Liquefaction, solidification, or separation of gases or gaseous mixtures by pressure and cold treatment (F25J)

F25J              Liquefaction, solidification, or separation of gases or gaseous mixtures by pressure and cold treatment (cryogenic pumps f04b0037080000; gas storage vessels, gas-holders f17; filling vessels with, or discharging from vessels, compressed, liquefied, or solidified gases f17c; refrigeration machines, plants, or systems f25b)(1150)

Complex method for extraction of gas-condensate liquids and liquefaction of natural gas // 2641778
FIELD: oil and gas industry.SUBSTANCE: cooling and partially condensing an incoming stream containing light hydrocarbons in one or more heat exchangers. Partially condensed stream is introduced into cold gas/liquid separator producing a gaseous stream extracted from the top and the bottom streams, which are introduced into a fractionating system containing (a) fractionating column of light fractions and fractionating column of heavy fractions or (b) methane-stripping column. The gaseous stream extracted from the top is expanded and introduced into (a) the lower zone of the fractionating column of light fractions or (b) the upper zone of the methane-stripping column. A stream of bottom liquid (b) is introduced in the (a) fractionating column of heavy fractions at its intermediate point or (b) to the methane-stripping column at its intermediate point. The stream of liquid products is removed from the bottom portion of the fractionating column of heavy fractions or (b) the bottom portion of the methane-stripping column. The top gaseous stream(a) from of the fractionating column of light fraction s or methane-stripping column (b) is removed. The stream of the bottom liquid is removed from the bottom zone of the fractionating column of light fractions and introduced into the upper zone of the fractionating column of heavy fractions. If the system contains a fractionating column of light fractions and a fractionating column of heavy fractions, by indirect heat exchange with the first portion of the gaseous stream taken from above the fractionating column of light fractions is cooled and partially condensed from the top of gaseous stream of the fractionating column of heavy fractions and introduced into the fractionating column of light fractions. A second portion of the gas stream extracted from above the gas stream from the fractionating column of light fractions is removed, cooled and partially condensed by indirect heat exchange. Partially liquefied side-cut distillate is introduced into an additional separation device, the liquid product is recovered and introduced into the fractionating column of light fractions and/or to the fractionating column of heavy fractions as liquid reflux stream. The upper steam flow is extracted from the additional separation device, cooled and condensed by indirect heat exchange and the produced steam and condensate are supplied to LNG separator where the final LNG product is produced. The upper steam flow is extracted from the additional separation device, compressed to form the residual gas. A method and a device wherein a methane stripping column is used instead of column of heavy fractions is also provided.EFFECT: reduced energy consumption by installing of liquefied natural gas.18 cl, 27 dwg

ethod of low-temperature separation of air in plant for air separation and plant for air separation // 2641766
FIELD: machine engineering.SUBSTANCE: cooled AIR (AIR) at a first separation pressure in a first separation column (S1) is separated into the head fraction enriched with nitrogen and the oxygen-enriched bottom fraction. Additional cooled AIR (AIR) in the mixing column (M) at the pressure of the mixing column is liquefied to obtain the bottom fraction of the mixing column by direct heat exchange with oxygen-enriched liquid flow. The oxygen- enriched flow is produced at least partially from the oxygen-enriched bottom fraction from the first separation column (S1). Additional cooled air (AIR) in the second separation column (S2) at the second separation pressure is also divided into the nitrogen-enriched head fraction and the oxygen-enriched bottom fraction. Nitrogen-enriched head fraction of second separating column (S2) is cooled at least partially by bottom fraction from mixing column (M). Nitrogen-enriched head fraction of second separating column (S2) is conducted at least partially through liquefaction chamber of dephlegmator (E2) of the second separating column (S2). The dephlegmator (E2) is made in form of condenser-evaporator whose evaporation chamber is operated at evaporator chamber pressure which is between the pressure of the mixing column and the third separating pressure. At the third separation pressure, a liquid oxygen-enriched flow is obtained in the third separation column (S3). The readily assembled dephlegmator (E2) in liquid form under pressure evaporator Chamber bring at least part of the lower fraction of mixing column (M), and as the first separation of pressure using the pressure at least 0.5 bar higher than the pressure, which is used as a second separating pressure. The air separation plant comprises a first separating column (S1), a mixing column (M), a second separating column (S2) and a third separating column (S3), executed with the possibility to perform the method.EFFECT: increased air separation efficiency.10 cl, 1 dwg

ethod of production of compromised natural gas at the gas distribution station and booster compressor for the realisation of such method // 2641416
FIELD: oil and gas industry.SUBSTANCE: invention relates to technologies for the production of compressed natural gas, and can be used at gas distribution stations (GDS). A method of producing compressed natural gas at a gas distribution station in which a natural gas booster compressor is installed in the gas supply network from the main network to the gas distribution network and the natural gas is sent to the booster compressor from the backbone network and this gas is used simultaneously as a drive and compressed gases. During the operation of the booster compressor, compressed natural gas is produced for technological needs and, at the same time, the spent natural gas from the booster compressor drive is sent to consumers in the gas transmission grid.EFFECT: increase of energy efficiency of production processes of compressed natural gas at gas distribution stations.2 cl, 1 dwg

ethod of production of liquefied natural gas and compressed natural gas at the gas distributing station and complex for its implementation // 2641410
FIELD: oil and gas industry.SUBSTANCE: method of production of liquefied natural gas and compressed natural gas at a gas distribution station (GDS), a non-volatile one, which simultaneously produces liquefied and compressed natural gas. Natural gas is taken from the main gas pipeline, divided into two streams: the first stream is directed to the liquefaction of natural gas and, at the same time, the second stream is directed to natural gas compression. The second stream is passed alternately through a second compressor and an air-cooling unit. Concurrently, the first liquefaction stream is filtered, purified in an adsorber, cooled in at least one heat exchanger and divided into two streams: process and production. The process flow is directed to the expander, with the generator of which the electrical connection of the first compressor engines is established, which is used when the production flow of the incoming first gas stream is liquefied, and the second compressor, which is used to compress the incoming second gas stream, as well as the fans of the air-cooling unit. The production stream is passed through the first compressor, cooled in an air-cooling unit, then it is additionally cooled in at least one heat exchanger and passed through a choke to produce a vapor-liquid mixture. Liquid phase is separated from it and, completing the production flow, directs it for download to the consumer of liquefied natural gas. Reverse flow is formed from the vapor phase, directed through the heat exchangers of the production stream, connecting with the expanded and low-temperature process stream leaving the expander. The complex for implementing the method includes two lines. The first natural gas supply line contains a filtration unit, an adsorber, a heat exchanger and is divided into a process, production and return line. The production line comprises a first compressor, an air-cooling unit, and at least one heat exchanger, a choke, a separator and is connected to a liquefied natural gas storage. The return line originates in the separator, passes through the heat exchangers of the production line and is connected at the outlet to the gas transmission grid. The process line contains an expander and is connected to the return line, at the same time the second natural gas supply line comprises a second compressor, an air-cooling unit and is connected to the consumers of compressed natural gas, and the expander generator is connected through electrical communication with the motors of the first and second compressors, as well as with fans of air cooling units.EFFECT: increase of productivity at reduction of energy consumption.7 cl, 4 dwg

ethod for controlling liquefaction of natural gas // 2640976
FIELD: machine engineering.SUBSTANCE: invention relates to methods for controlling liquefaction of natural gas (LNG), and can be used for liquefaction and supercooling of natural gas. Method of controlling liquefaction of natural gas by means of a plant operating on mixed refrigerant consists in periodical measurement of actual parameters of said process and controlling the composition of refrigerant fed to the main cryogenic heat exchanger in order to achieve optimal process parameters. The Carnot factor is used as a criterion for optimal process parameters. The composition of refrigerant is controlled by direct calculation based on actual process parameters and equations of state of substance components quantity of mixed refrigerant (for example, equations of state of Penga-Robinson) necessary to achieve temperature profile in the main cryogenic heat exchanger corresponding to the optimal parameters of the process and introducing said components in calculated quantity in the main cryogenic heat exchanger.EFFECT: invention makes it possible to increase efficiency of natural gas liquefaction cycle and thereby minimize the specific power of the compressor required for production of liquefied natural gas.2 cl, 2 dwg
ethod for extraction of liquefied hydrocarbon gases from natural gas of main gas pipelines and plant for its implementation // 2640969
FIELD: oil and gas industry.SUBSTANCE: flow of natural gas is sequentially cooled and sent to a first low temperature separation stage, then gas separated in the first stage is expanded in a turbo expander and sent to a second low temperature separation stage. Liquid hydrocarbon fraction produced at the first separation stage is also sent after throttling to the second separation stage. The flow of separated gas of methane-ethane fraction is directed by reverse flow for natural gas cooling. The produced liquid flow is fed to the top of deethaniser column, from which gas flow of methane-ethane fraction is taken and after throttling it is combined with reverse gas flow of methane-ethane fraction produced at the second separation stage, then after recuperation of cold, combined flow of methane-ethane gas is additionally cooled and withdrawn from the plant as a commercial gas. After throttling, liquid fraction C3+ produced in the deethaniser column is sent to the middle part of the depropanizer column, from which the gas flow of propane fraction is sent to reflux, after that the produced liquid propane fraction is divided into two flows, the smaller one is fed into the upper part of the depropanizer column as a reflux, and the larger one is withdrawn from the plant. After throttling, liquid flow of C4+ fraction from the bottom of the depropanizer column is sent to the middle part of the debutanizer column, from the top of which the gas flow of butane fraction is sent to reflux. After that, the produced liquid butane fraction is divided into two flows, the smaller one is fed into the upper part of the debutanizer column as reflux, the larger one is cooled and removed from the plant, and after cooling the flow of C5+ liquid fraction is withdrawn from the plant from the bottom of the debutanizer column. The plant comprises two recuperative heat exchangers, two low temperature separators, the deethanizer column, the depropanizer column equipped with reflux condenser including a third recuperative heat exchanger and a separator, the debutanizer column equipped with dephlegmator including water cooler and a separator, three pumps, three air-cooling devices, turbo-expander, four throttles and connecting pipelines.EFFECT: increased gas processing efficiency, possibility for production propane and butane fractions separately.2 cl, 1 dwg

ethod for producing xenon concentrate and krypton from natural or associated petroleum gas // 2640785
FIELD: oil and gas industry.SUBSTANCE: method is implemented by feeding natural or associated petroleum gas into the reactor. Together with natural or associated gas, dispersed water is supplied into the reactor and thermal baric conditions are created by pressure in the range from 0.1 to 20 MPa and temperature in the range from -50 to +50°C to form a concentrate of ethane gas hydrates, propane, isobutane and krypton. They are further subjected to decomposition with formation of xenon concentrate and krypton.EFFECT: increased yield of the end product.2 dwg, 3 ex
ethod for purifying exhaust gases of isopropyl benzene oxidization // 2640781
FIELD: chemistry.SUBSTANCE: method for purifying exhaust gases of isopropyl benzene oxidation consists in recovering isopropyl benzene by a low-temperature condensation. To create low temperatures, the energy of the exhaust gases of the isopropyl benzene oxidation is used.EFFECT: invention makes it possible to increase the recovery of isopropyl benzene from the exhaust gases.1 dwg

ethod for removing heavy hydrocarbons when liquefying natural gas and device for its implementation // 2640050
FIELD: oil and gas industry.SUBSTANCE: invention describes a method for removing heavy hydrocarbons in the liquefaction of natural gas comprising: preliminarily cleaned and dried natural gas is cooled, obtained vapour-liquid mixture is separated in a separator into liquid and vapour phases, withdrawing the liquid phase with increased content of heavy hydrocarbons for disposal, wherein cooling of natural gas is carried out in a heat exchanger, the vapour phase is directed from the separator to ejector passive flow inlet, from the natural gas liquefaction plant a portion of high pressure cold flow is withdrawn and sent to ejector active flow inlet, a flow from ejector is directed to additional separator, in which the flow is separated into gas and liquid, gas is directed to heat exchanger for recuperation of cold. After recuperation of cold, gas is directed to a compressor, after the compressor the gas is sent to the natural gas liquefaction plant. A device for removing heavy hydrocarbons is also disclosed.EFFECT: providing uninterrupted operation of natural gas liquefaction plant without increase of machine equipment fleet.7 cl, 3 dwg

ethod of low-temperature preparation of low-pressure oil gas at field // 2637792
FIELD: oil and gas industry.SUBSTANCE: method includes introducing hydrate formation inhibitor into gas flow, cooling said gas by prepared gas cold recuperation and evaporation of coolant, separating cooled gas from condensed liquid phase, and supplying condensed hydrocarbons and prepared gas to consumer. The required degree of gas preparation is determined by dew point temperature which is the temperature of its cooling, the pressure of prepared gas is calculated from 0.04 to 0.45 Mpa by power dependence and the corresponding pressure of its flow is set. Gas is cooled and inhibited by cooling agent-ammonia to the dew point temperature. For this purpose, coolant is fed directly into gas flow to be prepared and evaporated therein. From the liquid phase condensed in cooled gas, the used coolant-aqueous-ammonia solution is recovered and pumped, thereby coolant pressure is reduced before it is supplied for evaporation. Then ammonia and water which is used for the technological needs of the field are desorbed from coolant.EFFECT: increased gas preparation efficiency.5 cl, 3 dwg

ethod of complex preparation of gas // 2637517
FIELD: oil and gas industry.SUBSTANCE: invention describes method for complex preparation of gas, wherein gas of input separation is refluxed by cooling with gas of low-temperature separation to obtain reflux and reflux gas which is mixed with condensate of input separation, and is weathered to produce evaporated condensate and the weathering gas which together with reduced reflux gas is subjected to low-temperature separation to produce gas and condensate, stabilization of mixture of condensates is provided by stabilization gas and stable condensate, before input separation raw gas is reduced and mixed with stabilization gas by means of ejecting device, gas of the input separation is cooled by reduced weathered condensate and preheated low-temperature separation gas, and the mixture of input separation condensate and reflux is reduced and mixed with condensate of low-temperature separation with the help of ejecting device before weathering.EFFECT: increased yield of stable condensate and commercial gas.2 cl, 1 dwg

ethod for production of liquefied natural gas // 2636966
FIELD: oil and gas industry.SUBSTANCE: method includes feeding compressed natural gas stream from high pressure main pipeline from gas distribution station inlet and dividing the flow into production and process streams. The process stream is expanded in expander with performance of an operation, fed to main preliminary heat exchanger, and supplied to the consumer at low pressure. The production stream is cooled by heating the process gas to form gas-liquid mixture further cooled and expanded in a throttle valve, at which outlet the liquid phase is separated by separator. The liquid phase is sent to the storage facility or to consumers of liquefied natural gas. The remaining part of the stream is mixed with the main process stream and sent to cold inlet of the heat exchanger. The production stream is subjected to purification and drying in a block of regenerative heat exchangers due to crystallization of CO2 on surface of their plates. After passing through the process stream, CO2 is dissoluted and removed with the flow of gas supplied to the consumers in the low pressure line.EFFECT: increase the efficiency of the production process.1 cl, 1 dwg

Plant for processing natural gas // 2635946
FIELD: oil and gas industry.SUBSTANCE: natural gas processing plant contains an absorber, a first, a second and a third separators, a first, a second, a third and a fourth heat exchangers, a first, a second and a third three-phase separators, each of which are connected to a water-methanol phase discharge pipeline, a device for air cooling of primary separation gas, a methanol feed unit, a gas cooler, a fractionating column, a furnace with heat-exchanging surface and collecting vessel of degassing having first outlet connected to pipeline for withdrawal of commercial liquid hydrocarbon product. Liquid hydrocarbon product obtained from liquid hydrocarbon phase withdrawn from the first separator is used as absorbent in the absorber. The absorbent is obtained by sequentially separating the gas in the first three-phase separator, the second three-phase separator, the third three-phase separator and fractioning in the fractioning column. The gas from the absorber passes through the fourth and the first heat exchangers and enters the product gas discharge pipeline.EFFECT: improvement of natural gas processing quality.3 cl, 2 dwg

Gas compression // 2634991
FIELD: oil and gas industry.SUBSTANCE: proposed the method, which contains gas compression in the mixture by weathering, liquid hydrocarbons released during gas compression cooling due to the reflux heating in the conditions of its stabilisation and its further cooling under the refluxing conditions to obtain the compressed gas and reflux, which is stabilised by liquid hydrocarbons released during gas compression heating to obtain the condensate, which is subjected to weathering under the reduced pressure to obtain the weathering gas.EFFECT: higher yield of the compressed air and pressure reduction of the condensate saturated vapor.2 cl, 1 dwg

Low-pressure heavy hydrocarbon gas stripping unit (variants) // 2634897
FIELD: oil and gas industry.SUBSTANCE: low pressure heavy hydrocarbon gas stripping unit includes a compressor mounted on a feed gas line, and a dephlegmator with condensate discharge line and a heat-mass exchange unit cooled by cooling agent. The method is characterized by that a multi-phase pump is installed as a compressor. A semi-blind plate is arranged in the dephlegmator above compressed raw gas inlet connected to raw gas line before the multi-phase pump by circulating reflux line, a reducing device and the heat-mass-exchange unit of the dephlegmator are arranged on the reflux line, condensate discharge line is connected to the separator equipped with residue discharge line and a line for feeding separation gas into the feed gas line before the multi-phase pump, and the condensate discharge line is connected to multi-phase pump by circulating condensate supply line. A version of the stripping unit is also claimed.EFFECT: reduced power consumption by excluding the use of external coolant, which role is performed by recirculation reflux.6 cl, 1 dwg
ethod of purifying natural gas from heavy hydrocarbons // 2634653
FIELD: oil and gas industry.SUBSTANCE: natural gas is extracted from main gas line, pre-dried, water vapours are removed and sent to a turbo-expander for subsequent cooling. The gas extracted from the network before liquefaction is directed to a screen filter casing, the direction of the gas flow is abruptly changed by 90°, which results in separation of heavy hydrocarbon particles from main gas flow which are accumulated in filter casing and drained through a special hole therein. Then the flow is fed to a guide apparatus casing of the turbo-expander and the flow is cooled during saponification of the outer surfaces of the guide apparatus slats. Heavy hydrocarbons not separated from the main stream in the filter are condensed and accumulated in the lower part of the guide apparatus casing, and extracted through a special hole therein.EFFECT: increased efficiency of natural gas purification from heavy hydrocarbons by using natural conditions for separation of gas impurities introduced into the expander.4 cl, 1 dwg

Plant for absorption preparation of natural gas // 2633563
FIELD: oil and gas industry.SUBSTANCE: natural gas absorbtion plant contains an absorber, a first, a second and a third separators, a first, a second, a third and a fourth heat exchangers, a first, a second and a third three-phase separators, a device for air cooling of primary separation gas, a methanol feed unit, a gas cooler, a furnace with heat-exchanging surface and collecting vessel of degassing having an outlet connected to pipeline for withdrawal of commercial liquid hydrocarbon product. Liquid hydrocarbon product obtained from liquid hydrocarbon phase withdrawn from the first separator is used as absorbent in the absorber. The absorbent is produced by sequentially separating gas from said liquid hydrocarbon product in the first three-phase separator, the second three-phase separator, the third three-phase separator and the third separator with intermediate heating in the furnace. The gas from the absorber passes through the fourth and the first heat exchangers and enters the product gas discharge pipeline.EFFECT: improvement of natural gas processing quality.3 cl, 2 dwg

ethod for preparing gas in oil and gas fields // 2633262
FIELD: oil and gas industry.SUBSTANCE: method involves purification from hydrogen sulphide and carbon dioxide, separation from dropping liquid, introducing inhibitor of hydrate formation into stream of prepared gas, separation of condensed hydrocarbons from cooled gas and used inhibitor, regeneration of main inhibitor component, supply of prepared gas and condensed hydrocarbons after their cold recuperation to consumer. Solution of ammonia and gas is used as inhibitor of hydrate formation, gas is cooled in evaporator with coolant-ammonia regenerated by desorption from mixture of used inhibitor and solution, obtained in the process of absorption from desorption water and ammonia after evaporator, the mixture for desorption is supplied with a pump, the regeneration of the main component of the inhibitor and the cooling agent-ammonia is executed together, recuperation of cold of prepared gas is additionally carried out by withdrawal of heat energy in the process of ammonia absorption by water, excess water after desorption is used for process needs of the field, losses of ammonia with prepared gas are replenished directly by its synthesis from nitrogen and hydrogen at the field or from outside.EFFECT: increased efficiency.2 cl, 1 dwg

ethod of extracting c2+ fraction from raw gas and plant for its implementation // 2630202
FIELD: oil and gas industry.SUBSTANCE: proposed method allows to extract sales gas and C2+ fraction from natural gas by low-temperature separation, rectification and heat transfer. Plant for the extraction of C2+ fraction of raw gas contains a demethaniser column equipped with a boiler and plates, five recuperative heat exchangers, a low-temperature separator, three turbochargers, two turbo-expander units, each of which includes a turboexpander and a turbocharger mounted on a single shaft with a turboexpander, a choke, an air cooling unit, propane cooling section and connecting pipelines.EFFECT: improving efficiency of the proposed technology by simplifying gas processing scheme and reducing capital and energy costs without deteriorating the quality of the products.2 cl, 1 dwg, 2 tbl

Associated oil gas compression plant // 2629344
FIELD: oil and gas industry.SUBSTANCE: presented plant includes a compressor, a fractionator with dephlegmator and stripping sections, and is connected to oil preparation plant. In the course of plant operation, associated oil gas from oil preparation plant is compressed in the compressor and fed between the sections to the fractionator. A first part of prepared oil as absorbent is fed to the upper part of the dephlegmator, and a second part is supplied as coolant to the block of heat-mass-exchange elements of the dephlegmator section and after heating it is returned to the oil preparation plant. Compressed gas is discharged from the top of the fractionator, and condensate is discharged from its bottom to the oil preparation plant. Crude oil is supplied to the oil preparation plant, and water and prepared oil are taken out. In the distillation section, a part of the compressed gas is supplied as a heat carrier after the compressor.EFFECT: reduction of losses of heavy components with compressed gas and increase in oil yield.3 cl, 1 dwg
Complex for liquefaction, storage and offloading of natural gas // 2629047
FIELD: oil and gas industry.SUBSTANCE: complex for liquefaction, storage and offloading of natural gas includes the following stages united by direct and reverse communications, parametres of which are set in accordance with impurity contance in raw natural gas, as well as with region climate conditions and topography: strage for separating and measuring natural gas, stage for purifying natural gas from mercury and methanol, stage for purifying natural gas from acidic impurities, stage for drying and purifying natural gas from mercaptans, stage for purifying natural gas from heavy hydrocarbons C5 and above, stage for liquefying natural gas, stage for storing and compounding refrigerant components, stage for compressing refrigerant, stage for storaging liquefied natural gas, stage for offloading liquefied natural, stage for compressing stripping gas compressor and stage for purifying stable condensate from mercaptans.EFFECT: invention solves the problem for developing a system for transporting natural gas from the field to the consumer with intermediate processing of natural gas, which involves extraction of gas and petrochemicals from valuable raw materials and regenerated reagents, while minimizing the losses of natural gas to the environment.5 cl, 1 dwg

ethod of hydrocarbon gas treatment for transportation // 2627754
FIELD: oil and gas industry.SUBSTANCE: method of treating condensate-containing formation gas for transportation in a basic plant by a three-stage separation involves feeding the gas flow to the primary separation stage, compressing the gas flow and cooling it down with ambient air, cooling the gas flow down. The gas flow is fed to the secondary separation stage, secondary gas flow cooling stage, the stage of gas flow decompression and cooling, then to the final separation stage. The separation gas is heated up by the gas flow after the secondary separation, both decompressed and cooled, then heated up by the gas flow after the primary separation. The separation gas is withdrawn from the basic plant, the liquid phase is fed after the final separation to separate the gas into degassing gas, unstable condensate and a water-methanol solution. The degassing gas is fed to the gas flow after the decompression with cooling, the liquid phase is mixed after the secondary and final separation, the mixed liquid phase is separated into a low pressure degassing gas, unstable condensate and a water-methanol solution. The unstable condensate is mixed and supplied for separation into weathering gas, unstable condensate and a water-methanol solution. The unstable condensate and water-methanol solution are discharged from the basic plant. The low-pressure degassing gas, weathering gas and deethanization gas from the condensate deethanization unplant are mixed, the mixed gas is injected into the gas flow, the deethanization gas is cooled down with the unstable condensate, transported from other gas treatment plants, and with the unstable condensate of the basic gas treatment plant.EFFECT: increase in the efficiency of the low-temperature separation plant by preventing the reduction of the unstable condensate output by the joint treatment of a gas condensate mixture of wells in the basic plant and gas from the condensate deethanization plant.1 tbl, 1 dwg

ethod of obtaining co, h2 and methanol from synthesis gas, in particular from the waste gas production of acetylene // 2627398
FIELD: chemistry.SUBSTANCE: invention relates to a process of the preparation of a product of methanol, product H2 and a CO product from a synthesis gas containing H2 and CO, in particular from the exhaust gas of acetylene production. The method includes separating a syngas stream into first and second partial synthesis gas streams where only the CO present in the first partial synthesis gas stream is converted to CO2 and H2 using steam, washing the first partial synthesis gas stream and a portion of the second partial synthesis gas stream, each in a separate column with an amine-containing washing agent, in particular for washing from CO2, wherein in particular the washing agent is regenerated in a common column, wherein the methanol product stream is formed from one portion of the washed converted first partial synthesis gas stream and/or another portion of the unconverted second syngas stream so that the ratio (H2-CO2)/(CO+CO2), which is required for the synthesis of methanol, is regulated in the methanol product stream, in particular in the range of 2.0 to 2.1, where the washed one part of the second unconverted partial synthesis gas stream is used to produce the CO product stream and the H2 product stream and where the other portion of the washed first partial synthesis stream is synthesized, gas is used to produce the product stream H2.EFFECT: invention provides an efficient and economical preparation of three methanol products, H2 and CO from a synthesis gas containing H2 and CO.10 cl, 1 dwg

Plant for processing of low-pressure hydrocarbon gases and liquid hydrocarbons (versions) // 2626840
FIELD: oil and gas industry.SUBSTANCE: plant includes, in the first version, the compression units of the first and second stages, a reducing device, a low-temperature separator, two de-ethanizers, a heat exchanger. In the second and fourth versions, the plant is additionally includes a debutanizer, and in the third and fourth - a purification and/or drying unit. In operation of the plant in the first version, the feed gas is mixed with deethanization gases, compressed and refluxed in the first stage compression unit to obtain condensate, cooled in heat exchanger, compressed and refluxed in the second stage compression unit to produce condensate, fed to the heat exchanger as coolant, and compressed gas which through the reducing device is supplied to low temperature separator from which the gas is supplied as coolant to the second stage compression unit and withdrawn after heating as commercial gas, condensate is fed to the first deethanizer, where it is separated into gas, supplied to deethanization gas supply line and technical propane/automobile propane, withdrawn from the plant. Liquid hydrocarbons are fed to the second deethanizer together with condensates of the first and second stages, where they are separated into gas supplied to the feed gas line and technical propane-butane/technical butane, withdrawn from the plant.EFFECT: invention provides increased recovery of hydrocarbons, expansion of production range, co-processing of low-pressure hydrocarbon gases and liquid hydrocarbons.16 cl, dwg 1

ethod of yield increase and stabilization of fractional natural gas liquefaction plant located at gas distribution station // 2626615
FIELD: oil and gas industry.SUBSTANCE: gas stream is withdrawn from the main gas pipeline with a pressure relief during an increase in the gas pressure in the main gas pipeline and the gas flow in the gas distribution net to supply the gas to the consumer via the open first main flow regulator, after which the gas is sent to a natural gas partial liquefaction plant. At the same time, the reverse flow formed in the partial liquefaction plant of natural gas is sent through a regulator of the reverse gas flow, where pressure is released, to the gas distribution network to supply the gas to the consumer. When the gas pressure in the main gas pipeline and the gas flow in the gas distribution net for supplying gas to the consumer are being decreased, the first main gas flow regulator is closed and the gas flow from the main gas pipeline is directed through the open second regulator of the main gas stream, with the help of which the main gas flow pressure is reduced to the working pressure of the gas flows mixing to one of the inputs of the gas stream mixer. Then the gas flow is directed to a pressurized compressor device, and then to the inlet of the partial natural gas liquefaction plant. At the same time, the reverse flow formed in the natural gas partial liquefaction plant is directed, on the one side, through the gas return regulator to the gas distribution net to supply the gas to the consumer, and on the other side through the third gas flow regulator for recirculation and compression into the circulation compressor unit with its subsequent supply to another inlet of the gas flow mixer. In the mixer, the compressed circulating gas flow is mixed with the main gas flow and the resulting flow is fed to the suction drum of a pressurized compressor device feeding the gas flow to the inlet of the natural gas partial liquefaction plant.EFFECT: increasing of the liquefaction rate of the natural gas liquefaction complex and reducing of the dependence of the natural gas liquefaction process on the seasonal unevenness of changes of pressure and main flow gas flowrate from the main gas pipeline to the gas distribution station.4 cl, 2 dwg

Autonomous plant of liquefied natural gas cleaning (versions) // 2626612
FIELD: oil and gas industry.SUBSTANCE: plant contains a raw liquefied natural gas (LNG) heater, a compressor, a clean LNG tank separator with a separated vapor discharge line and a rectification column with a bottom liquid outlet branch pipe. The pipeline for discharging the heating medium from the raw LNG heater is connected to the supply line of the clean LNG tank separator and to the reflux liquid supply line to the rectification column. In the first, second and third embodiment, the plant comprises of an evaporator, and partially condensed compressed steam is used as the heating medium in the raw LNG heater. The cooling medium of the rectification column evaporator is the bottom liquid of the rectification column.EFFECT: improving the quality of liquefied natural gas cleaning.4 cl, 4 dwg

ethod of stripped gas compression // 2626270
FIELD: oil and gas industry.SUBSTANCE: stripped gas compression method involves heating the stripped gas obtained by separating hydrocarbons C2+above from the dried gas with its low-temperature condensation and rectification, compression of the stripped gas in the compressor part of the turbo expander and cooling of the stripped gas. At the same time, prior to the stripped gas compression in the compressor part of the turbo expander, a portion of the heated stripped gas flow is taken and its parallel compression is performed in the compressor. The amount of the taken portion of the flow is determined by calculation, depending on the power of the turbo expander, which is determined by the required degree of recovery of hydrocarbons C2+above, and the compression ratio of the compressor, determined by the required pressure of the commercial stripped gas. In addition, after parallel compression in the compressor, the flow of the stripped gas is combined with the flow of the stripped gas, exiting the compressor part of the turbo expander, ensuring that the pressure of the combined flows is equal, and then directed to cooling.EFFECT: reduction of operating and capital costs.1 dwg, 2 tbl

ethod of non-waste pretreatment of production fluid // 2625846
FIELD: oil and gas industry.SUBSTANCE: method for non-waste pretreatment of production fluid involves stepwise separation of wet gas to produce condensate and gas at each stage, separating the first stage gas under reflux conditions and reducing the second stage gas. The gas of the first stage and debutanization gas are dried. The dried first stage gas is reduced and separated in the second stage by cooling with the reduced second stage gas, which is then mixed with the dried debutanization gas and withdrawn as a sales one. The condensates of the first and second stages are reduced and debutanized to produce gas and sales condensate.EFFECT: elimination of hydrate formation inhibitor consumption, elimination of light gas components losses and improvement of condensate quality.1 dwg

Gas treatment plant // 2624710
FIELD: oil and gas industry.SUBSTANCE: gas treatment plant includes the inlet separator, the reflux exchager and the low-temperature separation unit. The gas/reduced condensate heat exchanger is installed before or after the inlet separator. The gas/low-temperature separation gas heat exchanger is positioned after the inlet separator, it is heated in the reflux exchager, which is made single-section. The unit is equipped with the condensate stabilisation unit.EFFECT: improvement of the traded gas and condensate quality.1 dwg

ethod of non-waste pretreatment of production fluid (versions) // 2624656
FIELD: oil and gas industry.SUBSTANCE: according to the first version of the proposed method, the raw gas is separated at the first stage with gas water and hydrocarbon condensates production, the latter is reduced and stabilised together with the second stage condensate with production of the first stabilisation gas and the residue. The first stage gas is reduced and separated in the mixture with the first stabilisation gas at the second stage by cooling under the reflux conditions to form the condensate and gas, which is reduced, mixed with the second stabilisation gas, and separated at the third stage to form the condensate and gas, which is heated and discharged as the traded one. The stabilisation residue is reduced and stabilised together with the third stage condensate to produce the traded condensate and the second stabilisation gas. According to the second version of the proposed method, the hydrocarbon condensate of the first stage is reduced and stabilised, and the stabilisation residue is reduced and stabilised together with the third stage condensate and the reduced condensate of the second stage.EFFECT: increase of the hydrocarbon recovery and the gas light components losses elimination.8 cl, 2 ex, 2 dwg

Device of intermediate gas separation (versions) // 2624654
FIELD: oil and gas industry.SUBSTANCE: two versions of the device are suggested. The device according to embodiment 1 includes the reflux exchanger with the reflux section, two reduction devices and two recovery heat exchangers. The reflux exchanger of version 2 is additionally equipped with the stripper. While operating the device of embodiment 1, the inlet separation gas is divided into two parts, one of which is cooled in the first recovery heat exchanger by the traded gas, and the other, is cooled in the second recovery heat exchanger by the reduced condensate, mixed and through the reduction device sent to the reflux exchanger below the reflux section, where it is cooled under the reflux conditions by the gas of low-temperature separation, and then removed after heating in the first recovery heat exchanger as the traded gas. From the top of the reflux exchanger the gas is sent to the low-temperature separation, and the condensate is removed from the bottom, reduced for cooling, heated in the second recovery heat exchanger and sent for stabilisation. The operation of the device according to the 2 version is characterised in that the coolant is supplied to the stripper.EFFECT: improvement of the traded gas quality and increase of the condensate yield.2 cl, 1 dwg

Three-product gas treatment plant // 2624652
FIELD: oil and gas industry.SUBSTANCE: three-product gas treatment plant includes the inlet separator, the reflux exchanger, the reduction device and the low-temperature separator. There is the ejector equipped with the debutanization gas feeding line before the input separator. The recuperation heat exchanger and the reduction device are installed before the reflux exchanger. The low-temperature separator is connected by the deethanization gas and the condensate feeding lines to the deethanizer, equipped with the propane-butane fraction outlet line, connected to the condensate feeding line reflux exchanger, at which the reduction device is installed. The plant includes the reduction device and the debutanizer, equipped with the debutanization gas lines and the stable condensate outlet. The heat exchanger for cooling at least the part of the debutanization gas is placed at the condensate feeding line from the reflux exchanger between the reduction device and the deethanizer.EFFECT: expansion of the products range and the quality of the traded gas and condensate improvement.2 cl, 1 dwg

Associated petroleum gas preparation plant // 2624626
FIELD: oil and gas industry.SUBSTANCE: invention discloses the associated petroleum gas preparation plant, including the heater and the converter, equipped with the converted gas exhaust line with the recovery device, wherein the plant is equipped with the selective methanation gas converter of the associated petroleum gas with the gas-vapor mixture input line and is equipped with the water preparation unit, connected by the prepared water supply line with the associated petroleum gas supply line and equipped with the salt concentrate discharge lines, the water input and the degassing water condensate supply from the reflux exchanger, which is mounted on the gas-vapor mixture input line.EFFECT: improvement of the prepared gas quality, reduction of the energy consumption and metal consumption of the plant.3 cl, 1 dwg

ethod of natural gas liquefaction // 2623021
FIELD: oil and gas industry.SUBSTANCE: refrigerant stream consisting of several components with different boiling points, is compressed in the first pressure stage, cooled in the intercooler, after the intercooler of the first stage of compression and mixing, the intermediate pressure stream is separated in the first separator into liquid and gas fractions. The gas fraction is compressed in the second pressure stage of the compressor and is sent to the second separator from which the high pressure liquid fraction expands to an intermediate pressure is heated in the fourth heat exchanger and returned to the second pressure stage before the first separator. The liquid fraction from the first separator is pre-cooled in the fourth heat exchanger due to the cold of the expanded liquid fraction from the second separator, then it is cooled in the first heat exchanger together with the natural gas, expanded to low pressure and mixed with the return flow. The liquid fraction from the third separator is cooled in the second heat exchanger along with the natural gas, expanded to low pressure and mixed with the return flow from the third heat exchanger which, after evaporation in the second and first heat exchangers, is sent to the first pressure stage of the compressor. The gas fraction from the third separator is sequentially liquefied together with the natural gas in the second and third heat exchangers, is expanded and directed to the return flow.EFFECT: increased energy efficiency of the process of natural gas liquefaction.1 dwg

Light fractions recovery unit // 2623001
FIELD: machine engineering.SUBSTANCE: light fractions recovery unit includes a compressor and a cooling and separation device installed in the gas supply line from the tanks, a gas blower is installed as a compressor. The apparatus further includes an adsorption unit comprising at least two adsorbers with heat exchange unit units disposed in the adsorbent bed, one of which is in the adsorption mode and the other in the regeneration and cooling mode. The device for cooling and separation is made in the form of a two-section reflux condenser with a separation zone and a feeding zone. The upper section of the reflux condenser is connected by the refrigerant input/output lines to the refrigeration machine, the lower section is connected by the intake line of the purified gas mixture to the adsorber in the adsorption mode and equipped with a line for its withdrawal. The separation zone is equipped with a condensate outlet line, the supply zone is connected to the compressor, and the top of the reflux condenser is with the adsorber in the adsorption mode. In addition, the adsorber in the regeneration mode is connected to the lines of the cleaned gas mixture outlet and the gas mixture to the compressor, and its heat exchange element block is connected to the refrigerating machine by the heat carrier supply line.EFFECT: elimination of restrictions on the volume of compressible gas mixture and reduction of energy consumption and metal consumption of equipment.3 cl, 1 dwg

ethod of condensing vapours of oil products // 2622948
FIELD: oil and gas industry.SUBSTANCE: method of condensing vapours of oil products involves the evacuation of hydrocarbon vapors from the storage tank of oil products, their cooling and condensation, the collection of condensate formed in the intermediate collector, the separation of water from liquid hydrocarbons, and the return of liquid hydrocarbons to the storage tank. A vapour compression heat pump is used in this method, which comprises a compressor, a condenser, a thermostatic expansion valve and a two-section evaporator, the operating and protection sections of which alternately operate in the condensing and regeneration modes, correspondingly. Hydrocarbon vapours from the storage tank are led to an evaporator section operating in a condensation mode, the water contained therein is condensed on the heat exchange surface in the form of an ice crust by recuperative heat exchange with a boiling refrigerant, and the condensed liquid oil product separated from the water is led to the intermediate collector to be returned to the oil product storage tank. The condensing heat of the refrigerant in the condenser of the heat pump is used to heat the intermediate heat carrier by means of recuperative heat exchange. The intermediate heat carrier heated in the condenser is divided into two streams, one of which is fed to the evaporator section operating in the regeneration mode to defrost the ice crust, and the second stream is fed to the wasteheat exchanger; the streams of the waste intermediate heat carrier and the wasteheat exchanger are combined after the evaporator section operating in the regeneration mode and are returned to the condenser in the closed cycle mode. The water formed during the defrost of the ice crust together with the water, containing traces of hydrocarbons, from the intermediate collector is preheated in the wasteheat exchanger and directed to the biological treatment stage.EFFECT: increasing the energy efficiency of the process of continuous condensation of vapour mixture containing vapours of oil products and water, creating an explosion-safe, environmentally clear and economically profitable technology for storing oil products.1 dwg

Three-product complex natural gas treatment plant (versions) // 2622930
FIELD: oil and gas industry.SUBSTANCE: four versions of plant are proposed, consisting of input separation units, gas treatment, condensate stabilisation and catalytic processing. During operation of the first plant verison, the raw gas is separated in the input separation unit to produce the water condensate, discharged from the unit, the separation gas supplied to the gas treatment unit, and the condensate supplied to the condensate stabilisation unit after mixing with a wide fraction of light hydrocarbons, supplied from the gas treatment unit. Stable condensate is discharged from the condensate stabilisation unit, and the stabilisation gas is supplied to the catalytic processing unit, from which at least one liquid product of catalytic processing is withdrawn, and the catalytic processing gas is supplied to the gas treatment unit, from which the commercial gas is withdrawn. During operation of the second and fourth verisons, the catalytic processing gas is supplied to the commercial gas exhaust line, and during operation of the third and fourth plant verisons, at least a portion of the liquid product from the catalytic processing unit is supplied to the condensate exhaust line.EFFECT: reducing energy costs and expanding the range of products.8 cl, 1 dwg

Low-temperature separation plant (versions) // 2622926
FIELD: oil and gas industry.SUBSTANCE: low-temperature separation plant includes a dephlegmator-stabiliser with upper dephlegmation and bottom stripping sections, as well as a low-temperature separator with a reducing device and a pump. The stripping section of the dephlegmator is equipped with a feed line of at least a portion of the inlet separation gas. In the feed line of the inlet separation gas, in front of the dephlegmator, a heat exchanger of inlet separation gas/commercial gas and a reducing device are installed. The pump is connected to the upper part of the dephlegmator above the dephlegmation section by a low-temperature separation condensate feed line. According to the second verison, the reducing device and the heat exchanger of a portion of the inlet separation gas/reduced condensate are located in the condensate outlet line.EFFECT: increased yield and quality of commercial gas.4 cl, 1 dwg

Installation of three-product preparation of sulfur dioxide gas // 2622925
FIELD: machine engineering.SUBSTANCE: installation of three-product preparation of sulfur dioxide gas includes an inlet separator, a dephlegmator, a reducing device and a low-temperature separator. Before the separator, an ejector with a debutanization gas feed line is installed in a mixture with the off-gas. A recuperative heat exchanger and a reducing device are installed before the reflux condenser. The low-temperature separator is connected by deethanization and condensate deethanizer lines to a deethanizer equipped with a propane-butane fraction recovery line. A reducing device and a debutanizer connected to the reflux condensate line with a reducing device, equipped with debutanization gas lines and a stable condensate outlet, are installed on the condensate outlet line from the inlet separator. On the commodity gas outlet line, following the recovery heat exchanger, there are desulfurization and dehydration units equipped with lines for the discharge of sulfur or its compounds and waste gas to the debutanization gas line, respectively.EFFECT: preparation of sulfur dioxide gas, expansion of product range and improvement of gas and condensate quality.1 dwg

ethod and device for removing nitrogen from cryogenic hydrocarbon composition // 2622212
FIELD: chemistry.SUBSTANCE: nitrogen is removed from the cryogenic hydrocarbon composition. The cryogenic hydrocarbon composition is divided into a first portion and a second portion having the same composition and phase as the first portion. The first part is fed to a desorption column of nitrogen operating at a desorption pressure, from which a nitrogen-depleted liquid is discharged. The second portion is fed to a nitrogen-depleted liquid or to a liquid hydrocarbon product stream or process steam that is produced from nitrogen-depleted liquid by performing at least a pressure-depletion stage of the nitrogen-depleted liquid to a flash point that is lower than the desorption pressure. The second portion bypasses the nitrogen desorption column between the flow division and the supply of the second portion to the nitrogen-depleted liquid, or the liquid hydrocarbon product stream, or process steam.EFFECT: reducing the size of the installation and increasing the reliability.20 cl, 2 dwg

System and method for producing liquefied hydrocarbons flow and method of compressor operation // 2621591
FIELD: engines and pumps.SUBSTANCE: at least part of the fluid medium is compressed in the compressor driven by an electric motor. The compressor includes adjustable inlet guide vanes, the rotation angle of which can be adjusted. The electric motor is supplied with electric power from the mains, and the signal indicating the mains state is controlled. The necessity of additional load reduction is determined automatically by this signal by means of comparing the received signal with a predetermined criterion. The adjustable inlet guide vanes are automatically adjusted when the predetermined criterion is met and the additional load reduction is necessary. The compressor and the method of its operation may be used as part of a system for producing the liquefied hydrocarbons flow and / or during the production of liquefied hydrocarbon flow. The compressor may be a refrigerant one, and the fluid medium may be a refrigerant.EFFECT: decreasing the compressor load.19 cl, 2 dwg

ethod of reversing liquefaction of the rich methane of fraction // 2621572
FIELD: chemistry.SUBSTANCE: method of reverse liquefaction of a methane-rich fraction, in particular a vaporized gas, is claimed. In this case, the methane-rich fraction is compressed to a pressure that is at least 20% higher than the critical pressure of the fraction to be compressed, liquefied and supercooled. Further, it is discharged to a pressure between 5 and 20 bar and is separated into a gaseous nitrogen-rich fraction and a liquid nitrogen-depleted fraction. The nitrogen-depleted fraction is discharged to a pressure between 1.1 and 2.0 bar. The resulting gaseous fraction without being heated and compressed is mixed in a methane rich fraction. The liquid fraction of the product is obtained by unloading the nitrogen-poor liquid has a nitrogen content ≤1.5 mol. %.EFFECT: reducing the costs.5 cl, 1 dwg

ethod of obtaining natural gas processed, fraction enriched by c3+ - hydrocarbons, and, optionally, flow enlarged by ethan, and also, installation appropriate for this method // 2620601
FIELD: chemistry.SUBSTANCE: method comprises the following steps: selecting a recycle stream in the upper stream exiting the separation column; establishing a certain heat exchange interaction between the recycle stream and at least one portion of the overhead stream exiting the separation column; repeated administration, after expansion, of the cooled and expanded recycle stream into the isolation column; selecting, in the bottom of the column, the separation of at least one reboiling bottoms stream and providing heat exchange between the re-boiling stream and at least one portion of the feed natural gas and/or with the recycle stream. The re-boiling of the bottom liquid is provided by calories absorbed from the original natural gas stream and/or the recycle stream. The invention also relates to a device.EFFECT: invention allows to reduce power consumption.15 cl, 6 dwg, 9 tbl

Liquefying of natural gas in moving environment // 2620310
FIELD: chemistry.SUBSTANCE: invention relates to a process for liquefying natural gas in the floating liquefaction installation. The method comprises: a) introducing a cooling agent in the separation vessel (42) to form the stream (6) of vapor cooling agent and stream (8) of liquid cooling agent; b) introducing a flow (8) of liquid cooling agent around the lower part situated externally with respect to the separation vessel (42) of the core (50) of the heat exchanger; c) introducing the warmer process stream (12) into the externally located core (50) of the heat exchanger above the stream (8) of liquid cooling agent; d) cooling of warmer process stream (12) through indirect heat exchange with the liquid cooling agent stream (8) in the externally located core (50) of the heat exchanger to form a cooled process stream (14) and stream (16) of partially vaporized cooling agent; e) removal of cooled process stream and stream of partially vaporized cooling agent from the externally located core (50) of the heat exchanger. The separating vessel (42) has movement damping baffles.EFFECT: invention improves efficiency of natural gas liquefaction in the floating installation.4 cl, 2 dwg

ethod and apparatus for separating co2 while cooling with using laval nozzle // 2619312
FIELD: chemistry.SUBSTANCE: method for separating carbon dioxide (CO2) from a gas stream and the apparatus for separating carbon dioxide (CO2) from a CO2-comprising stream are claimed. The method comprises cooling the gas stream at the cooling step to obtain a cooled gas stream, and cooling said cooled gas stream in the Laval nozzle to obtain one type of CO2 - solid or liquid, or both of these types of CO2. The method additionally includes separating at least a portion of one of the types of CO2 - solid or liquid, or both of these types of CO2 from the cooled gas stream in the Laval nozzle, to obtain the CO2 -enriched stream and the CO2-depleted gas stream. The method additionally comprises expanding the CO2 -depleted gas stream in the expander located below the Laval nozzle downstream to obtain the CO2 -depleted cooled gas stream and recycling at least part of the cooled CO2 - depleted gas flow to the cooling stage for cooling the gas stream.EFFECT: invention allows to reduce the nozzle surface erosion and to reduce the overall pressure drop.20 cl, 6 dwg

ethod and plant for deethanization gas variable processing // 2618632
FIELD: oil and gas industry.SUBSTANCE: plant includes a turbo-expander, distillation columns, wash column, stripping column, low temperature separators, filters, multithreaded plate heat exchanger, regenerative heat exchanger, air coolers, reboilers for columns, pumps, tank, septic tank, reflux tank, container collecting water-methanol solution, control valve and safety valves with inlet connections for input and output of the respective gaseous and liquid process flows. Cold recovery for low-temperature separation is carried out only by pressure reduction and expansion of the excessively compressed gas in the turbo-expander gas unit with cold transfer in the multithreaded heat exchanger. The methanol is introduced into crystalline hydrate stagnant concentration zones, at that the additional variability of gas deethanizer processing is provided by three modes, depending on climatic conditions: summer, transient and winter energy saving - and by fractional methanol introduction into the most vulnerable from the crystalline hydrates accumulation position places of devices.EFFECT: componentwise extraction of impurities in the low-cost cold production for distillation column, reduction of the crystalline hydrates formation.13 cl, 2 dwg, 5 tbl

Gas compression // 2617029
FIELD: oil and gas industry.SUBSTANCE: proposed the method, including the gas compression in the mixture with weathering gas, cooling of the obtained liquid hydrocarbons released during gas compression by absorbed substance in its stabilisation conditions and its further absorption purification at negative temperature gradient, created due to the chemical cooling, stabilisation of the obtained absorbed substance with getting compressed gas and absorbed substance, which is subjected to weathering under the reduced pressure to obtain the weathering gas and weathering absorbed substance.EFFECT: reduction of heavy components with the compressed gas losses.2 cl, 1 dwg

ethod for processing low-pressure hydrocarbon gases and liquid hydrocarbons // 2617028
FIELD: oil and gas industry.SUBSTANCE: gas is compressed and cooled under the condition of refluxing and stabilizing of the reflux liquid at the initial stages of compression, together with the gases of low pressure stabilization to obtain a low pressure condensate and compressed gas, which is dried, purified, and mixed with a gas of high pressure stabilisation, compressed and cooled under refluxing and stabilising of the reflux liquid in the third stage, using the gas of low temperature separation as the refrigerant to obtain propane-butane fraction and the compressed gas. The latter is reduced and separated, with obtaining the low-temperature separation gas, which is heated by the liquid hydrocarbons released during gas compression at the third stage, and extracted as the treated gas, and the condensate, which is stabilized with obtaining the stabilisation gas of high pressure and the propane fraction. The liquid hydrocarbons are stabilised together with the condensate of low pressure to obtain the stabilisation gas of low pressure and stable gasoline.EFFECT: improvement of the quality and range of the products.4 cl, 1 dwg

Small-size natural gas liquefaction unit // 2615862
FIELD: cryogenics.SUBSTANCE: invention relates to cryogenic equipment. Small-size natural gas liquefaction unit includes section of a gas pipeline, a cryogenic gas machine (CGM), operating at reverse Stirling cycle, heat exchangers freeze-out devices-condensers of natural gas (NG), a cryogenic tank for liquefied natural gas (LNG), gas blower and nitrogen heater. Cooling, cleaning PG from H2O and CO2 and its liquefaction is performed in alternating working heat exchangers freeze-out devices-condensers, cooled by liquid nitrogen, liquefied in CGM and circulating in closed circuit. Part of circulating nitrogen is collected in gas blower with further heating in a heater and is used for heating of heat exchangers with further return of said flow of nitrogen into circulation flow of nitrogen.EFFECT: technical result is providing prolonged continuous operation.1 cl, 1 dwg

ethod of gas condensate deposits complex processing with c3+ hydrocarbons deep extraction and plant for its implementation // 2615703
FIELD: gas industry.SUBSTANCE: invention relates to field of gas industry and can be used in field gas condensate deposits processing. Field gas condensate deposits production preparation method involves formation mixture separation with production of sour gas and unstable gas condensate, sour gas adsorption dehydration and unstable gas condensate deethanization, dried gas deep cooling with production of marketable natural gas and broad fraction of broad fraction of light hydrocarbons (BFLH) and BFLH low-temperature deethanization. Plant includes, at least, one slug catcher, which gas outlet is connected with absorption dehydration unit through cooling device, and condensate output is connected with tank-separator, which gas output through first gas pumping unit is also connected to absorption dehydration unit, which output is connected through first and second recuperative heat exchangers cooling channel and intermediate separator with turbo expanding assembly throttling device, which output is connected with low-temperature separator. Outputs of intermediate and low-temperature separators for condensate are connected via recuperative heat exchanger with low-temperature deethanization tower, to output of which are in series connected reflux exchanger, third recuperative heat exchanger, second gas pumping unit and marketable dried gas discharge line. Low-temperature separator gas output is in-series connected with reflux exchanger tube side and with marketable dried gas discharge line.EFFECT: reducing marketable gas dew point and minimization of hydrocarbons C3+ loss by deethanization gases.5 cl, 1 dwg
 
2551393.
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