US20180209725A1 - Production of helium from a stream of natural gas - Google Patents

Production of helium from a stream of natural gas Download PDF

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Publication number
US20180209725A1
US20180209725A1 US15/744,987 US201615744987A US2018209725A1 US 20180209725 A1 US20180209725 A1 US 20180209725A1 US 201615744987 A US201615744987 A US 201615744987A US 2018209725 A1 US2018209725 A1 US 2018209725A1
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Prior art keywords
helium
column
pressure
volume
nitrogen
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Abandoned
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US15/744,987
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English (en)
Inventor
Paul TERRIEN
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Assigned to L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE reassignment L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: TERRIEN, PAUL
Publication of US20180209725A1 publication Critical patent/US20180209725A1/en
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    • 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
    • F25J3/0204—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 characterised by the feed stream
    • F25J3/0209—Natural gas or substitute natural gas
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0233—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 characterised by the separated product stream separation of CnHm with 1 carbon atom or more
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0238—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 characterised by the separated product stream separation of CnHm with 2 carbon atoms or more
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/0257—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 characterised by the separated product stream separation of 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
    • 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
    • F25J3/0228—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 characterised by the separated product stream
    • F25J3/028—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 characterised by the separated product stream separation of noble gases
    • F25J3/029—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 characterised by the separated product stream separation of noble gases of 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) 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
    • F25J2290/34—Details about subcooling of liquids

Definitions

  • the present invention relates to a process for producing helium from a source gas stream comprising at least helium, methane and nitrogen.
  • Helium is commercially obtained virtually exclusively from a mixture of volatile components of natural gas, this mixture comprising, along with the helium, typically methane and nitrogen and traces of hydrogen, of argon, and of other noble gases.
  • helium is made available as a component of the gas which accompanies the mineral oil, or in the context of the production of natural gas. It is theoretically possible to obtain helium in the atmosphere, but it is not economical because of the low concentrations (typical concentration of helium in air of about 5.2 ppmv).
  • Crude natural gas can contain a large number of impeding impurities that need to be removed.
  • Nitrogen is one example of this. Starting from a certain concentration of nitrogen in natural gas, the latter is typically not saleable because of its low calorific value.
  • a cryogenic process carried out in a unit referred to as a nitrogen rejection unit (NRU) is usually used to remove the nitrogen.
  • the helium is concentrated in the cryogenic process and is finally purified in a PSA (pressure-swing adsorption) process.
  • PSA pressure-swing adsorption
  • the subject of the present invention is a process for producing a helium gas stream from a source gas stream comprising at least helium, methane and nitrogen, comprising at least the following steps:
  • step d) separating the mixture resulting from step c) in a first phase separator vessel into a liquid phase and a helium-enriched gas phase;
  • the subject of the present invention is also:
  • the solution which is the subject of the present invention makes it possible to separate a stream composed of methane, nitrogen and helium into three streams: a pure methane stream, a pure nitrogen stream and a helium-rich stream.
  • the present invention makes it possible to solve the problem of the solutions by partial condensation, by obtaining both a high helium yield (>85%) and a high helium content (>50%), this being without using a column dedicated to helium separation.
  • the process which is the subject of the invention consists of a double-column NRU unit in which total condensation (or virtually total condensation owing to the presence of uncondensable compounds) is carried out at the level of the condenser of the high-pressure HP column.
  • the liquid produced at the top of this HP column is partly used as reflux of the HP column and partly intended to be used as reflux of the low-pressure LP column.
  • flash gas is intended to mean: instantaneous vapor
  • FIG. 1 is a schematic representation of one embodiment of the present invention.
  • FIG. 1 The process which is the subject of the present invention is illustrated in FIG. 1 .
  • a source gas stream 1 comprising at least helium, methane and nitrogen is introduced at a pressure of approximately 50 bar absolute into a heat exchanger 2 .
  • the stream 3 at the outlet of said exchanger 2 is expanded by means, for example, of a valve 4 , before being introduced into a high-pressure column 5 of a double-column unit 6 comprising a high-pressure distillation column 5 , a low-pressure distillation column 7 and a condenser 8 linking the high-pressure column 5 with the low-pressure column 7 .
  • the source gas stream 1 comprises, for 100% by volume, for example, from 20% by volume to 80% by volume of methane, from 20% by volume to 80% by volume of nitrogen and from 1 ppm by volume to 1% by volume of helium.
  • the pressure of the high-pressure column is for example 30 bara and the pressure in the low-pressure column is for example 2 bara.
  • nitrogen rejection unit relates to a device in which the nitrogen and the methane are separated by cryogenic rectification.
  • a part ( 3 d ) of the stream 3 being introduced mainly in liquid form and a part ( 3 c ) is introduced mainly in gas form at the bottom of column 5 so as to vaporize the helium that would otherwise be entrained in the liquid methane.
  • a part 9 of the liquid stream 11 leaving the condenser 8 located in the bottom part of the low-pressure column 7 is used as reflux in the top part 10 of the high-pressure column 5 .
  • the remainder of the liquid 11 is cooled and then expanded so as to be directly used as reflux of the low-pressure column.
  • the subject matter of the present invention consists in using a part 12 of said liquid stream 11 for extracting therefrom the helium before using it as reflux of the low-pressure column.
  • This liquid stream 11 typically contains less than 2% by volume of methane, more that 95% by volume of nitrogen and from 0.5% by volume to 3% by volume of helium.
  • the temperature of the liquid stream 12 is for example between ⁇ 150° C. and ⁇ 165° C.
  • This liquid stream 12 is expanded to an intermediate pressure by means, for example, of a valve 13 .
  • This intermediate pressure is typically about 8 bara to 15 bara. It is for example 12 bara.
  • the liquid stream has been vaporized, that is to say that gas has been instantaneously formed (this is “flash” gas).
  • the stream 14 thus produced contains a majority of liquid and a minority of gas.
  • This gas is enriched in helium.
  • This helium-enriched gas comprises at least 80% by volume of the helium contained in the liquid stream 12 .
  • the two-phase stream 14 is introduced into a first phase separator vessel 15 .
  • the vessel 15 produces a liquid stream 16 and a gas stream 17 .
  • the gas stream 17 contains more than 80% by volume of the helium contained in the source stream 1 .
  • this gas stream 17 contains nitrogen.
  • the liquid stream 16 containing a majority of nitrogen, but also helium and methane, is introduced into the top part 18 of the low-pressure column 7 after having been expanded, for example by means of a valve 19 , in order to serve as reflux of the low-pressure column 7 .
  • the stream 20 at the outlet of the top 21 of the column 7 is introduced into a heat exchanger 22 or 2 in order to produce a stream 23 which is rich in nitrogen or even pure with respect to nitrogen, which does not contain helium and which contains less than 1.5% by volume of methane.
  • the helium-enriched gas stream 17 typically contains more than 70% by volume of nitrogen, more than 5% by volume of helium and less than 2% by volume of methane, for example 90% by volume of nitrogen, from 8% to 10% by volume of helium and less than 0.5% by volume of methane.
  • This gas stream 17 is introduced into a heat exchanger 24 in order to be at least partially condensed.
  • the mixture 25 thus condensed is introduced into a second phase separator vessel 26 .
  • a gas stream 27 is extracted at the top of the separator 26 .
  • This gas stream 27 comprises more than 50% by volume of helium, preferably more than 60% by volume of helium and more particularly more than 70% by volume of helium.
  • the gas stream 27 can optionally again pass through a heat exchanger 24 .
  • the liquid phase 28 from the separator 26 serves to cool the exchanger 24 after having been expanded to a pressure of less than 3 bara, for example by means of a pressure regulator such as a valve 29 .
  • This liquid stream 28 is pure with respect to nitrogen, for example it contains more than 99% by volume of nitrogen.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)
US15/744,987 2015-07-16 2016-07-12 Production of helium from a stream of natural gas Abandoned US20180209725A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR1556739 2015-07-16
FR1556739A FR3038973B1 (fr) 2015-07-16 2015-07-16 Production d'helium a partir d'un courant de gaz naturel
PCT/FR2016/051786 WO2017009573A1 (fr) 2015-07-16 2016-07-12 Production d'hélium à partir d'un courant de gaz naturel

Publications (1)

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US20180209725A1 true US20180209725A1 (en) 2018-07-26

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US15/744,987 Abandoned US20180209725A1 (en) 2015-07-16 2016-07-12 Production of helium from a stream of natural gas

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US (1) US20180209725A1 (ru)
EP (1) EP3322949B1 (ru)
FR (1) FR3038973B1 (ru)
PL (1) PL3322949T3 (ru)
RU (1) RU2717666C2 (ru)
WO (1) WO2017009573A1 (ru)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111981767A (zh) * 2020-08-20 2020-11-24 中国石油工程建设有限公司 一种天然气单塔深冷提氦装置和方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2736682C1 (ru) * 2020-06-05 2020-11-19 Андрей Владиславович Курочкин Установка подготовки природного газа с извлечением гелия

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4701200A (en) * 1986-09-24 1987-10-20 Union Carbide Corporation Process to produce helium gas
US4948405A (en) * 1989-12-26 1990-08-14 Phillips Petroleum Company Nitrogen rejection unit
US5617741A (en) * 1995-02-10 1997-04-08 Air Products And Chemicals, Inc. Dual column process to remove nitrogen from natural gas
US5771714A (en) * 1997-08-01 1998-06-30 Praxair Technology, Inc. Cryogenic rectification system for producing higher purity helium
US20110174017A1 (en) * 2008-10-07 2011-07-21 Donald Victory Helium Recovery From Natural Gas Integrated With NGL Recovery
US20110226009A1 (en) * 2008-10-07 2011-09-22 Henri Paradowski Process for producing liquid and gaseous nitrogen streams, a gaseous stream which is rich in helium and a denitrided stream of hydrocarbons and associated installation

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
SU127270A1 (ru) * 1959-05-18 1959-11-30 Л.С. Бабе Способ извлечени гели из природного газа
US4701201A (en) * 1986-09-24 1987-10-20 Union Carbide Corporation Process to produce cold helium gas for liquefaction
RU2502545C1 (ru) * 2012-08-08 2013-12-27 Открытое акционерное общество "Газпром" Способ переработки природного газа и устройство для его осуществления

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4701200A (en) * 1986-09-24 1987-10-20 Union Carbide Corporation Process to produce helium gas
US4948405A (en) * 1989-12-26 1990-08-14 Phillips Petroleum Company Nitrogen rejection unit
US5617741A (en) * 1995-02-10 1997-04-08 Air Products And Chemicals, Inc. Dual column process to remove nitrogen from natural gas
US5771714A (en) * 1997-08-01 1998-06-30 Praxair Technology, Inc. Cryogenic rectification system for producing higher purity helium
US20110174017A1 (en) * 2008-10-07 2011-07-21 Donald Victory Helium Recovery From Natural Gas Integrated With NGL Recovery
US20110226009A1 (en) * 2008-10-07 2011-09-22 Henri Paradowski Process for producing liquid and gaseous nitrogen streams, a gaseous stream which is rich in helium and a denitrided stream of hydrocarbons and associated installation

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111981767A (zh) * 2020-08-20 2020-11-24 中国石油工程建设有限公司 一种天然气单塔深冷提氦装置和方法

Also Published As

Publication number Publication date
FR3038973B1 (fr) 2019-09-27
WO2017009573A1 (fr) 2017-01-19
RU2018103764A (ru) 2019-07-31
EP3322949A1 (fr) 2018-05-23
FR3038973A1 (fr) 2017-01-20
RU2717666C2 (ru) 2020-03-24
PL3322949T3 (pl) 2022-07-25
EP3322949B1 (fr) 2022-02-23
RU2018103764A3 (ru) 2019-10-29

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