Key information

Title: Method and plant for CO2 capture
Application number: 20210813
Case type: National
Status: 15.07.2024 Patent meddelt (B1)
Filed: 24.06.2021
Effective date: 24.06.2021
Publicly available: 27.12.2022
Next annual fee due: 30.06.2027
Applicant: CO2 CAPSOL AS (NO)
Owner: CAPSOL TECHNOLOGIES ASA (NO)
Inventor: Stellan Hamrin (SE)
Agent: BRYN AARFLOT AS (NO)
Granted: 15.07.2024
Patent number: 348066
Expiry date: 24.06.2041

Abstract and drawing

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A method for removing CO2 from a CO2 rich gas, where the CO2 containing gas is cooled and compressed to a pressure of 5 to 30 bar and introduced into an absorber (10) where the CO2 rich gas is brought into countercurrent flow with an aqueous CO2 absorbent to give a CO2 lean gas flow and a CO2 rich absorbent which are removed from the absorber (10) from the top and the bottom of the absorber, respectively, where the CO2 lean gas is heated against the incoming CO2 containing gas in a heat exchanger (2) and thereafter expanded over an expander (21), wherein compressed air is introduced into heat exchanger (2) together with the CO2 lean gas, and a plant for performing the method, are described.

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Date

Date	Doc. No.	Process	Case number	In/Out	Journal description	To/from
07.09.2026	01-01	Overdragelse av søknad/rettighet Endring av søker/innehaver	2026/06814	INN	Generell henvendelse	CAPSOL TECHNOLOGIES ASA
18.07.2024	13-01	Saksbehandling	20210813(348066)	UT	PT Registreringsbrev nasjonal patent (15) (PT20210813)
02.05.2024	12-01	Saksbehandling	20210813	UT	PT Meddelelse om patent	BRYN AARFLOT AS
18.04.2024	11-07	Saksbehandling	20210813	INN	Response NIPO_[P6691NO00]	BRYN AARFLOT AS
18.04.2024	11-06	Saksbehandling	20210813	INN	Description-amended-marked	BRYN AARFLOT AS
18.04.2024	11-05	Saksbehandling	20210813	INN	Description-amended-clean	BRYN AARFLOT AS
18.04.2024	11-04	Saksbehandling	20210813	INN	claims-no	BRYN AARFLOT AS
18.04.2024	11-03	Saksbehandling	20210813	INN	Claims-amended-marked	BRYN AARFLOT AS
18.04.2024	11-02	Saksbehandling	20210813	INN	Claims-amended-clean	BRYN AARFLOT AS
18.04.2024	11-01	Saksbehandling	20210813	INN	Korrespondanse (Hovedbrev inn)	BRYN AARFLOT AS
19.01.2024	10-01	Saksbehandling	20210813	UT	Realitet patent	BRYN AARFLOT AS
20.06.2023	09-02	Saksbehandling	20210813	INN	Response NIPO	BRYN AARFLOT AS
20.06.2023	09-01	Saksbehandling	20210813	INN	Korrespondanse (Hovedbrev inn)	BRYN AARFLOT AS
04.05.2023	08-01	Saksbehandling	20210813	UT	PT Varsel om betaling av første årsavgift (3317) (PT20210813)	BRYN AARFLOT AS
19.04.2023	07-01	Saksbehandling	20210813	INN	Korrespondanse (Hovedbrev inn)	BRYN AARFLOT AS
15.02.2023	06-01	Saksbehandling	20210813	UT	PT Bekreftelse på fristutsettelse	BRYN AARFLOT AS
22.11.2022	05-01	Saksbehandling	20210813	UT	Realitet patent	CO2 CAPSOL AS
17.06.2022	04-04	Saksbehandling	20210813	INN	P6691NO00-Power of Attorney	PROTECTOR IP AS
17.06.2022	04-03	Saksbehandling	20210813	INN	P6691NO00-Brev_til_Patentstyret_Jun_17,_2022	PROTECTOR IP AS
17.06.2022	04-02	Saksbehandling	20210813	INN	P6691NO00-BGC erklæring	PROTECTOR IP AS
17.06.2022	04-01	Saksbehandling	20210813	INN	Korrespondanse (Hovedbrev inn)	PROTECTOR IP AS
11.01.2022	03-02	Saksbehandling	20210813	UT	PT report 05:14:53
11.01.2022	03-01	Saksbehandling	20210813	UT	Realitet patent	CO2 CAPSOL AS
30.06.2021	02-01	Saksbehandling	20210813	UT	Infobrev til oppfinner	CO2 CAPSOL AS
24.06.2021	01-05	Saksbehandling	20210813	INN	figur co2	CO2 CAPSOL AS
24.06.2021	01-04	Saksbehandling	20210813	INN	Erklæring om rettten til oppfinnelse	CO2 CAPSOL AS
24.06.2021	01-03	Saksbehandling	20210813	INN	Description and claims	CO2 CAPSOL AS
24.06.2021	01-02	Saksbehandling	20210813	INN	Abstract	CO2 CAPSOL AS
24.06.2021	01-01	Saksbehandling	20210813	INN	Søknadsskjema Patent	CO2 CAPSOL 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

Field of invention

[0001] The present invention relates to capture of CO2 from a CO2 containing gas flow, such as the exhaust gas from combustion of a carbonaceous material, or a waste gas from an industrial plant.

Background

[0002] The increase in atmospheric CO2 concentration leading to an increase in the greenhouse effect to result in global climate changes is of great concern and have caused an environmental pressure towards stopping, or at least dramatically reducing, the use of fossil fuels and towards a change to renewable energy resources. However, a rapidly growing global energy demand and the fact that a change from fossil to renewable energy sources takes time and is expensive, carbonaceous fuels are expected to be important as energy sources for decades to come. Carbon Capture and Storage (CCS) has therefore become important in reducing the global CO2 emission.

[0003] Many concepts and projects for CO2 capture have been suggested, but few of them have developed from idea or drawing to actual projects, due to both high investment and running cost of such plants, and the lack of political support.

[0004] Most of the proposed projects for CO2 capture are based on post combustion CO2 capture, where CO2 containing exhaust gas is introduced into an absorber, where the CO2 containing gas is brought in intimate contact with a CO2 absorbent to remove or at least substantially reduce the CO2 content of the exhaust gas before it is released into the surroundings. The absorbent having absorbed CO2 is then introduced into a stripper to regenerate the absorbent for re-use, and the captured CO2 is removed for deposition / storage.

[0005] The most commonly suggested absorbents are inorganic absorbents, normally aqueous solution of potassium carbonate, and organic absorbents, normally aqueous solution of one or more organic amines or amino acids. Organic absorbents are prone to degradation during use, especially in presence of oxygen. Some of the degradation products of amines known from operation of such plants are known as toxic and carcinogenic compounds and may be released into the surroundings together with the CO2 depleted exhaust gas. Operation of a capture plant using organic absorbents at a higher pressure than atmospheric pressure increases the problem of degradation as the partial pressure of oxygen is increase by compression. Potassium carbonate, at the other side, is relatively inexpensive, is chemically stable in the operating conditions of the capture plant and produces no toxic or carcinogenic degradation products.

[0006] The speed of reaction and system equilibria for capture of CO2 in a capture plant is highly dependent on the partial pressure of CO2 in the absorber, i.e., the part of the capture plant where the CO2 containing gas is brought in intimate contact with the absorbent. Additionally, using high pressure reduces the gas volume, and makes it possible to reduce the size of the plant significantly, and thus reducing the construction cost.

[0007] WO 0048709, to Norsk Hydro, relates to a method for capturing CO2 from an exhaust gas from a primary power plant, such as a gas turbine-based power plant. Expanded and cooled exhaust gas from the gas turbine power plant is re-compressed to a pressure of 5 to 30 bar, typically 7 to 20 bar, and cooled before the compressed gas is introduced into an absorber and brought in contact with an amine absorbent in an absorber of a CO2 capture plant. The CO2 depleted exhaust gas is reheated against the incoming exhaust gas before expansion of the gas over a turbine to give power for compression of the incoming exhaust gas. The drawback of this approach is that it needs a steam turbine plant and a separate HRSG to fully exploit the heat in the exhaust gas.

[0008] US2021060478A1 discloses a method and a plant for capturing CO2 from an incoming flue gas. The flue gas can be exhaust gas from coal and gas fired power plants, cement factories or refineries. The incoming exhaust gas is cooled, mixed with air and compressed, and thereafter introduced into a combustion chamber together with gas and/or liquid fuel. Part of the combustion is achieved by separate burners with cooling/combustion air feed with a volume equal to the volume of CO2 captured. Said burners will elevate the temperature in the combustion chamber allowing combustion of exhaust gas with low oxygen content. CO2 is captured at high partial pressure before expansion by the gas turbine to produce power and generate steam in the heat recovery unit.

Summary of the invention

[0009] According to a first aspect, the present invention relates to a method for removing CO2 from a CO2 rich gas, where the CO2 containing gas is cooled and compressed to a pressure of 5 to 30 bar and introduced into an absorber where the CO2 rich gas is brought into countercurrent flow with an aqueous CO2 absorbent to give a CO2 lean gas flow and a CO2 rich absorbent which are removed from the absorber from the top and the bottom of the absorber, respectively, where the CO2 lean gas is heated against the incoming CO2 containing gas in a heat exchanger and thereafter expanded over an expander, wherein compressed air is introduced, together with the CO2 lean gas, into the heat exchanger. Removal of CO2 from the incoming gas flow reduces the total heat capacity of the gas. By introduction of compressed air together with the lean exhaust gas, the mixed air / lean gas gets an increased capacity to cool the incoming CO2 containing gas and thereby to reduce heat loss in the system. This makes it possible to fully replace the commonly used HRSG/Steam Turbine with the Heat Exchanger/Expander that is already needed in the CO2 capture plant and only adding a smaller Air Compressor.

[0010] According to one embodiment, the incoming CO2 containing gas has a temperature of 200 to 700 deg. C.

[0011] According to a second aspect the invention relates to a plant for removing CO2 from a CO2 rich gas, the plant comprising an exhaust gas line for introduction of the CO2 rich gas into a heat exchanger for cooling of the incoming CO2 rich gas, compressor(s) for compression of the CO2 rich gas cooled in the compressor(s), a compressed exhaust gas line for introduction of the compressed exhaust gas into an absorber where the exhaust gas is brought in countercurrent flow against an aqueous CO2 absorbent, a lean absorbent line for introduction of lean absorbent into the absorber, a lean exhaust gas line for withdrawal of CO2 depleted, or lean, exhaust gas leaving and introduction thereof into the heat exchanger to be heated against the incoming exhaust gas, a heated gas line for leading the heated lean exhaust gas from the heat exchanger to an expander for expansion of the lean exhaust gas before being released into the surroundings via an expanded lean exhaust gas line, where a rich absorbent line is arranged for withdrawal of CO2 rich absorbent from the absorber and introduction of the absorbent into a regeneration column for separation of absorbed CO2 from the absorbent, where a CO2 line is arranged for withdrawal of CO2 and steam from the regeneration column, and the lean absorbent line is arranged for withdrawal of lean absorbent from the regeneration column and introduction thereof into the absorber, wherein a compressed air line is arranged for introduction of compressed air into the heat exchanger together with the lean exhaust gas introduced through the lean exhaust gas line.

[0012] According to one embodiment of the second aspect, the one or more air compressors for compression of air to the compressed air line are arranged on a common shaft together with the expander and the motor or combined motor and generator.

Short description of the figures

[0013]

Fig.1 is a principle sketch of an embodiment of the present invention.

Detailed description of the invention

[0014] A CO2 rich gas as used in the present description and claims, is a gas having a CO2 concentration being substantially higher than the CO2 concentration in air, i.e. a concentration substantially higher than 0.04 %, such as higher than 1%, 2%, 5%, or even higher than 10%. The CO2 rich gas, as used herein, is usually an exhaust gas from combustion of carbonaceous fuels, and more specifically fossil fuels. However, the present method may also be used for capturing CO2 from exhaust gas from combustion of non-fossil fuels, combination of fossil and non-fossil fuels, such as waste, or for CO2 capture from any industrial waste gas comprising CO2, and where the remaining waste gas may be released into the surroundings after CO2 capture.

[0015] A typical CO2 capture plant is shown in figure 1, where incoming CO2 rich gas, such as exhaust gas from combustion of carbonaceous material, such as a gas turbine, a coal fired plant power plant, an incarnation plant for waste, or an industrial exhaust gas, is introduced through an exhaust gas line 1, at about atmospheric pressure and typically at a temperature from 200 deg. C to 700 deg. C. The incoming gas in exhaust gas line 1 is introduced into a heat exchanger 2, where the gas is cooled against CO2 depleted gas as will be described further below, to a temperature from about 90 deg. C to 150 deg. C. The partly cooled exhaust gas excites the heat exchanger 2 through a gas line 3, is introduced into an exhaust gas cooler 4, where the gas is cooled to about 20 deg. C to 70 deg. C. The cooled exhaust gas is withdrawn through a cooled gas line 5 and led to serially connected compressors, here illustrated as three compressors, 6, 6’, 6’’, which are arranged on a common shaft 8. Intercoolers 7, 7’ are arranged between the compressors to cool the compressed gas before the next compressor step.

[0016] If the source for the incoming CO2 rich gas is a gas turbine, a fraction of the gas with drawn from the exhaust gas cooler 4 may be withdrawn from the gas line 5 in an optional withdrawal line 5’ and mixed with the air to be introduced into the gas turbine for combustion to reduce the oxygen concentration and increase the CO2 concentration in the exhaust gas.

[0017] The compressed exhaust gas leaving the serially connected compressors is led in a compressed exhaust gas line 9 and is introduced into an absorber 10 where the exhaust gas is brought in countercurrent flow against an aqueous potassium carbonate absorbent. The absorbent having absorbed CO2, “rich absorbent”, is collected at the bottom of the absorber column 10 and is withdrawn through a rich absorbent line 11.

[0018] The rich absorbent in line 11 is introduced into the upper part of a regeneration column 12, where the rich absorbent is brought into countercurrent flow to steam. CO2 is released from the absorbent by stripping with hot steam, and steam and CO2 is withdrawn through a CO2 line 15 for further treatment. The regenerated, or lean, absorbent is collected at the bottom of the regeneration column 12 in a lean absorbent line 16 and led to the upper part of the absorber 10 where the regenerated absorbent is introduced to absorb CO2. A part stream of the regenerated absorbent is withdrawn from the lean absorbent line 16 in a reboiler line 16’ and introduced into a reboiler 17 where the absorbent is boiled to produce steam. The steam produced in reboiler 17 is introduced into regeneration column 12 via a steam line 18.

[0019] The skilled person will understand that the CO2 capture part of the described plant, i.e. the absorber, the regeneration column, the connections between them and connected equipment is described without entering into specific details on optimalization to increase the energy efficiency of the CO2 capture / reduce the heat loss connected to CO2 absorption and desorption. The skilled person can identify several different solutions / measures and combination of measures possible to reduce heat loss.

[0020] CO2 lean exhaust gas, i.e. exhaust gas from which CO2 has been removed by absorption in absorber 10, is withdrawn from the absorber through a lean exhaust line 19 and introduced into the heat exchanger 2 where the lean exhaust gas is heated against the incoming CO2 rich exhaust gas introduced through line 1.

Additionally, compressed air at substantially the same pressure as the lean exhaust gas is introduced into the heat exchanger 2 from a compressed air line 27, to increase the total mass flow of gas to be heated therein. Air is taken in through an air intake 24, and compressed in a train of air compressors 25, 25’, 25’’. Preferably intercoolers 26, 26’ are arranged between the air compressors 25,25’, 25’’.

[0021] A heated gas flow, comprising lean exhaust gas and compressed air, is withdrawn from the heat exchanger 2 in a heated gas line 20 and is expanded to atmospheric pressure over an expander 21 before being released into the surroundings via an expanded lean exhaust gas line 23.

[0022] The compressors 6, 6’, 6’’, 25, 25’, 25’’, and the expander 21 are all preferably connected to a common shaft 8. Depending on the temperature at gas line 1 and heat loss in the present plant, the expander 21 might not be able to give the power needed to operate the compressors. A motor or combined motor and generator 22, is therefore connected to the shaft 8 to give the additional power needed, or to generate electrical power if the expander gives more power than needed by the compressors connected to the shaft.

[0023] According to the present invention, air is compressed and introduced into the heat exchanger 2 together with the lean exhaust to substitute the heat capacity flow lost in the lean exhaust gas due to the removal of CO2 from the exhaust gas in the absorber 10. By introducing a flow of air substantially equal in heat capacity of the captured CO2 a more efficient transfer of heat from the incoming exhaust gas in line 1 is transferred to the total volume of the compressed air and lean exhaust gas introduced into the heat exchanger 2 from lines 27, 19, respectfully. The power generated by the expander 21 depends on the temperature in line 1.The more of the heat energy that is transferred from the incoming exhaust gas in line 1 to the compressed lean exhaust gas and compressed air in heat exchanger 2, the more power is generated in expander 21 to reduce the necessary power input from the motor or combined motor and generator 22, and at higher temperatures more power is generated in the expander 21 than needed to operate the compressors 25, 25’, 25’’ and 6, 6’, 5’’ to make it possible to generate electrical power in the motor or combined motor and generator 22.

[0024] This way each extra kg/s of air filled in at line 24 can at 600 deg. C at line 1 add more than 150 kW of net mechanical work from the expander 21 and the compressors 25, 25’ and 25’’.

Claims

Patent claims

1. A method for removing CO2 from a CO2 rich gas, where the CO2 containing gas is cooled and compressed to a pressure of 5 to 30 bar and introduced into an absorber (10) where the CO2 rich gas is brought into countercurrent flow with an aqueous CO2 absorbent to give a CO2 lean gas flow and a CO2 rich absorbent which are removed from the absorber (10) from the top and the bottom of the absorber, respectively, where the CO2 lean gas is heated against the incoming CO2 containing gas in a heat exchanger (2) and thereafter expanded over an expander (21), characterized in that compressed air is introduced into heat exchanger (2) together with the CO2 lean gas, thereby mixing the compressed air with the CO2 lean gas in the heat exchanger.

2. The method of claim 1, wherein the incoming CO2 containing gas has a temperature of 200 to 700 deg. C.

3. A plant for removing CO2 from a CO2 rich gas, the plant comprising an exhaust gas line (1) for introduction of the CO2 rich gas into a heat exchanger (2) for cooling of the incoming CO2 rich gas, compressor(s) (6, 6’, 6’’) for compression of the CO2 rich gas cooled in the intercooler(s) (7, 7’, 7’’), a compressed exhaust gas line (9) for introduction of the compressed exhaust gas into an absorber (10) where the exhaust gas is brought in countercurrent flow against an aqueous CO2 absorbent, a lean absorbent line (16) for introduction of lean absorbent into the absorber (10), a lean exhaust gas line (19) for withdrawal of CO2 depleted, or lean, exhaust gas leaving and introduction thereof into the heat exchanger (2) to be heated against the incoming exhaust gas, a heated gas line (20) for leading the heated lean exhaust gas from the heat exchanger (2) to an expander (21) for expansion of the lean exhaust gas before being released into the surroundings via an expanded lean exhaust gas line (23), where a rich absorbent line (11) is arranged for withdrawal of CO2 rich absorbent from the absorber (10) and introduction of the absorbent into a regeneration column (12) for separation of absorbed CO2 from the absorbent, where a CO2 line (15) is arranged for withdrawal of CO2 and steam from the regeneration column (12), and the lean absorbent line (16) is arranged for withdrawal of lean absorbent from the regeneration column and introduction thereof into the absorber (10), characterized in that a compressed air line (27) is arranged for introduction of compressed air into the heat exchanger (2) together with the lean exhaust gas introduced through the lean exhaust gas line (19), thereby mixing the compressed air with the lean exhaust gas in the heat exchanger.

4. The plant according to claim 3, wherein one or more air compressors (25, 25’, 25’’) are arranged on a common shaft (8) together with the expander (21) and a motor or generator (22).

PATENTKRAV

1. En fremgangsmåte for fjerning av CO2 fra en CO2-rik gass, hvor den CO2-holdige gassen avkjøles og komprimeres til et trykk på 5 til 30 bar og føres inn i en absorber (10) hvor den CO2-rike gassen bringes i motstrøm med en vannholdig CO2-absorbent for å gi en CO2-mager gasstrøm og en CO2-rik absorbent som fjernes fra absorberen (10) fra henholdsvis toppen og bunnen av absorberen, hvor den CO2-magre gassen varmes opp mot den innkommende CO2-holdige gassen i en varmeveksler (2) og deretter ekspandert over en ekspander (21), karakterisert ved at komprimert luft føres inn i varmeveksleren (2) sammen med den CO2-magre gassen, for derved å blande den komprimerte luften med den CO2-magre gassen i varmeveksleren.

2. Fremgangsmåten ifølge krav 1, hvor den innkommende CO2-holdige gassen har en temperatur på 200 til 700 grader C.

3. Et anlegg for fjerning av CO2 fra en CO2-rik gass, anlegget omfattende en eksosgassledning (1) for innføring av den CO2-rike gassen inn i en varmeveksler (2) for kjøling av den innkommende CO2-rike gassen, kompressor(er) (6, 6', 6'') for komprimering av den CO2-rike gassen avkjølt i mellomkjøler(e) (7, 7', 7''), en komprimert eksosgassledning (9) for innføring av den komprimerte eksosgassen inn i en absorber (10) hvor eksosgassen føres i motstrøm mot en vannholdig CO2-absorbent, en mager absorbentledning (16) for innføring av mager absorbent i absorberen (10), en mager eksosgassledning (19) for uttak av CO2-utarmet, eller mager, eksosgass som går ut og innføring derav inn i varmeveksleren (2) for å varmes opp mot den innkommende eksosgassen, en oppvarmet gassledning (20) for å lede den oppvarmede magre eksosgassen fra varmeveksleren (2) til en ekspander (21) for ekspansjon av den magre eksosgassen før den slippes ut i omgivelsene via en ekspandert mager eksosgassledning (23), hvor en rik absorbentledning (11) er anordnet for uttak av CO2-rik absorbent fra absorberen (10) og innføring av absorbenten inn i en regenereringskolonne (12) for separering av absorbert CO2 fra absorbenten, hvor en CO2-ledning (15) er anordnet for uttak av CO2 og damp fra regenereringskolonnen (12), og den magre absorbentledningen (16) er anordnet for uttak av mager absorbent fra regenereringskolonnen og innføring derav inn i absorberen (10), karakterisert ved at en trykkluftledning (27) er anordnet for innføring av trykkluft inn i varmeveksleren (2) sammen med den magre eksosgassen innført gjennom den magre eksosgassledningen (19), for derved å blande den komprimerte luften med den magre eksosgassen i varmeveksleren.

4. Anlegget ifølge krav 3, hvor en eller flere luftkompressorer (25, 25', 25'') er anordnet på en felles aksel (8) sammen med ekspanderen (21) og en motor eller generator (22).

Drawings

Priority

No priority

Patent classes

IPC classes

B01D 53/00

B01D 53/18

B01D 53/34

B01D 53/40

B01D 53/62

B01D 53/77

B01D 53/78

B01D 53/96

B01D 3/00

B01D 3/38

F23J 15/00

F23J 15/04

F23J 15/06

CPC classes

B01D 53/00

B01D 53/18

B01D 53/34

B01D 53/40

B01D 53/62

B01D 53/77

B01D 53/78

B01D 53/96

B01D 3/00

B01D 3/38

F23J 15/00

F23J 15/04

F23J 15/06

Citations

US 2021/060478 A1 ( A1)

WO 2017/042163 A1 (A1)

US 2008/104938 A1 (A1)

Applicants, owners and inventors

Owners

CAPSOL TECHNOLOGIES ASA

Drammensveien 126A

0277 OSLO

NO (OSLO Municipality, Oslo county)

Org. number: 914620457

Inventors

Stellan Hamrin

Jägaråsvägen 82

73693 KUNGSÖR

Agent

BRYN AARFLOT AS

Stortingsgata 8

0161 OSLO

NO (OSLO Municipality, Oslo county)

Org. number: 979993269

Reference: P6691NO00-TK/MS

Status history

Payment history

Oppositions and appeals

No oppositions or appeals

Administrative limitation

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Liens and licences

Lien

NIPO's case number: 3053
Status: Anmerket i register
Agreement signed on: 04.05.2026
Notice received at NIPO: 03.06.2026
Agreement terminated: -
Info: Pantekravets størrelse er angitt til NOK 32 340 000. Melding om pant innkom Patentstyret 2026.06.03.
Propietor: CAPSOL TECHNOLOGIES ASA

CAPSOL TECHNOLOGIES ASA

Org. number: 914620457

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Drammensveien 126A

OSLO 0277

NO (OSLO Municipality, Oslo county)
Lienholder: DNB BANK ASA

DNB BANK ASA

Org. number: 984851006

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Postboks 1600 Sentrum

OSLO 0021

NO (OSLO Municipality, Oslo county)