WO2006112746A1 - Procede et dispositif destines a separer des melanges difficilement separables - Google Patents

Procede et dispositif destines a separer des melanges difficilement separables Download PDF

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Publication number
WO2006112746A1
WO2006112746A1 PCT/RU2005/000204 RU2005000204W WO2006112746A1 WO 2006112746 A1 WO2006112746 A1 WO 2006112746A1 RU 2005000204 W RU2005000204 W RU 2005000204W WO 2006112746 A1 WO2006112746 A1 WO 2006112746A1
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WO
WIPO (PCT)
Prior art keywords
column
steam
section
liquid
condenser
Prior art date
Application number
PCT/RU2005/000204
Other languages
English (en)
Russian (ru)
Inventor
Mikhail Jurievich Savinov
Vitaly Leonidovich Bondarenko
Original Assignee
Mikhail Jurievich Savinov
Vitaly Leonidovich Bondarenko
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Mikhail Jurievich Savinov, Vitaly Leonidovich Bondarenko filed Critical Mikhail Jurievich Savinov
Priority to PCT/RU2005/000204 priority Critical patent/WO2006112746A1/fr
Priority to DE112005003543T priority patent/DE112005003543T5/de
Publication of WO2006112746A1 publication Critical patent/WO2006112746A1/fr

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D59/00—Separation of different isotopes of the same chemical element
    • B01D59/02—Separation by phase transition
    • B01D59/04—Separation by phase transition by distillation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B23/00—Noble gases; Compounds thereof
    • C01B23/001—Purification or separation processes of noble gases
    • C01B23/0036—Physical processing only
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0026—Isotopes of the specific gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2210/00—Purification or separation of specific gases
    • C01B2210/0029—Obtaining noble gases
    • C01B2210/0032—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
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/90—Separating isotopes of a component, e.g. H2, O2
    • 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
    • F25J2270/12—External refrigeration with liquid vaporising loop
    • 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
    • F25J2270/60—Closed external refrigeration cycle with single component refrigerant [SCR], e.g. C1-, C2- or C3-hydrocarbons
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/30—Details about heat insulation or cold insulation
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.

Definitions

  • the invention relates to cryogenic technology, in particular to the purification and separation by distillation of gas mixtures of isotopes and isotopic compounds having a small separation coefficient, and can be used in the chemical industry.
  • a method is known concentration HD compound contained in the electrolytic hydrogen, by low-temperature distillation (see. Fig. 14.4 p. 345 "nick Cppavoch- physico-technical basis kpiogeniki” ed. M. P. Malkova g -s ed., Re - slave. and add. - M .: Energoatomizdat, 1985, 432 s).
  • the known method involves the separation of the mixture in a distillation column, obtaining reflux using a high pressure cycle and a low pressure cycle with an intermediate selection of a working fluid low pressure from a high pressure compressor, both cycles being used to obtain reflux directly.
  • the disadvantages of this method are significant metal and energy consumption in obtaining pure target components from difficult to separate mixtures having a separation coefficient of 1.002-1.1.
  • the distillation column will be approximately 100 m high.
  • the dimensions and metal consumption of the equipment determines such high values of heat loss to the environment and, accordingly, the energy intensity of the process, that tion of the known method is practically impossible.
  • an additional energy expenditure appears.
  • the aim of the invention is to reduce the metal and energy consumption in the separation of difficult to separate mixtures.
  • a distinctive feature is that at least one distillation column is divided into series-connected sections mounted side by side, while the liquid from the previous section is taken from under the contact space of this section and by a flow inducer is fed over the contact space of the subsequent section for irrigation, and steam is taken over the contact space of the subsequent section, which is sent under con the active space of the previous section, while a steam lift with liquid evaporation in the steam lift evaporator in the lower part and steam condensation in the steam lift condenser in the upper part is used as a flow inducer, the steam cavity is communicated with the contact space of the sections through hydraulic locks, liquid evaporation and steam condensation in parlift is carried out by supplying to the evaporator a parlift and a parlit condenser of a working fluid circulating in the low pressure cycle and in the high pressure cycle, and the circulation in the low pressure cycle I carry out using a separate compressor, while the reflux of the low-boil
  • a device for concentrating an HD compound from electrolytic hydrogen (see Fig. 14.4, p. 345 "Reference book on the physical and technical fundamentals of a cryogenics" under the pedagogue M. P. Malkova, -3 ⁇ ed., Revised and additional - M .: Energoatomazot, 1985-432 s).
  • the known device consists of a distillation column connected by lines of apparatuses, valves of high and low pressure cycles, a high pressure compressor.
  • the disadvantages of the known device are significant metal consumption and energy consumption in obtaining the target components from difficult to separate mixtures, the inability to obtain as a production low boiling component of the mixture.
  • the aim of the invention is to reduce the metal and energy consumption in the separation of difficult to separate mixtures.
  • This goal is achieved by the fact that in the device for the separation of difficult to separate mixtures, including distillation columns connected by pipelines, valves of high and low pressure refrigeration cycles, housed in a casing, a high pressure compressor, the distinctive feature is that at least one distillation column is broken on the head section of the column, the intermediate sections of the column and the section with the cube of the column, the head section of the column and each intermediate section of the column in the lower part under the contact space has nozzles for liquid outlet and steam inlet, the section with the cube of the column and each intermediate section of the column in the upper part over the contact space has nozzles for liquid inlet, steam outlet and a nozzle, nozzles for steam outlet and inlet of different sections connected in series by steam lines, and the nozzles for the outlet and inlet of the liquid of the same sections - liquid lines with additionally installed flow drivers, and the head section of the column at the top hour
  • inventive method of separation of difficultly separated mixtures can be implemented in the inventive device, schematically shown in the drawing.
  • the device (installation) contains the head section 1 of the column, several (K) intermediate sections 2-1 ⁇ 2-K columns, section 3 with the column cube installed side by side, high pressure cycle, low pressure cycle, block for the supply and preparation of the shared mixture , a vessel 4 with liquid refrigerant and a system of lines (pipelines) 51, 52, 55 ⁇ 57, 67 with fittings for supplying liquid refrigerant to the apparatus and for venting steam (gas), a casing 5 with equipment located inside, connected by a line 6 to a vacuum pump 7. Between the casing 5 and the equipment located inside the casing Expected Screen 68.
  • the head section 1 of the column and the intermediate sections 2-1 ⁇ 2-K columns in the lower part under the contact space have nozzles 8 for liquid outlet and nozzles 9 for steam inlet.
  • Section 3 with a column cube and intermediate sections 2-1 ⁇ 2-K columns in the upper part above the contact space have nozzles 10 of the liquid inlet, nozzles 1 1 of the steam outlet and fittings 12.
  • the steam outlet pipes 11 and the steam inlet pipes 9 of different sections are connected in series with the steam lines 72, the liquid outlet pipes 8 and the liquid inlet pipes 10 of the same sections are connected with the liquid lines 13 with additionally installed flow drivers 14-1 (pipes 8 ⁇ 11, fitting 12, steam lines 72, liquid lines 13, flow drivers 14-1, are conventionally designated only at the head section 1 of the column and the intermediate section 2-1 of the column).
  • Pumps or parlifters can be used as flow boosters 14-1.
  • the steam lifts each of which contains a steam lift evaporator 15 in the lower part
  • in the upper part there is a steam elevator condenser 16 and a traction pipe 73
  • nozzles of the outlet 8 and the liquid inlet 10 of the sections are connected by a liquid line 13 to the steam through the hydraulic locks 17, 18.
  • the condensation cavity each condenser 16 contains a fitting 19, which together with the fitting 12 are connected by impulse pipelines with a pressure comparing device 20, which generates a signal of influence on the heat flux regulating body 21 in the parlift condenser 16.
  • the high-pressure cycle consists of pipelines 48, 49, 50, 58 69 connected to the valves of the high-pressure compressor 22, recuperative gas heat exchangers 23, 24 of the immersion heat exchanger 25, and adsorbent 26 cooled by liquid refrigerant boiling under vacuum created by a vacuum pump 27, filter 28, a submersible evaporator-condenser 29 located in the cube of section 3 with the cube of the column, separator 30, condenser 31 of the column located in the upper part of the head section 1 of the column.
  • the device has a ramp 47 with cylinders filled with a working fluid, connected by line 58 to line 50 at the inlet of the high-pressure compressor 22 and line 69 to line 48 for discharge.
  • the low-pressure cycle consists of pipelines 49 53, 54, 62 connected with the valves of a low-pressure compressor 32, recuperative gas heat exchangers 33, 34, a submersible heat exchanger 35, an adsorber 36, cooled by liquid refrigerant boiling under vacuum, a filter 37, evaporators 15 parlifts, an evaporator -condenser 38, connected in parallel along the flow of the condensing working fluid, the fluid collector 39. separator 30, connected in parallel on the flow of the boiling working fluid of the condensers 16. Evaporators 15 of the elevator and condenser-evaporator 38 pos COROLLARY line 74 with valve 75 can be connected to a high pressure cycle.
  • the block for supplying and preparing the mixture to be divided includes a discharge ramp 39 connected with pipelines 64, 65, 66 with valves, and cylinders for the mixture to be separated, a gearbox 40 and compressor 41, recuperative gas heat exchangers 42, 43, immersion heat exchanger 44, adsorber 45, cooled by liquid refrigerant boiling under vacuum, filter 46.
  • the method of separation of a difficult to separate mixture by the example of separation of a mixture of neon isotopes is as follows.
  • the casing 5, the cavity of the apparatus and pipelines of the high and low pressure cycles, the distillation column sections, the supply and preparation unit for the shared mixture are evacuated, connecting them with lines 6, 59 ⁇ 61 with the vacuum pump 7.
  • cylinders filled with cleaned the working fluid is neon
  • the discharge ramp 39 there are cylinders with a cleaned separated neon mixture, which is a mixture of neon isotopes
  • the vessel 4 is filled along line 67 with liquid nitrogen, which is fed through lines 51, 55, 57 to the immersion heat exchangers 25, 35, 44 on cooling the adsorbers 26, 36, 45 and the screen 68.
  • a working fluid is fed through line 58 to a high pressure cycle.
  • the working fluid is liquefied, first sequentially cooled in a recuperative gas heat exchanger 23 due to reverse flows of a cold working fluid and nitrogen vapor, then in a submersible heat exchanger 26 due to liquid nitrogen boiling under vacuum, a regenerative gas heat exchanger 24 due to a reverse steam flow working fluid and, finally, in a submersible evaporator-condenser 29 due to the boiling of liquid neon with a mass number of 22 (in a stationary mode when there is liquid in the cube), and then they are drosellated to the separator 30.
  • the vapor of the working fluid formed during the cross-linking is sent via line 63 to the recuperative gas heat exchanger 22 as a return flow, and the liquid is sent via line 49 to the condenser of the column 31 and the condensers 16 of the elevators.
  • the vapor of the evaporated liquid from the condensers is returned via lines 62, 63 to the separator 30.
  • possible microimpurities are absorbed.
  • the column condenser 31 and all the condensers 16 of the risers are cooled down, a cooled separable mixture is supplied via line 66 to the column section and a low pressure cycle is started.
  • the separated mixture along the steam lines 72 enters all sections of the column and condenses in the condenser 31 of the column, forming phlegm and initially cooling the contact space.
  • the liquid appears at the bottom of the head section 1 of the column and from the pipe 8 through the liquid line 13 is discharged through the hydraulic lock 17 to the vaporizer 15 of the steam lift 14-1, where it partially or completely evaporates due to the condensation of the working fluid compressed and cooled in the low-pressure cycle .
  • the vapor-liquid (steam) stream through the traction pipe 73 enters the closed the condenser 16 of the steam lift 14-1, where at the same time the opening of the regulatory body 21 from the separator 30 through line 49 serves the liquid.
  • the vapor part of the flow received in the condenser 16 of the parlift of the stream is condensed, mixed with the liquid part of the stream and flows through the water trap 18 for irrigation to the upper part of the first intermediate section 2-1 of the column.
  • the process of starting the first intermediate section 2-1 of the column proceeds similarly to the process of starting the head section 1 of the column. So, sequentially launching the next intermediate sections of the column and, finally, section 3 with the cube of the column, include the entire installation.
  • the steam output of the steam lift evaporators 15 is controlled by valves 71 installed on the condensate drain line to the liquid collector 70, which leads to a change in the heat exchange surface due to a change in the level of condensate in the condensation cavity.
  • the heat flux in the elevator condensers 16 is controlled by changing the heat transfer surface by changing the level of the boiling medium by acting on the regulating bodies 21 depending on the pressure difference between the pressure in the condensation cavity of the elevator condenser, the pulse of which is taken from the nozzle 19, and the pressure in the upper part of the corresponding the intermediate section of the column or section 3 with the cube of the column, the pulse of which is taken from the nozzle 12.
  • the working fluid in the low-pressure cycle through line 53 is fed and subsequently cooled at the beginning in a recuperative gas heat exchanger 33 due to the reverse flows of the cold working fluid and nitrogen vapor, then in the submersible heat exchanger 35 due to boiling under vacuum liquid nitrogen, they are cleaned from possible impurities in the cooled adsorber 36, filtered in the filter 37, cooled in a recuperative gas heat exchanger 34 due to the return flow of steam of the working fluid, is fed to condensation in a submersible evaporator the condenser 38 and the vaporizer 15 evaporators, collect the condensate in the liquid collector 39 and cross into the separator 30.
  • the obtained liquid from the separator 30 is fed through line 49 to the vapor condensers 16 and the condenser 31 of the column for evaporation, and the formed vapors from the apparatus are taken back via line 62 back to the separator 30 and through line 54 through recuperative gas heat exchangers 34, 33 are directed to the inlet of the low pressure compressor 32.
  • the stream of the separated mixture is first fed through line 66 directly from the discharge ramp 39, cooling it in recuperative gas heat exchangers 42 and 43 due to the return production flows of the light component 20 Ne, 21 Ne of the separated mixture, taken out through line 65 from under the cover of the condenser 31 of the column, and the production stream of the heavy component 22 Ne of the separated mixture discharged along line 64 from the section cube 3 with a cube of columns.
  • the recuperative gas heat exchanger 42 the flow of the separated mixture is cooled in the submersible heat exchanger 44 by boiling under vacuum of nitrogen, it is cleaned of possible microimpurities in the adsorber 45 and filtered in the filter 46.
  • the booster compressor 41 and the flow are switched on the separated mixture along line 69 is fed to line 66.
  • the prepared separated mixture is directed to the intermediate section of the column, which, when the device is in operation, has a vapor composition close to that of the divided mixture.
  • the proposed invention allows to reduce the metal and energy consumption during the separation of difficultly separated mixtures, and also to obtain, in addition to the production stream of the heavy component of the mixture, the production stream of the light component.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Inorganic Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne le domaine de purification et de séparation de mélanges d'isotopes et de compositions d'isotopes ayant une faible valeur du coefficient de séparation. Le procédé comprend la séparation du mélange de rectification dans une colonne divisée en plusieurs sections reliées en séquence et montées côte à côte. Le liquide est prélevé dans l'espace de contact de la section précédente puis alimenté par un dispositif de stimulation de débit pour l'arrosage au-dessus de l'espace de contact de la section suivante. La vapeur est prélevée au-dessus de l'espace de contact par la section suivante et alimentée sous l'espace de contact de la section précédente. On utilise en tant que dispositif de stimulation de débit une conduite d'extraction par injection de vapeur, reliée à l'espace de contact des sections au moyen de plusieurs dispositifs de verrouillage hydraulique. L'évaporation du liquide et la condensation de la vapeur dans la conduite d'extraction par injection de vapeur s'effectuent par l'alimentation du fluide de travail circulant dans le circuit basse pression. L'invention propose un dispositif pour mettre en oeuvre le procédé de l'invention. L'invention permet de réduire la consommation de métal et la consommation d'énergie lors de la séparation des mélanges difficilement séparables.
PCT/RU2005/000204 2005-04-19 2005-04-19 Procede et dispositif destines a separer des melanges difficilement separables WO2006112746A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
PCT/RU2005/000204 WO2006112746A1 (fr) 2005-04-19 2005-04-19 Procede et dispositif destines a separer des melanges difficilement separables
DE112005003543T DE112005003543T5 (de) 2005-04-19 2005-04-19 Anlage zur Trennung von schwertrennbaren Mischungen

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/RU2005/000204 WO2006112746A1 (fr) 2005-04-19 2005-04-19 Procede et dispositif destines a separer des melanges difficilement separables

Publications (1)

Publication Number Publication Date
WO2006112746A1 true WO2006112746A1 (fr) 2006-10-26

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PCT/RU2005/000204 WO2006112746A1 (fr) 2005-04-19 2005-04-19 Procede et dispositif destines a separer des melanges difficilement separables

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WO (1) WO2006112746A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11058994B2 (en) 2019-01-18 2021-07-13 Savannah River National Solutions, LLC Tritium cleanup system and method
US11087897B2 (en) 2013-11-13 2021-08-10 Savannah River Nuclear Solutions, Llc Decontamination of tritiated water

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU851034A1 (ru) * 1979-09-04 1981-07-30 Предприятие П/Я А-3605 Установка разделени воздуха
EP1092467A2 (fr) * 1999-10-12 2001-04-18 Nippon Sanso Corporation Dispositif et méthode pour l'enrichissement de isotopes lourds d'oxygen et production d'eau lourde
RU2213609C1 (ru) * 2002-11-15 2003-10-10 Савинов Михаил Юрьевич Способ разделения криптоно-ксенонового концентрата и устройство для его осуществления
RU2254905C1 (ru) * 2004-02-13 2005-06-27 Савинов Михаил Юрьевич Способ разделения трудноразделимых смесей и устройство для его осуществления

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU851034A1 (ru) * 1979-09-04 1981-07-30 Предприятие П/Я А-3605 Установка разделени воздуха
EP1092467A2 (fr) * 1999-10-12 2001-04-18 Nippon Sanso Corporation Dispositif et méthode pour l'enrichissement de isotopes lourds d'oxygen et production d'eau lourde
RU2213609C1 (ru) * 2002-11-15 2003-10-10 Савинов Михаил Юрьевич Способ разделения криптоно-ксенонового концентрата и устройство для его осуществления
RU2254905C1 (ru) * 2004-02-13 2005-06-27 Савинов Михаил Юрьевич Способ разделения трудноразделимых смесей и устройство для его осуществления

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
MALKOVA M.P.: "Spravochnik po fiziko-tekhnicheskim osnovam kriogeniki", MOSCOW, ENERGOATOMIZDAT, 1985, pages 344 - 346 *

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11087897B2 (en) 2013-11-13 2021-08-10 Savannah River Nuclear Solutions, Llc Decontamination of tritiated water
US11058994B2 (en) 2019-01-18 2021-07-13 Savannah River National Solutions, LLC Tritium cleanup system and method

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