Method of low-temperature preparation of low-pressure oil gas at field

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

 



 

Same patents:

FIELD: oil and gas industry.

SUBSTANCE: method of hydrocarbon gas preparation for transportation includes the following stages. Formation gas is delivered to a separator of the first stage. Gas separated in the separator of the first stage is compressed and cooled down. Then gas separated in the separator of the first stage is delivered through heat exchanger of the first cooling stage to the separator of the second stage. Then gas separated in the separator of the second stage is delivered through heat exchanger of the second cooling stage and reducer to the separator of the third stage. Liquid from the separator of the second stage is delivered to the separator of the third stage. Gas from the separator of the third stage is delivered to reducer thus ensuring additional cold production. Then gas from the reducer is delivered to the heat-exchanger of the second cooling stage thus ensuring additional cold recovery. Gas is sent from the heat-exchanger of the second cooling stage to the reducer. Then gas is delivered from the reducer to the heat-exchanger of the first cooling stage and further this gas is outputted from the plant.

EFFECT: improved energy efficiency of gas preparation with multi-stage low-temperature gas separation.

1 dwg, 1 tbl

FIELD: oil and gas industry.

SUBSTANCE: method of gas mix separation is implemented in gas mix flow. Components are separated from gas mix flow by direct injection of low-temperature coolant into the gas flow mix. Coolant is formed of gas mix separation product obtained at each stage of mix cooling and component separation. A part of each separation product obtained is aftercooled using external cooling source and then returned directly to all stages of gas mix cooling and gas component separation. After all stages of cooling and gas component separation, the gas mix flow is aftercooled using external cooling source and then returned directly to previous stages of mix cooling and component separation, forming repeated gas mix flow transfer and cooling cycles.

EFFECT: reduced capital, operation and power costs, along with high separation degree of mixes of any composition.

3 cl, 1 dwg

FIELD: oil and gas industry.

SUBSTANCE: method includes wet gas separation at the first stage with the production of the water and HC condensates, and the first separation stage gas that is subjected to partial condensation due to counterflow cooling of the gas and condensate of the third separation stage with the production of gas and condensate of the second separation stage, as well as heated condensate of the third separation stage and commercial gas. The gas from the second separation stage is mixed up with weathering gas, its flow is restricted and separated with the production of the gas and condensate of the third separation stage, which are delivered as cooling agents to partial condensation of the gas from the first separation stage, at that the condensate of the third separation stage is delivered by a pump. The heated condensate of the third separation stage together with the hydrocarbon condensate of the first separation stage and condensate of the second separation stage are separated at a pressure close to the pressure of the first and second separation stages with the production of weathering gas, unstable condensate and water condensate. If necessary, in the gas line of the first and/or the second separation stage a hydrates inhibitor is injected, and the spent solution of the hydrates inhibitor is drained from the unit.

EFFECT: increased output of commercial gas, improved recovery degree of heavy components, excluding ejection of weathering gas.

2 cl, 1 dwg, 1 ex

FIELD: oil and gas industry.

SUBSTANCE: method of three-stage low temperature (LT) gas separation means wet gas separation at the first stage with production of the water and HC condensates, and first separation stage gas that is subjected to partial condensation due to counterflow cooling of the gas and condensate of the third separation stage with production of gas and condensate of the second separation stage, as well as heated condensate of the third separation stage and sales gas. Gas of the second separation stage is throttles under conditions of the weathering gas ejection, and is separated with production of gas and condensate of the third separation stage, that are supplied as refrigerants for the partial condensation of the gas of the first stage of separation. Heated condensate of the third stage of separation together with the throttled mixture of HC condensate and condensate of the second separation stage are separated with production of the weathering gas, unstable condensate and water condensate. If necessary, in the gas line of the first and/or the second separation stage the hydrates inhibitor is injected, and spent solution of the hydrates inhibitor is drained from the unit.

EFFECT: increased degree of heavy components recovery and reduced dew point of sales gas.

2 cl, 1 dwg, 1 ex

FIELD: machine building.

SUBSTANCE: separation device comprises a premix chamber with the device of twisting of medium flow installed in it, the nozzle channel connected with the premix chamber for separation, and the unit for separation of droplets and/or solid particles. The separation channel containing convergent, divergent, and located between them cylindrical sections, differing by that the cylindrical section has the length of the generatrix greater than 0.1D, where D - diameter of the cylindrical section, meanwhile the divergent section is designed with a ring ledge as a step the plane of which is perpendicular to the channel axis.

EFFECT: decrease of pulsation level in a flow and, as a result, increase of efficiency of separation and reduction of losses of total pressure of medium flow.

8 cl, 2 dwg

FIELD: oil and gas industry.

SUBSTANCE: invention is related to method for liquefaction of nitrogen-containing input fraction enriched with hydrocarbons, preferably natural gas. The method includes the following stages: a) the feed fraction (1) is burned (E1, E2); b) divided by fractional distillation (T1) to the fraction enriched with nitrogen (9), wherein methane content is max. 1 vol. %, and the nitrogen-depleted fraction enriched with hydrocarbons (4); c) the above fraction (4) is overcooled (E3) and expanded (b); d) the expanded nitrogen-depleted fraction enriched with hydrocarbons (5) is divided (D1) into liquid fraction enriched with nitrogen (6), wherein nitrogen content is max. 1 vol. %, and fraction enriched with nitrogen (7); and e) the fraction enriched with nitrogen (7) is added to the feed fraction (1).

EFFECT: method allows removal of all nitrogen contained in the feed fraction either by liquid product gas or by highly-concentrated nitrogen fraction.

7 cl, 2 dwg

FIELD: chemistry.

SUBSTANCE: method of separating inert gases from gases containing at least argon, xenon, krypton, nitrogen and hydrogen includes cooling a starting gas stream, liquefaction and separation via single-step fractionation. Said fractionation is carried out to obtain liquid separation products: argon and a krypton-xenon mixture, and gaseous separation products: nitrogen, mixture of carbon-nitrogen oxides and a nitrogen-hydrogen mixture. Before fractionation, a large part of the gas stream after cooling is condensed, separated and supercooled, and the smaller part is compressed before cooling. The mixture of carbon-nitrogen oxides is subjected to catalytic oxidation of carbon monoxide to obtain carbon dioxide, nitrogen and water at the output, and hydrogen is separated from the nitrogen-hydrogen mixture. An apparatus for separating inert gases is described.

EFFECT: reduced harmful emissions and extraction of valuable components - inert gases - from tail gases.

10 cl, 1 dwg, 1 tbl

Gas separation // 2528689

FIELD: oil-and-gas industry.

SUBSTANCE: proposed process includes gas feed to absorber. Cooled absorbent is fed to absorber top, dry gas being diverted therefrom and saturated absorbent being discharged from absorber bottom to rectifier tower. Propane-butane fraction is diverted the rectifier top and used as reflux. Gas gasoline is diverted is off-stream via evaporation section while absorbent is discharged from rectifier bottom. After cooling, said absorbent is fed to absorber top and, then, heat is fed to its bottom, rectifier bottom and heat evaporation section bottom. Fluid at absorber lower trays is heated by rectifier column residue preheated in boiler and fed to absorber bottom.

EFFECT: power savings.

2 dwg, 2 tbl

FIELD: oil-and-gas industry.

SUBSTANCE: invention relates to liquefying of natural or associated oil gas, i.e. propane-butane fraction. Initial flow is cooled, separated to isolate light portion of low-molecular hydrocarbon stock to be liquefied with extraction of liquid propane-butane fraction in power vortex separator. Said vortex separator is composed of three-section vessel accommodating vortex tube to divide the latter into three sections, top, mid and bottom, by horizontal walls. Note here that top section accommodates cold end with vortex tube coil heat exchanger, mid-section accommodating hot end. Bottom section houses hot flow rate regulator and separator of liquid phase from said flow equipped with the valve.

EFFECT: higher yield of pure hydrocarbon stock.

2 dwg

Gas compression // 2524790

FIELD: oil-and-gas industry.

SUBSTANCE: proposed method comprises gas compression, cooling of liquid hydrocarbons release during gas compression and its separation to get compressed gas and condensate. Said liquid hydrocarbons release during gas compression is pre-cooled by unstable condensate under conditions of its stabilisation. Then, liquid hydrocarbons release during gas compression is mixed with stabilisation gas and cooled by coolant and separated under conditions of partial condensation to get compressed gas and unstable condensate. Unstable condensate is stabilised to get stabilised gas and stabilisation gas via light components stripping by heating with liquid hydrocarbons release during gas compression.

EFFECT: higher yield of compressed air, reduced losses of target components.

3 cl, 1 dwg

FIELD: development of compressor plants designed for production of nitrogen-air mixture from atmospheric air in the field conditions in production operations in oil production and gas branches of industry.

SUBSTANCE: the method consists in the fact that atmospheric air is prepared to partial separation of oxygen, passed through a gas separation plant and compressed to the operating pressure. Preparation of gas mixture to gas separation is performed in parallel by two small-sized multi-step compressors. Partial separation of oxygen is performed after the third step with employment of the hollow fiber process. Final compression of the nitrogen-air mixture to the operating pressure is performed in the fourth step of the compressors. The device has two small-sized compressors providing for a parallel acting multistep process of preparation of air mixture to gas distribution, and a commutator. The drive of one compressor through a mechanical coupling and a cardan shaft is effected from a diesel engine truck, and that of the second compressor - from the truck chassis.

EFFECT: considerably reduced mass and overalldimensions of the plant, enhanced its mobility.

2 cl, 1 dwg

FIELD: cryogenic equipment, particularly for pure xenon production.

SUBSTANCE: method involves catalytic burning out hydrocarbons from gaseous mixture; removing moisture and carbon dioxide by sorption process; preliminary cooling and low-temperature rectifying the mixture with obtaining pure xenon and delivering pure xenon to consumer. Before carrying out catalytic burning out process initial gaseous mixture containing xenon is supplied to catalytic reactor to perform adsorption operation. The catalytic reactor is filled with at least one layer of adsorbent having a capacity for absorbing xenon 8-10 times greater than capacity for absorbing other components of gaseous mixture. Gas mixture composition is continuously determined at catalytic reactor outlet. Gas mixture exiting the catalytic reactor during adsorption process is discharged in atmosphere. Adsorption process is continued up to emergence of xenon in gaseous mixture at catalytic reactor outlet. Then adsorbent is regenerated. During adsorbent regeneration xenon is desorbed along with continuous supplying heat at temperature of 333-353 K. Desorption process is continued up to discontinuance of xenon extraction from adsorbent. Xenon and associated gases extracted from adsorbent during desorption process performing are used to carry out catalytic burning out operation. The obtained xenon has 99.99999% purity degree and the extraction ratio thereof is 0.99.

EFFECT: improved xenon purification and increased xenon extraction ratio.

13 cl, 1 dwg

FIELD: manufacture of compressors; production of nitrogen-based compressed inert gas mixture from atmospheric air.

SUBSTANCE: proposed compressor station mounted on truck chassis includes multi-stage piston-type air compressor, membrane-type gas distributing module and module-type nitrogen plant. Outlet of third compression stage of air compressor is connected via cooler and water-and-oil separator with inlet of gas-distributing module through filter unit. Outlet of gas-distributing module is connected with inlet of air compressor fourth stage. Air compressed preliminarily in compressor stages is cooled down and cleaned in coolers and water-and-oil separators, after which it is delivered through pipe lines to inlet of gas-distributing module and cleaned in filters and water-and-oil separators from condensed moisture, mechanical admixtures and oil and is fed to gas-distributing reservoirs through gas-distributing unit; gas-distributing reservoirs are interconnected and are located in series and/or in parallel; concentration of oxygen in these reservoirs is reduced to 0.1%. Inert nitrogen gas mixture is fed to compressor stages, cooled to temperature below 60°C and cleaned from moisture and oil in coolers and water-and-oil separators of subsequent stages; then, it is fed to consumer through receiver, check valve and cock. During start at negative temperatures, pre-start heater is switched on and high-temperature gases enter preheating chamber and truck body of mobile compressor station. As required temperature has been attained, diesel engine and compressor are started and high-temperature gases are fed from preheating chamber to thermostatted body of module-type nitrogen plant through warm sleeve.

EFFECT: extended field of application; increased service life of station; facilitated procedure of start.

9 cl, 8 dwg

FIELD: gas and oil industry.

SUBSTANCE: invention relates to production of propane by separating unstable hydrocarbon condensate obtained at reprocessing of hydrocarbon gases with wide fraction of light hydrocarbons and propane fraction as final products. Proposed plant has column-de-ethanizer with bottom heater and top sprayer unit and outlet of de-ethanization gas in upper part and stabilized condensate in lower part. Middle part of strengthening section of column-de-ethanizer is provided with outlet of liquid from plate, corresponding to required concentration of propane fraction, which is connected with upper part of propane production column. Said column is essentially stripper with bottom heater, propane outlet ion lower part and hydrocarbon vapors outlet in top part which is connected with upper part of column de-ethanizer.

EFFECT: reduced capital outlays by decreasing number and size of used equipment, reduced energy consumption.

1 tbl, 1 dwg

FIELD: oil and gas industry.

SUBSTANCE: method comprises supplying initial gas under pressure of 0.002-0.24 MPa (0.02-2.4 kg/cm2), separating the initial gas into gas and liquid phases downstream of each cooling stage, discharging liquid phase produced, and supplying the residual gas to the subsequent cooling, condensing, and separating. The device is modular and comprises heat exchanger-condenser, separator, and collector of the liquid fraction extracted. The device has at least two modules connected in series. The heat exchanger-condenser may be made of Peltier elements.

EFFECT: reduced cost.

3 cl, 1 dwg

FIELD: natural gas industry; methods of preparation of the natural gas for the non-pipeline transportation.

SUBSTANCE: the invention is pertaining to the field of natural gas industry, mainly, to production, storage and the non-pipeline transportation of the natural gas, to the power-saving technologies, and, in particular, to the processes of the utilization of the power at the gas-reducing plants. The preparation of the natural gas for the non-pipeline transportation includes the preliminary purification of the natural gas from heavy hydrocarbons, production of the gaseous hydrates by mixing of the purified gas with the water in the reactor, the continuous refrigeration and keeping of the necessary temperatures of the produced mixture with simultaneous pressure sustain of the no less than equilibrium, which is necessary for formation of the hydrates. Feeding of the natural gas into the reactor of the hydrate production lead from the high pressure gas transportation mains, and their continuous refrigeration is exercised due to the reduced temperature of the natural gas, which has passed the reduction and after the heat exchange is returned back into the mains of the low pressure. At that the pressure in the reactor Pr (MPa) is maintained equal to the mains pressurePm (MPa) and the temperature in the reactorchoke Tr (°K) is maintained in accordance with the following limiting ratio: 273.15 (°K) <Tr <Teq CH4 (Pm)(1), at that the last temperature is calculated using the formula:Teq CH4 = B1/(A1-(1nPm · z)) (2), where A1, B 1 - empirical coefficients for calculation of the equilibrium state of the hydrate - water - methane, z is the compressibility coefficient of the methane. Reduction of the pressure from the natural gas the mains high pressure of 3.0-5,5 MPa up to the low pressure of 0.6 MPa kept in the consuming networks conduct using the throttle-vortex method with refrigeration of the gas stream of the hot outlet from the vortex pipe due to the heat transfer into the environment. Then the stream is combined with the stream from the vortex pipe cold outlet, which has passed through the reactor. Then it is additionally choke down to the nominal (0.6 MPa)low pressure. The produced coldness is used for additional refrigeration the reactor. Realization of the invention allows to deliver the hydrocarbon fuel in the solid state to the customers without utilization of the cryogenic equipment, in the cases, where the low pressure gasification pipeline take-offs are unprofitable, or it is impossible because of any technological or natural reasons. At that the power for production of the gaseous hydrates is generated due to utilization of the energy of the gas pressure drop.

EFFECT: the invention allows to produce the hydrocarbon fuel in the solid state without utilization of the cryogenic equipment and to deliver it to the customers, where the low pressure gasification pipeline take-offs are unprofitable or there are any other technological or natural reasons.

2 cl, 1 ex, 1 dwg

FIELD: cryogenic engineering, in particular, devices for separation of crypton-xenon concentrate obtained at air-separating installations.

SUBSTANCE: the mass-transfer apparatus has a contact device including the concentration and exhausting sections filled with packings, inlet chamber, condenser-evaporator, still with an electric heater and evaporator, still with an electric heater and evaporator. In addition, the inlet chamber of the feed flow of the mass-transfer apparatus (rectifying column) has a packing section with a specific surface less than the specific surface of the packing of the concentration section, is provided with a heater and a thermal converter, and the feed flow branch pipe- with a thermal bridge. The concentration and exhausting sections have different dimensions of the free cross-sectional areas, have reflux distributors and redistributors spaced in height at distance L=(150 to 300)d equiv; where d equiv. - the equivalent diameter of the packing, perforated tubular vertical inserts are additionally installed in the drain holes of the bottoms of the reflux distributors and redistributors. The straight-tubular tube still of the condenser of the intermediate heat-transfer agent has at least one duct, whose cross-sectional area is commensurable with the total area of the flow areas of the heat-transfer tubes, and the still electric heater - the heat-transfer base with an electric heating element packed and covered with heat-transfer powder and pressed to the still bottom by pull rods provided with springs.

EFFECT: enhanced reliability of the mass-transfer apparatus and reduced specific amount of metal per structure.

6 dwg

FIELD: technology for processing gas-condensate hydrocarbon mixture.

SUBSTANCE: method includes three separation stages with feeding of methanol at second stage and absorption with production of hydrocarbon gas, prepared for following transportation to consumer. Mixture of liquid substances from first and second separation stages is fed into first separator, where hydrocarbon gas is separated from aforementioned mixture, which gas is then fed into absorber. Remaining mixture of liquid substances is divided on water-methanol solution, which is dispatched for regeneration, and liquid mixture, which is cooled down in first heat exchanger-cooler and mixed with liquid substance after third separation stage. Part of received liquid mixture is fed into second separator, while remaining part is fed as hydrocarbon absorbent into absorber. Liquid mixture from absorber is divided in second separator on water-methanol solution, which is dispatched for regenerated, and hydrocarbon phase, which is heated in heat exchanger up to temperature ranging from 3°C to 7°C and fed into third separator. In the latter from hydrocarbon phase water-methanol solution is isolated, which is dispatched for regeneration or recirculation to second separation stage, and hydrocarbon phase, which through second heat exchanger-cooler is dispatched to consumer.

EFFECT: decreased losses of methanol and increased quality of condensate dispensed to consumer.

1 ex, 2 tbl, 1 dwg

FIELD: technology for processing gas-condensate hydrocarbon mixture.

SUBSTANCE: method includes three separation stages with feeding of methanol at second stage and absorption with production of hydrocarbon gas, prepared for following transportation to consumer. Mixture of liquid substances from first and second separation stages is fed into first separator, where hydrocarbon gas is isolated from it, which is then fed into absorber. Remaining mixture of liquid substances is divided on water-methanol solution, which is fed to regeneration, and liquid mixture, which is cooled down in first heat exchanger-cooler and mixed with liquid substance after third stage of separation. A portion of received liquid mixture is fed onto second separator, while remaining portion is fed as hydrocarbon absorbent into absorber. Liquid mixture from absorber is divided in second separator in water-methanol solution, which is dispatched for regeneration, and hydrocarbon phase, containing 1-2 percents of mass of emulsion of water-methanol solution, which is fed into electro-dehydrator. In electro-dehydrator by means of heating up hydrocarbon phase to temperature not less than 3°C-7°C and affecting it with alternating electric field, water-methanol solution is isolated, which is dispatched for regeneration or recirculation to second stage of separation, and hydrocarbon phase, which through second heat exchanger-cooler is dispatched to consumer.

EFFECT: decreased losses of methanol, increased quality of condensate dispensed to consumer.

1 ex, 2 tbl, 1 dwg

FIELD: liquefying natural gas.

SUBSTANCE: method comprises cooling gas in the heat exchanger by supplying liquid nitrogen. The liquid nitrogen is produced from the air flow by adiabatic expanding and cooling down to a temperature of liquefying of nitrogen. The flow is mixed with the 500-nm carbon particles. The mass of carbon particles is 30-70% of the total mass of the mixture . The mixture is then accelerated up to the velocity exceeding the sound velocity.

EFFECT: enhanced efficiency.

1 dwg

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