Abstract: A natural gas liquefaction system and method for effectively and efficiently removing heavy hydrocarbons and converting natural gas into liquefied natural gas. Natural gas streams entering the system may consist of varied gas compositions, pressures, and temperatures. In embodiments the system may comprise a natural gas (NG)-to-liquefied natural gas (LNG) portion and a closed-loop refrigeration portion comprising a closed-loop single mixed refrigerant system. In other embodiments the system may comprise an NG-to-LNG portion and a closed-loop refrigeration portion comprising a closed-loop gaseous nitrogen expansion refrigeration system. All embodiments utilize an integrated heat exchanger with cold-end and warm-end sections and integrated multi-stage compressor and expander configurations (e.g. compander) in order to increase overall operation flexibility and efficiency.

Abstract: An offshore facility for producing a liquefied natural gas using an associated gas includes a crude oil production offshore facility having a crude oil processing device for refining crude oil collected from a subsea well to produce oil, and a gas reinjection device for compressing an associated gas separated in crude oil refining process to be reinjected into a reservoir, and a liquefied natural gas production offshore facility supplied with a feed gas including at least a part of the associated gas from the crude oil production offshore facility, and processing and liquefying the feed gas to generate a liquefied natural gas. The crude oil production offshore facility includes a feed gas supply unit for recovering a back-flow gas formed when an injection gas compressed by the gas reinjection device flows backward and generating the feed gas by using the back-flow gas.

Abstract: A method and system for liquefying a natural gas feed stream and removing nitrogen therefrom.

Abstract: Devices, systems, and methods for liquefied natural gas production facilities are disclosed herein. A liquefied natural gas (LNG) production facility includes a liquefaction unit and a gas turbine. The liquefaction unit condenses natural gas vapor into liquefied natural gas. The LNG production facility further includes at least one post-combustion capture unit that captures a carbon dioxide (CO2)-rich stream from a flue gas stream of the gas turbine. The LNG production facility also includes a sequestration compression unit that compresses at least one CO2-rich stream from the at least one post-combustion capture unit.

Abstract: The present invention relates to a method and system for producing liquefied natural gas (LNG) from a stream of pressurized natural gas which involves a combination of mechanical refrigeration.

Abstract: Process for eliminating the evaporation of a liquefied natural gas stream during the transfer thereof into a storage facility, comprising the following steps: Step a): liquefaction, by means of a refrigeration cycle, of a natural gas stream and of a nitrogen stream in a main heat exchanger; Step b): cooling of the liquefied natural gas stream from step a) in a second heat exchanger by circulation of said liquefied natural gas stream countercurrent to a liquid nitrogen flow that is vaporized while cooling said liquefied natural gas stream; wherein the liquid nitrogen flow used in step b) is from step a).

Abstract: Method of liquefaction of methane and filling a tank (2) with liquefied methane, said method comprising: a step of liquefaction of the methane comprising an operation of cooling the methane to its saturation temperature, a step of filling the tank with the liquefied methane, a step of reinjection of the vaporized methane into the liquefaction system.

Abstract: A system for reliquefying a boil off gas generated in a storage tank includes a first compressor compressing a partial amount (hereinafter, referred to as ‘fluid a’) of boil off gas discharged from the storage tank, a second compressor compressing another partial amount (hereinafter, referred to as ‘fluid b’) of boil off gas discharged from the storage tank, a second expanding unit expanding a partial amount (hereinafter, referred to as ‘fluid c’) of a flow formed as the fluid a and the fluid b join, a heat-exchanger cooling another partial amount (hereinafter, referred to as ‘fluid d’) of the flow formed as the fluid a and the fluid b join, and a first expanding unit expanding the fluid d cooled by the heat-exchanger, wherein the heat-exchanger heat-exchanges the fluid d with the fluid c as a coolant expanded by the second expanding unit to cool the fluid d.

Abstract: A ship comprises: a tank; a multistage compressor for compressing a boil-off gas discharged from a storage tank and comprising a plurality of compression cylinders; a first heat exchanger for heat exchanging a fluid, which has been compressed by the multistage compressor, with the boil-off gas discharged from the storage tank and thus cooling the same; a first decompressing device for expanding a flow (“flow a1”) partially branched from the flow (“flow a”) that has been cooled by the first heat exchanger; a third heat exchanger for heat exchanging, by “flow a1” which has been expanded by the first decompressing device as a refrigerant, the remaining flow (“flow a2”) of “flow a” after excluding “flow a1” that has been branched and thus cooling the same; and a second decompressing device for expanding “flow a2” which has been cooled by the third heat exchanger.

Abstract: Liquefaction of industrial gases or gas mixtures (hydrocarbon and/or non-hydrocarbon) uses a modified aqua-ammonia absorption refrigeration system (ARP) to chill the gas or gas mixture during the liquefaction process. The gas is compressed to above its critical point, and the heat of compression energy may be recovered to provide some or all of the thermal energy required to drive the ARP. A Joule Thomson (JT) adiabatic expansion process results in no requirement for specialty cryogenic rotating equipment. The aqua-ammonia absorption refrigeration system includes a vapour absorber tower (VAT) that permits the recovery of some or all of the heat of solution and heat of condensation energy in the system when anhydrous ammonia vapour is absorbed into a subcooled lean aqua-ammonia solution. The modified ARP with VAT may operate at pressures as low as 10 kPa, and the ammonia gas chiller may operate at temperatures as low as ?71° C.

Abstract: A method for producing liquefied natural gas and a stream of liquid nitrogen including step a): producing gaseous nitrogen in an air separation unit; step b): liquefying a stream of natural gas in a natural gas liquefaction unit including a main heat exchanger and a system for producing cold; step c): liquefying the nitrogen stream resulting from step a) in the main exchanger of the natural gas liquefaction unit in parallel with the liquefied natural gas in step b); wherein all the cold necessary for liquefying the stream of nitrogen and for liquefying the natural gas is supplied by the system for producing cold of the natural gas liquefaction unit.

Abstract: A liquefier device which may be a retrofit to an air separation plant or utilized as part of a new design. The flow needed for the liquefier comes from an air separation plant running in a maxim oxygen state, in a stable mode. The three gas flows are low pressure oxygen, low pressure nitrogen, and higher pressure nitrogen. All of the flows are found on the side of the main heat exchanger with a temperature of about 37 degrees Fahrenheit. All of the gasses put into the liquefier come out as a subcooled liquid, for storage or return to the air separation plant. This new liquefier does not include a front end electrical compressor, and will take a self produced liquid nitrogen, pump it up to a runnable 420 psig pressure, and with the use of turbines, condensers, flash pots, and multi pass heat exchangers. The liquefier will make liquid from a planned amount of any pure gas oxygen or nitrogen an air separation plant can produce.

Abstract: The present invention relates to a refrigerant composition comprising neon and hydrogen. The present invention further relates to the use of the refrigerant composition in liquefying gaseous substances such as hydrogen or helium.

Abstract: A vessel comprising an engine comprises: a first self-heat exchanger for heat-exchanging boil-off gas discharged from a storage tank; a multi-stage compressor for compressing, in multi-stages, the boil-off gas, which has passed through the first self-heat exchanger after being discharged from the storage tank; a second self-heat exchanger for precooling the boil-off gas compressed by the multi-stage compressor; a first decompressor for expanding a portion of a fluid which has been cooled by the second self-heat exchanger and the first self-heat exchanger; and a second decompressor for expanding the other portion of the fluid which has been cooled by the second self-heat exchanger and the first self-heat exchanger.

Abstract: A vessel includes an engine; a first self-heat exchanger for heat-exchanging boil-off gas discharged from a storage tank; a multi-stage compressor for compressing, in multi-stages, the boil-off gas, which has passed through the first self-heat exchanger after being discharged from the storage tank; a first decompressor for expanding a portion of the boil-off gas, which has passed through the first self-heat exchanger after being compressed by the multi-stage compressor; a second decompressor for expanding the other portion of the boil-off gas, which has passed through the first self-heat exchanger after being compressed by the multi-stage compressor; and a second self-heat exchanger for heat-exchanging and cooling the portion of the boil-off gas, which has been compressed by the multi-stage compressor, by using, as a refrigerant, a fluid which has been expanded by the first decompressor.

Abstract: Compression train for a natural gas liquefaction process. The compression train includes a driver machine and only one centrifugal compressor machine driven in rotation by the driver machine; the compressor is configured to compress a refrigerant gas with a molecular weight less than 30 g/mol from a suction pressure to a discharge pressure; the ratio between discharge and suction pressures is higher than 10. A LNG plant including a compression train.

Abstract: Described herein are methods and systems for the liquefaction of a natural gas feed stream using a refrigerant comprising methane. The methods and systems use a refrigeration circuit and cycle that employs two or more turbo-expanders to expand two or more streams of gaseous refrigerant down to different pressures to provide cold streams of at least predominantly gaseous refrigerant at different pressures that are used to provide refrigeration for precooling and liquefying the natural gas. The resulting liquefied natural gas stream is then flashed to produce an LNG product and a flash gas, the flash gas being recycled to the natural gas feed stream.

Abstract: Certain aspects of natural gas liquid fractionation plant waste heat conversion to simultaneous power, cooling and potable water using integrated mono-refrigerant triple cycle and modified MED system can be implemented as a system that includes two heating fluid circuits thermally coupled to multiple heat sources of a NGL fractionation plant. An integrated triple cycle system, which includes an organic Rankine cycle (ORC), a refrigeration cycle and an ejector refrigeration cycle, is thermally coupled to the first heating fluid circuit. A MED system, configured to produce potable water, thermally coupled to the second heating fluid circuit. The system includes a control system configured to actuate control valves to selectively thermally couple the heating fluid circuits to portions of the heat sources of the NGL fractionation plant.

Abstract: A ship includes: a boil-off gas heat exchanger which is installed on a downstream of a storage tank and heat-exchanges a compressed boil-off gas (“a first fluid”) by a boil-off gas discharged from the storage tank as a refrigerant to cool the boil-off gas; a compressor installed on a downstream of the boil-off gas heat exchanger and compresses a part of the boil-off gas from the storage tank; an extra compressor which is installed on a downstream of the boil-off gas heat exchanger and in parallel with the compressor and compresses the other part of the boil-off gas from the storage tank; a refrigerant heat exchanger which additionally cools the first fluid; and a refrigerant decompressing device which expands a second fluid, which is sent to the refrigerant heat exchanger, and then sends the second fluid back to the refrigerant heat exchanger.

Abstract: A ship includes: a boil-off gas heat exchanger installed on a downstream of a storage tank and heat-exchanges a compressed boil-off gas (“a first fluid”) by a boil-off gas discharged from the storage tank as a refrigerant, to cool the boil-off gas; a compressor installed on a downstream of the boil-off gas heat exchanger and compresses a part of the boil-off gas discharged from the storage tank; an extra compressor installed on a downstream of the boil-off gas heat exchanger and in parallel with the compressor and compresses the other part of the boil-off gas discharged from the storage tank; a refrigerant heat exchanger which additionally cools the first fluid which is cooled by the boil-off gas heat exchanger; and a refrigerant decompressing device which expands a second fluid, which is sent to the refrigerant heat exchanger, and then sends the second fluid back to the refrigerant heat exchanger.

Abstract: A system and method for cooling a gas using a mixed refrigerant includes a compressor system and a heat exchange system, where the compressor system may include an interstage separation device or drum with no liquid outlet, a liquid outlet in fluid communication with a pump that pumps liquid forward to a high pressure separation device or a liquid outlet through which liquid flows to the heat exchanger to be subcooled. In the last situation, the subcooled liquid is expanded and combined with an expanded cold temperature stream, which is a cooled and expanded stream from the vapor side of a cold vapor separation device, and subcooled and expanded streams from liquid sides of the high pressure separation device and the cold vapor separation device, or combined with a stream formed from the subcooled streams from the liquid sides of the high pressure separation device and the cold vapor separation device after mixing and expansion, to form a primary refrigeration stream.

Abstract: A system for supplying compressed gas to several gas-fed devices is based on a liquid piston gas multistage compressor (100). Gas pressure measurements performed at a gas intake (10), an intermediate gas outlet (20) and at an end gas outlet (30) of the system allow controlling respective gas capacities of the compressor stages. Easy and reliable control can thus be obtained for the system operation. Varying the number of the compressor stages allows matching any pressure requirements for the gas delivery to all the gas-fed devices, and varying the gas capacities of the compressor stages allows easy adaptation to variable gas consumptions of the gas-fed devices.

Abstract: Methods and systems for reducing the pressure of a hydrocarbon-containing stream so as to provide a cooled, reduced-pressure hydrocarbon-containing stream are provided. Facilities as described herein utilize a single closed-loop mixed refrigeration system in order to facilitate transportation, loading, and/or storage of a liquefied hydrocarbon-containing material at or near atmospheric pressure. In some aspects, the facilities can include at least one separation device for removing lighter components from the feed stream, which may separately be recovered as a vapor product for subsequent processing and/or use.

Abstract: A system and method is provided for increasing the capacity and efficiency of natural gas liquefaction processes by debottlenecking the refrigerant compression system. A secondary compression circuit comprising at least one double flow compressor is provided in parallel fluid flow communication with at least a portion of a primary compression circuit.

Abstract: A liquefied natural gas production facility and a method of designing and constructing a liquefied natural gas production facility are described. The facility includes space-apart modules for installation at a production location to form a production train including a major axis and a minor axis, each module including a module base for mounting a plurality of plant equipment associated with a selected function assigned to the module, the module base including a major axis and a minor axis. Heat exchangers are arranged to run parallel to the major axis of the production train to form a heat exchanger bank including a major axis and a minor axis, where the major axis of the bank is parallel to the major axis of the train. A subset of the plurality of heat exchangers is arranged on a first level vertically offset from the base of at least one module.

Abstract: A method for start-up of a liquefied natural gas (LNG) plant, the plant including a liquefaction unit arranged in a flow path of the plant, including removing LNG from a first location in the flow path downstream of the liquefaction unit; vaporizing the removed LNG, or heating the removed LNG so that the removed LNG is transformed to gas phase; and re-admitting the vaporized or transformed LNG to the flow path at a second location upstream of the liquefaction unit. A corresponding LNG plant is also provided.

Abstract: A method includes directing a refrigerant fluid mixture and a flow of natural gas through a first heat exchanger for exchanging heat between a natural gas flow path and a first refrigerant flow path. The method also includes expanding the flow of natural gas exiting from the first heat exchanger via a first throttle valve. Further, the method also includes directing a generated cold natural gas vapor and a slurry having a liquefied natural gas and solidified carbon dioxide through a filter sub-assembly. Moreover, the method also includes separating the solidified carbon dioxide by the filter sub-assembly to form a purified liquefied natural gas. Finally, the method includes directing a pulse of a cleaning fluid having at least one of methane and carbon dioxide through the filter sub-assembly to remove the solidified carbon dioxide therefrom and storing the purified liquefied natural gas in a storage tank assembly.

Abstract: A system and method for producing liquefied natural gas from a natural gas source is provided. The method may include feeding natural gas provided by the natural gas source to a liquefaction module. The method may also include flowing the natural gas through a product stream of the liquefaction module. The method may further include flowing a process fluid through a liquefaction stream of the liquefaction module to cool at least a portion of the natural gas flowing through the product stream to produce the liquefied natural gas.

Abstract: A ship includes: a boil-off gas heat exchanger which heat-exchanges a compressed boil-off gas (“a first fluid”) by means of a boil-off gas discharged from the storage tank as a refrigerant; a compressor installed on the downstream of the boil-off gas heat exchanger and compressing a part of the boil-off gas discharged from the storage tank; first and second extra compressors provided in parallel with the compressor on the downstream of the boil-off gas heat exchanger and compressing the other part of the boil-off gas discharged from the storage tank; a refrigerant heat exchanger which additionally cools the first fluid cooled by means of the boil-off gas heat exchanger; a refrigerant decompressing device which expands a second fluid, which has been sent to the refrigerant heat exchanger and cooled by means of the refrigerant heat exchanger, and then sending the expanded second fluid back to the refrigerant heat exchanger.

Abstract: A method for controlling the flow of natural gas and refrigerant in the main heat exchanger of a natural gas liquefaction facility. The method provides for the automated control of a flow rate of a natural gas feed stream through a heat exchanger based on one or more process variables and set points. The flow rate of refrigerant streams through the heat exchanger is controlled by different process variables and set points, and is controlled independently of the flow rate of the natural gas feed stream.

Abstract: A ship including a storage tank for storing a liquefied gas includes: a boil-off gas (BOG) heat exchanger installed on a downstream of a storage tank and heat-exchanges a compressed BOG (“a first fluid”) by a BOG discharged from the storage tank as a refrigerant, to cool the BOG; a compressor installed on a downstream of the BOG heat exchanger and compresses a part of the BOG discharged from the storage tank; an extra compressor installed on a downstream of the BOG heat exchanger and in parallel with the compressor and compresses the other part of the BOG discharged from the storage tank; a refrigerant heat exchanger which additionally cools the first fluid cooled by the BOG heat exchanger; and a refrigerant decompressing device which expands a second fluid sent to the refrigerant heat exchanger, and then sends the second fluid back to the refrigerant heat exchanger.

Abstract: A system and method for liquefaction of a natural gas stream utilizing a plurality of asymmetric parallel pre-cooling circuits. The use of asymmetric parallel cooling circuits allows for greater control over each refrigerant stream during the cooling process and simplifies process control by dedicating heat exchangers to performing similar duties.

Abstract: A non-air compressed gas-based energy storage and recovery system and method include receiving a quantity of non-air compressible gas and removing contaminants therefrom utilizing a separator/filter then powering a compressor to volumetrically compress the compressible gas. The gas is passed through a cooler to reduce the gas temperature and increase its density and is transferred to a storage vessel. The stored gas is then routed to a heater to increase the temperature of the gas and the gas is expanded in an expander to drive the expander and an electrical generator operably connected thereto in order to generate electric power.

Abstract: A system and method for providing refrigeration to a cryogenic separation unit is provided. The disclosed system and associated methods employ both a warm recycle turbine arrangement and cold turbine arrangement to provide the refrigeration required to produce a large amount of liquid products, such as liquid oxygen, liquid nitrogen and liquid argon when used in a cryogenic air separation unit.

Abstract: A method for pressure and temperature control of fluid in a series of cryogenic compressors. An actual speed for each compressor and an actual inlet pressure and actual inlet temperature at entry are determined. The maximum speed for each compressor and a desired inlet pressure for the first compressor is provided. A speed index for each compressor is determined from the maximum speed and actual speed of each compressor. A proportional value is determined from the deviation of the actual and desired inlet pressure. A priority value is determined from the smaller of the proportional value and the smallest speed index. A desired inlet temperature for the first compressor and a desired speed for each compressor are determined from the priority value. The actual inlet temperature is adjusted to the determined desired inlet temperature and the actual speed for each compressor is adjusted to the determined desired speed.

Abstract: A system that can offload compressed gas from a storage tank to a customer site. The system can have a fluid circuit that is configured to fit within a container structure, like a trailer, for mobility to remote locations. This fluid circuit can include a transfer unit to automatically switch between tanks. The transfer unit can couple with a heat exchanger. Downstream of the heat exchanger, the fluid circuit can reduce pressure of fluid from the tanks through multiple pressure reduction stages. Each of the pressure reduction stages can include a throttling device, for example, a pilot-type fluid regulator and a control valve assembly. The throttling device may be selected to maintain flow of fluid at least at, e.g., 35,000 scfh, in accordance with pressure drops in the incoming fluid from the tanks.

Abstract: A method of liquefying a contaminated hydrocarbon-containing gas stream includes cooling the stream in a first heat exchanger and cooling the cooled stream in an expander to obtain a partially liquefied stream. The method further includes separating the partially liquefied stream in a separator to obtain a gaseous stream and a liquid stream. The liquid stream is expanded to obtain a multiphase stream containing at least a vapour phase, a liquid phase and a solid phase. The multiphase stream is separated in a separator to obtain a gaseous stream and a slurry stream. The slurry stream is separated in a solid/liquid separator to obtain a liquid hydrocarbon stream and a concentrated slurry stream. The gaseous stream is passed through the first heat exchanger to obtain a heated gaseous stream. The heated gaseous stream is compressed and combined with the contaminated hydrocarbon-containing gas stream.

Abstract: A system for liquefying a gas includes a liquefaction heat exchanger having a feed gas inlet adapted to receive a feed gas and a liquefied gas outlet through which the liquefied gas exits after the gas is liquefied in the liquefying passage of the heat exchanger by heat exchange with a primary refrigeration passage. A mixed refrigerant compressor system is configured to provide refrigerant to the primary refrigeration passage. An expander separator is in communication with the liquefied gas outlet of the liquefaction heat exchanger, and a cold gas line is in fluid communication with the expander separator. A cold recovery heat exchanger receives cold vapor from the cold gas line and liquid refrigerant from the mixed refrigerant compressor system so that the refrigerant is cooled using the cold vapor.

Abstract: In a method for cooling a flow containing at least 35% carbon dioxide and at least 0.2 ?g/Nm3 of mercury, the mercury being in liquid and/or gas form, the flow is cooled in a first brazed aluminum plate-fin heat exchanger from a first temperature to a second temperature higher than ?38.6° C. to form a cold flow at the second temperature, and the flow cooled to the second temperature is cooled in a second heat exchanger, which is a tube and shell heat exchanger, to a third temperature lower than ?38.6° C.

Abstract: Embodiments of the present invention provide a process for liquefaction of a natural gas. The process includes cooling the natural gas with a first refrigerant provided by a first cooling system and cooling the natural gas with a second refrigerant provided by a second cooling system. The second cooling system is a single phase cooling system. The first and second cooling systems operate independently from each other. The second refrigerant is cooled with the first refrigerant so that the cooling capacity of the second refrigerant and the second cooling system is increased.

Abstract: A method for liquefying a natural gas primarily including methane, preferably at least 85% of methane, the other components essentially including nitrogen and C2-C4 alkanes, in which the natural gas to be liquefied is liquefied by circulating at a pressure P0 no lower than the atmospheric pressure (Patm), P0 preferably being higher than the atmospheric pressure, in at least one cryogenic heat-exchanger (EC1, EC2, EC3) by a counter-current closed-circuit circulation in indirect contact with at least one stream of coolant gas remaining in the compressed gaseous state at a pressure P1 that is entering the cryogenic heat-exchanger at a temperature T3? that is lower than T3, T3 being the liquefaction temperature of the liquefied natural gas at the pressure P0 at the output of said cryogenic exchanger, characterized in that the coolant gas includes a mixture of nitrogen and at least one other component selected from among neon and hydrogen.

Abstract: An installation for refrigerating a same application by means of a single refrigerator/liquefier or several refrigerators/liquefiers arranged in parallel, the refrigerator(s)/liquefier(s) using a working gas of the same type having a low molar mass, each refrigerator/liquefier comprising a compression station to compress the working gas, a cold box intended for cooling the working gas at the outlet of the compression station, the compression station comprising only compression machines of the lubricated screw type and systems for removing the oil from the working fluid at the outlet of the compression machines, and the compression station comprises a plurality of compression machines defining several levels of pressure for the working fluid, the compression station comprising at least two compression machines defining at least two levels of pressure increasing above the level of pressure of the fluid at the inlet of the compression station, two main compression machines being arranged in series and defining,

Abstract: A process for liquefying and subcooling a hydrocarbon-rich fraction, particularly natural gas, is described wherein, once cooled down, the fraction is subjected to a partial condensation to remove heavy hydrocarbons, particularly benzene, by the steps of: a) the liquefied hydrocarbon-rich fraction is subcooled in a separate heat exchanger (normal mode), b) the supply of the liquefied hydrocarbon-rich fraction to the heat exchanger is interrupted at the latest when a defined solid deposition value in the heat exchanger is reached (cleaning mode), c) the solid in the heat exchanger is melted with a defrost gas and drawn off from the heat exchanger and d) the liquefied hydrocarbon-rich fraction is subsequently returned to the heat exchanger.

Abstract: A system and method for producing liquefied natural gas are provided. The method may include compressing a process stream containing natural gas in a compression assembly to produce a compressed process stream. The method may also include removing non-hydrocarbons from the compressed process stream in a separator, and cooling the compressed process stream with a cooling assembly to thereby produce a cooled, compressed process stream containing natural gas in a supercritical state. The method may further include expanding a first portion and a second portion of the natural gas from the cooled, compressed process stream in a first expansion element and a second expansion element to generate a first refrigeration stream and a second refrigeration stream, respectively. The method may further include cooling the natural gas in the cooled, compressed process stream to a supercritical state with the first and second refrigeration streams to thereby produce the liquefied natural gas.

Abstract: A method of natural gas liquefaction includes at least two nitrogen refrigerant streams. Each stream undergoes a cycle of compression, cooling, expansion and heating, during which each of the nitrogen streams is expanded to a different pressure other than for the others of the at least two nitrogen streams, and, the heating occurs in one or more heat exchangers. The expanded nitrogen streams are in a heat exchanging relationship with a stream of the natural gas and with the one or more compressed nitrogen streams in at least one of the one or more heat exchangers. At least one expanded nitrogen stream is compressed as a side stream in a stage of a main nitrogen compressor so as to combine the compressed side stream with another compressed nitrogen stream after passing the nitrogen compressor stage.

Abstract: This disclosure describes a natural gas collection system utilizing a single compressor to manage collection of natural gas from both high-pressure and low-pressure sources. The operation of the single compressor is controlled by a PLC configured to receive pressure data from sensors and to direct compressor speed in order to maintain natural gas pressure at the user defined targets.

Abstract: A process for liquefying natural gas by; a) causing it to flow through three series connected heat exchangers, where gas is cooled to T3; T3 is less/equal to the liquefaction temperature of natural gas at atmospheric pressure; and b) causing the closed circuit circulation of a first stream of refrigerant gas at a pressure P1 lower than P3 entering the third exchanger and leaving the first exchanger, the first stream obtained using a first expander to expand a first portion of a second stream at P3 higher than P2, the second stream flowing relative to the natural gas stream entering the first exchanger and leaving the second exchanger; and a third stream at a pressure P2 higher than P1 and lower than P3 flowing relative to the first stream, entering the second exchanger and leaving the first exchanger; c) the second stream at the pressure P3 obtained by compression.

Abstract: A method includes forming a mixed vapor supply stream (MVSS) including measured amounts of water vapor, hydrocarbon vapor, and a carrier gas. For multiple target temperatures, the method includes (i) cooling the MVSS to form a first liquid stream and a mixed vapor outlet stream (MVOS), (ii) cooling the MVOS to condense vapor and form a second liquid stream, (iii) measuring an amount of a selected component in the second liquid stream, and (iv) calculating an amount of the selected component in the first liquid stream as the difference between the measured amounts of the selected component in the MVSS and the second liquid stream. The amount of the selected component as a function of the target temperature is analyzed to identify a lowest temperature at which the first liquid stream is expected to contain none of the selected component other than an amount soluble in the first liquid stream.

Abstract: A system for converting gaseous fuel into liquid fuel is provided. The system may have a combustor configured to receive a supply of gaseous fuel. The system may also have a gas compressor configured to direct gaseous fuel from the supply into the combustor. The system may also have an air compressor configured to direct compressed air into the combustor, and a turbine in fluid communication with an outlet of the combustor. The turbine may be connected to drive the gas compressor and the air compressor. The system may also have at least one heat exchanger in fluid communication with an outlet of the gas compressor and an outlet of the air compressor. The system may also have at least one expander in fluid communication with an outlet of the at least one heat exchanger. The system may also have a condenser in fluid communication with an outlet of the at least one expander.

Abstract: The described invention relates to processes and systems for treating a gas stream, particularly one rich in methane for forming liquefied natural gas (LNG), the process including: (a) providing a gas stream; (b) providing a refrigerant; (c) compressing the refrigerant to provide a compressed refrigerant; (d) cooling the compressed refrigerant by indirect heat exchange with a cooling fluid; (e) expanding the refrigerant of (d) to cool the refrigerant, thereby producing an expanded, cooled refrigerant; (f) passing the expanded, cooled refrigerant to a first heat exchange area; (g) compressing the gas stream of (a) to a pressure of from greater than or equal to 1,000 psia to less than or equal to 4,500 psia; (h) cooling the compressed gas stream by indirect heat exchange with an external cooling fluid; and heat exchanging the compressed gas stream with the expanded, cooled refrigerant stream.