WO2019226934A1 - Systèmes de mélange haute pression recirculés et procédés pour augmenter le débit et le facteur de concentration dans des systèmes d'osmose inverse. - Google Patents

Systèmes de mélange haute pression recirculés et procédés pour augmenter le débit et le facteur de concentration dans des systèmes d'osmose inverse. Download PDF

Info

Publication number
WO2019226934A1
WO2019226934A1 PCT/US2019/033820 US2019033820W WO2019226934A1 WO 2019226934 A1 WO2019226934 A1 WO 2019226934A1 US 2019033820 W US2019033820 W US 2019033820W WO 2019226934 A1 WO2019226934 A1 WO 2019226934A1
Authority
WO
WIPO (PCT)
Prior art keywords
pressure vessel
permeate
stream
retentate
feed inlet
Prior art date
Application number
PCT/US2019/033820
Other languages
English (en)
Inventor
Ronan MCGOVERN
Erin PARTLAN
Adam Weiner
John IOANNOU
Original Assignee
Sandymount Technologies Corporation
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 Sandymount Technologies Corporation filed Critical Sandymount Technologies Corporation
Publication of WO2019226934A1 publication Critical patent/WO2019226934A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12H—PASTEURISATION, STERILISATION, PRESERVATION, PURIFICATION, CLARIFICATION OR AGEING OF ALCOHOLIC BEVERAGES; METHODS FOR ALTERING THE ALCOHOL CONTENT OF FERMENTED SOLUTIONS OR ALCOHOLIC BEVERAGES
    • C12H3/00—Methods for reducing the alcohol content of fermented solutions or alcoholic beverage to obtain low alcohol or non-alcoholic beverages
    • C12H3/04—Methods for reducing the alcohol content of fermented solutions or alcoholic beverage to obtain low alcohol or non-alcoholic beverages using semi-permeable membranes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/025—Reverse osmosis; Hyperfiltration
    • B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
    • B01D61/12—Controlling or regulating
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12G—WINE; PREPARATION THEREOF; ALCOHOLIC BEVERAGES; PREPARATION OF ALCOHOLIC BEVERAGES NOT PROVIDED FOR IN SUBCLASSES C12C OR C12H
    • C12G3/00—Preparation of other alcoholic beverages
    • C12G3/04—Preparation of other alcoholic beverages by mixing, e.g. for preparation of liqueurs
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/06—Specific process operations in the permeate stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/14—Pressure control
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2311/00—Details relating to membrane separation process operations and control
    • B01D2311/25—Recirculation, recycling or bypass, e.g. recirculation of concentrate into the feed
    • B01D2311/251—Recirculation of permeate
    • B01D2311/2512—Recirculation of permeate to feed side
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2317/00—Membrane module arrangements within a plant or an apparatus
    • B01D2317/02—Elements in series
    • B01D2317/022—Reject series

Definitions

  • the present invention relates to concentration and/or dealcoholization systems and methods for fermented beverages or liquids.
  • Bonnome discloses a method of manufacturing alcoholic beverage concentrates using multiple passes of membrane filtration, involving the combination of retentates from two passes.
  • Galzy discloses a process for the concentration of small organic compounds below 200 in molecular weight using membranes capable of substantially retaining such compounds within the retentate.
  • McGovern discloses methods for concentrating and retaining compounds of small molecular weight in multi-pass membrane systems with recycle loops.
  • a method for producing a beverage from a starting liquid having an ethanol component includes providing a first set of reverse osmosis pressure vessels, each pressure vessel having a feed inlet for a feed stream, a retentate outlet for a retentate stream, and a permeate outlet for a permeate stream, the first set having at least a first pressure vessel, a second pressure vessel and a third pressure vessel, the retentate outlet of the first pressure vessel fluidly coupled to the feed inlet of the second pressure vessel along a flow path, the retentate outlet of the second pressure vessel fluidly coupled to the feed inlet of the third pressure vessel, and the permeate outlet of the third pressure vessel fluidly coupled to the feed inlet of the second pressure vessel.
  • the method further includes providing a pump coupled to the feed inlet of the first pressure vessel so that the starting liquid is pumped to the feed inlet of the first pressure vessel by the pump, blending the permeate stream of the third pressure vessel with the retentate stream of the first pressure vessel along the flow path to produce a blended stream having a pressure between about 850 psi to about 3000 psi, and obtaining the beverage from the retentate stream of the third pressure vessel.
  • the pressure of the blended stream may be between about 1250 psi to about 3000 psi.
  • the permeate stream of the second pressure vessel may be fluidly coupled to the feed inlet of the first pressure vessel.
  • the method may further include providing a check valve, within the pump or between the pump and the feed inlet of the first pressure vessel, configured to prevent the starting liquid from going back through the pump.
  • the method may further include providing a second pump coupled to the permeate outlet of the third pressure vessel so that the permeate stream of the third pressure vessel is pumped before blending with the retentate stream of the first pressure vessel.
  • the method may further include providing a check valve, within the second pump or between the second pump and the feed inlet of the second pressure vessel, configured to prevent the permeate stream of the third pressure vessel from going back through the second pump.
  • the method may further include providing a second set of reverse osmosis pressure vessels, each pressure vessel in the second set having a feed inlet for a feed stream, a retentate outlet for a retentate stream, and a permeate outlet for a permeate stream, the second set having at least a first pressure vessel and a second pressure vessel, the permeate outlet of the first pressure vessel in the first set fluidly coupled to the feed inlet of the first pressure vessel in the second set, the permeate outlet of the first pressure vessel in the second set fluidly coupled to the feed inlet of the second pressure vessel in the second set, the retentate outlet of the second pressure vessel in the second set fluidly coupled to the feed inlet of the first pressure vessel in the second set, the retentate outlet of the first pressure vessel in the second set
  • the method may further include providing a check valve, within the third pump or between the third pump and the feed inlet of the first pressure vessel in the second set, configured to prevent the second blended stream from going back through the third pump.
  • Each pressure vessel, in the first set of reverse osmosis pressure vessels may have a hydrostatic burst pressure between about 2,400 psi to about 12,000 psi.
  • FIG. 1 depicts a continuous reverse osmosis system separated into stages where a second liquid is introduced at a mid-point in the system according to embodiments of the present invention.
  • FIG. 2 shows a continuous reverse osmosis system separated into stages where a second liquid is introduced at high pressure to a high pressure flow at a mid-point in the system according to embodiments of the present invention.
  • FIG. 3 shows a prior art continuous reverse osmosis system separated into stages where the permeate from the second stage is returned to the feed flow to the system.
  • Fig. 4 depicts a continuous reverse osmosis system separated into stages where the permeates from the second and third stage are returned to the feed flow to the system according to embodiments of the present invention.
  • Fig. 5 depicts a continuous reverse osmosis system separated into stages where the permeate from the second stage is returned to the feed flow to the system and the permeate from the third stage is introduced at high pressure to a high pressure flow between the first and second stages of the system according to embodiments of the present invention.
  • Fig. 6 depicts a continuous three-pass reverse osmosis system where the first pass is separated into stages, where the permeate from the second stage of the first pass is returned to the feed of the first pass, where the permeate from the third stage of the first pass is introduced at high pressure to a high pressure flow between the first and second stages of the system, where the permeate from the first stage of the first pass is introduced via high pressure pump to the feed inlet of the second pass, where the retentate of the second pass is returned to the feed inlet of the first pass, where the permeate of the second pass is introduced without a pump to the feed inlet of the third pass, and where the retentate of the third pass is returned to the feed inlet of the second pass according to embodiments of the present invention.
  • A“set” has at least one member.
  • the term“manifold” as used herein is a coupling between a flow line and a plurality of upstream or downstream flow paths, wherein for example, the plurality of flow paths may be associated with outlets of pressure vessels.
  • “Beverage” as used herein refers to any alcoholic beverage, including beer, wine, and cider, to any solution having alcohol (for example, an ethanol solution), and to any beverage made from fermented products, including beer, wine, cider, mead, and kombucha.
  • “Real Extract”, expressed as a percent weight, is defined as the mass of non ethanol and non-water compounds within a liquid or beverage.
  • Multi-pass, multi-stage reverse osmosis systems for the concentration and/or dealcoholization of beverages (or other fermented liquids), including alcoholic beverages, that allow for boosted throughput or concentration factor.
  • Systems described include multi-stage reverse osmosis systems that operate at low temperatures and high pressures, which are capable of reaching high beverage concentrations and are easily cleanable.
  • Fig. 1 shows a reverse osmosis (RO) system having two pressure vessels or stages 100, 101 with a high pressure pump 102 that feeds a starting liquid or feed 105 into a feed inlet of the first stage 100.
  • the first stage 100 produces a permeate 106 and a retentate
  • the retentate 110 and the second stage 101 produces a permeate 107 and a retentate 108.
  • the retentate 110 of the first stage 100 is fed into a feed inlet of the second stage 101.
  • the system adds a feed 109 to an existing high pressure flow, in this example, retentate 110 from the first stage 100.
  • FIG. 2 shows a reverse osmosis system similar to Fig. 1 with an additional high pressure pump 203 adding the feed 109 into the retentate 110.
  • a check valve 204 or other method of preventing backflow, is important for initialization of pump 203 when high pressure exists in the first stage 100, such that the pressure of feed 109 is equal to the pressure of retentate 110 plus the resistance of check valve 204 before feed 109 can flow into the second stage 101.
  • feed 109 which may be either substantially the same or different from feed 105, is added to the second stage 101 of the reverse osmosis process without requiring a depressurization and repressurization of retentate 110.
  • the blended stream of retentate 110 and pumped feed 109 are coupled to the inlet of the second stage 101 in a series of reverse osmosis processes.
  • feed 105 is a fermented beverage
  • feed 109 is de-aerated water.
  • the system allows for a specific method of bringing de-aerated water to high pressure so water may be blended in with the retentate 110 between two stages 100, 101 of the RO system.
  • Pumps 102, 203 may have different ramp speeds, and this can result in unexpected reverse flow through one pump if the other pump has ramped up first.
  • the check valve 204 solves this problem as the check valve 204 allows the first pump 102 to be turned on, and then pump 203 to be turned on once pressure of retentate 110 is steady.
  • the check valve 204 is shown as a separate component.
  • the check-valve 204 may be built into the pump 203 or into pump 102 (in which case pump 102 is ramped up first).
  • a pump 102 or 203 may be employed that allows only for flow in one direction. Importantly, such a pump 102 or 203 should be able to withstand a back pressure of at least 600 psi when no power is provided to the pump 102 or 203.
  • FIG. 3 shows a prior art system with a two-stage reverse osmosis system designed for high overall retention.
  • the system includes a pump 102 and a feed 105 that is supplied to a feed inlet of the first stage 100.
  • the first stage 100 produces a permeate 106 and a retentate 110 and the second stage 101 produces a permeate 107 and a retentate 108.
  • Retentate 110 is higher in concentration than feed 105, and retentate 110 of the first stage 100 is fed into a feed inlet of the second stage 101, where again a higher concentration retentate 108 is produced.
  • permeate 107 will be of a higher concentration than permeate 106.
  • permeate 107 of the second stage 101 is returned to join with feed 105.
  • Fig. 4 shows a reverse osmosis system similar to Fig. 3 with a third stage 401 added.
  • the third stage 401 of the reverse osmosis system is fed by retentate 108 of the second stage 101.
  • the third stage 401 produces a permeate 402 and a retentate 403 .
  • permeate 107 is necessarily a higher concentration than permeate 106, so is permeate 402 a higher concentration than permeate 107.
  • both permeates 107 and 402 are returned to join with feed 105.
  • Fig. 5 shows a reverse osmosis system similar to Fig. 4, which is more efficient through the coupling of permeate 402 to the inlet of the second stage 101, where it blends with retentate 110 of the first stage 100 at high pressure.
  • the reason for an efficiency gain is because the concentration of permeate 402 from the third stage 401 is higher than permeate 107 from the second stage 101 and, where permeate 107 may be close in concentration to feed 105, then permeate 402 may be close in concentration to retentate 110 of the first stage 100.
  • the pressure at the blend point of the retentate 110 and the permeate 402 should be between 850 psi and 3000 psi, or more preferably 1250 psi to 3000 psi.
  • Table 1 displays data demonstrating improved efficiency allowing for achievement of a higher factor of concentration over the same number of membranes when high pressure blending to a mid-point is employed.
  • high pressure pump 203 with a check valve 204 (or high pressure pump 102 with a check valve) allows for the mixing of two high pressure streams.
  • a pump that does not allow for flow when the streams are not actively being pumped can alternatively serve as back-flow prevention in the place of pump 203 and check valve 204.
  • Table 1 Concentration factors achieved on the same number of membranes when high pressure blending is and is not employed.
  • FIG. 6 shows a reverse osmosis system similar to Fig. 5 with a three-stage, multi-pass system.
  • the three stages are described in Fig. 5, including the pump 203 with check valve 204 to allow for high pressure introduction of permeate 402 from the third stage 401 to the retentate 110 of the first stage 100 in the system between the first stage 100 and the second stage 101.
  • permeate 106 of the first stage 100 is fed using pump 603 into a second set of pressure vessels configured into a two-pass system having a first pass
  • the permeate 606 of the first pass 600 is fed to the feed inlet of the second pass 601.
  • Retentate 608, produced by the first pass 600 is kept within the system by returning the retentate 608 to join with feed 105 to be fed into the first stage 100.
  • the second pass 601 produces a permeate 602, the final permeate output of the entire system in Fig. 6, and does so via backpressure formed by throttling the flow of retentate 604.
  • backpressure to pressurize the second pass 601
  • the permeate 606 from the first pass 600 should be at a pressure between about 300 psi to about 1,500 psi.
  • the high concentration retentate 604 of the second pass 601 is kept within the system by joining with permeate 106 from the first stage 100 and fed to the feed inlet of the first pass 600.
  • the system is able to produce high concentration in retentate 403 of the third stage 401 and high overall retention with less energy than would otherwise be used if high pressure blending and backpressuring were not employed.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Nanotechnology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Biochemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • General Health & Medical Sciences (AREA)
  • Genetics & Genomics (AREA)
  • Wood Science & Technology (AREA)
  • Zoology (AREA)
  • Food Science & Technology (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

Un procédé de production d'une boisson comprend la fourniture d'un ensemble de récipients sous pression d'osmose inverse, chaque récipient sous pression ayant une entrée d'alimentation, une sortie de rétentat pour un flux de rétentat, et une sortie de perméat pour un flux de perméat, la sortie de rétentat du premier récipient sous pression étant en communication fluidique avec l'entrée d'alimentation du deuxième récipient sous pression, la sortie de rétentat du deuxième récipient sous pression étant en communication fluidique avec l'entrée d'alimentation du troisième récipient sous pression, et la sortie de perméat du troisième récipient sous pression étant en communication fluidique avec l'entrée d'alimentation du deuxième récipient sous pression, mélanger le flux de perméat du troisième récipient sous pression avec le flux de rétentat du premier récipient sous pression pour produire un flux mélangé ayant une pression comprise entre environ 850 psi et environ 3000 psi, et obtenir la boisson à partir du flux de rétentat du troisième récipient sous pression.
PCT/US2019/033820 2018-05-23 2019-05-23 Systèmes de mélange haute pression recirculés et procédés pour augmenter le débit et le facteur de concentration dans des systèmes d'osmose inverse. WO2019226934A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US201862675545P 2018-05-23 2018-05-23
US62/675,545 2018-05-23

Publications (1)

Publication Number Publication Date
WO2019226934A1 true WO2019226934A1 (fr) 2019-11-28

Family

ID=68617299

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2019/033820 WO2019226934A1 (fr) 2018-05-23 2019-05-23 Systèmes de mélange haute pression recirculés et procédés pour augmenter le débit et le facteur de concentration dans des systèmes d'osmose inverse.

Country Status (1)

Country Link
WO (1) WO2019226934A1 (fr)

Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160136578A1 (en) * 2014-11-17 2016-05-19 Massachusetts Institute Of Technology Flow control in multi-step filtration, and associated systems
US20160136579A1 (en) * 2014-11-17 2016-05-19 Massachusetts Institute Of Technology Minor component ratio balancing in filtration systems, and associated methods
US20170239620A1 (en) * 2016-02-22 2017-08-24 Massachusetts Institute Of Technology Batch Pressure-Driven Membrane Separation with Closed-Flow Loop and Reservoir
US20170320016A1 (en) * 2016-05-04 2017-11-09 Massachusetts Institute Of Technology Multi-Stage Reverse Osmosis Systems and Methods
US9925494B2 (en) * 2014-11-17 2018-03-27 Massachusetts Institute Of Technology Concentration control in filtration systems, and associated methods
WO2018134285A1 (fr) * 2017-01-18 2018-07-26 Anheuser-Busch Inbev S.A. Procédé de production d'un concentrat de bière ou de cidre
WO2018237015A1 (fr) * 2017-06-20 2018-12-27 Sandymount Technologies Corporation Système et procédé pour la production d'une bière à haute densité physiquement stable
US10273439B2 (en) * 2015-02-11 2019-04-30 Bedford Systems Llc Alcoholic beverage concentrate process
WO2019090340A1 (fr) * 2017-11-06 2019-05-09 Sandymount Technologies Corporation Régulation de débit dans des systèmes d'osmose inverse avec un grand nombre de réservoirs couplés en série
WO2019113544A1 (fr) * 2017-12-08 2019-06-13 Sandymount Technologies Corporation Réduction de perte lors du chargement et du déchargement de boissons dans les systèmes d'élimination d'eau

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20160136578A1 (en) * 2014-11-17 2016-05-19 Massachusetts Institute Of Technology Flow control in multi-step filtration, and associated systems
US20160136579A1 (en) * 2014-11-17 2016-05-19 Massachusetts Institute Of Technology Minor component ratio balancing in filtration systems, and associated methods
US9925494B2 (en) * 2014-11-17 2018-03-27 Massachusetts Institute Of Technology Concentration control in filtration systems, and associated methods
US10273439B2 (en) * 2015-02-11 2019-04-30 Bedford Systems Llc Alcoholic beverage concentrate process
US20170239620A1 (en) * 2016-02-22 2017-08-24 Massachusetts Institute Of Technology Batch Pressure-Driven Membrane Separation with Closed-Flow Loop and Reservoir
US20170320016A1 (en) * 2016-05-04 2017-11-09 Massachusetts Institute Of Technology Multi-Stage Reverse Osmosis Systems and Methods
WO2018134285A1 (fr) * 2017-01-18 2018-07-26 Anheuser-Busch Inbev S.A. Procédé de production d'un concentrat de bière ou de cidre
WO2018237015A1 (fr) * 2017-06-20 2018-12-27 Sandymount Technologies Corporation Système et procédé pour la production d'une bière à haute densité physiquement stable
WO2019090340A1 (fr) * 2017-11-06 2019-05-09 Sandymount Technologies Corporation Régulation de débit dans des systèmes d'osmose inverse avec un grand nombre de réservoirs couplés en série
WO2019113544A1 (fr) * 2017-12-08 2019-06-13 Sandymount Technologies Corporation Réduction de perte lors du chargement et du déchargement de boissons dans les systèmes d'élimination d'eau

Similar Documents

Publication Publication Date Title
US10561987B2 (en) Concentration control in filtration systems, and associated methods
US20180311618A1 (en) Methods of dewatering of alcoholic solutions via forward osmosis and related systems
US11541352B2 (en) Removing components of alcoholic solutions via forward osmosis and related systems
US8114191B2 (en) Energy efficient approach to CO2 capture process
EP3720820B1 (fr) Réduction de perte lors du chargement et du déchargement de boissons dans les systèmes d'élimination d'eau
US20160136579A1 (en) Minor component ratio balancing in filtration systems, and associated methods
CN106232210A (zh) 反渗透装置和方法
US20070158256A1 (en) Apparatus and method for micro or ultrafiltration
WO2018100042A1 (fr) Procédé de production d'un concentré de bière ou de cidre à faible teneur en alcool ou sans alcool
WO2019226934A1 (fr) Systèmes de mélange haute pression recirculés et procédés pour augmenter le débit et le facteur de concentration dans des systèmes d'osmose inverse.
CN101611131B (zh) 用于处理物质料流的方法
CN210905686U (zh) 一种提高膜浓缩倍数和浓液浓度的装置
CN111629812B (zh) 反渗透系统的大批串联联接容器中的流量控制
EP4260932A1 (fr) Procédé et système pour réduire la consommation d'eau dans un processus de désalcoolisation à membrane
CN107441934B (zh) 反渗透系统和使用反渗透系统进行流体浓缩的方法
US20220177816A1 (en) System and Method for the Production of High Gravity Non-Alcoholic Beer through Minimal Water Addition
US20200289986A1 (en) Concurrent desalination and boron removal (cdbr) process
US20210001272A1 (en) Membrane-Based Production of High Ethanol Content Solutions
CN212076622U (zh) 一种浓缩含低分子量醇类溶液的反渗透装置

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 19807278

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

32PN Ep: public notification in the ep bulletin as address of the adressee cannot be established

Free format text: NOTING OF LOSS OF RIGHTS PURSUANT TO RULE 112(1) EPC (EPO FORM 1205A DATED 13/04/2021).

122 Ep: pct application non-entry in european phase

Ref document number: 19807278

Country of ref document: EP

Kind code of ref document: A1