Method of producing multicomponent solution of krypton-xenon mixture and special purity solvent and apparatus for realising said method. RU patent 2520216.
 Method of nitrogen removal / 2514804Invention relates to method of removal of fractions with high content of nitrogen from initial fraction containing, mainly, nitrogen and hydrocarbons. Note here that initial fraction is separated by rectification into high nitrogen fraction and high methane fraction. High-methane fraction is evaporated and overheated at maximum possible pressure to produce cold. High-nitrogen fraction is at least temporarily and/or partially contracted and fed to rectification as a backflow. In compliance with this invention, at least temporarily, at least partially one partial flow (16) of compressed (C) fraction (9') with high nitrogen content after performed condensation (E1) is expanded (f) in valve and, to produce cold, at least partially, preferably completely, is evaporated (E1). |
 Multi-stage cyclone separator for fluid medium / 2509272Invention relates to a cyclone separator for fluid medium, comprising a neck part (4), which is placed between the section of inlet of the convergent fluid medium and the section of outlet of the divergent fluid medium. The cyclone separator for fluid medium is made with the capability to push the cyclone flow via the section of inlet of the convergent fluid medium and the neck part to the section of outlet of the divergent fluid medium in direction downstream the flow. The section of outlet of the divergent fluid medium comprises an inner primary outlet pipe (7) for fluid components depleted by condensing vapours and an outer secondary outlet pipe (6) for fluid components enriched with condensing vapours. The cyclone separator for fluid medium comprises an additional outer secondary outlet pipe (16). The outer secondary outlet pipe (6) is placed in the first position along the central axis (I) of the cyclone separator for fluid medium, and the additional outer secondary outlet pipe (16) is placed in the second position along the central axis (I) of the cyclone separator for fluid medium. |
 Method of dehydrating gas containing co2 / 2505763Method of dehydrating a gas containing CO2 is based on preparing a two-phase mixture with expansion thereof and separating the liquid phase from the mixture in a separator. Raw gas is cooled by adding liquid CO2 with water dissolved therein; the obtained mixture is separated into a gas phase and a liquid phase containing water; the gas phase is expanded to obtain a liquid containing liquid CO2 and water; the liquid is partially or completely fed for mixing with raw gas, wherein expansion is carried out to temperature below the hydrate formation point. |
 Improved nitrogen removal at natural liquefaction plant / 2502026In compliance with one version, nitrogen regeneration system comprises tank for multistage separation to extract nitrogen from cooled flow of natural gas. At least, a portion of obtained flow containing nitrogen escaping the tank for multistage separation can be used as a coolant and processed at nitrogen regeneration plant and/or used as a fuel gas for natural gas liquefaction plant. |
 Production of treated hydrocarbons gas from gas flow containing hydrocarbons and acid impurities / 2498175Invention is related to method for production of treated hydrocarbons gas from gas flow containing hydrocarbons and acid impurities that includes: (a) cooling of gas flow up to temperature at which mixture containing solid and potentially liquid acid impurities and vapour containing gaseous hydrocarbons is formed; (b) delivery of formed mixture to the unit and separation of solid and potentially liquid acid impurities from the mixture in this unit; in result treated hydrocarbon gas is produced; (c) delivery of heat to at least part of solid and potentially liquid acid impurities; in result at least part of solid impurities is melted and flow with concentrated impurities is formed; (d) extraction of heated flow with concentrated impurities from the unit; the method includes additionally (e) reheating of at least part of heated flow with concentrated impurities with formation of reheated recirculating flow; and (f) recirculation of at least part of heated flow with concentrated impurities to the unit. Invention is also related to LNG production. |
 Gas liquefaction method with fractionating at high pressure / 2495342Method proposes to liquefy natural gas by implementing the following stages: natural gas is cooled; cooled natural gas is introduced to a fractionating column so that a gas phase saturated with methane and a liquid phase saturated with compounds that are heavier than ethane are separated; the above liquid phase is extracted from lower part of the fractionating column and the above gas phase is extracted from upper part of the separation column; the above gas phase is partially liquefied so that condensate and gaseous flow can be obtained; at that, condensate is returned to upper part of the column for fractionating as reflux; the above gaseous flow is liquefied due to heat exchange at the pressure of more than 50 bar. Working conditions of the fractionating column functioning at the pressure in the range of 40 to 60 bar are chosen so that the above liquid phase can contain molar content of methane at the interval of 10% to 150% of molar content of ethane contained in the above liquid phase. |
 Method and device for separation of one or more c2+hydrocarbons from hydrocarbon flow with mixed phases / 2493510Separation method of one or more C2+hydrocarbons from liquid hydrocarbon flow involves supply of hydrocarbon raw material flow with mixed phases in the form of partially evaporated hydrocarbon raw material to the first gas-liquid separator. Hydrocarbon raw material flow with mixed phases is received from one or more storage tanks by means of passing through the heat exchanger of liquid hydrocarbon flow from one or more storage tanks. Then, flow of hydrocarbon raw material with mixed phases is separated in the first gas-liquid separator into the first gaseous flow leaving the first outlet and at least one liquid flow C2+. The first gaseous flow is passed through the compressor, and as a result, compressed flow is obtained, which is cooled in one or more heat exchangers, and as a result, flow of at least partially condensed hydrocarbon products is obtained. The second gaseous flow is added to the flow after the first outlet. The second gaseous flow includes evaporated gas accumulated from one or more storage tanks for liquid hydrocarbons in gaseous form. |
 Method of natural gas liquefaction with better propane extraction / 2491487Natural gas is partially combusted at cooling in E1 and separated in fractionating column 2 in methane-rich flow and that rich in hydrocarbons heavier than methane. Methane-rich flow is partially fludised in 3. Then separated condensates are cycled in cylinder 4 at column 2 via pipeline 7. Liquid fraction from cylinder 4 is liquefied in heat exchanger E2 to produce natural liquefied gas. Flow rich in hydrocarbons heavier than methane is separated in de-ethaniser into ethane-rich fraction and heavier hydrocarbons. In compliance with this invention, ethane-rich fraction is liquefied, at least, partially. Then, portion of liquefied ethane is recycled in cylinder 4 or to the line of low 7. |
 Method and device for cooling and separation of hydrocarbon flow / 2488759Method involves provision of hydrocarbon flow (10), cooling of hydrocarbon flow (10) to obtain liquefied hydrocarbon flow (20), supply at least of some part of liquefied hydrocarbon flow (20) to distillating column (12) through the first inlet opening (17), provision of bottom raw material flow (30), provision of cooling agent circuit (4) containing at least one cooling agent flow (40), heating of bottom raw material flow (30) with counterflow (40) of cooling agent to obtain heated bottom raw material flow (50) and flow (60) of cooled cooling agent; supply of heated bottom raw material flow (50) to distilling column (12) through the second inlet opening (18) located below the first inlet opening (17) and separation of partially liquefied hydrocarbon flow (20) in distilling column (12) to obtain the first upper gaseous flow (70) and the first bottom liquid flow (80). |
 Method to remove carbon dioxide / 2482407Method and system are proposed to remove one or several fractions containing carbon dioxide, which are contained in one or several places of fractionating and/or liquefaction process, such as, for instance, the natural gas liquefaction process. A fraction (fractions) containing carbon dioxide is exposed to treatment (B) and/or liquefaction (C) and then sequestrated (D). At least one partial flow (6) of the liquefied fraction (fractions) containing carbon dioxide is applied as a cooling agent (D) inside the process of fractionating and/or liquefaction. The system comprises at least one treatment unit (B) and/or at least one liquefaction unit (C), where the fraction (fractions) containing carbon dioxide is supplied, as well as facilities to supply treated and/or liquefied fraction (fractions) containing carbon dioxide for sequestrating (D). |
 Method of processing petroleum gases / 2244226Proposed method includes compression of initial gas followed by de-ethanization. Gas and condensate obtained after separation are mixed and gas-and-liquid flow is cooled and is delivered for low-temperature separation; then, part of this low-temperature condensate is throttled and cold thus obtained is used for cooling the compressed gas-and-liquid flow which is fed for separation of condensate, after which gas separated from condensate is mixed with initial gas and condensate is directed for de-ethanization. Second part of low-temperature condensate is fed for de-ethanization after use of its cold for cooling and condensing the de-ethanization gases. |
 Method of separation of difficult-to-separate mixtures and device for realization of this method / 2254905Proposed method includes separation of mixture by rectification in column divided into sections and taking the liquid from under contact space of previous section which is delivered by activator for sprinkling the subsequent section above contact space followed by taking vapor above contact space of subsequent section and delivery of it under contact space of previous section. Used as activator is steam lift communicated with contact spaces of sections through hydraulic seals; evaporation of liquid and condensation of steam in steam lift are performed by delivery of working medium circulating in high-pressure and low-pressure cycles. Description of device proposed for realization of this method is given in Specification. |
 Neon-helium mixture separation method and device / 2263861Method involves compressing neon-helium mixture flow, cooling thereof and separating under 28-29.5 K temperature and pressure exceeding critical neon pressure to form stripping gas and liquid fraction; additionally absorbing neon from stripping gas by adsorbers; purging adsorbers with helium during desorption thereof; mixing purging gas with neon-helium mixture before compressing thereof. Separation device comprises compressor with inlet pipeline, main heat-exchanger with stripping gas inlet and outlet connection pipes, low-temperature heat-exchanger, separator with stripping gas and liquid fraction outlet pipelines, rectifying column with evaporator in column bottom and alternating adsorbers. Gas inlet connection pipe of each adsorber is connected to stripping gas outlet pipeline of separator downstream of low-temperature heat-exchanger and to compressor inlet pipeline through pipelines provided with valves. Gas outlet connection pipe of each adsorber is linked with stripping gas inlet and outlet connection pipes of main heat-exchanger through pipelines provided with valves. Evaporator has capillary-porous coating applied from boiling side thereof. |
 Method of purifying and separating mixture / 2265778Method comprises supplying vapors of cooling agent to the cooling cycle for liquefying, mixing the liquid cooling agent with the liquefied cooling agent, and supplying the liquid cooling agent to the condenser-evaporators for evaporating. |
 Method and device for liquefied gas cooling / 2270408Method involves expanding above pressurized liquefied natural gas to obtain expanded liquefied gas flow; separating the obtained gas flow into the first head fraction having greater volatility and the first tail fraction having lesser volatility; accumulating the first tail fraction comprising cooled liquefied natural gas; heating the first head fraction, compressing thereof in the first compressor and cooling the first head fraction to obtain the first compressed fraction of combustible gas; accumulating the first fraction of combustible gas; extracting the second compressed fraction from the first compressed one; cooling the second compressed fraction and mixing thereof with expanded liquefied natural gas flow; compressing the second compressed fraction in the second compressor communicated with turboexpander to obtain the third compressed fraction; cooling the third compressed fraction and separating thereof into the forth and the fifth compressed fractions; cooling the forth compressed fraction and expanding thereof in turboexpander connected to the second compressor to obtain expanded fraction; heating the expanded fraction and introducing thereof into the first medium-pressure compressor stage; cooling the fifth fraction and mixing thereof with expanded liquefied natural gas flow. |
 Universal gas separation and liquefaction method (variants) and device / 2272228Method involves treating gas; separating thereof in membrane or cryogenic gas-separation unit; liquefying and separating gas in liquefying unit. Gas treatment includes cleaning gas of water droplets and mechanical injuries and supplying the cleaned gas to gas-separation unit inlet. Then natural gas is cleaned and supplied through gas distribution means to gas-separation vessels which increase methane concentration to 99.9%. Methane moves to gas liquefying unit inlet. Nitrogen and hydrocarbons are separated in serially connected gas-separation vessels into ethane, propane, butane and nitrogen. Ethane, propane and butane are directed to store means. Cryogenic unit is adapted for cleaned natural gas dividing into two flows, which are cooled, combined and then expanded. The expanded flow is supplied to rectification column. Flow of the first steam is cooled to -112°C - -150°C temperature to form vapor and liquid phases by passing the first steam through a row of heat exchangers in which the first steam is in counterflow with nitrogen flow circulating in cooling loop. The cooled flow of the first steam is separated into vapor and liquid phases to create flow of the second steam having methane and nitrogen ratio of 1:(1.0-2.0) and to create flow of the second liquid having methane and nitrogen ratio of 1:(4.0-2.0). Flow of the second liquid in phlegm form is returned to rectification column and the first liquid is removed from rectification column, wherein the first liquid is product having temperature exceeding -112°C. The product is directed to high-pressure natural gas store means and to liquefying unit, in which gas is separated inside de-methanizing, de-ethanizing, de-butanizing and de-propanizing columns. Then pressure and temperature of the gas flows exited from the columns are equalized and the flows are combined into single flow. Part of the flow is reduced and supplied to operator's compartment. |
 Method of low-temperature gas separation / 2272973Method comprises cooling mixture, expanding mixture or its portion, partial condensing of the mixture with its simultaneous expansion, and separating the mixture or its portion in the rectifying tower to produce liquid and gas phases. The expansion is performed by flowing the mixture through the nozzle passage. The nozzle passage swirls the flow of the mixture. The mixture flow is separated at the outlet of the nozzle passage at least into two flows. One of the flow is enriched by the components denser than methane, and the other one is depleted by these component. The enriched flow is directed to the rectifying tower. The gas products produced in the rectifying tower are directed to the mixture upstream of its expansion. According to the second version, the gas products are mixed completely or in part with the depleted flow. According to the third version, the enriched flow is directed completely or in part to the mixture upstream of its expansion. According to the fourth version, the enriched flow and gas products are directed in part or completely to the mixture upstream of its expansion. |
 Method of treating carbon-containing gas / 2283994Method comprises treating gas in one or several heat exchange stages to produce first raw flow cooled under pressure, expanding the first raw flow to decrease the pressure, supplying raw to the fractionating column, and fractioning cooled and expanded first raw flow at a lower pressure thus extracting relatively light components. The distillation flow is discharged from the fractioning column and heated. The heated distillation flow is returned to the fractioning column. |
 Method of the low-temperature separation of the hydrocarbon gas / 2286377The invention is pertaining to the field of the gases processing industry, in particular, to the methods of separation of the components of the gaseous mixtures by the low-temperature condensation and rectification for the purpose of production of the helium concentrate, ethane and the wide fraction of the light hydrocarbons, and may be used at the enterprises of the gas-processing industry. The method provides for: the preliminary cooling of the hydrocarbon gas and its partial condensation; separation of the first stage with separation of the liquid phase from the gaseous phase; the subsequent additional cooling and condensation of the gaseous phase; the separation of the second stage for the liquid and the vapor phases; condensation and rectification of the vapor phase in the flash tower, separation of the third stage of the part of the bottoms product of the flash tower for the liquid phase and the vapor phase; demethanization and deethanization of the whole separated liquid phase. At that the hydrocarbon gas is preliminary dressed with the pentane- hexane fraction, and the separation of the third stage is realized in the separator additionally equipped with mass-exchange nozzle, onto which the liquid phase flow is fed from the separator of the first stage. The technical result of the invention consists in provision of the additional extraction of ethane. |
 Method of control of the rectifying plant operation / 2295679The invention is pertaining to the field of the cryogenic engineering, in particular, to the control of the rectifying plants operation on rectification and separation of the krypton-xenon concentrate produced by the air-fractionating apparatus. The method of control of the rectification plant operation for reprocessing the compressed mixtures includes the control over consumptions of the source mixture in the plant and feeding of the rectifying columns, the pressures and amounts of the top and bottom products gated out of the columns. The rectifying columns are equipped with the sampling devices arranged in their concentration section and the condensers-evaporators with the intermediate coolant in the closed cavity. The mixture at the inlet of the plant is stabilized by the temperature and pressure. Consumption of the mixture by the plant is controlled by the throttle valve, ensuring the pressure drop on the throttle valve for the critical efflux of the mixture. In addition conduct the analysis from the still bottom evaporation area. At that for each column they determine the key components and their share in the preliminary analysis and the analysis from the still bottom evaporation area. The concentrations of the key components are regulated by variation in the contact device of the vapor and the condensate streams. The separation of the top product is conducted in the gaseous form with the constant consumption, the still bottom product is taken out permanently or periodically in the vapor and (or) fluidic form depending on the results of the share of the key component in the mixture from the still evaporation area with the subsequent gasification before the control valve. The useful volume of the still is magnified concerning the hourly productivity of the appropriate column for the bottom product no less than two times, and the pressure in the contact device of the columns is set by variation of the pressure and (or) amount of the intermediate coolant and the heat power of the still boiler of a beck. Usage of the invention ensures the power saving control over the rectifying plant at production of the especially pure target components. |
FIELD: chemistry.
SUBSTANCE: method of producing a multicomponent solution of a krypton-xenon mixture and a special purity solvent involves feeding a multicomponent solution into a precursor solution line, preliminary physical-chemical purification from explosive and hardening impurities, cooling and fractional separation in columns. Said columns are equipped with samplers in the concentration part or blow line and the vapour zone of the bottom. A krypton-xenon mixture containing volatile impurities and a stream of a solvent containing volatile impurities are obtained in the column for obtaining a krypton-xenon mixture. The method also includes purifying the stream of the solvent fraction in a column for obtaining special purity solvent from volatile impurities to obtain a special purity solvent. All impurities that are volatile relative to krypton are removed with the stream of the solvent fraction, wherein the part of said impurities which is semi-volatile relative to the solvent is removed in a column for purification from intermediate impurities. An apparatus for carrying out said method is described.
EFFECT: invention reduces content of impurities in a krypton-xenon mixture, simplifies and reduces the cost of processing said mixture.
3 cl, 1 dwg
The claimed invention relates to cryogenic engineering, in particular to the technology of low-temperature rectification mixtures, and can be used in chemical, petrochemical and metallurgical industries.
A method of obtaining from the solution of kryptonxenon concentrate and cleaning solvent (see RF patent №2430015 C1, IPC SB 23/00). The method provides for gasification of the liquid solution containing krypton and xenon, purification and distillation split with the formation of the flow of production of kryptonxenon concentrate and flow of solvent.
The disadvantage of this method is the low quality of kryptonxenon concentrate because of the content of volatile against the krypton impurities, which complicates and increases the cost of further processing.
A method of obtaining kryptonxenon mixture and purity oxygen (see RF patent №2406047 C1, IPC F25J 3/02, SW 23/00, SW/16, B01D 53/00). The method provides for rectifying the division of purified gas flow primary kryptonxenon concentrate with getting kryptonxenon mixture and thread dump of oxygen, which is then purified by distillation with getting purity oxygen.
The disadvantage of this method is the low quality of kryptonxenon mixture of volatile against the krypton impurities, which adds cost and complexity of its further processing.
The aim of the invention is increasing the quality of kryptonxenon mix and increase profitability.
This goal is achieved by the fact that in the way of reception of the multi-component of the solution kryptonxenon and solvent mixtures of high purity, including distillation division, the distinguishing feature is that when rectification of each column receive one component (or group of components) with adjustable purity, a change which, depending on the more measurements of the composition of the steam flows in Cuba and the concentration of the column.
A device for obtaining kryptonxenon mixture and purity oxygen (see RF patent №2406047 C1, IPC F25J 3/02, SW 23/00, SW/16, 01D 53/00). The device contains a consumption booster, site physico-chemical treatment of primary concentrate from explosive and stiffening of impurities and the rectification unit, consisting of two columns, one of which receive kryptonxenon mixture, and the other with pure oxygen.
The disadvantage of this device is a low quality of kryptonxenon mixture of volatile against the krypton impurities, which adds cost and complexity of its further processing.
The aim of the invention is increasing the quality of kryptonxenon mix and increase profitability.
This goal is achieved by the fact that the device is retrieved from multicomponent solution of kryptonxenon and solvent mixtures of high purity, containing block rectification, the distinguishing feature is that the block of rectification additionally contains the column selection of intermediate particles (impurities, volatile against the krypton and non-volatile against the solvent), and distillation columns unit equipped with a sampler composition of the medium in Cuba and concentration parts.
The stated method of obtaining of multicomponent solution of kryptonxenon mixture and especially pure solvent can be implemented in the claimed device is schematically shown on the drawing.
The device includes a line 1 primary solution, node 2 physico-chemical treatment and block 3 rectification. Site physico-chemical treatment contains a recuperative heat exchanger 4, the electrical heater 5, 6 reactor, water cooler 7 and alternately operating adsorbers 8. Unit 3 distillation distillation column contains 9 receiving kryptonxenon mixture, distillation column 10 highlight interim impurities, distillation column 11 of receipt of solvent purity, multithreaded exchanger 12, cooler 13, low-temperature heat exchanger 14, filter, 15, and 16 coolant supply and line 17 feeder dry compressed gas.
Each distillation column in the head has condenser-evaporator 18-9 to 18-11, and below - cube 19-9 to 19-11, equipped with a kettle 20-94 to 20-11, the sampler A1-9 to A1-11 out of steam cavity and line 21-9 to 21-11 output bottom of a liquid. Cube 19-9 columns obtain kryptonxenon mixture additionally contains a coil 22. Oral boil all capacitors-evaporators are connected with lines 16-9 to 16-11 line 16 of supplying coolant lines 23-9 to 23-11 line 23 liquefied gas and lines 24-9 to 24-11 line 24 out of vapor. The middle part of the contact space distillation columns 9 receiving kryptonxenon mixture contains a socket, connected by a line 25 of purified solution through a low-temperature heat exchanger 14 and filter 15 with node 2 physico-chemical treatment, and the head of the column - a branch pipe, coupled line 26 with a pipe in the middle part of the contact space columns 10 highlight interim impurities. The pipe at the head of the column 10 highlight interim impurities in turn is connected by a line 27 with a pipe in the middle part of the contact space columns 11 getting solvent purity. Socket head of the column 11 of receipt of solvent purity is connected by a line 28 through the cooler 13 and multithreaded exchanger 12 exits. Columns 9 receiving kryptonxenon mixture and 10 highlight interim impurities at the top (concentration) of a part of the contact space equipped with respectively samplers A2-9 and A2-10 for predictive analysis.
The way of reception of the multi-component of the solution kryptonxenon mixture and solvent high purity on the primary example of kryptonxenon concentrate obtained for air separation plants, and use as a refrigerant liquid nitrogen, and as dry compressed gas - air is as follows.
Gaseous solution of krypton Kr and xenon Xe oxygen O 2 (solvent) with nitrogen N 2 , argon Ar, neon Ne, helium Not, hydrogen H-2 , Oscoda WITH carbon, carbon dioxide, CO2 , hydrocarbons n C H m (mainly methane CH 4 and ethane With 2 N 6 ), ozone, O 3 , water, H 2 O, TETRAFLUOROMETHANE CF 4 , freon-C 2 F 6 , monitorability (freon 11) CFCl 3 , difenilamina (freon 12) CF2Cl 2, etc. served under pressure (0,16-0,3)MPa in line 1 primary solution and later in the node 2 physico-chemical treatment. In the node physico-chemical treatment the primary flow of kryptonxenon concentrate regenerative heat exchanger 4 and electrical heater 5, carry out catalytic oxidation of hydrocarbons in the reactor 6, cooling regenerative heat exchanger 4 and water fridge 7 and absorption of water and carbon dioxide in the adsorbers 8. From node 2 physico - chemical treatment the primary flow of kryptonxenon concentrate with traces of impurities methane, water, carbon dioxide, already not dangerous from the point of view of their setting in the columns at operating temperatures, served in line 25 cleaned of mud and then through the filter 15, low-temperature heat exchanger 14 and the coil 22 in the distillation column 9 receiving kryptonxenon mixture, phlegm which is the condensate oxygen (solvent). In the process of rectification columns in the cube is going krypton, xenon and less volatile against the krypton impurities, having at the same pressure higher boiling point (2 , O 3 , H 2 O, CF4, C 2 F 6 , CFCl 3 , CF 2 Cl 2 and others). This liquid in the form of the production kryptonxenon mixture on line 21-9 is removed from the unit for further processing.
The process of rectification in the column are the readings of measuring flow, level, pressure, temperature, hydraulic resistance (not shown)and is measured from the sampler A1-9 and maintain the minimum level (0 to 10 ppm), the methane concentration in the vapour space of the cube as substances with the closest, but low boiling points, compared with a boiling point of krypton. From the sampler A2-9 in the gas samples define and support in the steam flow concentration of column is the content of krypton, which eliminates the release of krypton in the head of the column. In my head the same columns concentrated stream of oxygen, which contains all the flying towards krypton impurities (CH 4 , N 2 , Ar, Ne, No, N 2 , and others). Its output and line 26 sent to the middle part of the distillation column 10 highlight interim impurities. In the scheme of the device there are also line 29, which will bring the flow of oxygen from the zone of possible increase of concentration of methane in the concentration of columns 9 or in the event of a failure mode of its work to prevent the ingress of krypton in the condenser-evaporator 18-9.
Flavoursome refrigerants in the device are liquid nitrogen and liquid air. Liquid nitrogen is served in the rectification unit 3 on line 16 coolant supply from an external source and forth along the lines 16-9 to 16-11 in the cavity evaporating condensers-evaporators 18-9 to 18-11. Liquid air to get the device in result of cooling and condensation to the flow of dry compressed air reverse cold streams of the evaporated refrigerant, otdelochnykh gases from the head of the column 11 of receipt of solvent purity, a production flow of solvent purity and removal of heat from the air in the boilers 20-9 to 20-11 Cuba columns. For this purpose, the flow of dry compressed air under pressure, for example, 0,57 - 0,93 MPa served in line 17 feeder dry compressed gas. A small part of the air supplied to the line 17-9 to regulate steam flow in a distillation column 9 receiving kryptonxenon mixture is cooled in the boiler 20-9 and then mixed at the entrance to the low-temperature heat exchanger 12 reverse cold-flow evaporated refrigerant. A greater part of the air is cooled in the low-temperature heat exchanger 12, along the lines 17-10 and 17-11 send respectively in boilers 20-10 and 20-11 where condense, the resulting condensate preobladayut in the cooler 13, direct in-line 23 liquefied gas and along the lines 23-9 to 23-11 drossellied respectively in the cavity evaporating condensers - evaporators 18-9 to 18-11.
Due to the fact that in the way of reception of the multi-component of the solution kryptonxenon and solvent mixtures of high purity, including distillation division, the distinguishing feature is that when rectification of each column receive one component (or group of components) with controllable cleanliness, the change of which carry depending on additional measurements of the composition of the steam flows in Cuba and concentration of columns, which improve the quality of kryptonxenon mix and profitability.
Due to the fact that the device is retrieved from multicomponent solution of kryptonxenon and solvent mixtures of high purity, including the rectification unit, the distinguishing feature is that the block of rectification additionally contains a distillation column highlight interim impurities, and distillation columns unit equipped with a sampler composition of the medium in Cuba and concentration parts, which increases the quality of kryptonxenon mix and profitability.
1. The way of reception of the multi-component of the solution kryptonxenon and solvent mixtures of high purity that includes the flow of multicomponent solution in line primary solution, pre-physical-chemical purification from hazardous and stiffening of impurities, cooling and rectifying the division into columns, equipped with samplers in the concentration of part or line Stripping and steam zone of Cuba, with the formation in the column obtain kryptonxenon the mixture kryptonxenon mixtures containing volatile impurities, and flow fraction of solvent containing volatile additives, cleaning flow fraction of solvent in a convoy of receipt of solvent purity from volatile impurities to produce solvent purity, the distinguishing feature is that the flow fraction of solvent take all volatile against the krypton impurities, volatile ingredients in relation to solvent part of which is removed into the column purification from intermediate impurities.
2. Way under item 1, characterized in that in a convoy of receiving kryptonxenon mixture in the analysis of the sampler steam space Cuba, monitor and support the minimum content of methane, and in the analysis of the sampler concentration of part - minimum content of krypton, in column purification from intermediate impurities in the analysis of the sampler steam space cube manage and keep safe methane, and in the analysis of the sampler concentration of part - the minimum content of the components of the mixture, relative to which the solvent is the least important factor in the relative volatility, in column obtain solvent-high purity in the analysis of the sampler steam space Cuba, monitor and support the minimum content of the components of the mixture with the lowest value of the coefficient of relative volatility against the solvent, and in the analysis of the sampler line Stripping - permissible content of the solvent.
3. The device receiving of multicomponent solution of kryptonxenon and solvent mixtures of high purity, line containing the primary solution, connected with the entrance to the site physico-chemical treatment, the line of purified solution with filter, low-temperature heat exchanger and coil boilers connected to the inlet nozzle in the distillation column obtain kryptonxenon mixtures containing line output kryptonxenon mixture of Cuba and the line fraction of solvent from the head of the column, which is connected with inlet nozzle power supply columns receive special solvent purity containing the output line of solvent purity of Cuba and the line of the blow-off, the distinguishing feature is that the line fraction of solvent supplied column purification from intermediate impurities with line output intermediate impurities from Cuba and the line of the pure solvent, which is connected with inlet nozzle power supply columns get solvent purity.