Abstract: Flowing a first buffer fluid and a second buffer fluid through a heat exchanger network thermally coupled to heat sources of a Natural Gas Liquid (NGL) fractionation plant, and transferring heat from the heat sources to the first buffer fluid and the second buffer fluid. Generating power via a first sub-system thermally coupled to the heat exchanger network and generating potable water from brackish water via a second sub-system thermally coupled to the heat exchanger network.

Abstract: A process for treating an H2S- and CO2-comprising fluid stream, in which a) the fluid stream is treated in a first absorber at a pressure of 10 to 150 bar with a first substream of a regenerated H2S-selective absorbent to obtain a treated fluid stream and an H2S-laden absorbent; b) the H2S-laden absorbent is heated by indirect heat exchange with regenerated H2S-selective absorbent; c) the heated H2S-laden absorbent is decompressed to a pressure of 1.

Abstract: A process for separating undesired, in particular acidic gas constituents from a raw gas, in particular raw synthesis gas, by absorption with cold methanol as physical detergent, wherein the methanol is cooled in a compression refrigeration machine by using a multi-component coolant. The use of the coolant according to the invention provides significant advantages with regard to the compressor capacity required in the compression refrigeration machine for the provision of a defined cooling capacity.

Abstract: A method and a device for separating off an electrolyte from a first synthesis gas and a second synthesis gas, each containing an electrolyte. The two synthesis gases are each subjected in a scrubbing column to a water scrubbing, in which a substantially electrolyte-free synthesis gas and also a scrubbing water loaded with an electrolyte that has been separated off are obtained. At least a part of the scrubbing water that was loaded with an electrolyte that has been separated off in the scrubbing of the first synthesis gas is used as scrubbing medium in the scrubbing of the second synthesis gas.

Abstract: A method is provided for fractionating a feed gas containing hydrogen and carbon dioxide, from which feed gas carbon dioxide is largely selectively removed by scrubbing in a first gas scrubber using a sulphur-free scrubbing agent, wherein a scrubbing agent stream laden with carbon dioxide and co-absorbed hydrogen is obtained which is subsequently expanded in an expansion vessel in order to convert co-absorbed hydrogen into the gas phase. The characterizing feature of the method is that the hydrogen-containing gas phase is drawn off from the expansion vessel and admixed with a sulphur-free gas mixture containing hydrogen and carbon dioxide, which gas mixture arises in a second gas scrubber operated in parallel to the first as a product at a pressure which is lower than the pressure of the feed gas.

Abstract: A method for recovering methane gas from a landfill involves the use of a main absorber, a flash system, an optional ancillary absorber and an optional polishing absorber. The recovered gas is maintained at a temperature that enhances a solvent's ability to absorb carbon dioxide from the recovered gas. While the main absorber uses the solvent for absorbing most of the carbon dioxide from the recovered gas, the flash system removes much of the carbon dioxide from the solvent exiting the main absorber. In some examples, at least portion of the flash system operates at subatmospheric pressure to create a vacuum that draws in a generally inert stripper gas (e.g., air, nitrogen, etc.) at atmospheric pressure. The stripper gas helps remove carbon dioxide from the solvent in the flash system.

Abstract: A system, method, and material that enables the pressure-activated reversible chemical capture of acid gasses such as CO2 from gas volumes such as streams, flows or any other volume. Once the acid gas is chemically captured, the resulting product typically a zwitterionic salt, can be subjected to a reduced pressure whereupon the resulting product will release the captures acid gas and the capture material will be regenerated. The invention includes this process as well as the materials and systems for carrying out and enabling this process.

Abstract: The invention relates to a method for operating a gas scrubber, in which a feed gas (1) containing hydrogen, carbon monoxide, carbon dioxide and carbonyl sulfide and/or hydrogen sulfide is scrubbed in a scrubbing apparatus (A1) using a scrubbing agent (3, 4) preladen with carbon dioxide in order largely selectively to separate the sulfur components from the feed gas and to produce a desulfurized gas stream (5, 9). The invention is distinguished in that a sulfur-free scrubbing agent (3, 4) is used which, on introduction thereof into the scrubbing apparatus (A1), has a carbon dioxide partial pressure which is greater than or equal to the carbon dioxide partial pressure in the feed gas (1) to be desulfurized.

Abstract: Physical solvent is regenerated using flashing and stripping processes to produce an ultra-lean solvent. In especially preferred aspects, flashed C1-C3 hydrocarbons are recycled to the absorber, while C4+ hydrocarbons are recovered from the CO2 that is removed from the solvent. It is further preferred that depressurization of the rich solvent provides most of the refrigeration duty.

Abstract: A natural gas dehydration system and method includes a contactor, a flash tank, and a still interconnected by a desiccant circulation system. A reboiler is coupled to the still and the flash tank to burn the flash gas from the flash tank and heat the desiccant. A secondary burner is associated with a vent stack of the reboiler to burn the flash gas from the flash tank when not firing the reboiler.

Abstract: A gas condensate production plant comprises a plurality of separation units in which C2 and/or C3 lighter components are stripped from the separator feeds using compressed heated stripping vapor produced from the feed in respective downstream separation units. Contemplated plants substantially reduce heating and cooling duties by using the waste heat from the compressor discharges in the separation process. Furthermore, the multi-stage fractionation according to the inventive subject matter provides improved gas condensate recovery at reduced energy costs.

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: An absorption medium which comprises water, an amine (A) of formula (I) in which R is an n-alkyl radical having 1 to 4 carbon atoms, and an alkanolamine (B) which is a tertiary amine or a sterically hindered primary or secondary amine has a high absorption capacity for CO2 with a high absorption rate. In the absorption of acid gases from a gas mixture a separation of the absorption medium into two liquid phases or the precipitation of a solid upon absorption of CO2 and regeneration of the absorption medium can be avoided with the absorption medium, even without addition of a solvent.

Abstract: A method of removing contaminates from sour water is provided. The method includes producing raw sour water within a syngas production system, and removing the contaminates from the raw sour water using a chemical reaction within a treatment unit to produce treated sour water. The treatment unit is in flow communication with the syngas production system.

Abstract: The present invention describes a method for recovery of high purity carbon dioxide, which is substantially free of nitrogen oxides. This high purity carbon dioxide is obtained by introducing into the method a step in which carbon dioxide absorbed in an absorbing agent is flashed. The present invention also discloses a plant for recovery of said high purity carbon dioxide comprising an absorption column, a flash column, a stripper column, and a down stream purification unit comprising a washing column, a dehydrator, a condenser and a distillation unit.

Abstract: The present invention provides a gas pressurized separation system to strip a product gas from a liquid stream and yield a high pressure gaseous effluent containing the product gas. The system comprises a gas pressurized stripping apparatus, such as a column, with at least one first inlet allowing flow of one or more liquid streams in a first direction and at least one second inlet allowing flow of one or more high pressure gas streams in a second direction, to strip the product gas into the high pressure gas stream and yield through at least one outlet a high pressure gaseous effluent containing the product gas; and two or more heat supplying apparatuses provided at different locations along the column. Processes for separating a product gas from a gaseous mixture to yield a high pressure gaseous effluent containing the product gas, utilize the gas pressurized separation system described above.

Abstract: A gas purification system including a hydrogen sulfide (H2S) absorber, a carbon dioxide (CO2) absorber, a flash tank, and a H2S concentrator. The gas purification system may also include a gas path though the H2S absorber prior to the CO2 absorber, a first solvent path sequentially through the CO2 absorber, the H2S absorber, and the H2S concentrator, and a second solvent path sequentially through the CO2 absorber, the flash tank, and the H2S concentrator, wherein the first and second solvent paths flow a common solvent.

Abstract: A dehydration system is provided. The dehydration system includes an absorber configured to produce a dry gas and a rich solvent from a wet gas and from a pure solvent and a flash drum coupled in flow communication with the absorber for receiving the rich solvent discharged from the absorber. The flash drum is configured to produce flash gas from the rich solvent. The dehydration further includes a reboiler configured to produce a semi-lean solvent from the rich solvent and an inert gas system configured to strip the semi-lean solvent using at least the flash gas to produce the pure solvent.

Abstract: The invention provides a process for producing purified gas from feed gas comprising H2S, CO2 and HCN and/or COS, the process comprising the steps of: (a) contacting feed gas comprising H2S, CO2 and HCN and/or COS with a HCN/COS hydrolysis sorbent in the presence of water in a HCN/COS hydrolysis unit, thereby obtaining gas depleted in HCN and/or COS; (b) contacting the gas depleted in HCN and/or COS with absorbing liquid in an H2S/CO2 absorber to remove H2S and CO2, thereby obtaining the purified gas and absorbing liquid rich in H2S and CO2; (c) heating and de-pressurizing at least part of the absorbing liquid rich in H2S and CO2 to obtain hot flash gas enriched in CO2 and absorbing liquid enriched in H2S; (d) contacting the absorbing liquid enriched in H2S at elevated temperature with a stripping gas, thereby transferring H2S to the stripping gas to obtain regenerated absorbing liquid and stripping gas rich in H2S; and (e) leading at least part of the flash gas enriched in CO2 to the HCN/COS hydrolysis unit

Abstract: Disclosed are methods for recovering CO2 and H2S from a feed gas including at least CO2 and H2S.

Abstract: The present invention provides a gas pressurized separation system to strip a product gas from a liquid stream and yield a high pressure gaseous effluent containing the product gas. The system comprises a gas pressurized stripping apparatus, such as a column, with at least one first inlet allowing flow of one or more liquid streams in a first direction and at least one second inlet allowing flow of one or more high pressure gas streams in a second direction, to strip the product gas into the high pressure gas stream and yield through at least one outlet a high pressure gaseous effluent containing the product gas; and two or more heat supplying apparatuses provided at different locations along the column. Processes for separating a product gas from a gaseous mixture to yield a high pressure gaseous effluent containing the product gas, utilize the gas pressurized separation system described above.

Abstract: A solvent based flue gas processing system for removing CO2 from a flue gas stream is described. A catalyst is provided to increase the efficiency of the solvent in capturing CO2 from the flue gas stream or in regenerating the solvent.

Abstract: Use of an absorbent for the removal of acid gases from a fluid stream, the absorbent consisting of an aqueous solution of 1,2 diaminopropane.

Abstract: Acid gas is removed from a high pressure feed gas that contains significant quantities of CO2 and H2S. In especially preferred configurations and methods, feed gas is contacted in an absorber with a lean and an ultra-lean solvent that are formed by flashing rich solvent and stripping a portion of the lean solvent, respectively. Most preferably, the flash vapors and the stripping overhead vapors are recycled to the feed gas/absorber, and the treated feed gas has a CO2 concentration of less than 2 mol % and a H2S concentration of less than 10 ppmv, and more typically less than 4 ppmv.

Abstract: A syngas treatment plant is configured to remove sulfurous compounds from syngas in a configuration having two flash stages for a physical solvent to so enrich the acid gas to at least 40 mol % H2S or higher as required by the Claus unit and to flash and recycle CO2 back to the syngas feed. Contemplated methods and configurations advantageously remove sulfur to less than 10 ppmv while increasing H2S selectivity at high pressure operation to thereby allow production of an H2S stream that is suitable as feed gas to a Claus plant.

Abstract: A solvent based flue gas processing system for removing CO2 from a flue gas stream is provided in which a catalyst coated on a support structure is provided. The catalyst selected is capable of retaining CO2, at least for a period of time, thereby increasing the residence time of CO2 and solvent.

Abstract: A method for removing acid gases from a fluid flow using an absorbent including an aqueous solution with at least two different amines. An amine in a proportion of greater than 50 wt. % of the total amine amount in the aqueous solution is the first amine component in the aqueous solution, and a sterically hindered amine in a proportion of less than 50 wt. % is the second amine component in the aqueous solution. The fluid flow is brought into contact with the absorbent at a partial pressure of <200 mbar.

Abstract: In a method for purifying biogas, components present in the biogas, such as carbon dioxide, sulfur compounds and ammonia, are separated in a plurality of different process stages. The method is characterized by low energy consumption and an increase in methane concentration of at least 10% while keeping methane losses low. In a first purifying step, carbon dioxide, hydrogen sulfide, ammonia and other organic water-soluble substances in the raw gas are removed at normal pressure or at overpressure of up to 6 bar in a wash column using fresh water, methane gas having a methane concentration of at least 65% is withdrawn at the head of the wash column. Methane and carbon dioxide dissolved in the washing water are sequentially separated from the contaminated washing water discharged from the washing stage in a first stripping column at normal pressure and subsequently in a second stripping column in a vacuum.

Abstract: The invention relates to a gas liquid contactor and effluent cleaning system and method and more particularly to an array of nozzles configured to produce uniformly spaced flat liquid jets with reduced linear stability. An embodiment of the invention is directed towards a stability unit used with nozzles of a gas liquid contactor and/or an enhancer for stable jet formation, and more particularly to reducing the stability of liquid jets formed from nozzles of the gas liquid contactor. Another aspect of the invention relates to operating the apparatus at a condition that reduces the stability of liquid jets, e.g., a droplet generator apparatus. Yet another aspect of the invention relates to operation of the apparatus with an aqueous slurry. Still another aspect of the invention is directed towards to an apparatus for substantially separating at least two fluids.

Abstract: Carbon dioxide and other acid gases are removed from gaseous streams using aqueous absorption and stripping processes. By replacing the conventional stripper used to regenerate the aqueous solvent and capture the acid gas with a matrix stripping configuration, less energy is consumed. The matrix stripping configuration uses two or more reboiled strippers at different pressures. The rich feed from the absorption equipment is split among the strippers, and partially regenerated solvent from the highest pressure stripper flows to the middle of sequentially lower pressure strippers in a “matrix” pattern. By selecting certain parameters of the matrix stripping configuration such that the total energy required by the strippers to achieve a desired percentage of acid gas removal from the gaseous stream is minimized, further energy savings can be realized.

Abstract: The invention provides a process for producing purified gas from feed gas comprising H2S, CO2 and HCN and/or COS, the process comprising the steps of: (a) contacting feed gas comprising H2S, CO2 and HCN and/or COS with a HCN/COS hydrolysis sorbent in the presence of water in a HCN/COS hydrolysis unit, thereby obtaining gas depleted in HCN and/or COS; (b) contacting the gas depleted in HCN and/or COS with absorbing liquid in an H2S/CO2 absorber to remove H2S and CO2, thereby obtaining the purified gas and absorbing liquid rich in H2S and CO2; (c) heating and de-pressurising at least part of the absorbing liquid rich in H2S and CO2 to obtain hot flash gas enriched in CO2 and absorbing liquid enriched in H2S; (d) contacting the absorbing liquid enriched in H2S at elevated temperature with a stripping gas, thereby transferring H2S to the stripping gas to obtain regenerated absorbing liquid and stripping gas rich in H2S; and (e) leading at least part of the flash gas enriched in CO2 to the HCN/COS hydrolysis unit

Abstract: An absorption medium for removing acid gases from a fluid stream comprises an aqueous solution of A) at least one cyclic amine compound having solely tertiary amine groups and/or sterically hindered secondary amine groups and B) at least one cyclic amine compound having at least one sterically unhindered secondary amine group. The absorption medium comprises, e.g., an aqueous solution of A) 1-hydroxyethylpiperidine and/or triethylenediamine and B) piperazine. The absorption medium is particularly suitable for separating off carbon dioxide from flue gases and satisfies the following criteria: (i) sufficient capacity at low CO2 partial pressures; (ii) sufficiently rapid absorption rate at low CO2 partial pressures; (iii) stability toward oxygen; (iv) low vapor pressure for reducing solvent losses; and (v) low energy requirement for regeneration of the absorption medium.

Abstract: The present invention describes a method for recovery of high purity carbon dioxide, which is substantially free of nitrogen oxides. This high purity carbon dioxide is obtained by introducing into the method a step in which carbon dioxide absorbed in an absorbing agent is flashed. The present invention also discloses a plant for recovery of said high purity carbon dioxide comprising an absorption column, a flash column, a stripper column, and a down stream purification unit comprising a washing column, a dehydrator, a condenser and a distillation unit.

Abstract: The invention relates to a method for producing a high-molecular polycondensate from a solidified polycondensate prepolymer by solid phase polycondensation. According to said method, the polycondensation cleavage products of the solid phase polycondensation reaction are extracted from the product by means of a process gas, and the process gas is then cleaned of the polycondensation cleavage products and essentially recycled. According to the invention, the specific energy input is less than 120 kWh/t, preferably less than 110 kWh/t and especially between 70 and 100 kWh/t. The invention also relates to an installation for producing a high-molecular polycondensate, said installation comprising a heating appliance (1), followed by a crystallisation appliance (2), a reaction appliance (4), and a cooling appliance (5).

Abstract: A description is given of a process for removing carbon dioxide from gas streams in which the partial pressure of the carbon dioxide is less than 200 mbar, in particular flue gases, the gas stream being contacted with a liquid absorption medium which comprises an aqueous solution (A) of a tertiary aliphatic alkanolamine and (B) an activator of the formula R1—NH—R2—NH2, where R1 is C1-C6-alkyl and R2 is C2-C6-alkylene, the sum of the concentrations of A and B being 2.5 to 7 mol/l, and the molar ratio of B to A being in the range of 1:3 to 1.5:1. The activator is, for example, 3-methylaminopropylamine, the tertiary aliphatic amine methyldiethanolamine, methyidiisopropanolamine or n-butyldiethanolamine. The process permits substantial removal of carbon dioxide and the regeneration of the absorption medium is possible with relatively low energy consumption.

Abstract: Carbon dioxide and other acid gases are removed from gaseous streams using aqueous absorption and stripping processes. By replacing the conventional stripper used to regenerate the aqueous solvent and capture the acid gas with a matrix stripping configuration, less energy is consumed. The matrix stripping configuration uses two or more reboiled strippers at different pressures. The rich feed from the absorption equipment is split among the strippers, and partially regenerated solvent from the highest pressure stripper flows to the middle of sequentially lower pressure strippers in a “matrix” pattern. By selecting certain parameters of the matrix stripping configuration such that the total energy required by the strippers to achieve a desired percentage of acid gas removal from the gaseous stream is minimized, further energy savings can be realized.

Abstract: Method and system for processing natural gas containing contaminants through the use of one or more rotary screw compressors. A natural gas containing a contaminant (e.g., water or carbon dioxide and/or hydrogen sulfide) and a contaminant removing agent are combined and processed within a rotary screw compressor. The contaminant removing agent may be a dehydrating agent such as a glycol or a carbon dioxide and/or hydrogen sulfide removing agent such an amine. The method and system of the present invention also may employ a series of rotary screw compressors to process natural gas containing a plurality of contaminants.

Abstract: A method and apparatus for the dehydration of glycol, comprising a gas compressor unit including an engine which produces a flow of hot exhaust gas; a glycol dehydrator unit including a reboiler for heating and dehydrating the glycol; transferring heat from the exhaust gas to the reboiler to heat the glycol; and a support platform, wherein the gas compressor unit, the glycol dehydrator unit and the circuit for transferring heat are all supported on the support platform.

Abstract: A combined compressor and dehydrator apparatus including a gas compressor unit with an exhaust through which exhaust gas is expelled from said gas compressor unit; a glycol dehydrator unit with a glycol reboiler; a means of transferring heat from said exhaust of said gas compressor unit to said glycol reboiler of said glycol dehydrator unit; and a skid; wherein said gas compressor unit, said glycol dehydrator unit and said means of transferring heat are fixedly attached to said skid.

Abstract: Method and system for compressing and dehydrating wet natural gas produced from a low-pressure well using a rotary screw compressor. A dehydrating agent is combined with wet natural gas within a rotary screw compressor. Operation of the rotary screw compressor causes compression and dehydration of the wet natural gas to produce a compressed dry natural gas. Engine exhaust produced by the engine which powers the rotary screw compressor may be used to remove water absorbed by the dehydrating agent and thereby recover the dehydrating agent for re-circulation in the system.

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: 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: 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: 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: 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 method for removing residual VOC components from a fluid stream used in the sweetening of sour gas at gas processing plants. In a retrofit configuration, the method includes interposing a supplemental VOC removal station after a primary VOC removal station in an absorbent fluid stream. The absorbent fluid stream incorporates fluid into which sour gas components and VOC have been absorbed from a treated gas stream such as produced natural gas. The primary VOC removal station is configured to remove an initial portion of the absorbed VOC from the absorbent fluid stream. The supplemental VOC removal station is configured to liberate a portion of residual absorbed VOC remaining in the absorbent fluid stream downstream from the primary VOC removal station. Further, the supplemental VOC removal station is configured to avoid liberating absorbed sour gas components from the absorbent fluid stream.

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 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 system for regenerating chemical solvent loaded with acid gas with improved energy efficiency wherein the chemical solvent is partially flash vaporized, heated, and passed in countercurrent mass transfer contact with nitrogen gas.

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.