity chlorine being drawn off from a middle region of the chlorine separation column.

Abstract: A process for purifying a raw natural gas stream is provided by contacting the gas stream with an absorbant to remove water and hydrocarbon impurities, separating the water and hydrocarbon impurities and absorbant from the gas stream, separating the absorbant from the water and hydrocarbon impurities to provide a liquid absorbant stream and a water vapor and hydrocarbon vapor stream, condensing the water vapor and a portion of the hydrocarbon vapor stream to provide a mixed liquid/vapor stream, passing the mixed stream through a pump capable of pumping a mixed stream, and disposing of the thus-reduced volume, higher pressure, mixed stream. One aspect of the invention provides for the reintroduction of the mixed stream to the process with the raw natural gas, thereby eliminating volatile organic compound disposal concerns.

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: 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: 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: 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 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: An organic emissions elimination apparatus, and process for same, for substantially eliminating the emission of potentially harmful organic constituents, such as benzene, toluene and xylene ("BTX") into the ambient environment during dehydration of water bearing gas. The apparatus includes a first chamber which incorporates a membrane for use in association with a water absorbing material (such as triethylene glycol) which is operably displaceable and retained within the membrane fibers. Although the water vapors from the gas will permeate the membrane (and become absorbed by the triethylene glycol), the BTX will not be able to permeate the membrane. Accordingly, the BTX and the dehydrated gas will be discharged from the first chamber toward a point of use by conventional dehydrated gas using equipment.