Key information

Title
Device and method for CO2 up-concentration
Application number
20240382
Case type
National
Status
25.08.2025 Patent meddelt (B1)
Filed
19.04.2024
Effective date
19.04.2024
Publicly available
25.08.2025
Next annual fee due
30.04.2027
Applicant
LUNNA EIENDOM AS (NO)
Owner
LUNNA EIENDOM AS (NO)
Inventor
Torbjørn Kvia (NO)
Agent
ACAPO ONSAGERS AS (NO)
Granted
25.08.2025
Patent number
349006
Expiry date
19.04.2044

Abstract and drawing

Disclaimer: This text has been machine-scanned and may contain errors – please refer to "Publications" for legally binding content.
A device for enriching a CO2 concentration in a gas stream is configured for receiving a first gas stream at a first end of a main pipe and for transporting the gas stream in the main pipe. The main pipe is configured on top with a separation pipe having a cross-sectional area of at least 1200 cm2 and a length of at least 4800 mm. The separation pipe is configured with means to release a top gas with a predetermined rate. A second gas stream is provided at the second end of the main pipe with a higher CO2 concentration than the first gas stream.

Publications

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Documents

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Date
 Date Doc. No. Process Case number In/Out Journal description To/from
 28.08.2025 11-01 Saksbehandling 20240382(349006) UT PT Registreringsbrev nasjonal patent (15) (PT20240382)
21.05.2025 10-01 Saksbehandling 20240382 UT PT Meddelelse om patent CURO AS
 16.05.2025 09-06 Saksbehandling 20240382 INN P31523NO00 Norsk kravsett ACAPO ONSAGERS AS
 16.05.2025 09-05 Saksbehandling 20240382 INN P31523NO00 NO20240382 Description Clean ACAPO ONSAGERS AS
 16.05.2025 09-04 Saksbehandling 20240382 INN P31523NO00 NO20240382 Description Annot ACAPO ONSAGERS AS
 16.05.2025 09-03 Saksbehandling 20240382 INN P31523NO00 NO20240382 Claims Clean ACAPO ONSAGERS AS
 16.05.2025 09-02 Saksbehandling 20240382 INN P31523NO00 NO20240382 Besvarelse ACAPO ONSAGERS AS
 16.05.2025 09-01 Saksbehandling 20240382 INN Korrespondanse (Hovedbrev inn) ACAPO ONSAGERS AS
 08.04.2025 08-02 Saksbehandling 20240382 INN PDF_675386534 ACAPO ONSAGERS AS
 08.04.2025 08-01 Saksbehandling 20240382 INN Korrespondanse (Hovedbrev inn) ACAPO ONSAGERS AS
 19.03.2025 07-02 Saksbehandling 20240382 UT PT report 04:59:57
19.03.2025 07-01 Saksbehandling 20240382 UT Realitet patent CURO AS
 20.09.2024 06-06 Saksbehandling 20240382 INN Svar realitet CURO AS
 20.09.2024 06-05 Saksbehandling 20240382 INN kravsett ren 0924 CURO AS
 20.09.2024 06-04 Saksbehandling 20240382 INN kravsett annot 0924 CURO AS
 20.09.2024 06-03 Saksbehandling 20240382 INN beskrivelse ren 0924 CURO AS
 20.09.2024 06-02 Saksbehandling 20240382 INN beskrivelse annot 0924 CURO AS
 20.09.2024 06-01 Saksbehandling 20240382 INN Korrespondanse (Hovedbrev inn) CURO AS
 09.07.2024 05-02 Saksbehandling 20240382 UT PT report 10:50:20
09.07.2024 05-01 Saksbehandling 20240382 UT Realitet patent CURO AS
 23.04.2024 04-02 Saksbehandling 20240382 INN Fullmakt 22 4 24 CURO AS
 23.04.2024 04-01 Saksbehandling 20240382 INN Korrespondanse (Hovedbrev inn) CURO AS
 22.04.2024 03-01 Saksbehandling 20240382 UT Formalia 1 CURO AS
 22.04.2024 02-01 Saksbehandling 20240382 UT Informasjon til oppfinner Torbjørn Kvia
 19.04.2024 01-03 Saksbehandling 20240382 INN U4476 textAF CURO AS
 19.04.2024 01-02 Saksbehandling 20240382 INN U4476 figAF CURO AS
 19.04.2024 01-01 Saksbehandling 20240382 INN Søknadsskjema Patent CURO AS

Description, claims and drawings

Disclaimer: This text has been machine-scanned and may contain errors – please refer to "Publications" for legally binding content. Description
3490061Device and method for CO2 up-concentrationThe present invention concerns a device for up-concentration of CO2 in a gas stream as indicated by the preamble of claim 1. The invention further concerns a method for up-concentration of CO2 in a gas stream and a use of such up-concentrated CO2.5 BackgroundUp-concentrating of CO2 from gas streams such as a flue gas stream is necessary in order to utilise the CO2 (carbon-capture-and-utilisation, CCU) or to enable long-time storage (carbon-captureand-storage, CCS). The demand in both cases is to reduce CO2 emissions with negative consequences for the climate. Different technologies have been developed and are applied for 10 up-concentrating of CO2 from gas streams.EP4321234 A1, EP4074409 A1 and EP2512622 A1 disclose separation and up-concentration of CO2 from gas streams such as flue gas streams. Multi-stage separation is feasible and CO2-concentrations of 98 %vol and higher can be achieved. A disadvantage of membrane technology is the low flux rate through the membrane which limit the productivity of the separation process.15 Another disadvantage is possible fouling of the membranes causing short maintenance intervals and further limitation of productivity. In addition, the energy consumption of the separation process is considerable.EP4265318 A1, EP4182055 A1 and WO12092176 A2 disclose devices, processes and means for separation and up-concentrating of CO2 from gas streams by adsorption. and CO2-concentrations 20 of 98 %vol and higher can be achieved. The disadvantage is that the separation process is energyintensive due to the desorption process. Energy consumption is high for other processes such as cryogenic distillation or electrochemical reduction, too.BR102018005769 A2 relates to a method of gravitational separation of CO2 from natural gas in caves of salt that allows the delivery of the natural gas and CO2 capture and storage (CCS). The 25 mixture of CO2 and natural gas is pumped into the cave of salt with pressure of typically 20-50 MPa. The cave is closed and after the CO2 is settled on the bottom of the cave the natural gas is extracted from the top of the cave. The CO2 is left in the cave as a form of CCS. High energy consumption for preparing the cave, the transport of the gas mixture to the cave and the pumping of the gas mixture into the cave is required. In spite of a possible large volume of the 30 cave the productivity is limited because the cave cannot be re-used for CO2 separation.WO 2018/152238 A1 discloses a process and an apparatus for the capture of carbon dioxide. A vapor comprising carbon dioxide and at least one other component is compressed to form a compressed mixture comprising a dense carbon dioxide fluid and the at least one other component. The compressed mixture comprising the dense carbon dioxide fluid and the other 3490062components is fed to a high-pressure density-driven separator wherein a stream enriched in the dense carbon dioxide fluid and a stream enriched in the at least one other component are formed. The stream enriched in the dense carbon dioxide and the stream enriched in the at least one other component fluid are removed from the separator. The process requires high pressure 5 and high energy consumption.AU 2021/287233 A discloses systems and methods to separate carbon dioxide from flue gases and sequester carbon dioxide. By using the properties of carbon dioxide and the temperature in a body of water (e.g., the ocean or freshwater body of water) or the temperatures of the ambient atmosphere, gaseous carbon dioxide can be converted to a liquid and separated from other gases.10 Pressure used to separate carbon dioxide from other gases may also be used to sequester liquid carbon dioxide. The liquid carbon dioxide is inert and can be discharged into the ocean without dissolving in seawater and acidifying the ocean. The liquid carbon dioxide may further be densified to be denser than seawater. The liquid carbon dioxide can then sink to the bottom of the ocean or be injected into ocean sediments or sediments and rocks beneath the ocean floor, 15 inert and sequestered for the long term. The process requires high pressure and high energy consumption.US 2022401879 A1 discloses systems for separating and concentrating CO2 from air or a gas including a vortex tube designed for separating and concentrating CO2 from a gaseous input stream. The vortex tube has an operating design pressure of between 105 psi (7.2 bar) and 280 20 psi (19.3 bar) above atmospheric pressure and produces a concentrated CO2 outlet stream. The concentrated CO2 outlet stream is in fluid connection with a conversion system capable of converting the separated CO2 into another chemical compound.The drawback of the known methods for CO2 separation is high energy consumption, short maintenance intervals and limited productivity in relation to the size and cost of the separation 25 device.It is therefore a need for devices and methods for CO2 separation and up-concentrating which are straight forward without being energy-intensive.ObjectiveIt is thus an objective of the present invention to provide a method and device for scalable and 30 energy saving separation of CO2.The present inventionThe above objective is achieved by the method according to the present invention as defined by claim 1. 3490063The method disclosed in claim 13 constitutes a further aspect of the present invention.Preferred embodiments are disclosed by the dependent claims.According to the present invention a device comprising at least one main pipe and at least one separation pipe on top of the main pipe is configured for receiving a first gas stream at a first end 5 of a main pipe. The first gas stream may be a flue gas stream from a combustion facility. The gas stream proceeds through the main pipe and fills the main pipe and the separation pipe. The separation pipe is configured with means to release a top gas with a predetermined rate. The CO2 gas has a density of about 1,98 g/cm3 which is about 1,53 times higher than the density of air. CO2 is therefore up-concentrated in the separation pipe with the least concentration on top of the 10 separation pipe. Release of top gas at the predetermined rate makes sure, that the subsequently fed first gas at the first end of the main pipe does not lead to a pressure increase.A steady state is obtained in the separation tube with about 99% vol CO2 gas in the bottom and about 99% air at the top of the separation pipe. The main pipe right below the separation pipe and towards a second end of the main pipe has about 99% vol CO2 gas, too. This CO2 gas acts like 15 a plug towards the subsequently following first gas due to the density difference between air and CO2 and the air in the following gas stream is forced to move upwards into the separation pipe. At the second end of the main pipe a second gas stream is provided with about 99% vol CO2.The separation pipe must have a cross-sectional area of at least 1200 cm2 and a length of at least 4800 mm. The pressure difference between the feeding of the first gas at the first end of the main 20 pipe and the branch of the main pipe with the separation pipe is 3 to 20 mbar. Higher pressure would reduce the enrichment of CO2 in the gas stream. Lower pressure would reduce the productivity in terms of provided CO2 at the second end of the main tube in a predetermined time.Optionally filters for filtering solid particles from the gas stream may be installed.25 In a first embodiment the top gas has a CO2 concentration of less than 1 % vol. A CO2 concentration of less than 0,5 % vol is more preferred and a CO2 concentration of less than 0,1 % vol is most preferred. The top gas is released at the upper end of the separation pipe. The lower the concentration of CO2 in the top gas, the better is the separation in the separation pipe and the higher the concentration of CO2 at the second end of the main tube.30 In another embodiment the means to release the top gas is a controllable valve. The valve may be a mechanically controlled valve, a valve comprising at least one spring, a valve comprising at least one balance weight, a ventilating flap and electrically controlled valve, a valve with actuator, a valve with nozzle, a throttle valve, a throttle valve comprising at least one balance weight or a 3490064different type of valve. The type of valve or other means to release the top gas is not essential for the function of the invention provided the top gas is released at the predetermined rate.In another embodiment the main pipe has a length of at least 1000 m, preferably at least 700 m, more preferred at least 400 m and most preferred at least 200 m. The length of the main pipe is 5 not essential for the function of the invention. Nevertheless, the pressure between the feeding of the first gas at the first end of the main pipe and the branch of the main pipe with the separation pipe may be adjusted due to a change in the length of the main pipe.In another embodiment the separation pipe has a length of at least 8000 mm, preferably at least 6000 mm, more preferred at least 5500 mm and most preferred at least 5000 mm. A longer 10 separation pipe will contribute to a better separation between CO2 and air. However, a longer separation pipe may involve issues on cost and mechanical stability of the device.In another embodiment the pressure difference between the feeding of the first gas at the first end of the main pipe and the branch of the main pipe with the separation pipe is preferably 4 to 10 mbar and more preferred 5 to 6 mbar. Higher pressure provides more gas at the second end of 15 the main pipe, however with reduced enrichment of CO2 in the provided gas stream.In yet another embodiment the first gas stream is a flue gas stream from a combustion facility of carbon comprising material selected from the group consisting of biomass, natural gas, biogas and oil. The nature of the combusted material is not essential for the function of the invention.Materials of natural origin are preferred.20 In another embodiment the bottom of the main pipe is provided with at least one valve configured for releasing condensed water. Water vapour which is comprised by the gas stream may condense and needs to be removed from the main pipe.In another embodiment the concentration of CO2 in the first gas stream is at least 3 % vol, preferably at least 10 % vol, more preferred at least 20 % vol and most preferred at least 25 % vol.25 The higher the concentration of CO2 in the first gas stream the easier is it to reach the target concentration of 99% vol CO2.In another embodiment the enriched CO2 concentration in the second gas stream is at least 80 % vol, preferably at least 90 % vol, more preferred at least 95 % vol and most preferred at least 99 % vol. Up-concentration of CO2 demands normally a concentration of at least 98% vol CO2. However, 30 if lower concentrations are sufficient for a given application, the device may by adapted in order to maximise the productivity and reduce the CO2 concentration to the requested value.In another embodiments the device may further comprise means for cooling, compression and storage of CO2 which are known within industrial handling of gases. 3490065In yet another embodiment the device may comprise two, three, four or more main pipes. The main pipes may have one separation pipe each or being connected before the junction with the separation pipe.The liquified CO2 may be delivered to food and beverage producers, metal manufacturers, 5 manufacturers of cooling devices, manufacturers of devices for fire suppression, greenhouse horticultures and manufacturers for fuels, chemicals and building materials.Certain means and devices described herein for performing steps of the invented method are not described in detail herein since they are somewhat conventional in this technical field. For example, the disclosed embodiments may use elements such as sensor(s) for measuring10 properties; receiver(s) for receiving measurements or other data transmitted by another element;processor(s) for calculating and comparing data; data storage; display unit(s) for displaying data; measurements and instructions; and communication lines between such elements. The novelty and inventiveness of the disclosed method and device are inherent in the relationships and the specific way with which means and devices are combined and used.15 Example:A device for enriching a CO2 concentration in a gas stream comprises four circular main pipes of 500 mm diameter which join a separation pipe of 400 mm diameter and a cross-section area of 1260 cm2. The separation pipe has a length of 5000 mm and a mechanically controlled valve on top and is configured with a supply pipe for the gas stream with the enriched CO2 concentration.20 The device is fed with 21,5 million cubic meters of flue gas per year at the first end of the main pipes and at the end of the supply pipe (second end of the main pipes) 8500 tons of CO2 with a purity of 99% are provided. The pressure difference between the feeding site of the flue gas into the main pipes and the joining site of the main pipes with the separation pipe is 5 to 6 mbar. Below, the invention will be described in further detail in the form of non-limiting exemplary 25 embodiments illustrated by drawings, whereFigure 1 shows a device for enriching a CO2 concentration in a gas stream before the gas stream reaches the separation pipe.Figure 2 shows a device for enriching a CO2 concentration in a gas stream after a steady state in the separation process has been obtained.30 Figure 1 shows a device for enriching a CO2 concentration in a gas stream right after the feeding of the first gas (3) stream has been started. The gas stream comprising CO2 (7) and air (8) has not reached the separation pipe (2) and the mixture of air (8) and CO2 (7) moves through the main pipe (1). No second gas stream (4) with an up-concentrated CO2 concentration is provided at the second end of the main pipe. The water valve (6) is visible. The valve (5) for releasing top gas is 35 closed. 3490066Figure 2 shows a device for enriching a CO2 concentration in a gas stream after the gas stream (3) has reached the separation pipe (2) and a steady state in the separation process has been obtained. Air (8) and CO2 (7) are mixed on the left side of the main pipe (1) and separated on the right side of the main pipe (1) where air (8, 18) is released as top gas and the second gas stream 5 (4) with up-concentrated CO2 (7, 17) is provided. The valve (5) is open in order to release the predetermined amount of top gas. Condensed water may be released through the water valve (6).
Claims
3490067Claims1. Device for enriching a CO2 (7) concentration in a gas stream, the device configured for receiving a first (3) gas stream at a first end of at least one main (1) pipe, the device further configured for transporting the gas stream in the at least one main (1) pipe and configured to 5 provide a second (4) gas stream with a higher CO2 (17) concentration than the first (3) gas stream at a second end of the at least one main (1) pipe characterized in that the at least one main (1) pipe is configured on top with at least one separation (2) pipe having a cross-sectional area of at least 1200 cm2 and a length of at least 4800 mm, thereby generating a branch of the main (1) pipe, wherein the separation (2) pipe is configured with means (5) to release a top (18) gas with a 10 predetermined rate, thereby generating the second (4) gas stream being found at the second end of the main (1) pipe, wherein the pressure difference between the feeding of the first (3) gas at the first end of the main (1) pipe and the branch of the main (1) pipe with the separation (2) pipe is 3 to 20 mbar.2. Device according to claim 1, wherein the top (18) gas has a CO2 (7, 17) concentration of less 15 than 1 % vol, more preferred less than 0,5 % vol and most preferred less than 0,1 % vol.3. Device according to claim 1 or 2, wherein the means (5) to release the top (18) gas is a controllable valve chosen among the group consisting of mechanically controlled valve, electrically controlled valve, valve comprising at least one spring, valve comprising at least one balance weight, ventilating flap, valve with actuator, valve with nozzle, throttle valve, throttle 20 valve comprising at least one balance weight.4. Device according to any of the previous claims, wherein the main (1) pipe has a length of at least 1000 m, preferably at least 700 m, more preferred at least 400 m and most preferred at least 200 m.5. Device according to any of the previous claims, wherein the separation (2) pipe has a length of 25 at least 8000 mm, preferably at least 6000 mm, more preferred at least 5500 mm and most preferred at least 5000 mm.6. Device according to any of the previous claims, wherein the pressure difference between the feeding of the first (3) gas at the first end of the main (1) pipe and the branch of the main (1) pipe with the separation (2) pipe is preferably 4 to 10 mbar and most preferred 5 to 6 mbar.30 7. Device according to any of the previous claims, wherein the first (3) gas stream is a flue (7, 8) gas stream from a combustion facility of carbon comprising material selected from the group consisting of biomass, natural gas, biogas and oil.8. Device according to any of the previous claims, wherein the bottom of the main (1) pipe is provided with at least one valve (6) configured for releasing condensed water.34900689. Device according to any of the previous claims, wherein the concentration of CO2 (7) in the first (3) gas stream is at least 3 % vol, preferably at least 10 % vol, more preferred at least 20 % vol and most preferred at least 25 % vol.10. Device according to any of the previous claims, wherein the enriched CO2 (17) concentration 5 in the second (4) gas stream is at least 80 % vol, preferably at least 90 % vol, more preferred at least 95 % vol and most preferred at least 99 % vol.11. Device according to any of the previous claims, wherein the device further comprises means for cooling, compression and storage of CO2 (17).12. Device according to any of the previous claims, wherein the device comprises at least two 10 main (1) pipes, preferably at least three main (2) pipes and most preferred at least four (1) main pipes, wherein the main (1) pipes share a common separation (2) pipe or wherein each main (1) pipe is configured with an own separation (2) pipe.13. Method for enriching a CO2 (7) concentration in a gas stream, comprising the steps of- providing a first (3) gas stream at a first end of a main (1) pipe,15 - transporting the first (3) gas stream in the main (1) pipe- receiving a second (4) gas stream with the enriched CO2 (17) concentration at a second end of the main (1) pipe,characterized in that- the main (1) pipe is provided on top with a separation (2) pipe having a cross-sectional 20 area of at least 1200 cm2 and a length of at least 4800 mm, thereby providing a branch of the main (1) pipe and the separation (2) pipe is further provided with means (5) to release a top (18) gas with a predetermined rate, wherein the pressure difference between the feeding of the first (3) gas at the first end of the main (1) pipe and the branch of the main (1) pipe with the separation (2) pipe is 3 to 20 mbar.25 14. Method according to claim 13, wherein the second (4) gas stream is cooled, compressed and stored in liquid state in a CO2-tank.15. Use of the device of claim 1 and/or the method of claim 13 for supplying CO2 (17) to at least one receiver selected from the group consisting of food and beverage producer, metal manufacturer, manufacturer of cooling devices, manufacturer of devices for fire suppression, 30 greenhouse horticulture and manufacturer for fuels, chemicals and building materials.3490069Patentkrav1. Anordning for anrikning av en CO2 (7)-konsentrasjon i en gasstrøm, hvor anordningen er innrettet til å motta en første (3) gasstrøm ved en første ende av minst ett hovedrør (1), idet anordningen videre er innrettet til å transportere gasstrømmen i det minst ene hovedrøret (1) og 5 innrettet til å levere en andre (4) gasstrøm med en høyere CO2 (17)-konsentrasjon enn den første (3) gasstrømmen ved en andre ende av det minst ene hovedrøret (1), karakterisert ved at det minst ene hovedrøret (1 på dets overside ) er innrettet med minst ett separasjonsrør (2) som har et tverrsnittsareal på minst 1200 cm2 og en lengde på minst 4800 mm, og derved danner en forgrening av hovedrøret (1), idet separasjonsrøret (2) er innrettet med midler (5) til å frigjøre en 10 toppgass (18) med en forutbestemt hastighet, og derved genererer den andre (4) gasstrømmen som befinner seg ved den andre enden av hovedrøret (1), idet trykk-forskjellen mellom tilførselen av den første (3) gassen ved den første enden av hovedrøret (1) og forgreningen av hovedrøret (1) med separasjonsrøret (2) ,er 3 til 20 mbar.2. Anordning ifølge krav 1, hvor toppgassen (18) har en CO2-konsentrasjon (7, 17) på mindre enn 1 15 % vol, mer foretrukket mindre enn 0,5 % vol og mest foretrukket mindre enn 0,1 % vol.3. Anordning ifølge krav 1 eller 2, hvor midlene (5) for å frigjøre toppgassen (18) er en styrbar ventil valgt fra gruppen bestående av mekanisk styrt ventil, elektrisk styrt ventil, ventil som omfatter minst en fjær, ventil som omfatter minst en balansevekt, ventilasjonsklaff, ventil med aktuator, ventil med dyse, strupeventil og strupeventil som omfatter minst en balansevekt.20 4. Anordning ifølge et hvilket som helst av de foregående krav, hvor hovedrøret (1) har en lengde på minst 1000 m, fortrinnsvis minst 700 m, mer foretrukket minst 400 m og mest foretrukket minst 200 m.5. Anordning ifølge et hvilket som helst av de foregående krav, hvor separasjonsrøret (2) har en lengde på minst 8000 mm, fortrinnsvis minst 6000 mm, mer foretrukket minst 5500 mm og mest 25 foretrukket minst 5000 mm.6. Anordning ifølge et hvilket som helst av de foregående krav, hvor trykkforskjellen mellom tilførselen av den første (3) gassen ved den første enden av hovedrøret (1) og forgreningen av hovedrøret (1) med separasjonsrøret (2) fortrinnsvis er 4 til 10 mbar, og mest foretrukket 5 til 6 mbar.30 7. Anordning ifølge et hvilket som helst av de foregående krav, hvor den første (3) gasstrømmen er en røykgasstrøm (7, 8) fra et forbrenningsanlegg av karboninneholdende materiale valgt fra gruppen bestående av biomasse, naturgass, biogass og olje.8. Anordning ifølge et hvilket som helst av de foregående krav, hvor nedre del av hovedrøret (1) er utstyrt med minst en ventil (6) som er innrettet til å slippe ut kondensert vann.349006109. Anordning ifølge et hvilket som helst av de foregående krav, hvor konsentrasjonen av CO2 (7) i den første (3) gasstrømmen er minst 3 % vol, fortrinnsvis minst 10 % vol, mer foretrukket minst 20 % vol og mest foretrukket minst 25 % vol.10. Anordning ifølge et hvilket som helst av de foregående krav, hvor konsentrasjonen av anriket 5 CO2 (17) i den andre (4) gasstrømmen er minst 80 % vol., fortrinnsvis minst 90 % vol., mer foretrukket minst 95 % vol. og mest foretrukket minst 99 % vol.11. Anordning ifølge et hvilket som helst av de foregående krav, hvor anordningen videre omfatter midler for kjøling, komprimering og lagring av CO2 (17).12. Anordning ifølge et hvilket som helst av de foregående krav, hvor anordningen omfatter minst 10 to hovedrør (1), fortrinnsvis minst tre hovedrør (2) og mest foretrukket minst fire hovedrør (1), idet hovedrørene (1) deler et felles separasjonsrør (2), eller hvor hvert hovedrør (1) er innrettet med et eget separasjonsrør (2).13. Fremgangsmåte for å anrike en CO2-konsentrasjon (7) i en gasstrøm, omfattende følgende trinn15 - å tilveiebringe en første (3) gasstrøm ved en første ende av et hovedrør (1)- å transportere den første (3) gasstrømmen i hovedrøret (1)- å motta en andre (4) gasstrøm med den anrikede CO2-konsentrasjonen (17) i en andre ende av hovedrøret (1),karakterisert ved at20 - hovedrøret (1) er utstyrt på oversiden med et separasjonsrør (2) som har et tverrsnittsareal på minst 1200 cm2 og en lengde på minst 4800 mm, og derved danner en forgrening av hovedrøret (1), samt at separasjonsrøret (2) videre er utstyrt med et middel (5) for å frigjøre en toppgass (18) med en forutbestemt hastighet, idet trykkforskjellen mellom tilførselen av den første (3) gassen ved den første enden av hovedrøret (1) og forgreningen av hovedrøret (1) med separasjonsrøret 25 (2), er 3 til 20 mbar.14. Fremgangsmåte ifølge krav 13, hvor den andre (4) gasstrømmen avkjøles, komprimeres og lagres i flytende tilstand i en CO2-tank.15. Bruk av anordningen ifølge krav 1 og/eller fremgangsmåten i krav 13 for tilførsel av CO2 (17) til minst én mottaker valgt fra gruppen bestående av næringsmiddel- og drikkevareprodusenter, 30 metallprodusenter, produsenter av kjøleinnretninger, produsenter av innretninger for brannslukking, drivhusgartnerier og produsenter av drivstoff, kjemikalier og byggematerialer.
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Patent classes

IPC classesB01D 53/00CPC classesB01D 53/00

Citations

WO 2018/152238 A1 (A1)AU 2021/287233 A (A)US 2022/401879 A1 (A1)WO 2006/098637 A1 (A1)WO 2008/140319 A1 (A1)

Applicants, owners and inventors

Owners
LUNNA EIENDOM AS
Skysetveien 7A 1481 HAGAN NO (NITTEDAL Municipality, Akershus county)Org. number: 981238370Inventors
Torbjørn Kvia
Kjerrevegen 7 4365 NÆRBØ NO (HÅ Municipality, Rogaland county)

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ACAPO ONSAGERS AS
ACAPO ONSAGERS AS

Org. number: 932214636

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Org. number: 932214636
Reference: P31523NO00

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