Abstract: A process and apparatus for separating a fraction rich in C2+ from liquefied natural gas (LNG) is disclosed. In an embodiment, partial evaporation of the liquefied natural gas occurs in a heat exchanger. The partially evaporated natural gas is separated into a first gas fraction rich in C1 and a first liquid fraction rich in C2+. In a separation column, rectification separation of the first liquid fraction rich in C2+ into a second gas fraction rich in C1 and a second liquid fraction rich in C2+ occurs. The first gas fraction rich in C1 is re-liquefied in the heat exchanger. At least one sub-stream of the re-liquefied gas fraction rich in C1 is fed as a reflux to the rectification separation.

Abstract: A method and system for the separation of a synthesis gas and methane mixture which contains carbon monoxide, hydrogen and methane with the process producing synthesis gas and liquid natural gas (LNG).

Abstract: A process for the recovery and purification of ethylene and optionally propylene from a stream containing lighter and heavier components that employs an ethylene distributor column and a partially thermally coupled distributed distillation system.

Abstract: The present invention related to a flexible hydrocarbon gas separation process that could dehydrate the water-saturated hydrocarbon gas mixture and recover thereof the required higher hydrocarbons (NGL) therein with a controllable ethane recovery rate (ranging from >95% to <2%) while keeping high recovery rate of all other heavier components. The flexible process comprises the following steps: deep-cooling and dehydrating the raw gas and get the NGL condensate; flowing the deep-dehydrated gas into the flexible absorber to get the rich oil with desirable ethane content; completely demethanizing and partially deethanizing as desired the rich oil and the NGL condensate to get purified rich oil and purified NGL condensate, respectively; separating the NGL vapor from the purified rich oil; cooling and compressing the NGL vapor; mixing the NGL vapor with the purified NGL condensate; and liquefying the mixture to get the final NGL product.

Abstract: The disclosed invention relates to a process for distilling a fluid mixture in a microchannel distillation unit, the microchannel distillation unit comprising a plurality of microchannel distillation sections, the fluid mixture comprising a more volatile component and a less volatile component, the process comprising: flowing a vapor phase of the fluid mixture in a first microchannel distillation section in contact with a liquid phase of the fluid mixture, part of the more volatile component transferring from the liquid phase to the vapor phase to form a more volatile component rich vapor phase, part of the less volatile component transferring from the vapor phase to the liquid phase to form a less volatile component rich liquid phase; separating the more volatile component rich vapor phase from the less volatile component rich liquid phase; flowing the less volatile component rich liquid phase to another microchannel distillation section upstream from the first microchannel distillation section; and flowing

Abstract: The invention relates to a method for fractionating a gas produced by the pyrolysis of hydrocarbons (1) for the recovery of C2 and higher hydrocarbons, in particular ethylene and ethane, comprising an operation (70) for compressing and drying gas (1) as a result of it passing into a series of compressors (3, 10, 17, 24, 36), an operation (80) for progressively cooling and partially liquefying the gas produced by compression and drying operation (70) as a result of it successively passing into a cryogenic exchanger (62), and a distillation operation (90) in a column (64), and the corresponding installation. According to the invention, cryogenic exchanger (62) is cooled by at least one cooling liquid (400) which is liquid natural gas (LNG).

Abstract: Improved methodology for starting up a LNG facility employing a refluxed heavies removal column. The improved methodology involves varying the temperature of the feed to the heavies removal column between start-up and normal operation. This allows a larger amount of the stream produced from the top of the heavies removal column during start-up to be used to more rapidly start up the LNG facility.

Abstract: The recovery of ethylene from light gases at low temperature by the use of a mixed refrigeration system comprising methane, ehtylene and/or ethane, and propylene and/or propane.

Abstract: Method for the rejection of nitrogen from condensed natural gas which comprises (a) introducing the condensed natural gas into a distillation column at a first location therein, withdrawing a nitrogen-enriched overhead vapor stream from the distillation column, and withdrawing a purified liquefied natural gas stream from the bottom of the column; (b) introducing a cold reflux stream into the distillation column at a second location above the first location, wherein the refrigeration to provide the cold reflux stream is obtained by compressing and work expanding a refrigerant stream comprising nitrogen; and (c) either (1) cooling the purified liquefied natural gas stream or cooling the condensed natural gas stream or (2) cooling both the purified liquefied natural gas stream and the condensed natural gas stream, wherein refrigeration for (1) or (2) is obtained by compressing and work expanding the refrigerant stream comprising nitrogen.

Abstract: Improved methodology for starting up a LNG facility employing a refluxed heavies removal column. The improved methodology involves varying the temperature of the feed to the heavies removal column between start-up and normal operation. This allows a larger amount of the stream produced from the top of the heavies removal column during start-up to be used to more rapidly start up the LNG facility.

Abstract: In a refrigerant cycle apparatus, an energy-saving operation is performed by using a refrigerant which is used in a supercritical state. A refrigeration cycle apparatus is constituted by a main compressor, an expander, a sub compressor independently placed in an upstream side of the main compressor, a use side heat exchanger, a heat source side heat exchanger and the like. A refrigerant such as a carbon dioxide or the like which is used in a supercritical state is employed as the refrigerant. The sub compressor is driven by utilizing a recovered energy by the expanding device. Further, a refrigerant tank is provided, and properly controls an amount of the refrigerant circulating in the refrigerant cycle.

Abstract: Method for the rejection of nitrogen from condensed natural gas which comprises (a) introducing the condensed natural gas into a distillation column at a first location therein, withdrawing a nitrogen-enriched overhead vapor stream from the distillation column, and withdrawing a purified liquefied natural gas stream from the bottom of the column; (b) introducing a cold reflux stream into the distillation column at a second location above the first location, wherein the refrigeration to provide the cold reflux stream is obtained by compressing and work expanding a refrigerant stream comprising nitrogen; and (c) either (1) cooling the purified liquefied natural gas stream or cooling the condensed natural gas stream or (2) cooling both the purified liquefied natural gas stream and the condensed natural gas stream, wherein refrigeration for (1) or (2) is obtained by compressing and work expanding the refrigerant stream comprising nitrogen.

Abstract: The invention is an absorption process for recovering C2+ components from a pressurized liquid mixture comprising C1 and C2+. The pressurized liquid mixture is at least partially vaporized by heating the liquid mixture in a heat transfer means. The heat transfer means provides refrigeration to an absorption medium that is used in treating the vaporized mixture in an absorption zone. The vaporized mixture is passed to an absorption zone that produces a first stream enriched in C1 and a second stream enriched in C2+ components. The pressurized liquid mixture is preferably pressurized liquid natural gas (PLNG) having an initial pressure above about 1,724 kPa (250 psia) and an initial temperature above −112° C. (−170° F.). Before being vaporized, the pressurized liquid mixture is preferably boosted in pressure to approximately the desired operating pressure of the absorption zone.

Abstract: A method for the recovery of hydrogen and one or more hydrocarbons having one or more carbon atoms from a feed gas containing hydrogen and the one or more hydrocarbons, which process comprises cooling and partially condensing the feed gas to provide a partially condensed feed; separating the partially condensed feed to provide a first liquid stream enriched in the one or more hydrocarbons and a first vapor stream enriched in hydrogen; further cooling and partially condensing the first vapor stream to provide an intermediate two-phase stream; and separating the intermediate two-phase stream to yield a further-enriched hydrogen stream and a hydrogen-depleted residual hydrocarbon stream. Some or all of the cooling is provided by indirect heat exchange with cold gas refrigerant generated in a closed-loop gas expander refrigeration cycle.

Abstract: The invention relates to a process of manufacturing a pressurized multi-component liquid from a pressurized, multi-component stream, such as natural gas, which contains C5+ components and at least one component of C1, C2, C3, or C4. The process selectively removes from the multi-component stream one or more of the C5+ components that would be expected to crystallize at the selected temperature and pressure of the pressurized multi-component liquid product and leaves in the multi-component stream at least one C5+ component. The multi-component stream is then liquefied to produce a pressurized liquid substantially free of crystallized C5+ components. The removal of the C5+ components can be by selective fractionation or crystallization.

Abstract: A refrigerant mixture for a mixture throttle process contains from 0.06 mol/mol to 0.20 mol/mol propane, from 0.26 mol/mol to 0.36 mol/mol nitrogen and from 0.20 mol/mol to 0.38 mol/mol methane, the remainder being ethane.

Abstract: The invention is an absorption process for recovering C2+ components from a pressurized liquid mixture comprising C1 and C2+. The pressurized liquid mixture is at least partially vaporized by heating the liquid mixture in a heat transfer means. The heat transfer means provides refrigeration to an absorption medium that is used in treating the vaporized mixture in an absorption zone. The vaporized mixture is passed to an absorption zone that produces a first stream enriched in C1 and a second stream enriched in C2+ components. The pressurized liquid mixture is preferably pressurized liquid natural gas (PLNG) having an initial pressure above about 1,724 kPa (250 psia) and an initial temperature above −112° C. (−170° F.). Before being vaporized, the pressurized liquid mixture is preferably boosted in pressure to approximately the desired operating pressure of the absorption zone.

Abstract: The present invention is directed to methods and apparatus for improving the recovery of the relatively less volatile components from a methane-rich gas feed under pressure to produce an NGL product while, at the same time, separately recovering the relatively more volatile components which are liquified to produce an LNG product. The methods of the present invention improve separation and efficiency within the NGL recovery column while maintaining column pressure to achieve efficient and economical utilization of the available mechanical refrigeration. The methods of the present invention are particularly useful for removing cyclohexane, benzene and other hazardous, heavy hydrocarbons from a gas feed. The benefits of the present invention are achieved by the introduction to the NGL recovery column of an enhanced liquid reflux lean on the NGL components. Further advantages can be achieved by thermally linking a side reboiler for the NGL recovery column with the overhead condenser for the NGL purifying column.

Abstract: A process is described for separating the heavier hydrocarbons from a gaseous hydrocarbon feed wherein a first separator is employed to separate partially condensed gaseous feed and wherein the vapour portion undergoes work expansion and is fed to a fractionation column. The liquid portion is subcooled in heat exchange with the overhead vapour from the fractionation column, expanded, evaporated to provide refrigeration at a low temperature level, and fed to the fractionation column. The rewarmed residual vapour is subsequently compressed to a pressure suitable for export, with a portion of the compressed gas being cooled, condensed and recycled back to reflux the top section of the fractionation column. Also described is a process wherein a first separator is employed to separate partially condensed gaseous feed and wherein the vapour portion undergoes work expansion and is fed to a high pressure wash column. The liquid portion is expanded and fed to the base of the high pressure wash column.

Abstract: In the liquefaction of a hydrocarbon by indirect heat exchange with the refrigerant mixture of a refrigerant mixture cycle, the refrigerant mixture being compressed in multiple stages, the compressed refrigerant mixture (23) is at least partially condensed (E4) downstream of the penultimate compressor stage and is fractionated (D4) into a higher-boiling liquid fraction (26) and a lower-boiling gas fraction (24). The lower-boiling gas fraction (24) is compressed to the final pressure, partially condensed (E5) and fractionated (D5) into a lower-boiling gas fraction (10) and a higher-boiling liquid fraction (27). The higher-boiling liquid fraction (27) is added to the partially condensed refrigerant mixture stream (23), and the gas fraction (10) forms the lower-boiling refrigerant mixture fraction and the liquid fraction (26) forms the higher boiling refrigerant mixture fraction of the refrigerant mixture cycle.

Abstract: A process for enhancing the recovery of less volatile components, from a multi component gas mixture, in a cryogenic distillation column, which involves withdrawing a stream from the cryogenic distillation column and processing it to yield a stream leaner in the component to be recovered, which will be cooled and fed to the cryogenic distillation column as a reflux. The processing step may include heating or cooling the side draw and then further contacting the side draw with another stream which is substantially condensed.

Abstract: An efficient and easier to operate distillation process separates mixtures containing three of more components into streams enriched in one of the components. The invention converts a two-way communication between two distillation columns of a prior art thermally coupled distillation system into a one-way communication. Either a distillation section is added to one of the two distillation columns or a new distillation column is added, and only a liquid stream is transferred from one distillation column to another distillation column thereby eliminating the implementation of the return vapor stream between the same locations of the two columns. More than one distillation column produces product streams of at least one of the most volatile or the least volatile major constituent components.

Abstract: C2 and C3 hydrocarbons, particularly ethylene and propylene, are recovered from refinery or petrochemical plant gas mixtures by cooling and fractionating a feed gas mixture containing these hydrocarbons and lighter components. Refrigeration for the process is provided by a closed-loop gas expander refrigeration process cycle which preferably uses nitrogen as the recirculating refrigerant. Cooling and fractionation may be effected in a dephlegmator.

Abstract: A process is described for separating the heavier hydrocarbons from a gaseous hydrocarbon feed wherein a first separator is employed to separate partially condensed gaseous feed and wherein the vapour portion undergoes work expansion and is fed to a fractionation column. The liquid portion is subcooled in heat exchange with the overhead vapour from the fractionation column, expanded, evaporated to provide refrigeration at a low temperature level, and fed to the fractionation column. The rewarmed residual vapour is subsequently compressed to a pressure suitable for export, with a portion of the compressed gas being cooled, condensed and recycled back to reflux the top section of the fractionation column.

Abstract: This invention relates to a method of refrigeration purification and power generation of industrial gas and apparatus therefor. The apparatus is comprised of two parts, the front part of which is constituted by a multi-stage phase changeable refrigeration cycle of pure-phase changeable non-heat refrigeration technique for effectively obtaining cool quantity; the rear part of which makes use of the feature that the toxic and harmful gas in the waste gas has the higher boiling point than clean gas, the waste gas is firstly condensed and liquefied to be separated; the liquefied clean gas and the liquid refrigeration medium of the last stage absorb heat from waste gas in order to be evaporated into steam to drive expansion turbine groups respectively to work, while collecting a mechanical power in a negative compression region and adding a mechanical energy loss of initial cooled waste gas during compression.

Abstract: A process is disclosed for reliquefying boil-off gas produced by pressurized liquid natural gas. In this process, refrigeration duty is provided to a heat exchanger by means of a refrigeration cycle. Pressurized natural gas is cooled by the heat exchanger and then expanded to a lower pressure to produce a liquid stream that is passed to a first phase separator. A boil-off vapor is passed through the heat exchanger and it is then compressed and cooled before being recycled back through the heat exchanger. The compressed, cooled boil-off gas is then expanded and passed to a second phase separator. A vapor stream produced by the second separator is removed from the process. A liquid stream produced by the second phase separator is passed to the first phase separator to produce a pressurized liquid having a temperature above about −112° C. and a pressure sufficient for the liquid to be at or below its bubble point.

Abstract: LPG and gasoline are recovered from catalytic reformer plant treat gas and net gas by refrigeration-induced condensation and separation, using reformer plant waste heat to produce the refrigeration in an ammonia absorption refrigeration unit. Referring to FIG. 2, reformer waste heat from exchanger 21 powers absorption refrigeration unit 22, which supplies refrigeration to chiller 25. Net gas and treat gas is recuperatively cooled in recuperator 24, chilled in chiller 25, and separated in separator 26. Absorption refrigeration may also be supplied to cool FCC compressor inlet vapor to below ambient, either in conjunction with treat gas chilling or independently. Other waste heat streams may also be used.

Abstract: A high purity methane product is recovered from a feed gas mixture containing methane and one or more hydrocarbons heavier than methane by cooling, condensing, and rectifying the feed in a dephlegmator. The high purity methane product, containing at least 98 mole % methane, can be liquefied and stored for use as a fuel for internal combustion engines. A hydrocarbon product containing components heavier than methane is also recovered.Methane recovery and C.sub.2.sup.+ hydrocarbon product purity can be improved by the use of a combined stripping heat exchanger and feed gas cooler. External refrigeration is utilized and can be supplemented in part by autorefrigeration provided by vaporizing dephlegmator liquid.

Abstract: This invention relates to a process for producing pressurized liquid rich in methane from a multi-component feed stream containing methane and a freezable component having a relative volatility less than that of methane. The multi-component feed stream is introduced into a separation system having a freezing section operating at a pressure above about 1,380 kPa (200 psia) and under solids forming conditions for the freezable component and a distillation section positioned below the freezing section. The separation system produces a vapor stream rich in methane and a liquid stream rich in the freezable component. At least a portion of the vapor stream is cooled to produce a liquefied stream rich in methane having a temperature above about -112.degree. C. (-170.degree. F.) and a pressure sufficient for the liquid product to be at or below its bubble point. A first portion of the liquefied stream is returned to the separation system to provide refrigeration to the separation system.

Abstract: This invention relates to a process for liquefying a pressurized gas stream rich in methane in which the liquefication of the gas stream occurs in a heat exchanger being cooled by a closed-loop multi-component refrigeration system to produce a methane-rich liquid product having a temperature above about -112.degree. C. (-170.degree. F.) and a pressure sufficient for the liquid product to be at or below its bubble point. The liquefied gas product is then introduced to a storage means at a temperature above about -112.degree. C. (-170.degree. F.).

Abstract: A method for gas mixture demethanization is suitable for decreasing the loss of the target product (ethylene) and power requirements for gas mixture demethanization process.

Abstract: An ultra-high purity nitrogen trifluoride production method comprises: pressurizing a nitrogen trifluoride feed gas, eliminating moisture and carbon dioxide from the feed gas, and cooling down the same feed gas; causing the cooled feed gas to pass through adsorption columns, and introducing it into a medium-pressure rectification column by way of a reboiler in the medium-pressure rectification column, where it is rectified in the medium-pressure rectification column; introducing the resulting gas obtained by this rectification into a middle stage of a low-pressure rectification column, where it is rectified; and taking out ultra-high purity nitrogen trifluoride obtained by virtue of this rectification from the lower part of the low-pressure rectification column.

Abstract: The present invention relates to a system for separating a mixture containing at least two components, each component having a different volatility. The separation is achieved through the use of a fractional distillation column and upper and lower storage vessels in conjunction with a chilling unit for forming a liquid phase of the mixture and a generator for forming a gas phase of the mixture.

Abstract: A pressurized natural gas is liquefied through at least one cooling cycle, in which a mixture of cooling fluids is used, comprising at least the following steps:a) at least some of the said cooling mixture is condensed by compression and cooling, for example, using an external cooling fluid to obtain at least one vapor fraction and one liquid fraction,b) at least some of each of the vapor and liquid fractions is expanded separately to obtain a light fluid M1 comprising mostly a vapor phase and a heavy fluid M2 comprising mostly a liquid phase,c) the fluids M1 and M2 are at least partially mixed to obtain a low-temperature mixture, andd) the natural gas is liquified and undercooled under pressure by a process of heat exchange with the low-temperature mixture produced during step c).

Abstract: An improved closed loop single mixed refrigerant process and system for cooling a fluid material through a temperature range exceeding 200.degree. F.

Abstract: This invention relates to a gas liquefying method in which a power saving of a compressor for refrigerant can be attained.

Abstract: The present invention is a process of high efficiency rectification zone separation of cracked or other ethylene-containing gas chilled primarily by two closed mixed refrigerant loops and at least part of the dephlegmated overhead gas. The composition of the mixed refrigerants is optimally chosen to obtain an extremely close approach between the process condensation temperatures in the high efficiency rectification zone and the temperature of the chilling streams. An approach of about 3.degree. F. to 8.degree. F. can be achieved for the full condensation curve in the high efficiency rectification zone operating with either ethane or naphtha derived cracked gas. Highly reliable and stable operation is obtained by closed refrigeration loops in the present invention, in addition to reducing high efficiency rectification zone design cost.

Abstract: This invention concerns a novel process and apparatus for producing relatively small quantities of liquefied natural gas (LNG) by processing a side stream at a conventional NGL expander gas plant.

Abstract: An ethane-rich fraction for refilling the refrigerant circuit, using an ethane-containing refrigerant in a process for liquefaction of a hydrocarbon-rich fraction, is obtained by removing a partial flow of liquefied hydrocarbon-rich fraction and supplying same to a C.sub.1 /C.sub.2 /C.sub.3+ separation column. Roughly in the middle of this C.sub.1 /C.sub.2 /C.sub.3+ separation column, an ethane-rich fraction is withdrawn and, optionally after intermediate storage in a buffer tank, is added to the ethane-containing refrigerant.

Abstract: A vapor recovery system is provided which includes a vapor recovery cycle and a regeneration cycle. The vapor recovery is condensation of the vapors in an air-vapor mixture utilizing a chiller cooled by a refrigerant gas to condense and remove vapor and to vent the air. The refrigerant cooling is provided by a compression-condensation-expansion refrigeration cycle. During the vapor recovery cycle ice tends to build up in the chiller due to the small amounts of water contained in the air-vapor mixture. In the regeneration cycle the hot refrigerant gas from the compressor by-passes the condenser and expansion valve to heat the "chiller", which heats the air-vapor mixture and melts any accumulated ice. During the regeneration cycle there is no venting and the entire air-vapor mixture is recycled to the chiller until the regeneration is completed. In addition to heating and meting ice in the system, the heated air-vapor mixture may be used to dry and regenerate desiccant material in the system.