Key information

Title
System for injecting flue gas to a subterranean formation
Application number
20150079
Case type
National
Status
03.11.2017 P.g.a. manglende svar. Søker har ikke begjært gjenopptakelse
Filed
17.01.2015
Effective date
17.01.2015
Publicly available
12.03.2015
Applicant
INTERNATIONAL ENERGY CONSORTIUM AS (NO)
Inventor
Gunnar Myhr (NO)
Agent
BRYN AARFLOT AS (NO)

Abstract and drawing

Disclaimer: This text has been machine-scanned and may contain errors – please refer to "Publications" for legally binding content.
A system (100) for injecting flue gas to a subterranean formation, wherein the system (100) is configured to receive an initial mixture of N2, C02 and less than 2% other components and comprises a compressor (110) for obtaining and maintaining a predetermined downhole pressure. The system (100) has a control system (200) for maintaining the amount of C02 in an injection mixture in the range 12-90% and can be configured for EOR.

Publications

Latest published versionA1

Documents

 Expand Download files (44)
Date
 Date Doc. No. Process Case number In/Out Journal description To/from
 26.03.2018 21-01 Saksbehandling 20150079 UT Endelig Henleggelse BRYN AARFLOT AS
 15.11.2017 20-01 Saksbehandling 20150079 UT Henlagt manglede svar Bryn Aarflot AS
 03.07.2017 19-02 Saksbehandling 20150079 UT PT report 10:09:42
03.07.2017 19-01 Saksbehandling 20150079 UT Realitet patent Bryn Aarflot AS
 07.04.2017 18-04 Saksbehandling 20150079 INN Hovedbrev Bryn Aarflot AS
 07.04.2017 18-03 Saksbehandling 20150079 INN Krav Bryn Aarflot AS
 07.04.2017 18-02 Saksbehandling 20150079 INN Krav Bryn Aarflot AS
 07.04.2017 18-01 Saksbehandling 20150079 INN Korrespondanse (Hovedbrev inn) Bryn Aarflot AS
 03.03.2017 17-01 Saksbehandling 20150079 UT Realitet patent Bryn Aarflot AS
 08.12.2016 16-03 Saksbehandling 20150079 INN Krav Bryn Aarflot AS
 08.12.2016 16-02 Saksbehandling 20150079 INN Hovedbrev Bryn Aarflot AS
 08.12.2016 16-01 Saksbehandling 20150079 INN Korrespondanse (Hovedbrev inn) Bryn Aarflot AS
 08.12.2016 02-01 Endring av fullmektig 2016/12538 UT GH Forespørsel Bryn Aarflot AS
 05.12.2016 01-02 Endring av fullmektig 2016/12538 INN Fullmakt Bryn Aarflot AS
 05.12.2016 01-01 Endring av fullmektig 2016/12538 INN Generell henvendelse Bryn Aarflot AS
 14.11.2016 15-01 Saksbehandling 20150079 UT PT Batch Varsel om betaling av første årsavgift (3317)
26.10.2016 14-02 Saksbehandling 20150079 UT PT report 02:56:02
26.10.2016 14-01 Saksbehandling 20150079 UT Realitet patent Aidi - BK Mølmann
 12.10.2016 13-01 Saksbehandling 20150079 INN Korrespondanse (Hovedbrev inn) INTERNATIONAL ENERGY CONSORTIUM AS
 26.09.2016 12-02 Saksbehandling 20150079 INN Hovedbrev Aidi - BK Mølmann
 26.09.2016 12-01 Saksbehandling 20150079 INN Korrespondanse (Hovedbrev inn) Aidi - BK Mølmann
 07.06.2016 11-01 Saksbehandling 20150079 UT Henlagt manglede svar Aidi - BK Mølmann
 26.02.2016 10-01 Saksbehandling 20150079 UT Realitet patent Aidi - BK Mølmann
 04.12.2015 09-04 Saksbehandling 20150079 INN Krav merket Aidi - BK Mølmann
 04.12.2015 09-03 Saksbehandling 20150079 INN Krav ren Aidi - BK Mølmann
 04.12.2015 09-02 Saksbehandling 20150079 INN Hovedbrev Aidi - BK Mølmann
 04.12.2015 09-01 Saksbehandling 20150079 INN Korrespondanse (Hovedbrev inn) Aidi - BK Mølmann
 03.07.2015 08-02 Saksbehandling 20150079 UT PT report 01:30:09
03.07.2015 08-01 Saksbehandling 20150079 UT Realitet patent Aidi - BK Mølmann
 18.03.2015 07-01 Saksbehandling 20150079 UT Generelt Brev Patent Aidi - BK Mølmann
 12.03.2015 05-04 Saksbehandling 20150079 INN Erklæring Søkers rett til oppfinnelse Aidi - BK Mølmann
 12.03.2015 05-03 Saksbehandling 20150079 INN Hovedbrev Aidi - BK Mølmann
 12.03.2015 05-02 Saksbehandling 20150079 INN Fullmakt Aidi - BK Mølmann
 12.03.2015 05-01 Saksbehandling 20150079 INN Korrespondanse (Hovedbrev inn) Aidi - BK Mølmann
 23.01.2015 04-01 Saksbehandling 20150079 UT Formalia 1 Aidi - BK Mølmann
 22.01.2015 03-02 Saksbehandling 20150079 INN Sammendrag Engelsk Aidi - BK Mølmann
 22.01.2015 03-01 Saksbehandling 20150079 INN Korrespondanse (Hovedbrev inn) Aidi - BK Mølmann
 22.01.2015 02-01 Saksbehandling 20150079 UT Infobrev til oppfinner Aidi - BK Mølmann
 17.01.2015 01-06 Saksbehandling 20150079 INN Beskrivelse
17.01.2015 01-05 Saksbehandling 20150079 INN Krav
17.01.2015 01-04 Saksbehandling 20150079 INN Sammendrag
17.01.2015 01-03 Saksbehandling 20150079 INN drawings
17.01.2015 01-02 Saksbehandling 20150079 INN Hovedbrev
17.01.2015 01-01 Saksbehandling 20150079 INN Søknadsskjema Patent

Description, claims and drawings

Disclaimer: This text has been machine-scanned and may contain errors – please refer to "Publications" for legally binding content. Description
[01] The present invention concerns a system for injecting flue gas to a subterranean formation.[02] In the following description and claims, a subterranean formation is any geological formation that can be used for storing N2 and CO2. Examples include aquifers and reservoirs. Here, a reservoir means a layer of porous rock, e.g. sandstone, limestone or shale, contain hydrocarbons, i.e. oil and/or natural gas.[03] An oilfield comprises one or more production wells, and may be located onshore or offshore. Each production well has a riser for conveying oil from a reservoir to a rig or platform on the surface. In some instances, the pressure in the reservoir is sufficient to force hydrocarbons, including oil, to the surface. However, it may be necessary or desired to inject a fluid into the reservoir in order to maintain or increase the pressure in the reservoir, and thereby increase the amount of hydrocarbons produced from the reservoir. The fluid, i.e. liquid or gas, is injected into the reservoir through one or more injection wells on the oil field. The injection wells are similar to the production wells. Indeed, a former production well may serve as injection well at a later time in order to force oil or gas toward new production wells.[04] The process of injecting a fluid to increase production of hydrocarbons, i.e. from a field is known as enhanced oil recovery (EOR). Both production of hydrocarbons and EOR may involve phase transitions. For example, methane (CH4) is gaseous at standard conditions 1 bar and 298 K, but may be liquid in a subterranean formation or solid under other conditions. The phase transitions also depend on the fluid composition. For example, methane may form methane clathrate or 'hydrate' in the presence of water. Phase transitions and their associated phase diagrams are further discussed below.[05] As used herein, flue gas is the gas produced by any combustion process, e.g. a fireplace, an oven, a power plant or a steam generator. A typical flue gas from a standard combustion in air at atmospheric pressure may contain, for example, 70 - 75 % N2, 10 -15 % O2, 5 -10 % CO2, and a small percentage of other components. All percentages here and in the following are by mole. The other components in the flue gas depend mainly on the fuel and may include soot, CO, nitrogen oxides, sulphur oxides, noble gases etc. Fuel gas from industrial combustion, e.g. a power plant, is often treated to remove sulphur, nitrogen oxides(NOx), etc. These processes are known as 'scrubbing', and are not described in detail herein. Rather, it is assumed that an input gas may comprises a mixture of mainly N2, O2 and CO2 and less than 2% other components.[06] Of these, CO2 is of particular interest because it contributes to the greenhouse effect. Several techniques have been proposed for so-called carbon capture and storage (CCS), including long time storage in aquifers or depleted hydrocarbon reservoirs. As the pressure and temperature at the reservoir differ significantly from standard conditions, i.e. 1 bar and 298 K, some or all components in a mixture may change phase during compression and injection. Moreover, interaction between the components may cause the phase diagrams different for different concentrations of the constituents. For example, some applications use pure CO2, which has a well known phase diagram and which is most likely liquid at the pressures and temperatures of a reservoir. Due to low compressibility at these conditions, pure CO2 may be well suited for EOR applications. Moreover, the phase diagram can be used to avoid undesired clogging, i.e. a phase transition to solid state in pumps, pipes etc, during purification and compression. A major disadvantage of using pure CO2 is the cost associated with purification.[07] Mixtures of CO2 and other gases have less defined properties, in general because interactions between constituents cause the mix to behave differently than each single component. That is, each mixture has a phase diagram that depends on the components and their relative concentrations. A disadvantage of such systems is that different compositions of similar constituents may have different phases at identical pressure and temperature. Thus, the composition of the mixture must be controlled in addition to pressure and temperature. Some systems are relatively well studied. There is no guarantee that all possible fractions of CO2 in a mixture behave in the same manner. In addition, a particular mixture suitable for deposit in an aquifer may not be suited for EOR.[08] As an alternative to CCS methods using amines or other methods for extracting CO2, a mixture of CO2 and other gases can be stored after far less extensive treatment. The flue gas with mainly N2, O2 and 5-10% CO2 mentioned above is an example of a gas that may be deposited, e.g. in an aquifer. To avoid corrosion, bacterial growth etc, it may be desirable to reduce the amount of O2. This may also increase efficacy. For example, by manipulating a combined cycle or two step combustion process, where the flue gas from e.g. the gas turbine is used in a closed loop in subsequent combustion processes, it is possible to obtain O2 levels «1 %. By utilizing high pressure in the HRSG or boiler unit and fuel with gas (e.g. pure CH4), O2 levels could become at the ppm level. In this way the fume gas may comprise approximately 87 % N2, 12 % CO2 and small amounts of other components. Such methods are provided in, for example, W099/64719 and NO 332044.[09] Phase diagrams for N2 -CO2 mixtures with over 90 mole% CO2 are known from Goos et al., "Phase diagrams of CO2 and CO2 - N2 gas mixtures and their application in compression processes", Energy Procedia 4 (2011) 3778-3785, presented at the IO* International Conference on Greenhouse Gas Control Technology (GHGT-10), and available online since 1. April 2011. However, obtaining high concentrations of CO2 tends to impose costs, e.g. for membranes or other equipment to remove N2 and/or time for achieving the desired result with lower process capacity.[010] The objective of the present invention is to provide a system solving at least one of the problems above while retaining the benefits of prior art.[011] This is achieved by a system according to claim 1.[012] More particularly, the above objective is achieved by a system for injecting flue gas to a subterranean formation, wherein the system is configured to receive an initial mixture of N2, CO2 and less than 2% other components and comprises a compressor for obtaining and maintaining a predetermined downhole pressure. The system is distinguished by a control system for maintaining the amount of CO2 in an injection mixture in the range 12-90%.[013] The initial mixture is output from systems and processes briefly discussed in the introduction, i.e. a mixture comprising less than 2% oxygen and other components. It has been found, surprisingly, that mixtures of N2 and CO2 with as little as 12% CO2, are comparable to water for maintaining the pressure in a reservoir, and that mixtures with 20% or more CO2 are practically indistinguishable from water in this respect. As a larger amount of N2 may remain in the output gas, i.e. the gas to be injected, the costs associated with removing N2 are decreased. These results are also useful for injection into other subterranean formations, notably aquifers.[014] Preferably, the amount of CO2 in the injection mixture is maintained in the range 20-90%. In this range, the properties of the mixture is nearly indistinguishable from water as pressure support for typical reservoir pressures.[015] In a preferred embodiment, the compressor and injection mixture are configured for enhanced oil recovery.[016] The control system may comprise a membrane for reducing the amount of N2. As the N2 exits into the ambient air, the concentration of CO2 in the injection mixture increases.[017] In addition or alternatively, the control system may comprise a mixer for adding CO2 to the initial mixture.[018] Additional features and benefits appear from the detailed description and accompanying claims.[019] The invention will be described in greater detail by means of exemplary embodiments and reference to the accompanying drawings, in which: Figure 1 illustrates a system according to the invention;[020] Figure 1 is a schematic illustration of a system 100 according to the invention. As indicated in the introduction, a flue gas from any combustion can be treated to provide a suitable gas mixture for the present invention. At the system boundary 1, a treated flue gas containing N2, < 12% CO2 and < 2% other components is assumed. For example, a combined cycle may be present upstream on a main feed 101 as described. Similarly, an afterburner or other device (not shown) to reduce the O2 content may be present upstream on a supply line 120 for adding CO2 from an external source. Downstream from the system boundary 2, i.e. to the right in figure 1, a pipeline conveys a compressed injection mixture to a subterranean formation.[021] The system 100 comprises a control system 200 for controlling the composition of the injecting mixture, which is compressed to a desired pressure by a compressor 110. The system 100 may comprise other parts, e.g. an intercooler 120. The intercooler 120 is a commercially available, standard system component in many compression systems.[022] The control system 200 comprises a membrane 210 for separating N2 and a mixer 220, e.g. a controllable valve. A sensor 230 is shown downstream frm the membrane 210 and mixer 220 to illustrate a feedback loop. The sensor 230 may alternatively be disposed upstream to implement a feed forward loop. Either way, a controller 240 receives input from the sensor 230 and provides a response to an actuator, in fig. 1 represented by the mixer 220. The controller 240 comprise hardware and software to execute a cybernetic algorithm, e.g. a feedback or feed forward algorithm. The controller and algorithms are known to one skilled in the art.[023] In the following, we use measured values from a combined cycle as a numerical example. In particular, the initial flue gas from a typical gas turbine contains 5 % CO2, 74 % N2, 15.5 % O2 and 5.5 % other components. This O2 content is too high for EOR applications. A secondary step involving a steam generator and a steam turbine provides a reference flue gas containing 11.4 % C02, 86.9 % N2, 1 % Ar, 0.6 % 02 and 0.03 % H20.[024] This mixture can be passed through a commercially available filter in order to reduce the content of N2. A numerical example is provided in table 1, which is computed from the mixture above using an Aspen Process Simulation System, provided by Air Products Ltd.[025] The row 'Released' contain fractions released to the atmosphere, and the row'Deposited' contains the components that do not pass the membrane, and thus are eligible for injection. Disregarding the fractions released to the atmosphere and noting that the fraction in the 'Deposited' row add to about 50%, it is readily seen that the 'Deposit' fraction or injection mixture contains about 72.6% N2, 3.4% 02, 21.5% C02 and 2.5% Ar. The value provided for Ar should be interpreted as the fraction of 'other components', e.g. NOx.[026] An alternative to membrane filtering is to add CO2 from some external source to achieve a fraction of CO2 above 12%, preferably above 20%, in the injection mixture.[027] Several alternatives for EOR using flue gas as injection fluid have been compared to a base line using water as injection fluid. More particularly, The Eclipse 300 2013.2 software was used for EOR simulations and the Eclipse PVTi 2013 package was applied for the associated PVT models. First, the baseline was established using 5000 m3 at 58 kg/s water injection. Next, flue gas injections was simulated using different gas mixtures and alternating gas injection with water injection. The 'other components' were treated as N2 in the simulations.[028] The following assumptions, corresponding to sandstone, were made for the reservoir:Netto-gross: 0.56 to 0.76 (net formation thickness contributing to oil and gas production/gross thickness of formation)[029] Figure 2 illustrates the oil recovery rate or efficiency as a function of time (15 years). The baseline 10 was obtained using water at a flow rate of 58 kg/s. The efficiency after 15 years is 28 %. The curve 20 represents an alternative using flue gas directly, and was obtained using the reference flue gas containing 11.4% CO2 at a flow rate of 40 kg/s. The efficiency after 15 years is 20.5 %. Curve 22 was obtained using the reference flue gas, i.e. as for curve 20, but at an increased flow rate of 80 kg/s. This case is actually better up to year 2, but then a breakthrough from injection well to production well caused a large area with poor sweeping effects between the wells, so that gas injection became circulation.[030] Figure 3 illustrates the oil recovery rate or efficiency as a function of time (15 years, commencing in 2015), i.e. as in figure 2. The baseline 10 represents water injection at 58 kg/s as in figure 2. Curve 30 represents a preferred alternative, i.e. a flue gas with increased CO2 content, and was obtained using the injection mixture with 21.5% CO2 specified above at a mass flow rate 17 kg/s. Up to year 11 (2028), the oil recovery rate is identical. The efficiency after 15 years is approximately 27 %.[031] From figure 3, it appears that an injection mixture of N2 and CO2, where the CO2 fraction is above 20 mole%, has the same EOR effects as water injection, even with flow rates at 1/3 of the water injection rate.[032] The above results are generally due to the properties of N2-CO2 mixtures in the range 12% to 90%, in particular to the PVT-properties or phase diagrams. Thus, they may be applicable in other compression applications, e.g. depositing CO2 in aquifers or other subterranean formations.
Claims
1. System (100) for injecting flue gas to a subterranean formation, wherein the system (100) is configured to receive an initial mixture of N2, CO2 and less than 2% other components, comprises a compressor (110) for obtaining and maintaining a predetermined downhole pressure and is characterised bya control system (200) for maintaining the amount of CO2 in an injection mixture in the range 12-90%.2. System (100) according to claim 1, wherein the amount of CO2 in the injection mixture is maintained in the range 20-90%.3. System (100) according to claim 1 or 2, wherein the compressor (110) and injection mixture are configured for enhanced oil recovery.4. System (100) according to any preceding claim, wherein the control system (200) comprises a membrane (210) for reducing the amount of N2.5. System (100) according to any preceding claim, wherein the control system comprises a mixer (220) for adding CO2 to the initial mixture.
Drawings

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Patent classes

IPC classesE21B 43/16

Citations

WO 2013/036132 A2 (A2)WO 2007/090275 A1 (A1)SHOKOYA et al. Effect of CO2 Concentration on Oil Recovery in Enriched Flue Gas Flood. The Petroleum Society´s 6th Canadian International Petroleum Conference, Calgary, Alberta, Canada, 7-9 Juni, 2005. PAPER 2005-246. ()SHOKOYA et al. Effect of Oil and Flue-Gas Compositions on Oil Recovery in th Flue-Gas/Light-Oil Injection Process. The 2005 SPE (Society of Petroleum Engineers) Annual Technical Conference and Exhibition held in Dallas, Texas, USA, 9-12 Oktober 2005. SPE 97262. ()GODWIN et al. A Small Independent Producer´s Design, Construction and Operation of a Flue Gas Injection Project, East Edna Field, Okmulgee County, Oklahoma. The 1998 SPE/DOE Eleventh Symposium on Improved Oil Recovery held in Tulsa, Oklahoma, USA, 19-22 April 1998. SPE 39637. ()WO 99/64719 A2 (A2)RADOSZ et al. Flue-Gas Carbon Capture on Carbonaceous Sorbents: Toward a Low-Cost Multifunctional Carbon Filter for «Green» Energy Producers. Soft Materials Laboratory, Department of Chemical and Petroleum Engineering, University of Wyoming, Laramie, Wyoming 82071. American Chemical Society, 10.1021/ie0707974, publisert på internett 2008.04.29. ()Kazama, S. CO2 Separation With Molecular Gate Membrane. GCEP Energy Workshops At Stanford University April 27, 2004.[Hentet 2017.06.16 fra internett].(https://gcep.stanford.edu/pdfs/ energy_workshops_04_04/carbon_kazama.pdf) ()"Air Products PRISM PA nitrogen membrane separators" datablad, copyright 2013. Air Products and Chemicals, Inc. [Hentet 2017.06.16 fra internett].(http://www.airproducts.com/~/media/ downloads/data-sheets/P/ prism-pa-nitrogen-membrane-separators.pdf?la=en) ()GOOS et al. Phase diagrams of CO2 and CO2-N2 gas mixtures and their application in compression processes. 10th International Conference on Greenhouse Gas Control Technologies (GHGT-10) 19-23.september 2010, RAI, Amsterdam, Nederland. Tilgjengelig på internett siden 1.april 2011 i Energy Procedia 4 (2011) 3778–3785 at http://dx.doi.org/10.1016/j.egypro.2011.02.312 doi:10.1016/j.egypro.2011.02.312. ()

Applicants, owners and inventors

Applicants
INTERNATIONAL ENERGY CONSORTIUM AS
Thorleif Haugs vei 5 0791 OSLO NO (OSLO Municipality, Oslo county)Org. number: 912678296Inventors
Gunnar Myhr
Putten 50 1676 KRÅKERØY NO (FREDRIKSTAD Municipality, Østfold county)

Agent

BRYN AARFLOT AS
BRYN AARFLOT AS

Org. number: 979993269

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Stortingsgata 8 0161 OSLO NO (OSLO Municipality, Oslo county)
Org. number: 979993269
Reference: 127621/LAH

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