Abstract: An LNG production plant is constructed from a plurality of containerised LNG liquefaction units. Each containerised LNG liquefaction unit can produce a predetermined quantity of LNG. For example, up to 0.3 MPTA. A manifold system enables connection between the plurality of containerised LNG liquefaction units, and at least a feed stream of natural gas, a source of electrical power, and an LNG storage facility. The production capacity of the plant is incrementally changed by connecting or disconnecting containerised LNG liquefaction units to or from the plant via the manifold system. Each unit contains its own liquefaction plant having a closed loop SMR circuit. Refrigerant within the SMR circuit is circulated solely by pressure differential generated by refrigerant compressors in the liquefaction plant.

Abstract: Implementations described and claimed herein provide systems and methods for processing liquefied natural gas (LNG). In one implementation, a solvent is injected into a feed of natural gas at a solvent injection point. A mixed feed is produced from a dispersal of the solvent into the feed of natural gas. The mixed feed contains heavy components. A chilled feed is produced by chilling the mixed feed. The chilled feed includes a vapor and a condensed liquid. The condensed liquid contains a fouling portion of the heavy components condensed by the solvent during chilling. The liquid containing the fouling portion of the heavy components is separated from the vapor. The vapor is directed into a feed chiller heat exchanger following separation of the liquid containing the fouling portion of the heavy components from the vapor, such that the vapor being directed into feed chiller heat exchanger is free of freezing components.

Abstract: A method for recovering a helium product or intermediate product, wherein a first natural gas stream containing helium is supplied to a first natural gas processing unit and at least one second natural gas stream containing helium is supplied to at least one second natural gas processing unit, at least the first natural gas processing unit comprising helium recovery means via which the helium product is formed from at least a part of the first natural gas stream. At least temporarily a helium transfer from the at least one second natural gas stream to the first natural gas stream by means of a helium transfer arrangement comprising a membrane unit is performed before the first natural gas stream is provided to the first natural gas processing unit and before the at least one second natural gas stream is provided to the at least one second natural gas processing unit.

Abstract: In a method for separating argon by cryogenic distillation, in which a flow containing argon, oxygen and nitrogen and being more rich in argon than the air is sent to a distillation column, and an argon-rich gas flow is withdrawn at the top of the column, a portion of the argon-rich gas flow is mixed with beads to form a gas mixture containing beads, the beads being capable of adsorbing oxygen in the presence of argon at the column operating temperatures; the portion of the argon-rich gas flow mixed with the beads is condensed and then sent to the top of the column; and a bottom liquid containing beads is withdrawn from the column and treated to remove the beads, the beads removed being regenerated to remove the adsorbed oxygen and being again mixed with the argon-rich gas flow.

Abstract: Disclosed herein are improved methods and devices for recycling lithium cathodes from batteries using a Soxhlet extractor.

Abstract: A method to recover hydrocarbonfractions from refineries gas streams involves a pre-cooled heat refinery fuel gas stream mixed with a pre-cooled and expanded supply of natural gas stream in an inline mixer to condense and recover at least C3+ fractions upstream of a fractionator. The temperature of the gas stream entering the fractionator may be monitored downstream of the in-line mixer. The pre-cooled stream of high pressure natural gas is sufficiently cooled by flowing through a gas expander that, when mixed with the pre-cooled refinery fuel gas, the resulting temperature causes condensation of heavier hydrocarbon fractions before entering the fractionator. A further cooled, pressure expanded natural gas reflux stream is temperature controlled to maintain fractionator overhead temperature. The fractionator bottoms temperature may be controlled by a circulating reboiler stream.

Abstract: In a process for the combined production of a) a hydrogen-enriched gas and a carbon monoxide-enriched gas and/or b) a mixture of hydrogen and carbon monoxide by cryogenic distillation and scrubbing, a still liquor is extracted from a scrubbing column and sent to a stripping column, a still liquor is extracted from the stripping column and sent to a separating column for carbon monoxide and methane and a cooling fluid is used at a pressure greater than that of the head of the separating column for cooling at least one fluid extracted at an intermediate level from the scrubbing column.

Abstract: A process and apparatus reboil a propylene splitter bottoms by heat exchange and/or a deethanizer bottoms stream with a compressed propylene splitter overhead stream. Use of single splitter compressor and operation of the propane-propylene splitter column at lower pressure are enabled, whereas conventionally two splitter compressors and higher splitter pressure were necessary to provide a propylene product stream and a propane recycle stream of equivalent quality.

Abstract: A system includes a purification unit configured to process a vapor stream including sulfur dioxide. The purification unit includes an inlet configured to allow the vapor stream to enter the purification unit. The purification unit includes a steam coil configured to circulate steam and provide a source of heat. The purification unit includes a packed bed. The purification unit includes a tray configured to accumulate sulfur. The purification unit includes an absorber section configured to remove at least a portion of the sulfur dioxide from the vapor stream. The purification unit includes an outlet configured to allow an effluent with a lower sulfur dioxide content than the vapor stream to exit the purification unit. The system includes a sulfur tank including a vent line in fluid communication with the inlet. The vent line is configured to allow vapor to flow from the sulfur tank to the purification unit.

Abstract: A method for improved operation of a natural gas liquids stabilizer column, particularly a small-scale, is provided.

Abstract: A process and an apparatus are disclosed for the recovery of components from a hydrocarbon gas stream which is divided into first and second streams. The first stream is cooled, expanded to lower pressure, and supplied to a fractionation tower. The second stream is cooled and separated into vapor and liquid streams. The vapor stream is divided into two portions. A first portion is cooled, expanded to tower pressure, and supplied to the tower at an upper mid-column feed position. The second portion and the liquid stream are expanded to tower pressure and supplied to the tower. After heating, compressing, and cooling, a portion of the tower overhead vapor is cooled, expanded, and supplied to the tower at the top feed position. The quantities and temperatures of the feeds to the tower maintain the overhead temperature of the tower whereby the major portion of the desired components is recovered.

Abstract: A natural gas conditioning system for conditioning unconditioned natural gas for use in a gas lift system at a wellbore comprises a series of coolers to receive and cool unconditioned natural gas, and a high-pressure, three-phase separator. The separator receives cooled unconditioned natural gas from the coolers and results in separate flows of conditioned lift gas, waste water and hydro-carbon liquids. The conditioned lift gas can be directed to a first heat exchanger, and the hydro-carbon liquids can be directed to a second heat exchanger. A chiller can be coupled to a third heat exchanger. All the components can be carried by a skid.

Abstract: A design is provided to convert a gas subcooled process plant to a recycle split vapor process for recovering ethane and propane from natural gas. When in operation, the recovery of ethane and propane can exceed 97 to 99 wt. % of the stream being processed. A second smaller demethanizer column is added to the gas subcooled process plant as well as the addition of several cryogenic pumps.

Abstract: The claimed invention provides a method and an apparatus for separating hydrocarbons, wherein the method and the apparatus are used for separating a hydrocarbon having 3 or more carbon atoms including at least propane (hereinafter sometimes called “C3+ NGL”. NGL: Natural Gas Liquid) from liquefied natural gas (LNG).

Abstract: A LNG liquefaction plant includes a propane recovery unit including an inlet for a feed gas, a first outlet for a LPG, and a second outlet for an ethane-rich feed gas, an ethane recovery unit including an inlet coupled to the second outlet for the ethane-rich feed gas, a first outlet for an ethane liquid, and a second outlet for a methane-rich feed gas, and a LNG liquefaction unit including an inlet coupled to the second outlet for the methane-rich feed gas, a refrigerant to cool the methane-rich feed gas, and an outlet for a LNG. The LNG plant may also include a stripper, an absorber, and a separator configured to separate the feed gas into a stripper liquid and an absorber vapor. The stripper liquid can be converted to an overhead stream used as a reflux stream to the absorber.

Abstract: A system and method for producing an NGL product stream in either an ethane retention or rejection mode. Rejection modes include (a) two heat exchange stages between a feed stream and first separator bottoms stream and cooling a side stream withdrawn from a fractionation tower through heat exchange with both the fractionation tower and second separator overhead streams; or (b) warming the first separator bottoms stream and fractionation overhead stream through heat exchange with the side stream prior to heat exchange with the feed stream, to achieve 4-15% ethane recovery and 97%+ propane recovery. In ethane retention mode, a portion of the feed stream and portions of a first separator overhead and bottoms streams are separately cooled through heat exchange with other process streams, including the entireties of a recycled residue gas and fractionation column overhead streams, resulting in around 99% ethane and around 100% propane recovery.

Abstract: Process for the combined production of a mixture of hydrogen and nitrogen, and of carbon monoxide by cryogenic distillation and cryogenic scrubbing, wherein a methane-rich liquid is introduced at a first intermediate level of a scrubbing column as first scrubbing liquid and at least one nitrogen-rich liquid is introduced at a level higher than the first level of the scrubbing column as second scrubbing liquid and a mixture of hydrogen and nitrogen is drawn off as overhead gas from the scrubbing column.

Abstract: Recovering heat from a Natural Gas Liquid (NGL) fractionation plant via a waste heat recovery heat exchanger network including heating a buffer fluid in a heat exchanger with a stream from the NGL fractionation plant and discharging the heated buffer fluid to an integrated triple cycle system. Generating cooling capacity for the NGL fractionation plant via the integrated triple cycle system with heat from the buffer fluid.

Abstract: Certain aspects of natural gas liquid fractionation plant waste heat conversion to simultaneous power and potable water using Kalina Cycle and modified multi-effect-distillation system can be implemented as a system. The system includes a waste heat recovery heat exchanger network coupled to multiple heat sources of a Natural Gas Liquid (NGL) fractionation plant. The heat exchanger network is configured to transfer at least a portion of heat generated at the multiple heat sources to a first buffer fluid and a second buffer fluid flowed through the first heat exchanger network. The system includes a first sub-system configured to generate power. The first sub-system is thermally coupled to the waste heat recovery heat exchanger. The system includes a second sub-system configured to generate potable water from brackish water. The second sub-system is thermally coupled to the waste heat recovery heat exchanger.

Abstract: An apparatus, system and method for capture, utilization and sendout of latent heat in boil off gas (“BOG”) onboard a cryogenic storage vessel is described. A liquefied gas vessel comprises a cryogenic cargo tank onboard a liquefied gas vessel, the cargo tank comprising a liquefied gas and a BOG, a latent heat exchanger fluidly coupled to a stream of the liquefied gas and a stream of the BOG, wherein the latent heat exchanger transfers a heat between the BOG stream and the liquefied gas stream to produce a condensed BOG, means for combining the condensed BOG and the liquefied gas stream to obtain a combined stream, the means for combining the condensed BOG and the liquefied gas stream fluidly coupled to the latent heat exchanger, and a liquefied gas regasifier onboard the vessel and fluidly coupled to the combined stream, wherein the liquefied gas regasifier regasifies the combined stream.

Abstract: A process and an apparatus are disclosed for a compact processing assembly to remove C5 and heavier hydrocarbon components from a hydrocarbon gas stream. The hydrocarbon gas stream is expanded to lower pressure and supplied to the processing assembly between an absorbing means and a mass transfer means. A distillation vapor stream is collected from the upper region of the absorbing means and cooled in a first heat and mass transfer means inside the processing assembly to partially condense it, forming a residual vapor stream and a condensed stream. The condensed stream is supplied to the absorbing means at its top feed point. A distillation liquid stream is collected from the lower region of the mass transfer means and directed into a second heat and mass transfer means inside the processing assembly to heat it and strip out its volatile components.

Abstract: In a process for the cryogenic separation of a methane-rich feed stream containing between 3 and 35% of oxygen and also nitrogen, the feed stream is cooled in order to produce a cooled stream, at least one portion of the cooled stream is sent to a distillation column, a bottom stream is withdrawn from the distillation column, the bottom stream being enriched in methane compared to the feed stream, a stream enriched in oxygen compared to the feed stream is withdrawn from the distillation column, and a nitrogen-rich stream is sent to the column.

Abstract: Water-saturated desiccant in a dehydration unit, having previously been used to dehydrate natural gas, is regenerated in a closed loop process using liquid petroleum gas (LPG). LPG is pumped from a storage tank, vaporized and superheated. The superheated LPG gas enters the dehydration unit such that the hot gas passes over the desiccant thereby regenerating the desiccant. An overhead stream from the dehydration unit passes to a condenser where the temperature of the hot gas from the dehydration unit is dropped to form a fluid stream containing LPG, water and non-condensable gases. The fluid stream passes to a three phase separator for separating the fluid stream into a gas stream, a water stream, and a liquid stream containing LPG which is then returned to the storage tank for reuse in the closed loop process.

Abstract: The apparatus for liquefying a gaseous stream received from a pipeline that is comprised predominantly of ethane and a relatively small amount of other components by using a mixed refrigerant refrigeration cycle loop incorporating heavy hydrocarbons, as well as a distillation column to remove constituents lighter than ethane.

Abstract: A method for operating a natural gas liquids processing (NGL) system, the system being selectively configured in either an ethane rejection configuration or an ethane recovery configuration, the method comprising, when the NGL system is in the ethane rejection configuration, collecting a reboiler bottom stream that, in the ethane rejection configuration, includes ethane in an amount of less than 5% by volume, and when the NGL system is in the ethane recovery configuration, collecting a reboiler bottom stream that, in the ethane recovery configuration, includes ethane in an amount of at least about 30% by volume.

Abstract: Embodiments described herein provide methods and systems for separating a mixed ethane and CO2. A method described includes generating a liquid stream including ethane and CO2. The liquid stream is flashed to form an ethane vapor stream and solid CO2. The solid CO2 is accumulated in an accumulation vessel and the gas is removed from the top of the accumulation vessel.

Abstract: A process and apparatus for separating a feed containing hydrogen, carbon monoxide, methane, and optionally nitrogen to form a product gas having a desired H2:CO molar ratio and optionally a hydrogen product gas and a carbon monoxide product gas. The feed is partially condensed to form a hydrogen-enriched vapor fraction and a carbon monoxide-enriched liquid fraction. The hydrogen-enriched vapor fraction and carbon monoxide-enriched liquid fraction are combined in a regulated manner to form an admixture, which is cryogenically separated to form the product mixture having the desired H2:CO molar ratio.

Abstract: A distillation apparatus of the present invention includes high-pressure column 1 corresponding to a region above a heat exchanging section located at a lowermost part of a region including a trayed section or a packed bed section, which is used as a rectifying section; and low-pressure column 2 that is located above as seen from high-pressure column 1, which integrates a region including a trayed section or a packed bed section which is used as a stripping section, with rectifying section corresponding portion 2g that corresponds to a region locating below the heat exchanging section located at the lowermost part in the rectifying section. Rectifying section corresponding portion 2g is located on top 2c of the stripping section in low-pressure column 2 so that rectifying section corresponding portion 2g continues to the stripping section.

Abstract: The process for liquefying a gaseous stream received from a pipeline that is comprised predominantly of ethane and a relatively small amount of other components by using a mixed refrigerant loop incorporating heavy hydrocarbons (butane, and/or pentane), as well as a distillation column to remove constituents lighter than ethane. Prior to cooling in a main heat exchanger, the gaseous stream is split into two fractions. The first fraction is cooled in the main heat exchanger and introduced to the distillation column. The second fraction is expanded to produce a two phase fluid, with the liquid fraction being introduced to the distillation column below the first fraction, and the gas fraction being cooled and then introduced to the distillation column at a point above the first fraction.

Abstract: The apparatus for liquefying a gaseous stream received from a pipeline that is comprised predominantly of ethane and a relatively small amount of other components by using a mixed refrigerant refrigeration cycle loop incorporating heavy hydrocarbons, as well as a distillation column to remove constituents lighter than ethane. Prior to cooling in a main heat exchanger, the gaseous stream is split into two fractions. The main heat exchanger is configured to cool the first fraction before heading to the distillation column for separation therein. An expansion device expands the second fraction to produce a two phase fluid, which is separated in a gas/liquid separator, with the liquid fraction being introduced to the distillation column below the first fraction, and the gas fraction being cooled and then introduced to the distillation column at a point above the first fraction.

Abstract: A propane dehydrogenation and propylene purification process in which a stream comprising propylene, propane, and methyl acetylene and propadiene (MAPD) is mixed with a hydrogen stream then reacted in at least three distinct reaction zones in a hydrogenation reactor system where MAPD is hydrogenated by a high-selectivity hydrogenation catalyst in a first reaction zone, and a second and a third reaction zones each have a low-selectivity hydrogenation catalyst to remove unreacted hydrogen. The outlet stream leaving the hydrogenation reactor system is MAPD-free and can be fed to a splitter column, which now mainly serves to separate propylene from propane. Various embodiments of reaction zone arrangements in a single or multiple reactors are also provided.

Abstract: A system and method for removing nitrogen and producing a high pressure methane product stream from natural gas feed streams having wide variations in nitrogen and methane content are disclosed. Optional add-on systems may be incorporated into the nitrogen and methane separation to produce an NGL sales stream to reduce excess hydrocarbons in the nitrogen vent stream, or to recover helium. The system and method of the invention are particularly suitable for use with feed streams in excess of 50 MMSCFD and up to 300 MMSCFD and containing up to 100 ppm carbon dioxide. Typical power requirements for compressing the methane product stream to produce a suitably high pressure stream for sale are reduced according to the systems and methods of the invention.

Abstract: A process and an apparatus are disclosed for a compact processing assembly to fractionate lighter components from mixed hydrocarbon streams. The hydrocarbon stream is supplied to the processing assembly between an absorbing means and a mass transfer means. A distillation vapor stream is collected from the upper region of the absorbing means and cooled in a first heat and mass transfer means inside the processing assembly to partially condense it, forming a volatile stream and a condensed stream. The condensed stream is supplied to the absorbing means as its top feed. A distillation liquid stream is collected from the lower region of the mass transfer means and heated in a second heat and mass transfer means inside the processing assembly to strip out its volatile components, forming a relatively less volatile stream and a vaporized stream. The vaporized stream is supplied to the mass transfer means as its bottom feed.

Abstract: In a process for the separation of a gas rich in carbon dioxide and containing at least one component lighter than carbon dioxide, the feed gas rich in carbon dioxide is cooled in a first heat exchanger, partially condensed and separated to form a gaseous portion and a liquid, sending the liquid portion to the top of a distillation column, removing a liquid stream richer in carbon dioxide than the feed gas from the bottom of the distillation column, removing a gaseous stream less rich in carbon dioxide than the feed gas from the top of the distillation column and warming the gaseous stream in the first heat exchanger, sending the gaseous portion to a shell and tube heat exchanger having tubes in a bath of triple point carbon dioxide, in which it condenses at least partially to form a liquid fraction, sending the liquid fraction to the top of the distillation column, vaporizing a liquid stream from the bottom of the distillation column outside or within the distillation column to form a gas which is subsequent

Abstract: The method according to the invention comprises the separation of a feed stream (16) into a first fraction (60) and a second fraction (62) and the injection of at least part of the second fraction (62) into a second dynamic expansion turbine (46) to form a second expanded fraction (80). It comprises the cooling of the second expanded fraction (80) through heat exchange with at least part of the first headstream (84) coming from a first column (28) and the formation of a second feed stream (82) of the first column (28) from the second cooled expanded fraction.

Abstract: A natural gas liquids plant uses a demethanizer and a deethanizer in a two-column or single column configuration that can be used for ethane recovery and ethane rejection. During ethane recovery, 95% ethane recovery and 99% propane recovery are achieved, while during ethane rejection the sales gas Wobbe Index requirement is maintained while maintaining 95% propane recovery. A residue gas recycle exchanger is most preferably configured to use the demethanizer overhead product to either cool a portion of the residue gas and a portion of the feed gas during ethane recovery, or to cool a portion of the feed gas using two distinct heat transfer areas to produce a feed gas reflux at significantly lower temperature.

Abstract: Described herein is a method for separating C2+-hydrocarbons or C3+-hydrocarbons from a hydrocarbon-rich fraction is described, whereby the separation is carried out in a rectification fractionation. The rectification fractionation is provided with at least three heating circuits via which intermediate fractions are drawn off from rectification fractionation, partially evaporated and fed back again to rectification fractionation. In the method, removal of the intermediate fraction circulating in the heating circuit located at the highest temperature level is at least temporarily interrupted. During this interruption, a partial stream of a bottom fraction from the rectification fractionation is partially evaporated against an external medium and is fed as a bottom heating to the rectification fractionation.

Abstract: A distillation apparatus includes a rectifying column, a stripping column, a first pipe that communicates a column top of the stripping column with a column bottom of the rectifying column, and a compressor configured to compress vapor from the stripping column and then to feed the compressed vapor to the rectifying column. The distillation apparatus further includes a heat exchanger located at a predetermined stage of the rectifying column, a liquid withdrawal unit located at a predetermined stage of the stripping column and configured to withdraw a part of liquid from the predetermined stage to an outside of the column, a second pipe that introduces the liquid from the liquid withdrawal unit to the heat exchanger, and a third pipe that introduces fluids introduced through the second pipe to the heat exchanger and then discharged out of the heat exchanger to a stage directly below the liquid withdrawal unit.

Abstract: A distillation apparatus includes a rectifying column, a stripping column located above seen from the rectifying column, a liquid sump unit located at a predetermined stage of the stripping column and configured to hold liquid that has flowed downward, a heat exchanger located in the liquid sump unit, a second pipe for introducing vapor in the rectifying column to the heat exchanger of the stripping column, and a third pipe for introducing fluids flowing out from the heat exchanger of the stripping column to the rectifying column. Further, a flare line having lower pressure than pressure in the rectifying column is connected to a downstream side of the third pipe. The distillation apparatus can switch a first flow toward an inside of the rectifying column through the third pipe to a second flow branching from the third pipe toward a pipe at a lower pressure side.

Abstract: Provided is a method for operating a fuel supply system for a marine structure. The fuel supply system includes a BOG compression unit configured to receive and compress BOG generated in a storage tank, a reliquefaction apparatus configured to receive and liquefy the BOG compressed by the BOG compression unit, a high-pressure pump configured to compress the liquefied BOG generated by the reliquefaction apparatus, and a high-pressure gasifier configured to gasify the liquefied BOG compressed by the high-pressure pump. The fuel supply system includes a recondenser installed at an upstream side of the high-pressure pump, and the recondenser recondenses a portion or all of the generated BOG by using liquefied gas supplied from the storage tank. During a ballast voyage process, all of the BOG is supplied to and recondensed by the recondenser, and an operation of the reliquefaction apparatus is interrupted.

Abstract: A process and an apparatus are disclosed for the recovery of ethane, ethylene, propane, propylene, and heavier hydrocarbon components from a hydrocarbon gas stream in a compact processing assembly. The gas stream is cooled and divided into first and second streams. The first stream is further cooled to condense substantially all of it and is thereafter expanded to lower pressure and supplied as the top feed to an absorbing means inside the processing assembly. The second stream is also expanded to lower pressure and supplied as the bottom feed to the absorbing means. A distillation vapor stream is collected from the upper region of the absorbing means and directed into one or more heat exchange means inside the processing assembly to heat it while cooling the gas stream and the first stream.

Abstract: A process and an apparatus are disclosed for recovering ethane, ethylene, and heavier hydrocarbon components from a hydrocarbon gas stream. The stream is cooled, expanded to lower pressure, and supplied to a first fractionation tower at a mid-column feed position. A distillation liquid stream is withdrawn from the first fractionation tower below the feed position of the expanded stream, heated, and directed into a second fractionation tower that produces an overhead vapor stream and a bottom liquid stream. The overhead vapor stream is cooled to condense it, with a portion of the condensed stream directed to the second fractionation tower as its top feed and the remainder directed to the first fractionation tower at a lower column feed position. The bottom liquid stream from the second fractionation tower is cooled and directed to the first fractionation tower as its top feed.

Abstract: In a process for the cryogenic separation of a feed mixture of at least carbon monoxide, hydrogen and methane, the feed mixture is separated in a methane wash column fed by a liquid methane stream at the top of the methane wash column to produce a gas enriched in hydrogen, a liquid stream from the bottom of the methane wash column is treated to produce a mixture of carbon monoxide and methane, the mixture of carbon monoxide and methane is separated in a separation column to produce a gas enriched in carbon monoxide and a liquid methane flow at least part of which forms a purge stream, the purge stream being varied to take account of load variations.

Abstract: A system and method for removing nitrogen and producing liquefied natural gas (“LNG”) from methane without the need for external refrigeration. The invention also relates to a system and method for removing nitrogen from methane and for producing liquefied nitrogen in addition to LNG. The system and method of the invention are particularly suitable for use in recovering and processing comparatively small volumes of methane from coal mines or from flash gas captured at an LNG loading site.

Abstract: The invention relates to a method for the separation of a hydrocarbon-rich, nitrogen-containing feed fraction (1, 101), preferably natural gas, wherein the feed fraction (1, 101) is at least in part liquefied (E1, E2) and divided by rectification (T1) into a nitrogen-enriched fraction (14, 110) and a hydrocarbon-rich, nitrogen-depleted fraction (11, 111) and wherein, in the upper region of the rectification (T1), a nitrogen-enriched stream (14) is taken off, cooled (E3) and applied (20) at least in part to the rectification (T1) as reflux and/or the nitrogen-enriched fraction (110) is cooled and partially condensed (E3), applied at least in part to the rectification (T1) as reflux (115) and the remaining stream (116) of the nitrogen-enriched fraction (110) is subjected to a double-column process (T3).

Abstract: A method and device for the cryogenic separation of a methane-rich flow is provided.

Abstract: A process and an apparatus are disclosed for a compact processing assembly to improve the recovery of C2 (or C3) and heavier hydrocarbon components from a hydrocarbon gas stream. The preferred method of separating a hydrocarbon gas stream generally includes producing at least a substantially condensed first stream and a cooled second stream, expanding both streams to lower pressure, and supplying the streams to a fractionation tower. In the process and apparatus disclosed, the expanded first stream is heated to form a vapor fraction and a liquid fraction. The vapor fraction is combined with the tower overhead vapor, directed to a heat and mass transfer means inside a processing assembly, and cooled and partially condensed by the expanded first stream to form a residual vapor stream and a condensed stream. The condensed stream is combined with the liquid fraction and supplied to the tower at its top feed point.

Abstract: A process and an apparatus are disclosed for a compact processing assembly to fractionate lighter components from mixed hydrocarbon streams. The hydrocarbon stream is supplied to the processing assembly between an absorbing means and a mass transfer means. A distillation vapor stream is collected from the upper region of the absorbing means and cooled in a first heat and mass transfer means inside the processing assembly to partially condense it, forming a volatile stream and a condensed stream. The condensed stream is supplied to the absorbing means as its top feed. A distillation liquid stream is collected from the lower region of the mass transfer means and heated in a second heat and mass transfer means inside the processing assembly to strip out its volatile components, forming a relatively less volatile stream and a vaporized stream. The vaporized stream is supplied to the mass transfer means as its bottom feed.

Abstract: Fractionation systems utilizing a rectifying column with a stripping column are described. The liquid from the rectifying column bottoms is sent to the first tray of the stripping column, while the overhead stream from the stripping column is sent to the bottom of the rectifying column. Processes for separating feed streams are also described.

Abstract: Fractionation systems utilizing a single rectifying column with a stripping column housed in the same vessel and having a uniform diameter are described. Methods of separating feed streams using the fractionation systems are also described.