WO2006031148A1 - Procede et dispositif de separation d'un melange neon-helium - Google Patents
Procede et dispositif de separation d'un melange neon-helium Download PDFInfo
- Publication number
- WO2006031148A1 WO2006031148A1 PCT/RU2005/000219 RU2005000219W WO2006031148A1 WO 2006031148 A1 WO2006031148 A1 WO 2006031148A1 RU 2005000219 W RU2005000219 W RU 2005000219W WO 2006031148 A1 WO2006031148 A1 WO 2006031148A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- neon
- heat exchanger
- helium
- mixture
- helium mixture
- Prior art date
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04642—Recovering noble gases from air
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04945—Details of internal structure; insulation and housing of the cold box
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/08—Separating gaseous impurities from gases or gaseous mixtures or from liquefied gases or liquefied gaseous mixtures
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/30—Helium
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/32—Neon
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
Definitions
- the invention relates to cryogenic technology, in particular, to the purification and separation of a neon-helium mixture obtained in air separation plants, and can be used in the chemical and oil and gas industry.
- the disadvantage of this method is the low profitability caused by large losses of neon in the stripping gas and the inability to produce production helium along with production neon, and the high metal consumption of the equipment.
- the aim of the invention is to increase efficiency by maximizing the extraction of production neon and helium from the initial mixture, reducing metal consumption.
- a distinctive feature is that neon is additionally absorbed from the stripping gas stream in adsorbers formation of production helium at the outlet, adsorbers are purged with helium during desorption, and the flow of the purged gas is mixed with the flow of the neon-helium mixture before compression, and separated the flow of the neon-helium mixture at a temperature of 28–29.5 K and a pressure exceeding the critical pressure for neon, which is 2.654 MPa.
- a device for producing high-purity neon including a neon-helium mixture compressor, a main heat exchanger, an adsorber on the feed stream, a low-temperature heat exchanger, a condenser-evaporator, a distillation column with an evaporator in a cube, a steam separator connected by pipelines (lines) to valves, additional circulation neon refrigeration cycle.
- the aim of the invention is to increase efficiency by maximizing the extraction of production neon and helium from the initial mixture, reducing metal consumption.
- the separation device of the neon-helium mixture which includes a compressor with a suction line, a main heat exchanger with inlet and outlet pipes of the exhaust gas, a low temperature heat exchanger, a separator with exhaust gas and liquid fraction exit lines, a distillation column with an evaporator in cube
- the device further comprises switching adsorbers with gas inlet and outlet pipes, and the gas inlet pipe of each adsorber is connected by a line equipped with valves, with the exhaust gas outlet line from the separator after the low-temperature heat exchanger and with the compressor suction line, the gas outlet pipe of each adsorber is connected by lines equipped with valves, with the exhaust gas inlet pipe to the main heat exchanger and with the exhaust gas outlet pipe from the main heat exchanger, and the column evaporator has a capillary-porous coating on the boiling side.
- the inventive method of separation of the neon-helium mixture can be implemented in the inventive device, schematically shown in the drawing (Fig. 1).
- the device (installation) comprises a compressor 1 with an suction line 22, a main heat exchanger 2, an adsorber 3, a low-temperature heat exchanger 4, a separator 5, a distillation column 6 with an evaporator 7, which has a capillary-porous coating on the boiling side, a condenser evaporator 8, switching adsorbers 9-1, 9-2, each of which is placed in a cooled jacket 10-1, 10-2, equipped with a heating element 1 1-1, 1 1-2, water ring vacuum pump 12, mechanical vacuum pump 13 Low-temperature equipment installation about in the casing 14 under the discharge created by the vacuum pump 13.
- the nozzle for pumping the compressor 1 by line 15 of the flow of neon-helium mixture is connected through the main heat exchanger 2, adsorber 3, low-temperature heat exchanger 4, condenser-evaporator 8, evaporator 7 with the nozzle of the separator 5, located in the middle.
- the pipe located in the lower part of the separator 5 is connected by a line 16 of the liquid fraction stream equipped with a throttle valve 17 to the head of the distillation column 6, and the side located in the upper part of the separator 5 is connected by a flue gas flow line 18 provided with a throttle valve 19, through a low-temperature heat exchanger 4 and valves 18-1, 18-2 provided with valves, with gas inlet pipes of switching adsorbers 9-1, 9-2, the gas outlet nozzles of which are connected by lines 20-1, 20-2, equipped with valves, and line 20 with the nozzle of the inlet of the exhaust gas into the main heat exchanger 2.
- Lines 21-1, 21-2, equipped with valves, and line 21 are connected gas inlet nozzles of switching adsorbers 9-1, 9-2 with suction line 22 compressor 1, and lines 23-1, 23-2, equipped with valves, and lines 23 and 24 connect the gas outlet pipes of the switching adsorbers 9-1, 9-2 with the outlet pipe of the exhaust gas from the main heat exchanger 2.
- 9-1, 9-2, as well as the jacket of the adsorber 3 in the lower part are connected by lines 26-1, 26-2, 26-3, equipped with valves, with a line 26 of liquid nitrogen flow, and in the upper part - by lines 27-1, 27-2, 27-3, equipped with valves, with a line 27 of a stream of nitrogen vapor in the liquid ring vacuum pump 12.
- a pipe located in the lower part of the cube of the column 6 is connected by a line 25 of the flow of production neon through a condenser-evaporator 8, a low-temperature heat exchanger 4, the main heat exchanger 2 with the exit of the installation.
- the pipe located at the top of the column head is connected by a gaseous fraction flow line 28 through a low-temperature heat exchanger 4 and a main heat exchanger 2 with a compressor suction line 22.
- the method for separating a neon-helium mixture is as follows.
- the apparatus is cooled with liquid nitrogen.
- liquid nitrogen is fed through line 26 of the liquid nitrogen stream and lines 26-1, 26-2, 26-3 to the shirts 10-1, 10-2 of adsorbents 9-1 and 9-2 and adsorber 3, the formed nitrogen vapors are discharged along lines 27-1, 27-2, 27-3 and further along line 27 of a stream of nitrogen vapor through the main heat exchanger 2 into the atmosphere.
- a water ring vacuum pump 12 is turned on, maintaining the pressure in the jacket of the adsorbers approximately 0.015 MPa, providing thermostatting of the adsorbers when operating at a temperature of ⁇ 64 K.
- the neon-helium mixture preliminarily purified from impurities of nitrogen, oxygen, and hydrogen, obtained in air separation plants, is fed via suction line 22 to compressor 1, where it is compressed to a pressure exceeding the critical pressure
- I nie for neon mainly up to a pressure of 1 1-15 MPa.
- the compressed neon-helium mixture is sent to the neon-helium mixture flow line 15 where it is cooled down sequentially due to reverse flows discharged from the installation, first in the main heat exchanger 2, then in the low-temperature heat exchanger 4, condenser-evaporator 8.
- the neon-helium mixture is cooled to a temperature of 28-29.5 K to obtain a liquid phase and fed to a separator 5, where it is separated to form a liquid fraction and stripping gases.
- the adsorber 3 possible trace elements are absorbed from the neon-helium mixture.
- the liquid fraction through line 16 of the liquid fraction stream after throttling in the throttle valve 17 is fed to the head of the column 6 as a reflux for irrigation.
- high-purity production neon is concentrated in the cube of column 6, and a gaseous fraction is concentrated in the head, which, along the line 28 of the gaseous fraction flow through the low-temperature heat exchanger 4, the main heat exchanger 2, is cooled by a direct stream, and sent to compressor suction line 22 .
- production neon is fed sequentially to the condenser-evaporator 8, the low-temperature heat exchanger 4, the main heat exchanger 2, in which the neon-helium mixture is evaporated and heated by the flow of the neon-helium mixture, and removed from the unit.
- the exhaust gases from the upper part of the separator 5 are fed into the exhaust gas flow line 18 and, after throttling in the throttle valve 19, are directed through a low-temperature heat exchanger 4 to one of the switching adsorbers, for example, via line 18-1 to the adsorber 9-1, where neon is absorbed.
- the flow of production helium leaves the adsorber 9-1, which is sent through lines 20-1.20 to the main heat exchanger 2 and, via line 24, the flow of production helium is removed from the installation.
- a neon surface with capillary-porous properties for example, an aluminum capillary-porous coating with a thickness of 0.3-0.6 mm with an open porosity of at least 25-30% and an average equivalent pore diameter of not more than 70 microns, allows you to reduce the temperature head between the heat-exchanging media at the outlet of the apparatus to -0.5 K and to cool the neon-helium mixture deeper to a temperature of 28-29.5 K.
- the proposed method and device for separating a neon-helium mixture allows to increase the neon extraction coefficient to 0.99995 while producing production helium with the same extraction coefficient, which increases the efficiency of the device compared to the known solution.
- the metal consumption of the device is reduced both by reducing the mass of neon adsorbers, and by eliminating the additional refrigeration cycle.
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation Of Gases By Adsorption (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
RU2004126268 | 2004-09-01 | ||
RU2004126268/06A RU2263861C1 (ru) | 2004-09-01 | 2004-09-01 | Способ разделения неоногелиевой смеси и устройство для его осуществления |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2006031148A1 true WO2006031148A1 (fr) | 2006-03-23 |
Family
ID=35865472
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/RU2005/000219 WO2006031148A1 (fr) | 2004-09-01 | 2005-04-22 | Procede et dispositif de separation d'un melange neon-helium |
Country Status (3)
Country | Link |
---|---|
RU (1) | RU2263861C1 (ru) |
UA (1) | UA78867C2 (ru) |
WO (1) | WO2006031148A1 (ru) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114562852A (zh) * | 2022-03-22 | 2022-05-31 | 北京中科富海低温科技有限公司 | 一种氦气脱氖系统及其方法 |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
RU2528727C2 (ru) * | 2013-01-09 | 2014-09-20 | Виталий Леонидович Бондаренко | Установка для мембранного разделения неоно-гелиевой смеси |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
SU760751A1 (ru) * | 1978-04-03 | 1986-11-15 | Obedinennyj I Yadernykh I | "cпocoб paздeлehия cmecи гaзob" |
SU1388679A1 (ru) * | 1986-04-22 | 1988-04-15 | Объединенный Институт Ядерных Исследований | Установка дл разделени неоногелиевой смеси |
RU2166354C2 (ru) * | 2000-08-29 | 2001-05-10 | Савинов Михаил Юрьевич | Устройство получения первичного криптоно-ксенонового концентрата |
-
2004
- 2004-09-01 RU RU2004126268/06A patent/RU2263861C1/ru active
-
2005
- 2005-04-22 WO PCT/RU2005/000219 patent/WO2006031148A1/ru active Application Filing
- 2005-04-25 UA UAA200503954A patent/UA78867C2/uk unknown
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
SU760751A1 (ru) * | 1978-04-03 | 1986-11-15 | Obedinennyj I Yadernykh I | "cпocoб paздeлehия cmecи гaзob" |
SU1388679A1 (ru) * | 1986-04-22 | 1988-04-15 | Объединенный Институт Ядерных Исследований | Установка дл разделени неоногелиевой смеси |
RU2166354C2 (ru) * | 2000-08-29 | 2001-05-10 | Савинов Михаил Юрьевич | Устройство получения первичного криптоно-ксенонового концентрата |
Non-Patent Citations (1)
Title |
---|
BONDARENKOV V.L. ET AL: "Opyt expluatatsii ustanovki dlya polucheniya neona vysokoi chastoty", VESTNIK MGTU, SER. MASHINOSTROENIE, 1996, pages 79 - 80 * |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN114562852A (zh) * | 2022-03-22 | 2022-05-31 | 北京中科富海低温科技有限公司 | 一种氦气脱氖系统及其方法 |
CN114562852B (zh) * | 2022-03-22 | 2022-09-06 | 北京中科富海低温科技有限公司 | 一种氦气脱氖系统及其方法 |
Also Published As
Publication number | Publication date |
---|---|
RU2263861C1 (ru) | 2005-11-10 |
UA78867C2 (en) | 2007-04-25 |
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