WO2024094969A1 - Extraction d'huile - Google Patents

Extraction d'huile Download PDF

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Publication number
WO2024094969A1
WO2024094969A1 PCT/GB2023/052810 GB2023052810W WO2024094969A1 WO 2024094969 A1 WO2024094969 A1 WO 2024094969A1 GB 2023052810 W GB2023052810 W GB 2023052810W WO 2024094969 A1 WO2024094969 A1 WO 2024094969A1
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WO
WIPO (PCT)
Prior art keywords
gas
ppm
carbon dioxide
liquid
degassing
Prior art date
Application number
PCT/GB2023/052810
Other languages
English (en)
Inventor
Thomas John Mckechnie
David GLEESON
Original Assignee
Gigaton Co2 Ltd
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
Priority claimed from GBGB2216114.5A external-priority patent/GB202216114D0/en
Application filed by Gigaton Co2 Ltd filed Critical Gigaton Co2 Ltd
Publication of WO2024094969A1 publication Critical patent/WO2024094969A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0005—Degasification of liquids with one or more auxiliary substances
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/0036—Flash degasification
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1412—Controlling the absorption process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1431—Pretreatment by other processes
    • B01D53/1443—Pretreatment by diffusion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
    • E21B43/164—Injecting CO2 or carbonated water
    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/34—Arrangements for separating materials produced by the well
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/01—Engine exhaust gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/06—Polluted air
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1462—Removing mixtures of hydrogen sulfide and carbon dioxide

Definitions

  • the present invention relates to the extraction of oil from a reservoir.
  • the invention relates to an apparatus and a method for producing carbon dioxide which may be used in an oil extraction process.
  • oil may be extracted using a variety of techniques.
  • the initial, primary recovery stage uses natural mechanisms to move the oil within the reservoir to a lower part thereof where the wells are located.
  • the mechanisms include natural water displacing oil, expansion of the associated petroleum gas at the top of the reservoir, expansion of the associated gas initially dissolved in the crude oil and gravity drainage.
  • the pressure due to these mechanisms will drive the oil to the surface.
  • 5 to 15% of the oil in a well is extracted in the primary recovery stage.
  • the natural pressure within the reservoir will fall as the oil is extracted.
  • Secondary recovery methods may be used. These rely on supplying external energy to the reservoir by injecting fluids to increase reservoir pressure. Secondary recovery techniques increase the reservoir's pressure by water injection, gas reinjection and gas lift. Gas reinjection and lift each use associated gas, carbon dioxide or some other inert gas to reduce the density of the oil-gas mixture, and thus improve its mobility.
  • the typical recovery factor from water-flood operations is about 30%, depending on the properties of the oil and the characteristics of the reservoir rock. On average, the recovery factor after primary and secondary oil recovery operations is between 35 and 45%.
  • EOR Enhanced oil recovery
  • tertiary recovery is the extraction of crude oil from an oil field that cannot be extracted otherwise.
  • EOR can enable the extraction of up to 60% or more of a reservoir's oil.
  • Many EOR methods require carbon dioxide gas to be injected into the reservoir.
  • an apparatus for oil extraction comprising: a degasser, comprising a degassing chamber, a liquid inlet configured to feed an input liquid comprising carbon dioxide, and/or a precursor thereof dissolved therein into the degassing chamber, and a liquid outlet, configured to remove an output liquid from the degassing chamber, wherein the degasser is configured to degas a liquid in the degassing chamber to obtain an output gas comprising carbon dioxide, and the degasser further comprises a gas outlet to remove the output gas from the degassing chamber; and transportation means, or a transporter, configured to transport at least a portion of the output gas to an oil reservoir.
  • the apparatus can generate carbon dioxide in situ which can then be used to extract oil.
  • the apparatus maybe used in an enhanced oil recovery (EOR) method.
  • EOR enhanced oil recovery
  • the apparatus could be used offshore to enable EOR methods to be used with offshore oil reservoirs.
  • the apparatus could be used with onshore oil reservoirs.
  • the apparatus enables C0 2 to be removed from the environment near a particular well, or cluster of wells. Accordingly, not only does this enable C0 2 to be removed from the environment but that C0 2 could be used for EOR thus extending field life, generating more income and helping to mitigate the climate crisis. It is estimated that there are in the region of approximately 24 billion EOR barrels of oil in the North Sea and around 284 billion in the US which gives a lot of potential for the use of the apparatus of the first aspect. Additionally, the carbon dioxide which is generated is taken out of the environment. It maybe appreciated that the apparatus would generate an output liquid having a lower concentration carbon dioxide and/ or the precursor thereof to the input liquid.
  • the output liquid may subsequently be allowed to equilibrate with air, which could cause carbon dioxide from the air to dissolve into the output liquid. Accordingly, the apparatus may thereby have the effect of removing carbon dioxide from the atmosphere.
  • the oil reservoir maybe understood to be an active oil reservoir, i.e. an oil reservoir which is still producing oil.
  • the output gas may comprise a concentration of carbon dioxide of at least 750 ppm, at least 1,000 ppm, at least 5,000 ppm, at least 10,000 ppm, at least 20,000 ppm, at least 30,000 ppm, at least 40,000 ppm or at least 45,000 ppm.
  • the output gas may comprise a concentration of carbon dioxide of at least 50,000 ppm, at least 75,000 ppm, at least 100,000 ppm, at least 200,000 ppm, at least 300,000 ppm, at least 400,000 ppm, at least 500,000 ppm, at least 600,000 ppm, at least 700,000 ppm, at least 800,000 ppm, at least 900,000 ppm, or 1,000,000 ppm.
  • the input liquid preferably comprises water. Accordingly, the input liquid may be understood to be a water based medium comprising carbon dioxide, and/ or a precursor thereof.
  • the input liquid may be or comprise any suitable water based medium.
  • the input liquid may be or comprise fresh water, seawater, produced water, brackish water, wastewater, rainwater, sewerage water, deionized water and/ or water containing brine.
  • the water containing brine may be a brine waste stream from a desalination plant.
  • the input liquid may be or comprise produced water. It may be appreciated that produced water is water that comes out of an oil well with crude oil during crude oil production. Produced water may be combined with any other suitable water based medium. It is noted that produced water can contain a high concentration of carbonates, and so an input liquid comprising produced water would advantageously be able to provide an output gas with a significant concentration of carbon dioxide.
  • the apparatus may be configured to contact the input liquid with a gas with a high concentration of carbon dioxide prior to degassing the input liquid.
  • the apparatus may comprise a contacting chamber configured to contact the input liquid and the gas with a high concentration of carbon dioxide.
  • the contacting chamber may be disposed upstream of the degassing chamber.
  • the contacting chamber may be configured to bubble the gas with the high concentration of carbon dioxide through the input liquid. This would be advantageous where the gas with the high concentration of carbon dioxide may comprise an impurity.
  • the method may advantageously produce an output gas, with a high concentration of carbon dioxide, which does not contain the impurity.
  • the contacting chamber may comprise a liquid inlet, configured to feed the input liquid into the contacting chamber.
  • the contacting chamber may comprise a gas inlet configured to feed the gas with a high concentration of carbon dioxide into the contacting chamber.
  • the contacting chamber may comprise a gas outlet configured to remove a gas from the contacting chamber.
  • the contacting chamber may be configured to contact the input liquid and the gas with a high concentration of carbon dioxide at an increased pressure. The increased pressure may be as defined below.
  • the contacting chamber may comprise a contacting conduit.
  • the contacting conduit may define one or more high points therein.
  • the gas outlet may be disposed at the high point in the contacting conduit.
  • a gas outlet may be disposed at each high point.
  • the gas outlet is disposed downstream of the gas inlet.
  • the gas outlet is disposed upstream of the degasser.
  • downstream and upstream may be understood to refer to downstream and upstream relative to the direction that the input liquid is designed to flow.
  • the apparatus may comprise one or more valves on the contacting conduit.
  • the one or more valves may be a one-way valve, a flow control valve, an isolation valve, adjustable pressure relief valve and/ or combinations thereof.
  • the contacting conduit may be configured to feed the input liquid directly to the degasser, preferably directly to the liquid inlet in the degasser.
  • the contacting chamber may comprise a separation tank.
  • the separation tank may be disposed downstream of the contacting conduit.
  • the separation tank may be configured to separate the input liquid and undissolved gas.
  • the separation tank may comprise the gas outlet configured to remove undissolved gas from the contacting chamber.
  • the separation tank may comprise an emergency vent configured to vent a gas in the separation tank if a pressure in the separation tank exceeds a predetermined pressure.
  • the emergency vent may comprise a relief valve.
  • the apparatus may comprise an input liquid conduit extending between the separation tank and the degasser, and configured to transport the input liquid from the separation tank to the degasser.
  • the apparatus may comprise one or more valves on the input liquid conduit.
  • the one or more valves may be a one-way valve, a flow control valve, an isolation valve, adjustable pressure relief valve and/or combinations thereof.
  • the contacting chamber may be configured to contact the input liquid and the gas with a high concentration of carbon dioxide at approximately atmospheric pressure.
  • it may be desirable to contacting the input liquid and the gas with a high concentration of carbon dioxide at approximately atmospheric pressure when there is a high volume of the gas with a high concentration of carbon dioxide and/ or in embodiments where the gas with a high concentration of carbon dioxide comprises less than 400,000 ppm, less than 350,000 ppm, less than 300,000 ppm, less than 250,000 ppm, 200,000 ppm, less than 150,000 ppm, less than 100,000 ppm, less than 75,000 ppm or less than 5o,oooppm.
  • the contacting chamber may be configured to contact the input liquid and the gas with a high concentration of carbon dioxide at approximately atmospheric pressure when the gas with a high concentration of carbon dioxide is a flue and/or exhaust gas.
  • the apparatus may be understood to be configured to contact the input liquid and gas at approximately atmospheric pressure if it is conducted at a pressure between 50 and 500 kPa, between 60 and 250 kPa, between 70 and 150 kPa, between 80 and 120 kPa, between 90 and 110 kPa or between 95 and 105 kPa.
  • the contacting chamber may be configured to contact the input liquid and the gas with a high concentration of carbon dioxide at an increased pressure.
  • the increased pressure maybe a pressure of greater than 101 kPa, more preferably at least 200 kPa, at least 400 kPa, at least 600 kPa, at least 800 kPa or at least 1 MPa.
  • the increased pressure may be a pressure of greater than 2 MPa, greater than 4 MPa, greater than 6 MPa, greater than 8 MPa, greater than 10 MPa, greater than 25 MPa, greater than 50 MPa, greater than 75 MPa, greater than 100 MPa or greater than 125 MPa. It may be appreciated that increasing the pressure will increase the amount of carbon dioxide which is absorbed into the input liquid.
  • the gas with a high concentration of carbon dioxide maybe a flue and/or exhaust gas.
  • the flue and/ or exhaust gas may be from burning a carbon containing fuel and/ or from an industrial plant.
  • the industrial plant may be a chemical plant, a refining plant, a desalinating plant, a cement plant, a steel plant and/or other metal smelting plant (e.g. a lead or copper smelting plant) and/or an anaerobic biogas plant.
  • the exhaust gas from burning a carbon containing fuel may be from a power station, an internal combustion engine and/ or an open flame.
  • the gas with a high concentration of carbon dioxide may comprise a concentration of carbon dioxide of at least 500 ppm, at least 1,000 ppm, at least 5,000 ppm, at least 10,000 ppm, at least 20,000 ppm, at least 30,000 ppm, at least 40,000 ppm or at least 50,000 ppm, at least 75,000 ppm, at least 100,000 ppm, at least 125,000 ppm, at least
  • 150,000 ppm 150,000 ppm, at least 175,000 ppm, at least 200,000 ppm, at least 300,000 ppm, at least 400,000 ppm, at least 500,000 ppm, at least 600,000 ppm, at least 700,000 ppm, at least 800,000 ppm or at least 900,000 ppm.
  • the gas with a high concentration of carbon dioxide may comprise a concentration of carbon dioxide of between 100 and 950,000 ppm, between 500 and 800,000 ppm, between 1,000 and 700,000 ppm, between 5,000 and 600,000 ppm, between 20,000 and 500,000 ppm, between 50,000 and 400,000 ppm, between 100,000 and 300,000 ppm, between 125,000 and 250,000 ppm or between 150,000 and 200,000 ppm.
  • an exhaust gas from a gas fired power station has a concentration of carbon dioxide of about 30,000 to 50,000 ppm
  • an exhaust gas from a diesel engine has a concentration of carbon dioxide of about 120,000 ppm
  • an exhaust gas from a coal fired power station has a concentration of carbon dioxide of about 150,000 ppm
  • an exhaust gas from a cement or steel plant has a concentration of carbon dioxide of about 300,000 to 350,000 ppm.
  • the apparatus a plurality of degassing chambers.
  • Each degassing chamber maybe arranged in series or in parallel.
  • the apparatus may be configured to feed the output gas from the gas outlet in a first degassing chamber to a gas inlet in a contacting chamber.
  • the contacting chamber may be as defined above.
  • the apparatus may be configured to feed the input liquid from the contacting chamber into a subsequent degassing chamber. Accordingly, the concentration of carbon dioxide in the output gas may increase with each subsequent degassing chamber.
  • the apparatus may comprise: a first degasser, comprising a degassing chamber, a liquid inlet configured to feed a first input liquid comprising carbon dioxide, and/or a precursor thereof dissolved therein into the degassing chamber, and a liquid outlet, configured to remove a first output liquid from the degassing chamber, wherein the degasser is configured to degas a liquid in the degassing chamber to obtain a first output gas comprising carbon dioxide, and the degasser further comprises a gas outlet to remove the first output gas from the degassing chamber; a contacting chamber configured to contact a second input liquid and the first output gas therein, wherein the contacting chamber comprises a liquid inlet, configured to feed the second input liquid into the contacting chamber, a gas inlet configured to feed the first output gas into the contacting chamber, a gas outlet configured to remove a gas from the contacting chamber; a second degasser, comprising a degassing chamber, a liquid inlet configured to feed the second input
  • the apparatus could comprise further contacting chambers and/or degassers arranged in series.
  • the apparatus is disposed, or configured to be disposed, in a body of water.
  • the degassing chamber may be disposed, or configured to be disposed, submerged or partially submerged in the body of water.
  • the degassing chamber may be disposed, or configured to be disposed, such that the liquid inlet is disposed below the surface of the body of water.
  • the degassing chamber may be disposed, or configured to be disposed, such that the liquid outlet is disposed above, below or substantially adjacent to the surface of the body of water.
  • the body of water may be a pond, lake, reservoir, sea, ocean or any other suitable body of water.
  • the apparatus may comprise a structure configured to support the apparatus in the body of water, such as a floating platform, and/or configured to anchor the apparatus in a specific location.
  • the apparatus may be disposed or configured to be disposed on or adjacent to the seabed.
  • the apparatus may comprise an anchor configured to anchor the apparatus to the seabed.
  • the apparatus may be configured to be attached to a structure in a body of water, such as an oil or gas structure. The input liquid may be taken directly from the body of water.
  • the carbon dioxide, and/ or the precursor thereof, may be present intrinsically in the input liquid.
  • a precursor of carbon dioxide may be a carbonate, a bicarbonate and/or carbonic acid.
  • the carbonate could be sodium carbonate and the bicarbonate could be sodium bicarbonate.
  • the concentration of carbon dioxide and/ or precursors thereof in the input liquid may be at least 1 pmol/kg, at least 10 pmol/kg, at least 50 pmol/kg, at least too pmol/kg, at least 500 pmol/kg, at least 1 mmol/kg or at least 1.5 mmol/kg.
  • the concentration of carbon dioxide and/or precursors thereof in the input liquid may be at least 5 mmol/kg, at least 10 mmol/kg, at least 50 mmol/kg, at least too mmol/kg, at least 250 mmol/kg, at least 500 mmol/kg or at least 750 mmol/kg.
  • the concentration of carbon dioxide and/ or precursors thereof may be at least 2 mmol/kg, at least 5 mmol/kg, at least 10 mmol/kg, at least 50 mmol/kg, at least too mmol/kg, at least 500 mmol/kg, at least 1,000 mmol/kg, at least 2,000 mmol/kg, at least 3,000 mmol/kg or at least 4,000 mmol/kg.
  • the concentration of carbon dioxide and/ or precursors thereof in the input liquid may be between 1 pmol/kg and
  • brines or produced water can have carbonate concentrations of up to 4,500 mmol/kg. Additionally, the solubility of sodium bicarbonate in water at room temperature is about 0.75 to 1.034 mol/kg.
  • concentrations of carbon dioxide and/ or precursors thereof in the input liquid given above may be understood to be the concentration of carbon dioxide and/ or precursors thereof prior to the input liquid having been contacted with the gas with a high concentration of carbon dioxide.
  • the apparatus may comprise a first pH adjuster configured to adjust the pH of the input liquid.
  • the first pH adjuster maybe configured to reduce the pH of the input liquid.
  • the first pH adjuster maybe configured to reduce the pH of the input liquid prior to or consecutively to the degasser degassing the input liquid.
  • the first pH adjuster may comprise a first injector configured to inject an acidic and/or buffering species into the input liquid.
  • the first pH adjuster maybe configured to remove an alkaline and/or buffering species from the input liquid.
  • the first pH adjuster may comprise an ion exchange resin to capture the alkaline and/or buffering species.
  • the buffering species may be boric acid, a borate, a carbonate, a bicarbonate, a phosphate or a mixture thereof.
  • the first pH adjuster is configured to inject an acidic species into the input liquid.
  • the acidic species maybe a liquid, a solid and/or a gas and/or maybe provided as a solution.
  • the acidic species may be or comprise hydrochloric acid, sulphuric acid, nitric acid, acetic acid and/or formic acid.
  • the gas maybe or comprise carbon dioxide, a nitrous oxide, a sulfur oxide, hydrogen sulfide, hydrogen chloride, bromide and/ or fluoride.
  • the first pH adjuster maybe configured to inject produced water. It is noted that some produced water is acidic. Accordingly, this could be used alone or in addition to an acidic species to adjust the pH of the input liquid.
  • the first pH adjuster may comprise an acid generator.
  • the acid generator maybe configured to generate an acidic species from a suitable water based medium, such as seawater. Suitable acid generators are known in the art, for instance see US 9,303,323 B2 and US 9,719,178 B2.
  • the acid generator may be configured to produce a gas stream.
  • the apparatus may be configured to combine the gas stream and the output gas.
  • the first pH adjuster may be configured to pass a sufficient electrical current through the input liquid and separate out the acidic stream.
  • the first pH adjuster may be configured to contact the input liquid with a chemical waste product produced by a biological process.
  • the chemical waste product may be or comprise a chemical waste product produced by an acid producing and/or alkali depleting species and/or acidic effluent from a species.
  • the acid producing and/or alkali depleting species maybe bacteria, algae and/or fungi.
  • the effluent from a species may be from an animal.
  • the animal may be a fish or a bird.
  • the first pH adjuster may comprise a first pH sensor configured to sense the pH of the input liquid.
  • the first pH sensor is preferably disposed downstream of the first injector.
  • the first pH sensor may be disposed in the degassing chamber.
  • the first pH adjuster may be configured to reduce the pH of the input liquid to less than 7, less than 6, less than 5, less than 4 or less than 3.5.
  • the first pH adjuster may be configured to reduce the pH of the input liquid to between o and 7 or between 1 and 6.
  • the first pH adjuster is configured to reduce the pH of the input liquid to between 2 and 5 or between 3 and 4.
  • the inventors have found that the lower the pH of the input liquid, the higher the concentration of carbon dioxide in the output gas. However, in some embodiments it may not be desirable to lower the pH too low as doing so might then mean that the output liquid has to be treated. Accordingly, in alternative embodiments, the first pH adjuster is configured to reduce the pH of the input liquid to between 2 and 6, between 3 and 6, between 4 and 6 or between 5 and 6. Removing carbon dioxide from the input liquid will increase the pH thereof.
  • the apparatus may comprise a second pH adjuster configured to adjust the pH of the output liquid.
  • the second pH adjustor may be configured to increase the pH of the output liquid.
  • the second pH adjustor may be configured to increase the pH of the output liquid to at least 4, at least 5, at least 6, at least 7 or at least 7.5.
  • the second pH adjustor may be configured to increase the pH of the output liquid to between 4 and 11, between 5 and 10, between 6 and 9.5, between 6.5 and 9 or between 7 and 8.5. It is noted that the pH of river water generally falls between 6.5 and 8.5, and the pH of seawater is about 8.1. For the avoidance of doubt, all pH measurements defined herein are taken at 20°C unless otherwise specified.
  • the second pH adjuster may be configured to dilute the output liquid by contacting it with a further liquid stream.
  • the further liquid stream may be or comprise any suitable water based medium.
  • the further liquid stream may be or comprise fresh water, seawater, produced water, brackish water, wastewater, rainwater, sewerage water, deionized water and/or water containing brine.
  • the further liquid stream may be taken directly from the body of water.
  • the second pH adjuster may comprise a second injector configured to inject an alkaline species into the output liquid.
  • the second pH adjuster maybe configured to remove an acidic species from the output liquid.
  • the second pH adjuster may comprise an ion exchange resin configured to capture the acidic species.
  • the second pH adjuster may be configured to contact the output liquid with a chemical waste product produced by a biological process.
  • the chemical waste product may be or comprise a chemical waste product produced by an alkali producing and/or acid depleting species and/or alkaline effluent from a species.
  • the alkali producing and/or acid depleting species maybe bacteria, algae and/or fungi.
  • the effluent from a species may be from an animal.
  • the animal may be a fish or a bird.
  • the second pH adjuster comprises a second injector configured to inject an alkaline species into the output liquid.
  • the alkaline species may be a liquid, a solid and/or a gas and/or may be provided as a solution.
  • the alkaline species may be or comprise an amine, ammonia, a hydroxide and/or a carbonate.
  • the amine maybe or comprise monoethanolamine, diethanolamine or triethanolamine.
  • the hydroxide may be or comprise ammonium hydroxide, an alkali metal hydroxide and/ or an alkaline earth metal hydroxide.
  • the alkali metal hydroxide and/or an alkaline earth metal hydroxide may be or comprise sodium hydroxide, potassium hydroxide, calcium hydroxide and/or magnesium hydroxide.
  • the carbonate maybe or compromise ammonium carbonate, an alkali metal carbonate and/or an alkaline earth metal carbonate.
  • the alkali metal carbonate and/ or an alkaline earth metal carbonate may be or compromise sodium carbonate, potassium carbonate, calcium carbonate and/or magnesium carbonate.
  • the second pH adjuster may be configured to pass a sufficient electrical current through the output liquid and separate out the alkaline stream.
  • the second pH adjuster may comprise a second pH sensor configured to sense the pH of the output liquid.
  • the second pH sensor is preferably disposed downstream of the second injector. It is noted that it is still possible to obtain an output gas comprising carbon dioxide even when the input liquid is not acidified. Accordingly, in some alternative embodiments, the apparatus may not comprise a first and/or second pH adjuster.
  • the apparatus may comprise solid media disposed in the degassing chamber.
  • the solid media is preferably chemically inert.
  • the solid media may be a porous solid and/ or a foamed solid.
  • the solid material is a porous foamed solid.
  • the solid media may comprise or be a plastic, a ceramic, a metal and/ or a rock.
  • the solid media is or comprises a porous foamed ceramic material.
  • the solid media is a porous rock, preferably a porous volcanic rock.
  • the solid media may have a surface area of at least 1 m 2 /g, at least 2 m 2 /g, at least 5 m 2 /g, at least 10 m 2 /g, at least 20 m 2 /g, at least 30 m 2 /g, at least 40 m 2 /l, at least 50 m 2 /g, at least 75 m 2 /g, at least too m 2 /g, at least 250 m 2 /g, at least 500 m 2 /g, at least 750 m 2 /g, at least 1,000 m 2 /g or at least 1,500 m 2 /g.
  • the solid media may define a plurality of shapes.
  • the solid media may define a plurality of cylindrical or spherical shapes.
  • the solid media may be randomly orientated in the degassing chamber.
  • the solid media may comprise a grid or mesh.
  • the solid media may be configured to disperse the input liquid and/ or slow the flow of the input liquid.
  • the solid media may be configured to provide a nucleation site.
  • the apparatus may comprise an agitator, configured to agitate the input liquid within the degassing chamber.
  • the agitator may consist of a mechanical agitator, an axial flow impeller, a radial flow impeller, a tangential flow impeller, a close clearance impeller, a coil impeller, a dispersion blade impeller, a hydrofoil impeller, a retreat curve impeller, a screw impeller, an anchor impeller, a helical ribbon impeller, a paddle impeller, a turbine impeller, a high shear mixer, a magnetic agitator, a sonic agitation device and/or an ultrasonic agitation device.
  • the apparatus may be configured to degas the input liquid in a batch process. It may be appreciated that the batch size could vary depending upon the desired application.
  • the degassing chamber may be configured to degass a batch of input liquid which is at least i litre, at least 5 litres, at least 10 litres, at least 20 litres or at least 40 litres. In some embodiments, the degassing chamber maybe configured to degas a batch of input liquid which is at least 50 litres, at least too litres, at least 500 litres, at least 750 litres, at least 1,000 litres, at least 2,500 litres, at least 5,000 litres, at least 7,500 litres or at least 10,000 litres.
  • the degassing chamber may be configured to degas a batch of input liquid which is between 1 and 500,000 litres, between 5 and 250,000 litres or between 10 and 100,000 litres. In some embodiments, the degassing chamber may be configured to degas a batch of input liquid which is between 20 and 500 litres, between 30 and 100 litres or between 40 and 60 litres. In alternative embodiments, the degassing chamber may be configured to degas a batch of input liquid which is between 100 and 50,000 litres, between 500 and 20,000 litres or between 1,000 and 10,000 litres.
  • the apparatus may be configured to degas the input liquid in a continuous process.
  • the degassing chamber may comprise or define a degassing conduit.
  • the degassing conduit may have a length of at least 0.25 m, at least 0.5 m, at least 1 m, at least 2 m, at least 5 m, at least 10 m, at least 25 m, at least 50 m, at least 75 m, at least 100m, at least 250 m, at least 500 m, at least 1000 m, at least 5000 m or at least 10,000 m.
  • the degassing conduit has a length between 0.2 and 1,000 m, between 0.4 and 500 m, between 0.5 and 100 m, between 0.6 and 50 m, between 0.7 and 25m, between 0.8 and 10 m, between 0.9 and 5 m or between 1 and 1.25 m.
  • the degassing conduit may have an internal diameter of at least i mm, at least 5 mm, at least 10 mm, at least 25 mm, at least 50 mm, at least too mm, at least 200 mm, at least 300 mm or at least 400 mm.
  • the degassing conduit may have an internal diameter of less than or equal to too m, than or equal to 50 m, than or equal to 25 m, than or equal to 15 m, than or equal to 10 m, than or equal to 5 m, than or equal to 2 m, than or equal to 1.5 m, than or equal to 1 m, less than 800 mm or less than 600 mm.
  • the degassing conduit may have an internal diameter of between 1 mm and too m, between 2 mm and 50 mm, between 3 mm and 25 m, between 5 mm and 15 m, between 10 mm and 10 m, between 25 mm and 5m, between 50 mm and 2 m, between too mm and 1.5 m, between 200 mm and 1 m, between 300 and 800 mm, between 400 and 600 mm.
  • the degassing conduit may comprise a first portion adjacent a first end and a second portion adjacent a second end.
  • the liquid inlet may be disposed in the first portion.
  • the liquid outlet may be disposed in the second portion. Accordingly, it will be appreciated that in use the input liquid would flow in a direction from the first end to the second end.
  • the liquid inlet may be disposed substantially adjacent the first end.
  • the degassing conduit may be disposed or configured to be disposed so that it is substantially horizontal.
  • the degassing conduit may be disposed or configured to be disposed so that the first end may be higher than the second end.
  • the degassing conduit may be disposed or configured to be disposed so that the second end is higher than the first end.
  • the degassing conduit is disposed or configured to be disposed in a substantially vertical configuration.
  • the degasser may comprise a plurality of degassing chambers.
  • each degassing chamber may be as defined above. Accordingly, each degassing chamber may comprise a gas outlet, a liquid inlet and a liquid outlet as defined above.
  • the apparatus may comprise a cradle supporting the plurality of degassing chambers.
  • the apparatus comprises a liquid pump configured to pump an input liquid into the liquid inlet.
  • the liquid pump may be configured to pump the input liquid into each liquid inlet.
  • the apparatus may not comprise a liquid pump.
  • the apparatus may be configured to cause an input liquid to flow through the liquid inlet by using wave motion.
  • the apparatus may be configured to cause an input liquid to flow through the liquid inlet by causing an input gas to flow through the gas inlet.
  • the input gas causes the input liquid to flow due to a gas uplift.
  • the degasser is configured to contact the input liquid with an input gas.
  • the degasser may comprise a gas inlet configured to feed an input gas into the degassing chamber.
  • the apparatus may further comprise a gas pump, configured to pump an inlet gas into the degassing chamber.
  • the gas inlet may be configured to be disposed below the surface of the body of water.
  • the input gas preferably comprises less than 10,000 ppm carbon dioxide, more preferably less than 1,000 ppm carbon dioxide, less than 800 ppm carbon dioxide, less than 700 ppm carbon dioxide, less than 600 ppm carbon dioxide or less than 500 ppm carbon dioxide, and most preferably comprises less than 450 ppm or less than 430 ppm carbon dioxide.
  • the input gas may comprise between o and 1,000 ppm carbon dioxide, between 50 and 1,000 ppm carbon dioxide, between 100 and 800 ppm carbon dioxide, between 200 and 700 ppm carbon dioxide, between 300 and 600 ppm carbon dioxide, between 350 and 500 ppm carbon dioxide, between 400 and 450 ppm carbon dioxide or between 410 and 430 ppm carbon dioxide.
  • the input gas could be selected to be compatible with a specific membrane or for use with pressure swing adsorption (PSA), to allow concentration of a carbon dioxide gas stream.
  • the input gas is atmospheric air.
  • the input gas is or comprises nitrogen, helium, methane and/or hydrogen.
  • the input gas comprises at least 600,000 ppm nitrogen, at least 700,000 ppm nitrogen, at least 750,000 ppm nitrogen, at least 780,000 ppm nitrogen, at least 800,000 ppm nitrogen, at least 900,000 ppm nitrogen, at least 950,000 ppm nitrogen or at least 990,000 nitrogen.
  • atmospheric air comprises about 780,840 ppm nitrogen.
  • the degasser may comprise an emergency vent configured to vent a gas in the degasser if a pressure in the degasser exceeds a predetermined pressure.
  • the emergency vent may comprise a relief valve.
  • the apparatus may comprise one or more valves on a conduit upstream of the liquid inlet in the degasser.
  • the apparatus may comprise one or more valves on a conduit downstream of the gas outlet in the degasser.
  • the apparatus may comprise one or more valves on a conduit downstream of the liquid outlet in the degasser.
  • the one or more valves may be a one way valve, a flow control valve, an isolation valve, adjustable pressure relief valve and/ or combinations thereof.
  • the degasser may be configured to bubble the input gas through the input liquid.
  • the bubbles may have an average diameter of less than too cm, less than 50 cm, less than 25 cm, less than 10 cm, less than 5 cm or less than 1 cm. In some embodiments, the bubbles may have an average diameter of less than 800 pm, less than 600 pm, less than 400 pm, less than 200 pm or less than too pm.
  • each degassing chamber may comprise a gas inlet, a gas outlet, a liquid inlet and a liquid outlet as defined above.
  • the gas pump may be configured to pump the inlet gas into the multiple gas inlets of the multiple degassing chambers.
  • the gas inlet maybe disposed in the first portion.
  • the gas outlet maybe disposed in the second portion. Accordingly, it will be appreciated that in use the gas would flow in a direction from the first end to the second end.
  • the gas outlet maybe disposed substantially adjacent the second end.
  • the degassing conduit may be disposed or configured to be disposed so that the second end is higher than the first end. Accordingly, in this embodiment, the input gas may flow in the same direction as the input liquid. In this embodiment, the input gas may cause the input liquid to flow. Accordingly, there may be no need for a water pump. This advantageously reduces the energy required to run the apparatus.
  • the gas inlet may be disposed in the second portion.
  • the gas outlet may be disposed in the first portion.
  • the liquid inlet may be disposed between the gas outlet and gas inlet.
  • the gas inlet may be disposed between the liquid outlet and the liquid inlet. Accordingly, it will be appreciated that in use the gas would flow in a direction from the second end to the first end.
  • the gas outlet maybe disposed substantially adjacent the first end.
  • the degassing conduit may be disposed or configured to be disposed so that the first end is higher than the second end. Accordingly, in this embodiment, the input gas may flow in the opposite direction to the input liquid.
  • the apparatus may comprise a gas trap or gas recirculation unit.
  • the gas trap or gas recirculation unit maybe configured to separate a gas from the output liquid.
  • the gas trap or gas recirculation unit may comprise a further gas outlet.
  • the further gas outlet may be disposed between the gas inlet and the liquid outlet.
  • the gas trap or gas recirculation unit may comprise a recirculation conduit configured to feed gas from the further gas outlet to the capture means and/ or to a location in the degassing conduit between the further gas outlet and the first end of the degassing conduit.
  • the recirculation conduit may be configured to feed gas from the further gas outlet to the capture means and/or to a location in the degassing conduit between the gas inlet and the first end of the degassing conduit.
  • the degasser maybe configured to subject the input liquid to a reduced pressure.
  • the apparatus may be configured to crease a pressure differential in the degassing chamber, such that a headspace is at a lower pressure than the input liquid.
  • the headspace may be a portion of the degassing chamber which comprises a gas prior to reduction of pressure. It may be appreciated that as long as the pressure in the headspace is lower than the pressure in the liquid then carbon dioxide may be extracted.
  • the input liquid may be pressurized at a pressure greater than atmospheric pressure.
  • input liquid may be pressurized at a pressure greater than atmospheric pressure if the apparatus comprises a contacting chamber upstream of the degasser.
  • a skilled person could select a suitable reduced pressure.
  • the degasser may comprise a pressure reduction system configured to create a pressure differential in the vacuum chamber, such that the headspace within the degassing chamber is at a lower pressure than liquid in the degassing chamber.
  • the degasser may comprise one or more valves configured to reduce the pressure of the input liquid.
  • the one or more valves may comprise a flow control valve, an isolation valve and/or an adjustable pressure relief valve.
  • the degasser may comprise a vacuum system, wherein the vacuum system is configured to reduce the pressure and/or creating a vacuum in the degassing chamber.
  • the vacuum system may comprise a vacuum pump, a rotary pump, a diaphragm pump, a liquid ring vacuum pump, a gas transfer pump, a kinetic transfer pump, a positive displacement pump, an entrapment pump, a centrifugal pump and/or an ejector.
  • the degassing chamber may be a vacuum chamber.
  • the vacuum system may be configured to reduce the pressure inside the degassing chamber during a degassing phase.
  • the vacuum system is configured to reduce the pressure of a head space in the degassing chamber.
  • the head space may be a portion of the degassing chamber which comprises a gas prior to reduction of pressure. It may be appreciated that as long as the pressure in the head space is lower than the pressure in the liquid then carbon dioxide may be extracted. If the apparatus is disposed in a body of water, then the input liquid may be pressurized. Accordingly, the pressure in the headspace required to produce the output gas at a reasonable rate would not need to be as low as it would be at sea level. A skilled person could select a suitable pressure.
  • the pressure reduction system may be configured to create a pressure differential in the vacuum chamber, such that the headspace within the degassing chamber is at a lower pressure than liquid in the degassing chamber.
  • the pressure reduction system may be configured to reduce the pressure in the degassing chamber, and optionally in the headspace in the degassing chamber, to a pressure which is less than 10 MPa, less than 8 MPa, less than 6 MPa, less than 4 MPa or less than 2 MPa.
  • the pressure reduction system may be configured to reduce the pressure in the degassing chamber, and optionally in the headspace in the degassing chamber, to a pressure which is less than 1 MPa, less than 800 kPa, less than 600 kPa, less than 400 kPa, less than 200 kPa, or less than 101 kPa.
  • the pressure reduction system maybe configured to reduce the pressure of the headspace inside the degassing chamber to less than 150 kPa, less than 125 kPa, less than 101.325 kPa, less than 100 kPa, less than 75 kPa, less than 50 kPa, less than 25 kPa, less than 10 kPa, less than 5 kPa or less than 1 kPa.
  • the pressure reduction system optionally the vacuum system, may be configured to reduce the pressure of a gas phase inside the degassing chamber to less than 750 Pa, less than 50 Pa, less than 25 Pa, less than 10 Pa, less than 5 Pa or less than 1 Pa.
  • the vacuum system may be configured to continuously act to reduce the pressure in the degassing chamber during a degassing phase.
  • the vacuum system may be configured to alternate between a state where it is acting on the degassing chamber and a state where it is not acting on the degassing chamber during the degassing stage.
  • the apparatus comprises two or more degassing chambers and the vacuum system is configured sequentially act on the two or more degassing chambers such that when it is not acting on one degassing chamber it is acting on an alternative degassing chamber.
  • the vacuum system may be configured to continuously act of the degassing chamber during a pressure reduction period, and to then alternate between a state where it is acting on the degassing chamber and a state where it is not acting on the degassing chamber during an extraction period, wherein the extraction period is after the degassing period.
  • the vacuum system may be configured to act on the degassing chamber for periods of time of at least 10 seconds, at least 20 seconds, at least 30 seconds, at least 40 seconds, at least 50 seconds or at least 1 minute.
  • the vacuum system may be configured to act of the degassing chamber for between 10 seconds and 30 minutes, between 20 seconds and 20 minutes, between 30 seconds and 10 minutes, between 40 seconds and 5 minutes, between 50 seconds and 30 minutes or between 60 and 90 seconds.
  • the vacuum system may be configured to not act on the degassing chamber for periods of time of at least to seconds, at least 20 seconds, at least 30 seconds, at least 40 seconds, at least 50 seconds or at least 1 minute.
  • the vacuum system may be configured to act of the degassing chamber for between 10 seconds and 30 minutes, between 20 seconds and 20 minutes, between 30 seconds and 10 minutes, between 40 seconds and 5 minutes, between 50 seconds and 30 minutes or between 60 and 90 seconds.
  • the apparatus may comprise a vent configured to selectively vent an output gas.
  • the apparatus may be configured to vent the output gas during a venting period in the degassing phase.
  • the apparatus may be configured to capture the output gas during a capture period in the degassing phase which is after the venting period.
  • the venting period may correspond to the pressure reduction period.
  • the capture period may correspond to the extraction period.
  • the transportation means or transporter may be configured to transport at least a portion of the captured output gas.
  • the venting period may be directly after the vacuum system is activated to reduce the pressure inside the degassing chamber.
  • venting the gas which is initially produced vents gas with a low concentration of carbon dioxide.
  • the apparatus may comprise a C0 2 sensor configured to sense the concentration of the carbon dioxide in the output gas.
  • the apparatus may be configured to switch to the capture period, and thereby start capturing the output gas, after the C0 2 sensor senses that the concentration of carbon dioxide in the output gas has risen above a predetermined first concentration.
  • the predetermined first concentration may be a concentration of carbon dioxide of at least 750 ppm, at least 1,000 ppm, at least 5,000 ppm, at least 10,000 ppm, at least 20,000 ppm, at least 30,000 ppm, at least 40,000 ppm or at least 45,000 ppm.
  • the predetermined first concentration may be a concentration of carbon dioxide of at least 50,000 ppm, at least 75,000 ppm, at least 100,000 ppm, at least 200,000 ppm, at least 300,000 ppm, at least 400,000 ppm, at least 500,000 ppm, at least 600,000 ppm, at least 700,000 ppm, at least 800,000 ppm, at least 900,000 ppm or at least 920,000 ppm.
  • the apparatus may be configured to switch to the capture period, and thereby start capturing the output gas, after a predetermined first time period.
  • the predetermined first time period may be selected by the skilled person, and may vary depending upon factors such as the volume of liquid and the volume of the degassing chamber. In some embodiments, the predetermined first time period may be between to seconds and 30 minutes, between 15 seconds and 10 minutes, between 30 seconds and 5 minutes or between 1 minute and 3 minutes.
  • the apparatus may be configured to turn off the vacuum system and/ or vent the output gas after the C0 2 sensor senses that concentration of carbon dioxide in the output gas has dropped below a predetermined second concentration.
  • the predetermined second concentration may be less than 920,000 ppm, less than 900,000 ppm, less than 800,000 ppm, less than 700,000 ppm, less than 600,000 ppm, less than 500,000 ppm, less than 400,000 ppm, less than 300,000 ppm, less than 200,000 ppm, less than 100,000 ppm, less than 75,000 pp or less than 50,000 ppm.
  • the predetermined second concentration may be less than 45,000 ppm, less than 40,000 ppm, less than 30,000 ppm, less than 20,000 ppm, less than 10,000 ppm, less than 5,000 ppm or less than 750 ppm.
  • the apparatus may be configured to turn off the vacuum system and/ or vent the output gas after a predetermined second time period. It may be appreciated that the predetermined second time period may vary depending upon various factors including the volume of liquid and the pressure used. The skilled person could select a suitable second time period.
  • the apparatus may comprise a heater configured to heat the input liquid.
  • the heater may be configured to heat the gas inlet.
  • the heater may be configured to heat the input liquid and/or input gas upstream of the liquid inlet and/ or the gas inlet. Alternatively, or additionally, the heater may be configured to heat the input liquid and/ or input gas in the degassing chamber.
  • the heater may be configured to heat the input liquid and/or input gas to a temperature of at least 5°C, at least io°C, at least 15°C, at least 20°C, at least 25°C, at least 30°C, at least 35°C, at least 40°C, at least 45°C or at least 50°C.
  • the heater may be configured to heat the input liquid and/or input gas to a temperature of between 5 and ioo°C, between 10 and 95°C, between 15 and 9O°C, between 20 and 85°C, between 25 and 8o°C, between 30 and 75°C, between 35 and 7O°C, between 40 and 65°C, between 45 and 6o°C or between 50 and 55°C.
  • the heater may comprise one or more solar panels configured to heat the input liquid and/or input gas.
  • the heater may comprise a heat exchanger.
  • the heater may be configured to heat the input liquid and/ or input gas using heat energy generated from the oil reservoir, from geothermal heating and/ or from an ocean heat pump.
  • the transportation means may be configured to transport the output gas directly from the degassing chamber to the oil reservoir.
  • the output gas may have a high enough concentration of carbon dioxide, e.g. at least 920,000 ppm, it may be suitable for use in EOR without the need for further processing.
  • the apparatus may comprise an output gas processing unit, wherein the output gas processing unit is configured to separate the output gas into a first output gas stream with a high concentration of carbon dioxide and a second output gas stream with a low concentration of carbon dioxide.
  • the apparatus may comprise an output gas conduit extending between the gas outlet of the degasser and the output gas processing unit.
  • the output gas processing unit may be integrated within the degasser.
  • the apparatus may comprise a first output gas processing unit integrated within the degasser and a second output gas processing unit which is separate to the degasser.
  • the apparatus may comprise an output gas conduit extending between the degasser and the second output gas processing unit, and configured to transport at least a portion of the output gas from the degasser to the second output gas processing unit.
  • the output gas conduit may be configured to transport a carbon dioxide rich portion of the output gas from the degasser to the second output gas processing unit.
  • the output gas processing unit may comprise any means known in the art to separate carbon dioxide from a gas stream.
  • the output gas processing unit may comprise a membrane, a deaerator, a pressure swing adsorption (PSA) apparatus, a cryogenic separation apparatus and/or a gas scrubbing apparatus.
  • the membrane may be a polymeric and/ or inorganic membrane.
  • the membrane may be or comprise a size sieving membrane, a surface diffusion membrane, a solution diffusion membrane and/ or a facilitated transport membrane.
  • the membrane may be or comprise an alumina membrane, a silica membrane, a carbon membrane, a polyimide membrane, a polyvinyl chloride membrane, a polybenzimidazole membrane, a cellulose acetate membrane, a polyimide membrane, a polysulfone membrane and/ or a polycarbonate membrane.
  • Suitable membranes will be known to the skilled person and are described in Han et al. (Journal of Membrane Science, Volume 628, 15 June 2021, 119244) and lulianelli et al. (Advanced Membrane Science and Technology for
  • the solvent used for gas scrubbing may react chemically with the carbon dioxide or may physically absorb it.
  • the solvent may be an organic solvent, such as an those containing an alcohol chemical group, an alkane, a carboxylic acid chemical group, an ester chemical group, an aldehyde chemical group, a phosphate chemical group, a phosphate ester chemical group, an ether chemical group, or a molecule or formulation containing any combination of the previously mentioned chemical groups.
  • the alcohol maybe methanol.
  • the ester maybe propylene carbonate or methyl acetate.
  • the carboxylic acid may be acetic acid.
  • output gas processing unit may be configured to contact the carbon dioxide with an absorbent or adsorbent material and/or a reactive compound.
  • the absorbent or adsorbent material may be or comprise a molecular sieve, an inorganic framework material, an organic framework material, a silica material, activated carbon, an amine, a metal hydroxide and/or an organic solvent.
  • the absorbent or adsorbent material maybe a porous material.
  • the porous material may be any suitable porous material.
  • the porous material maybe microporous, mesoporous and/ or macroporous. It may be understood that a microporous material has an average pore size of less than 2 nm, a mesoporous material has an average pore size between 2 and 50 nm, and a macroporous material has an average pore size of greater than 50 nm.
  • the organic framework material may be a metal organic framework material.
  • the molecular sieve may be a zeolite.
  • the organic solvent may be as defined above. Suitable adsorbent materials are known, for instance see Lai et al. (Greenhouse Gases: Science and Technology, vol. 11(5), pages 1076-1117).
  • any solvents, liquids, and/ or formulations used in the apparatus and methods of the invention may be OSPAR compliant for discharge.
  • the OSPAR Convention requires that registration and hazard assessment is completed on the chemicals used and discharged offshore by the Oil and Gas Industry as well as a process whereby operations permits are issued.
  • the contracting parties to the OSPAR convention regulate the discharge of chemicals and typically require registration data to include information on the chemical composition of the substance / mixture being discharged, as well as information on the biodegradation, bioaccumulation and ecotoxicity of all components which are determined using internationally accredited test methods such as those published by the Organization for Economic Cooperation and Development (OECD), International Organization for Standardization (ISO), ASTM International (ASTM), and OSPAR Commission (PARCOM).
  • Any solvents, liquids and/ or formulations may also be compliant with other discharge regulations across the worldwide known to those skilled in the art including but not limited to the NDPES General Permit for discharge to the Gulf Of Mexico. Additionally, specific regulations relating to Carbon Capture and Storage are in place around the world and will be known to those skilled in the art.
  • a gas scrubbing apparatus may comprise: a carbon dioxide absorption unit, configured to contact the output gas with a solvent, wherein the solvent is configured to absorb carbon dioxide; a regeneration zone, configured to cause carbon dioxide to be released from the solvent; a rich solvent conduit, configured to transport the solvent comprising the absorbed carbon dioxide from the carbon dioxide absorption unit to the regeneration zone; and a regenerated solvent conduit, configured to transport regenerated solvent from the regeneration zone to the carbon dioxide absorption unit.
  • the carbon dioxide absorption unit may comprise a packed tower and/ or a spray scrubber.
  • the regeneration zone may comprise a stripping column and/or a flash drum.
  • the regeneration zone may be configured to heat the solvent to a temperature of at least 3O°C, at least 4O°C, at least 5O°C, at least 6o°C, at least 7O°C, at least 8o°C, at least 9O°C or at least ioo°C.
  • the regeneration zone may be configured to heat the solvent to a temperature of between to and i,5OO°C, between 20 and i,ooo°C, between 30 and 5OO°C, between 40 and 3OO°C, between 50 and 25O°C, between 60 and 225°C, between 70 and 200°C, between 80 and i8o°C, between 90 and i6o°C, or between too and 15O°C.
  • the apparatus may comprise one or more solar panels configured to heat the regeneration zone.
  • the regeneration zone may comprise a heat exchanger.
  • the heat exchanger may be configured to heat the regeneration zone using heat energy generated from the oil reservoir, from geothermal heating and/ or from an ocean heat pump.
  • the regeneration zone maybe disposed, or configured to be disposed, downhole of the oil reservoir. Accordingly, the elevated temperatures downhole could heat the regeneration zone.
  • the regenerated solvent conduit may be configured to cool the regenerated solvent.
  • the regenerated solvent conduit may extend through the body of water and may be configured to lose heat thereto.
  • the regenerated solvent conduit may be configured to cool the regenerated solvent to a temperature of less than ioo°C, less than 9O°C, less than 8o°C, less than 7O°C, less than 6o°C or less than 5O°C.
  • the regenerated solvent conduit may be configured to cool the regenerated solvent to a temperature between o and ioo°C, between 5 and 9O°C, between 15 and 8o°C, between 20 and 7O°C, between 25 and 6o°C or between 30 and 5O°C.
  • the apparatus may comprise a conduit, or other transportation means or transporter, configured to transport the second output gas stream from the output gas processing unit to the gas inlet.
  • the apparatus may comprise a compressor configured to compress the first output gas stream from the output gas processing unit.
  • the transportation means or transporter may be configured to transport the first output gas stream from the output gas processing unit to the oil reservoir.
  • the transportation means or transporter is configured to transport the compressed first output gas stream from the compressor to the oil reservoir.
  • the transportation means or transporter is configured to transport the first output gas stream from the output gas processing unit or compressor to a location downhole in the oil reservoir. It may be appreciated that the term “downhole” refers to an underground portion of the oil reservoir.
  • the transportation means or transporter may comprise a transportation conduit.
  • the transportation conduit may extend between the output gas processing unit or the compressor and the oil reservoir.
  • the transportation means or transporter may further comprise a pump configured to pump the first output gas stream of gas from the gas processing unit or the compressor to the oil reservoir.
  • the apparatus may further comprise a generator, configured to generate electricity.
  • the generator may comprise a turbine, wherein the generator is configured to generate electricity when the turbine is rotated.
  • the apparatus may comprise a conduit between the gas outlet and the turbine. Accordingly, the apparatus maybe configured to cause the output gas to generate the turbine.
  • a method for extracting oil comprising: providing an input liquid, wherein the input liquid comprises carbon dioxide, and/or a precursor thereof, dissolved therein; degassing the input liquid to obtain an output gas comprising carbon dioxide; and
  • the input liquid and output gas may be as defined in relation to the first aspect.
  • the carbon dioxide, and/ or the precursor thereof may be present intrinsically in the input liquid.
  • the method may comprise increasing the concentration of carbon dioxide and/or the precursor thereof in the input liquid prior to contacting the input liquid and input gas.
  • the concentration of carbon dioxide and/or the precursor thereof in the input liquid may be increased by contacting the input liquid with a gas with a high concentration of carbon dioxide.
  • the method may comprise pre-treating the gas with a high concentration of carbon dioxide to remove one or more contaminants therefrom prior to contacting the input liquid and the gas with a high concentration of carbon dioxide.
  • the one or more contaminants may comprise sulphur dioxide, sulphuric acid, carbon monoxide, nitrogen oxides, hydrochloric acid, heavy metals (e.g. mercury), hydrocarbons, particulates, and/or ash.
  • Suitable pre-treatment steps maybe known in the art.
  • the method may comprise pre-treating the gas with a high concentration of carbon dioxide to increase the concentration of carbon dioxide therein prior to contacting the input liquid and the gas with a high concentration of carbon dioxide.
  • concentration of carbon dioxide may be increased using any known technique, such as a membrane, pressure swing adsorption, a microporous and or mesoporous molecular sieve, cryogenic separation, etc.
  • Contacting the input liquid with the gas with the high concentration of carbon dioxide may comprise bubbling the gas with the high concentration of carbon dioxide through the input liquid.
  • contacting the input liquid with the gas with the high concentration of carbon dioxide may comprise contacting the gas with the high concentration of carbon dioxide with a spray of the input liquid.
  • contacting the input liquid with the gas with a high concentration of carbon dioxide may comprise contacting the gas with the high concentration of carbon dioxide utilizing any mixing device known to those skilled in the art.
  • contacting the input liquid with the gas with the high concentration of carbon dioxide could be used where the gas with the high concentration of carbon dioxide may comprise an impurity. Accordingly, the method may advantageously produce an output gas, with a high concentration of carbon dioxide, which does not contain the impurity.
  • the gas with a high concentration of carbon dioxide may be as defined above.
  • the method may comprise: providing a first input liquid, wherein the input first liquid comprises carbon dioxide, and/or a precursor thereof, dissolved therein; degassing the input first liquid to obtain a first gas with a high concentration of carbon dioxide; - contacting the gas with a high concentration of carbon dioxide and a second input liquid; and degassing the second input liquid to obtain a further gas with a high concentration of carbon dioxide.
  • the method may comprise: contacting a first gas with a high concentration of carbon dioxide and a first input liquid; degassing the input first liquid to obtain a second gas with a high concentration of carbon dioxide; - contacting the second gas with a high concentration of carbon dioxide and a second input liquid; and degassing the second input liquid to obtain a further gas with a high concentration of carbon dioxide.
  • the further gas with a high concentration of carbon dioxide has a higher concentration of carbon dioxide than the first gas with a high concentration of carbon dioxide.
  • the further gas with a high concentration of carbon dioxide has a higher concentration of carbon dioxide than the second gas with a high concentration of carbon dioxide.
  • the further gas with a high concentration of carbon dioxide may be the output gas.
  • the method may comprise transporting at least a portion of the output gas to an oil reservoir to thereby extract oil.
  • the method may comprise: contacting the further gas with a high concentration of carbon dioxide and a further input liquid; degassing the further input liquid to obtain a still further gas with a high concentration of carbon dioxide.
  • the above steps may be repeated until a gas with a desired concentration of carbon dioxide is obtained.
  • the method may then comprise transporting at least a portion of this gas to an oil reservoir to thereby extract oil.
  • the steps above enable a user to increase the concentration of carbon dioxide in the output gas with each iteration of the method.
  • the inventors have found that the above method can significantly increase the concentration of carbon dioxide in the output gas, to a concentration greater than that in the gas with a high concentration of carbon dioxide. Accordingly, this method can enable the inventors obtain an output gas with a high concentration of carbon dioxide, so no further treatment is necessary.
  • the gas with a high concentration of carbon dioxide may comprise a concentration of carbon dioxide as recited above.
  • the method may comprise venting gas subsequent to contacting the input liquid with the gas with a high concentration of carbon dioxide.
  • the method may comprise venting gas prior to degassing the input liquid.
  • this will vent undissolved gas.
  • the method may comprise contacting the input liquid with the gas with a high concentration of carbon dioxide in a gassing conduit.
  • the method may comprise causing the gas with a high concentration of carbon dioxide to flow in a first direction along the gassing conduit.
  • the method may comprise causing the gas with a high concentration of carbon dioxide to flow in the first direction from a first point, where the input liquid with the gas with a high concentration of carbon dioxide are contacted, to a second point, where the gas is vented.
  • the second point may be higher than the first point.
  • the second point is or defines a local high point in the gassing conduit.
  • the method may comprise causing the input liquid to travel or flow in the first direction along the gassing conduit.
  • the method may comprise causing the input liquid to travel or flow in a second direction, opposite to the first direction, along the gassing conduit.
  • the method may comprise contacting the input liquid and the gas with a high concentration of carbon dioxide at approximately atmospheric pressure.
  • the method may comprise contacting the input liquid and the gas with a high concentration of carbon dioxide at an increased pressure.
  • the increased pressure may be as defined above.
  • the gas with a high concentration of carbon dioxide comprises at least 50,000 ppm, at least 75,000 ppm, at least 100,000 ppm, at least 150,000 ppm, at least 2oo,oooppm, at least 250,000 ppm, at least 300,000 ppm, at least 350,000 ppm or at least 400,000 ppm.
  • the gas with a high concentration of carbon dioxide could have been obtained from degassing an input liquid in a previous step of the method.
  • the method may comprise subsequently maintaining and storing the input liquid at the high pressure.
  • the method may comprise reducing the pressure of the input liquid to obtain a further gas with a high concentration of carbon dioxide, and using the further gas with a high concentration of carbon dioxide to drive a turbine and thereby generate electricity.
  • the method may comprise reducing the pressure of the input liquid at times of high energy demand. Accordingly, the input liquid could be used to store energy like a compressed air battery.
  • the method may comprise conducting each subsequent step of contacting a gas with a high concentration of carbon dioxide and an input liquid at a higher pressure to the previous step of contacting a gas with a high concentration of carbon dioxide and an input liquid.
  • the method may comprise: contacting a first gas with a high concentration of carbon dioxide and a first input liquid at a first pressure; degassing the input first liquid to obtain a second gas with a high concentration of carbon dioxide; contacting the second gas with a high concentration of carbon dioxide and a second input liquid at a second pressure, which is greater than the first pressure; and degassing the second input liquid to obtain a further gas with a high concentration of carbon dioxide.
  • the method may comprise: - contacting the further gas with a high concentration of carbon dioxide and a further input liquid at a third pressure, which is greater than the first pressure; degassing the further input liquid to obtain a still further gas with a high concentration of carbon dioxide.
  • the third pressure may be greater than the second pressure.
  • the method may be configured to contact the input liquid and the gas with a high concentration of carbon dioxide at an increased pressure.
  • the increased pressure may be as defined above.
  • the method may comprise degassing the input liquid in a degasser comprising a degassing chamber.
  • the degassing chamber may comprise a solid media.
  • the degasser and/or the solid media maybe as defined in relation to the first aspect. Accordingly, the method may comprise feeding the input liquid into the degassing chamber, degassing the input liquid to provide the output gas and an output liquid and removing the output gas and output liquid from the degassing chamber.
  • Degassing the input liquid maybe a batch process. Accordingly, the method may comprise: - feeding a volume of input liquid into the degassing chamber; subsequently degassing the input liquid to obtain an output gas and removing the output gas from the degassing chamber; and subsequently removing the output liquid from the degassing chamber. In an alternative embodiment, degassing the input liquid is a continuous process.
  • the method may comprise continuously feeding the input liquid into the degassing chamber.
  • the method may further comprise continuously removing the output liquid and the output gas from the degassing chamber.
  • the method may comprise adjusting the pH of the input liquid.
  • the method may comprise adjusting the pH of the input liquid prior to or simultaneously with degassing the input liquid.
  • the method comprises lowing the pH of the input liquid.
  • the pH of the input liquid may be lowered to a pH as defined in relation to the first aspect.
  • Lowering the pH of the input liquid may comprise injecting an acidic and/or buffering species into the input liquid and/or removing an alkaline and/or buffering species from the input liquid.
  • the method comprises injecting an acidic species into the input liquid.
  • the method may comprise contacting the input liquid with a chemical waste product.
  • the chemical waste product may be as defined above.
  • the method may comprise passing an electrical current through the input liquid and separating out the acidic stream.
  • the method may comprise generating an acidic species from a suitable water based medium, such as sea water. Suitable methods for generating acidic species are known in the art and discussed above.
  • the method may comprise adjusting the pH of the output liquid. Preferably, the method comprises increasing the pH of the output liquid. The pH of the output liquid maybe increased to a pH as defined in relation to the first aspect.
  • Increasing the pH of the output liquid may comprise diluting the output liquid.
  • increasing the pH of the output liquid may comprise injecting an alkaline species into the output liquid and/or removing an acidic species from the input liquid.
  • increasing the pH of the output liquid comprises injecting an alkaline species into the output liquid.
  • the method may comprise contacting the output liquid with a chemical waste product.
  • the chemical waste product may be as defined above.
  • the method may comprise passing an electrical current through the output liquid and separating out the alkaline stream.
  • the method comprises using a liquid pump to cause the input liquid to flow through the degassing chamber.
  • the method does not comprise the use of a water pump to cause the input liquid to flow through the degassing chamber.
  • the method may comprise using a gas pump to cause the input gas to flow through the degassing chamber.
  • degassing the input liquid may comprise contacting the input liquid with an input gas.
  • the input gas may be as defined in relation to the first aspect.
  • the method may comprise continuously feeding the input gas into the degassing chamber.
  • Contacting the input liquid and input gas may comprise bubbling the input gas through the input liquid.
  • the method may comprise contacting the input liquid and the input gas while the input liquid is flowing in a first direction.
  • the method may comprise contacting the input liquid and the input gas while the input gas is flowing in the first direction.
  • the flow of the input liquid may be assisted by the flow of the input gas.
  • the method may comprise contacting the input liquid and the input gas while the input gas is flowing in a second direction. The second direction maybe opposite to the first direction.
  • the method may comprise capturing gas present in the output liquid.
  • the method may comprise combining the output gas and the captured gas.
  • degassing the input liquid may comprise subjecting the input liquid to a reduced pressure.
  • the method may comprise subjecting the input liquid to a reduced pressure during a degassing phase.
  • the reduced pressure may be as described above.
  • Subjecting the input liquid to a reduced pressure may comprise reducing the pressure of a headspace in the degassing chamber.
  • subjecting the input liquid to a reduced pressure during a degassing phase may comprise causing the input liquid to flow through one or more valves configured to reduce the pressure of the input liquid.
  • the one or more valves may comprise a flow control valve, an isolation valve and/or an adjustable pressure relief valve.
  • the method may comprise applying a vacuum system to the degassing chamber, where the degassing system is as described above.
  • the method may comprise causing the vacuum system to continuously act on the degassing chamber during the degassing phase.
  • the method may comprise causing the vacuum system to alternatively act on the degassing chamber and not act on the degassing chamber.
  • the method may comprise alternatively switching the vacuum system on and off during the degassing phase.
  • the method may comprise switching the vacuum system to sequentially act on two or more degassing chambers, such that when it is not acting on one degassing chamber it is acting on an alternative degassing chamber.
  • the method may comprise causing the vacuum system to continuously act on the degassing chamber during a pressure reduction period, and to then cause the vacuum system to alternatively act on the degassing chamber and not act on the degassing chamber during an extraction period, wherein the extraction period is after the degassing period.
  • the method may comprise subjecting the input liquid to a reduced pressure during which in a venting period, the method comprises venting the output gas which is obtained and, in a capture period, which is after the venting period, the method comprises capturing the output gas. At least a portion of the captured output gas may be transported to the oil reservoir.
  • the venting period may be directly after the input liquid is subjected to the reduced pressure.
  • venting the gas which is initially produced vents gas with a low concentration of carbon dioxide.
  • the method may comprise capturing the output gas after the concentration of carbon dioxide rises above a predetermined first concentration.
  • the predetermined first concentration may be as defined above.
  • the method may comprise capturing the output gas after a predetermined first time period.
  • the predetermined first time period may be as defined above.
  • the method may comprise stopping degassing the liquid and/or capturing the output gas after the C0 2 concentration I the output gas has dropped below a predetermined second concentration.
  • the predetermined second concentration maybe as defined above.
  • the method may comprise stopping degassing the liquid and/or capturing the output gas after a predetermined second time period.
  • the method may comprise heating the input liquid.
  • the method may comprise heating the input gas.
  • the method may comprise heating the input liquid and/ or input gas prior to or consecutively with degassing the input liquid.
  • the method may comprise heating the input liquid and/or input gas using solar energy, heat energy generated from the oil reservoir, heat energy generated from geothermal heating and/or heat energy generated from an ocean heat pump.
  • the method may comprise processing the output gas to obtain a first output gas stream with a high concentration of carbon dioxide and a second output gas stream with a low concentration of carbon dioxide.
  • the method may comprise using the second output gas stream as the input gas.
  • Processing the output gas may use any method known in the art.
  • the method may comprise passing the output gas through a membrane, using pressure swing adsorption, using cryogenic separation and/or gas scrubbing.
  • processing the output gas comprises: contacting the output gas with a solvent, wherein the solvent is configured to absorb carbon dioxide, such that the second output gas stream and a carbon dioxide rich solvent are generated; and degassing the carbon dioxide rich solvent to obtain the first output gas stream and a regenerated solvent.
  • Processing the output gas maybe a batch or continuous process.
  • processing the output gas is a continuous process.
  • the solvent may comprise an amine.
  • the amine may be any suitable amine absorbent known in the art.
  • the amine may be monoethanolamine (MEA), diethanolamine (DEA), methyldiethanolamine (MDEA), diisopropylamine (DIPA), aminoethoxyethanol (diglycolamine) (DGA) and/ or a combination thereof.
  • the solvent may comprise water.
  • the absorbent may comprise between 20 and 99%, between 30 and 95%, between 40 and 90% or between 50 to 80% by volume of water.
  • Degassing the carbon dioxide rich solvent may comprise heating the carbon dioxide rich solvent.
  • the carbon dioxide rich solvent maybe heated to a temperature of at least 3O°C, at least 4O°C, at least 5O°C, at least 6o°C, at least 7O°C, at least 8o°C, at least
  • the carbon dioxide rich solvent may be heated to a temperature of between 30 and 5OO°C, between 40 and 3OO°C, between 50 and 25O°C, between 60 and 225°C, between 70 and 200°C, between 80 and i8o°C, between 90 and i6o°C, or between too and 15O°C.
  • the method may comprise heating the carbon dioxide rich solvent using solar energy, heat energy generated from the oil reservoir, heat energy generated from geothermal heating and/or heat energy generated from an ocean heat pump.
  • the method comprises degassing the carbon dioxide rich solvent downhole.
  • degassing the carbon dioxide rich solvent may comprise subjecting the carbon dioxide rich solvent to a reduced pressure.
  • the method may comprise flashing the carbon dioxide rich solvent.
  • the method may comprise compressing the first output gas stream.
  • the method may comprise feeding the first output gas stream into the oil reservoir.
  • the method comprises feeding the compressed first output gas stream into the oil reservoir.
  • the method may comprise feeding the first output gas stream or the compressed first output gas stream downhole in the oil reservoir.
  • Figure 1 is a schematic overview of a system for generating an output gas comprising carbon dioxide from a liquid
  • FIG 2 is a schematic overview of a system for processing output the output gas
  • Figure 3 shows a section of an apparatus used in accordance with the invention
  • Figure 4 shows the apparatus from Figure 3 in use
  • Figure 5 is a schematic diagram of a further system for extracting carbon dioxide from a liquid.
  • Figure 6 is a schematic diagram of a further system for extracting carbon dioxide from a liquid.
  • FIG. 1 shows a schematic diagram of a system too for extracting carbon dioxide from a liquid.
  • the system too is preferably disposed in the vicinity of an offshore oil well or reservoir.
  • the liquid is a water based medium (WBM).
  • WBM water based medium
  • the WBM comprises carbon dioxide, and/or a precursor thereof, dissolved therein.
  • an aqueous solution may be used as the WBM. This includes, but is not limited to, fresh water, seawater, produced water, brackish water, wastewater, rainwater, sewerage water, deionized water and water containing brines.
  • the WBM is pumped, or otherwise flows into a WBM/gas mixing vessel 102.
  • the WBM/gas mixing vessel 102 is submerged or partially submerged in a body of water, preferably a sea or ocean.
  • the WBM/gas mixing vessel 102 may be submerged or partially submerged in a sea or ocean.
  • the WBM may flow directly into the WBM/gas mixing vessel 102.
  • the WBM first flows through an inlet 104 and into an inlet WBM manipulation system 106.
  • the inlet WBM manipulation system 106 is configured to manipulate the chemical or physical properties of the WBM.
  • the inlet WBM manipulation system 106 may be configured to modify the pH and/or temperature of the WBM. After any modification has been achieved, the WBM is pumped, or otherwise flows, along conduit 108 into the WBM/gas mixing vessel 102.
  • the WBM preferably flows into a first end of the WBM/gas mixing vessel 102.
  • an inlet gas is pumped, or otherwise flows, through a gas inlet 110.
  • the gas can also flow directly into a WBM/gas mixing vessel 102.
  • the gas first flows into an inlet gas manipulation system 112.
  • the inlet gas manipulation system 112 is configured to manipulate the chemical or physical properties of the inlet gas.
  • the inlet gas manipulation system 112 maybe configured to modify the composition and/or temperature of the inlet gas.
  • the inlet gas is pumped, or otherwise flows, along conduit 114 into the WBM/gas mixing vessel 102.
  • the inlet gas preferably flows into the first end of the WBM/gas mixing vessel 102.
  • the system may comprise an in-vessel manipulation system 116, configured to manipulate the chemical or physical properties of the WBM and/or the gas which is present in the WBM/gas mixing vessel 102.
  • the in-vessel manipulation system 116 may modify the properties of the WBM and/ or the gas similarly to the inlet WBM and/ or gas manipulation systems 106, 112 described above.
  • the gas comprising an increased concentration of carbon dioxide, is then pumped, or otherwise flows out of the WBM/gas mixing vessel 102 along conduit 118.
  • the gas may be further processed, as described below.
  • the WBM comprising a reduced concentration of carbon dioxide, is also pumped, or otherwise flows out of the WBM/gas mixing vessel 102.
  • the gas and WBM preferably flow out of a second end of the WBM/gas mixing vessel 9.
  • the second end is opposite and at a greater height to the first end.
  • the WBM may flow directly out of an outlet 120.
  • the WBM could be disposed of, for instance by returning it to the environment.
  • the WBM first flows along conduit 122 into an outlet WBM manipulation system 124.
  • the outlet WBM manipulation system 124 is configured to manipulate the chemical or physical properties of the WBM.
  • the outlet WBM manipulation system 124 may be configured to modify the pH of the WBM. This may ensure that the WBM can be returned to the environment without the risk of harm. After any modification has been achieved, the WBM is pumped, or otherwise flows, out of the outlet 120.
  • conduit 118 may supply the gas to a carbon dioxide absorber 126.
  • the carbon dioxide absorber 126 may comprise a packed tower or spray scrubber.
  • the gas is contacted with an amine absorbent, such that carbon dioxide is absorbed into the solvent.
  • the amine absorbent may be any suitable amine absorbent known in the art.
  • the amine absorbent comprises an amine.
  • the amine maybe monoethanolamine (MEA), diethanolamine (DEA), methyldiethanolamine (MDEA), diisopropylamine (DIPA), aminoethoxyethanol (diglycolamine) (DGA) and/or a combination thereof.
  • the absorbent may comprise up to about 90 % by volume of water, for example from about 50 to about 90 % by volume of water.
  • the gas which will now have a low concentration of carbon dioxide, may exit the carbon dioxide absorber 126 through conduit 128. The gas maybe vented to the atmosphere.
  • a rich amine stream comprising the amine absorbent and carbon dioxide
  • the regeneration zone 136 is configured to separate the carbon dioxide from the amine absorbent.
  • the regeneration zone 136 may be a distillation column operated under stream stripping conditions. It may be appreciated that such columns operate at an elevated temperature, at least 75°C.
  • the regeneration zone 136 may be disposed downhole in the oil reservoir. This would heat the rich amine stream to the desired temperature.
  • the regenerated, carbon lean amine solvent may then be returned to the carbon dioxide absorber 126 by conduit 134.
  • the conduit 134 may be submerged in a body of water. Accordingly, the water may cool the amine solvent before it reaches the carbon dioxide absorber 126.
  • the carbon dioxide which has been released may be transferred via conduit 136 into the oil reservoir.
  • a system to extract C0 2 from a water-based media was set up utilizing a vertical clear pipe which had a 40mm outside diameter and a 34mm inside diameter.
  • the pipe was approximately 1 m long.
  • the pipe was packed with elongate plastic media.
  • the plastic media defined a hollow cylindrical shape open at one end and with slots down the sides thereof (70mm long, 17 mm outer diameter, 8 - 12 mm inner diameter).
  • the pipe contained a total of 1L of water-based media, which was either tap water or sea water.
  • a variable speed airflow (o - 16 Liters per minute) was connected to a 12.5 mm diameter aperture near the bottom of the pipe, and exhaust gas was emitted through a further 12.5 mm diameter aperture near the top of the pipe.
  • a system similar to that in example 1 was set up.
  • This system comprised a wider diameter pipe (265 mm outside diameter, 225 mm internal diameter) with a maximum useable internal height of the pipe was 2.7 meters.
  • the pipe was again packed with plastic media, as described above.
  • a water inlet 2.3 meters above the bottom of the pipe was connected to mains tap water, which typically flows at a rate of 4 to 6 Liters per minute.
  • a water outlet was provided near the base of the pipe.
  • An air pump rated at 55 Liters per minute was connected to an aperture near the base of the pipe, and a gas outlet was provided near the top of the pipe, and the exhaust gas flow was then passed over a o - 100,000 ppm C0 2 sensor which measured the C0 2 level every 2 seconds.
  • a variable concentration acid dosing system was also provided, which added diluted HC1 to the incoming water stream.
  • the amount of HC1 added to the water stream was increased as the experiment progressed.
  • the resultant pH of the water was measured at the water outlet at various C0 2 emission levels. The results are shown in Table 2.
  • Example ,2 - Aerating water to extract carbon dioxide in a further continuous test A system similar to example 1 was set up. However, in this system the pipes had differing heights.
  • the column was a clear pipe with a 40mm outside diameter and 34mm inside diameter, and was packed with porous plastic media (70mm long, 17 mm outer diameter, 8 - 12 mm inner diameter).
  • a variable speed airflow (0 - 7 Liters per minute) was passed through 12.5 mm diameter aperture near the bottom of the tube.
  • the inlet gas flow rate was kept constant at about 7 liters per minute.
  • Exhaust gas was emitted through a further 12.5 mm diameter aperture near the top of the pipe.
  • Example 4 Aerating water taken from a large body of water in a continuous test The inventors subsequently investigated using the system in a larger body of water. The apparatus used is shown in Figures 3 and 4.
  • the apparatus 11 comprises a first conduit 12, extending between a first end 14 and a second end 16.
  • An air inlet 18 is disposed closer to the second end 16 than the first end 14.
  • a water inlet 20 is disposed between the air inlet 18 and first end 14.
  • the first end 14 comprises a gas outlet and the second end 16 comprises a water outlet.
  • a recirculation unit comprises a gas outlet 22, disposed between the air inlet 18 and the second end 16, and a second conduit 24 extending between the gas outlet 22 and a point between the water inlet 20 and the first end 14.
  • a valve (not shown) was disposed in the second conduit. The inventors ran some experiments with the valve open, and some with it closed.
  • Figure 4 shows the apparatus 11 in situ in a body of water 25.
  • the body of water 25 is a pond.
  • the apparatus could be disposed in any suitable body of water, such as a reservoir, a lake, the sea or the ocean.
  • the first conduit 12 is substantially vertical with the first end 14 disposed above the water 25 and the second end 16 disposed below the water25.
  • the water inlet 20 was disposed at, or marginally below the water line.
  • a third conduit 26 extends between an air pump 28 and the air inleti8.
  • the air pump 28 could provide air at a flow rate of up to 551/minute.
  • a fourth conduit extends between the body of water and the water inlet 20.
  • a water pump (not shown) is disposed on the fourth conduit and can pump water at a flow rate of up to 151/minute.
  • a fifth conduit 30 extends between the first end 14 and a C0 2 sensor 32.
  • the inventors then decided to test a large scale batch setup.
  • the used a cylindrical test chamber purpose built from a section of corrugated tubing with an internal diameter of 225mm, suitably sealed at each end using drainage pressure test plugs.
  • the height of water within the test vessel could be selected at between 0-2 meters.
  • a water height of 1.25 m, resulting in a water volume of 501 was used.
  • Testing was conducted at ambient temperature and pressure.
  • the chamber was filled with test golfballs, which provided additional surface area and were a means to avoid air pockets forming in the system.
  • Air could be added via up to 3 available entry points provided adjacent to the base of the chamber, and utilised a range of potential air stones disposed in the base of the chamber to diffuse the input gas within the input liquid. In the testing described below, air was added via all three entry points.
  • the water was added to the chamber using a standard diaphragm pump, but any suitable pump could be used.
  • gas lift i.e. by pumping air through the capture apparatus while it is submerged in water and using the increased buoyancy to replace the air in the apparatus chamber, as described in example 4.
  • Test i demonstrates that obtaining an average of too tonnes of C0 2 per billion litres of water while using acid is achievable. As demonstrated by test 2, when no acid is used, a lesser average of around 10 tonnes of C0 2 is achievable. This confirms that it is desirable to use acid, where possible, to increase yields.
  • Example 6 Applying a vacuum to extract carbon dioxide from water
  • the inventors then decided to investigate the possibility of degassing water using a vacuum.
  • a small scale vacuum chamber typically a BACOENG 12L (25cm X 25cm) with 30" Hg ⁇ 1 Max Reading pressure gauge and manifold;
  • a vacuum pump in the experiments described below a VEVOR 10CFM, 1HP 2 stage rotary vane vacuum pump was used.
  • the vacuum pump was attached to the vacuum chamber via a tA” vacuum hose with tA” SAE Fittings;
  • a high end C0 2 sensor in the experiments described below a 0-300, oooppm sensair K33 ICB with top hats was used;
  • a simple test was utilised to determine the amount of C0 2 remaining in the water after each vacuum test. This involved taking 500ml of the test fluid from the chamber before and after the test and bubbling air through it with the Hitop ‘shark’ 6.9 litre per minute (max) air pump to establish the amount of CO2 released.
  • a typical result for the acidified tap water pre-vacuum was a maximum height reached of approximately 9,oooppm- io,oooppm on the K30 1% senseair C0 2 unit.
  • a typical result after a vacuum had been applied ranged between i,5ooppm and about 3,oooppm, depending on a variety of factors.
  • a maximum height of around 2,000 ppm was considered a good result.
  • a finding of 70-85% removal of C0 2 in comparison to air treatment was considered acceptable.
  • nucleation materials were trialled with a particular focus on biomedia including lava rocks, Oase Hel-Xi3, XX1000, bio balls, ceramic rings, ceramic balls, alfagrog, plastic golfballs etc.
  • the inventors investigated a number of ways of using a vacuum pump, and analysed the amount of C0 2 left in the water after each run, as described above.
  • the lid While leaving the first vacuum pump running and the first valve closed, the lid was moved to the second 12 litre vacuum chamber. Once the lid was in place, the second vacuum chamber was evacuated using a second vacuum pump which was connected to a second valve in the lid. Once the second vacuum chamber had been evacuated, the second valve was closed and the second vacuum pump was turned off.
  • Test fluid was extracted using a vacuum pump, as described in example 6.
  • 4.51 of test fluid was provided in a 121 test vessel, with lava rock nucleation material.
  • Test fluid was approximately 10 cm from the top of vessel.
  • a small magnetic stirrer bar was operational at the bottom of the vessel to help mix the fluid layers. Tests were run for 7 and 15 minutes.
  • the peak level of C0 2 exiting the chamber was measured using the high end sensor. After each test, 500 ml of test fluid was aerated and the peak level of C0 2 was measured using the low end sensor. A sample of the tap water and seawater, which had been treated with HC1 to a pH of 5.5, but had not undergone vacuum, was also aerated. It is noted that the peak level of C0 2 measured for the untreated tap water was 9,000 ppm, and for the untreated seawater it was 6,500 ppm. These values were used to estimate the percentage of carbon dioxide removed during the vacuum extraction process.
  • Lava rocks were used, approximately 40 litres of acidified tap water to pH 5.5 with HC1 were added to the chamber.
  • Results obtained were similar to the 12I chamber in terms of amounts evacuated (70- 80%) and timing to evacuate (5-iomins, 7 median). This indicates that scale up of the method should be fairly straightforward. Meanwhile, it is noted that a much higher concentration of carbon dioxide was observed on the C0 2 capture sensor. This is due to the increased volume of water used. In particular, the inventors noted that the 320,000 ppm sensor quickly reached its maximum cut off, and stayed above this maximum value long enough to suggest the potential for a 500,000 ppm result.
  • Typical flow rates were 0.351/min for 1 minute, 0.251/min for 1 minute, 0.21/min for a minute then a drop to approximately 0.11/min for 4 minutes and approximately 0.05 1/min for the remaining 3 minutes.
  • the initial air in the chamber was removed prior to this measurement and this flow rate is thought to represent the gases being removed from the water phase. This gave an overall quantity of around 1.35 litres of gas in total over the 10 minutes. This measurement is not exact as the needle is not completely static but it felt to be a fair approximation.
  • the maximum ppm was 225,oooppm
  • the maximum ppm was 32o,oooppm
  • the maximum ppm was 37O,oooppm
  • the maximum ppm was 38o,oooppm
  • Example 11 Modelling carbon dioxide extraction from produced water
  • 2 g/litre of NaHC0 3 Sodium Bicarbonate
  • This testing was conducted in the 121 test chamber as described above, and the concentration of C0 2 measured using the Sprint IRW 100% C0 2 sensor.
  • Example 12 Increasing the concentration of carbon dioxide in the water
  • Exhaust gases from power stations and diesel engines/generators/powerplants etc. have a higher percentage of C0 2 in them than atmospheric air.
  • exhaust gas from a gas fired power station contains circa 5% C0 2
  • exhaust gas from a diesel engines contains circa 12% C0 2
  • exhaust gas from a coal-fired power station contains circa 15%
  • exhaust gas from a cement or steel plant contains circa 30-35%.
  • Figure 5 shows a system that is configured for use with flue gases at pressures of about 10 to 15 bar.
  • the system comprises a water inlet 34, where water is fed into a first conduit 36.
  • a pump assembly 38 may be provided on the first conduit
  • a first flow control valve/isolation valve 40 may be disposed on the first conduit 36 downstream of the pump 38.
  • a gas inlet 42 may feed a flue gas, which is preferably at a pressure between 10 and 15 bar, along a second conduit 44.
  • a second flow control valve/isolation valve 46 may be disposed on the second conduit 44.
  • the second conduit 44 may feed the gas through a gas inlet 48 into the first conduit, preferably downstream of the first flow control valve/isolation valve 40.
  • the first conduit 36 may extend between the gas inlet 48 and a pressure vessel 50.
  • Carbon dioxide is more soluble in water than other gases, and so will dissolve preferentially.
  • the solubility of nitrogen and oxygen in water at atmospheric pressure and 20°C is about 20 mg/L and 40 mg/L, respectively.
  • the solubility of carbon dioxide in water at atmospheric pressure and 20°C is about 1,700 mg/L. Accordingly, contacting the flue gas and water in the first conduit 36 will significantly increase the concentration of the carbon dioxide in the water.
  • the length of the first conduit 36 between the gas inlet 48 and the pressure vessel 50 may be maximized to increase the contact time for the gas and water therein.
  • the pressure vessel 50 comprises a first vent 52 and a third flow control valve/isolation valve 54 configured to vent undissolved gas which is present in the pressure vessel 50.
  • the pressure vessel 50 may further comprise an emergency vent 56 comprising a relief valve 58 to protect the pressure vessel 50.
  • the pressure vessel 50 is disposed at a local high point in the apparatus, to better enable undissolved gas to collect therein.
  • a third conduit 60 extends between the pressure vessel 50 and a carbon dioxide capture tank 62.
  • the third conduit 60 is configured to carry water saturated with dissolved carbon dioxide 64 from the pressure vessel 50 to the capture tank 62.
  • a fourth flow control valve/isolation valve 66 and/or an adjustable pressure relief valve 68 may be disposed on the third conduit 60.
  • the fourth flow control valve/isolation valve 66 and/ or the adjustable pressure relief valve 68 are configured to reduce the pressure of the water 64.
  • carbon dioxide will be released from the water 64 into the capture tank 62 to provide a gas with a high concentration of carbon dioxide 70.
  • the capture tank 62 may comprise a gas outlet 72 to enable the gas 70 to be released from the tank and transported along a fourth conduit 74.
  • the fourth conduit 74 may comprise a fifth flow control valve/isolation valve 76.
  • the capture tank 62 may further comprise an emergency vent 78 comprising a relief valve 80 to protect the capture tank 62. Additionally, the capture tank 62 would further comprise a water outlet 82 to enable water to be removed from the capture tank 62.
  • a fifth conduit 84 may be configured to transport water from the water outlet 82.
  • An isolation valve 86 maybe disposed on the fifth conduit 84.
  • the fifth conduit 84 may be disposed to have a high point 88 which would correspond to the height that water would reach in the capture tank 62.
  • the gas with a high concentration of carbon dioxide 70 may be removed from the apparatus at outlet 90.
  • the gas with a high concentration of carbon dioxide 70 may then be further processed to increase the concentration of carbon dioxide.
  • the gas with a high concentration of carbon dioxide 70 may be transported directly to an oil well for use in EOR.
  • the gas with a high concentration of carbon dioxide 70 could be combined with a flue gas.
  • the flue gas may be fed through an isolation valve 92 into the fourth conduit 74 at a flue gas inlet 94.
  • the gas with a high concentration of carbon dioxide 70 may then be fed through an isolation valve 96 into a further system 98 similar to the one described above, and contacted with water. This will provide an output gas with an even higher concentration of carbon dioxide. This output gas can then be transported to an oil well for use in EOR.
  • Figure 6 is similar to Figure 5, except that the apparatus is designed for pressures exceeding 10-15 bar.
  • the apparatus does not comprise a pressure vessel 50. Instead the first conduit 36 extends between the gas inlet 48 and the capture tank 62. Vents 90 are disposed at multiple high points along the first conduit 36. Each vent comprises a conduit 92 with a flow control/isolation valve 94 disposed thereon. Additionally, the fourth flow control valve/isolation valve 66 and/or an adjustable pressure relief valve 68 are be disposed on the first conduit 35.
  • the inventors’ calculations suggest that if the flue gas 38 has a concentration of >10 vol% C0 2 , then the output gas 48 could comprise about 92 vol% C0 2 . If the C0 2 levels in the flue gas 38 were higher, then higher levels of C0 2 in the output gas could be obtained. As indicated above, if the output gas does not have a high enough concentration of C0 2 it can be contacted with an input liquid, which is subsequently degassed to provide a further output gas with a higher concentration of carbon dioxide.

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  • Environmental & Geological Engineering (AREA)
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  • Oil, Petroleum & Natural Gas (AREA)
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Abstract

La divulgation concerne un appareil d'extraction d'huile. L'appareil comprend un dégazeur et un moyen de transport ou un transporteur. Le dégazeur comprend une chambre de dégazage, une entrée de liquide conçue pour alimenter un liquide d'entrée comprenant du dioxyde de carbone, et/ou un précurseur de celui-ci dissous dans celle-ci dans la chambre de dégazage, et une sortie de liquide, conçue pour éliminer un liquide de sortie de la chambre de dégazage. Le dégazeur est conçu pour dégazer un liquide dans la chambre de dégazage afin d'obtenir un gaz de sortie comprenant du dioxyde de carbone. Le dégazeur comprend en outre une sortie de gaz pour éliminer le gaz de sortie de la chambre de dégazage. Le moyen de transport, ou transporteur, est conçu pour transporter au moins une partie du gaz de sortie vers un réservoir d'huile.
PCT/GB2023/052810 2022-10-31 2023-10-27 Extraction d'huile WO2024094969A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
GB2216114.5 2022-10-31
GBGB2216114.5A GB202216114D0 (en) 2022-10-31 2022-10-31 Oil extraction
GB2217716.6 2022-11-25
GBGB2217716.6A GB202217716D0 (en) 2022-10-31 2022-11-25 Oil extraction

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WO2024094969A1 true WO2024094969A1 (fr) 2024-05-10

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Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007077137A1 (fr) * 2005-12-30 2007-07-12 Shell Internationale Research Maatschappij B.V. Procede de recuperation tertiaire de petrole et procede de sequestration de dioxyde de carbone
GB2521116A (en) * 2013-10-23 2015-06-17 Statoil Petroleum As Method for enhanced hydrocarbon recovery using captured acidic gas
US20170341942A1 (en) * 2016-05-24 2017-11-30 Harper Biotech Llc D/B/A Simbuka Energy, Llc Methods and systems for large scale carbon dioxide utilization from lake kivu via a co2 industrial utilization hub integrated with electric power production and optional cryo-energy storage
US20170342006A1 (en) * 2016-05-26 2017-11-30 Google Inc. Method for efficient co2 degasification
US20180002623A1 (en) * 2014-12-29 2018-01-04 Aker Solutions As Subsea fluid processing system
US20200240255A1 (en) * 2017-10-06 2020-07-30 Oxy Usa Inc. System and method for oil production separation
GB2602806A (en) * 2021-01-14 2022-07-20 Tigre Tech Limited Closed circuit natural gas extraction and sequestration of carbon dioxide

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2007077137A1 (fr) * 2005-12-30 2007-07-12 Shell Internationale Research Maatschappij B.V. Procede de recuperation tertiaire de petrole et procede de sequestration de dioxyde de carbone
GB2521116A (en) * 2013-10-23 2015-06-17 Statoil Petroleum As Method for enhanced hydrocarbon recovery using captured acidic gas
US20180002623A1 (en) * 2014-12-29 2018-01-04 Aker Solutions As Subsea fluid processing system
US20170341942A1 (en) * 2016-05-24 2017-11-30 Harper Biotech Llc D/B/A Simbuka Energy, Llc Methods and systems for large scale carbon dioxide utilization from lake kivu via a co2 industrial utilization hub integrated with electric power production and optional cryo-energy storage
US20170342006A1 (en) * 2016-05-26 2017-11-30 Google Inc. Method for efficient co2 degasification
US20200240255A1 (en) * 2017-10-06 2020-07-30 Oxy Usa Inc. System and method for oil production separation
GB2602806A (en) * 2021-01-14 2022-07-20 Tigre Tech Limited Closed circuit natural gas extraction and sequestration of carbon dioxide

Non-Patent Citations (4)

* Cited by examiner, † Cited by third party
Title
FONT-PALMA ET AL., JOURNAL OF CARBON RESEARCH, vol. 7, 2021, pages 58
GREENHOUSE GASES: SCIENCE AND TECHNOLOGY, vol. 11, no. 5, pages 1076 - 1117
HAN ET AL., JOURNAL OF MEMBRANE SCIENCE, vol. 628, 15 June 2021 (2021-06-15), pages 119244
IULIANELLI ET AL., ADVANCED MEMBRANE SCIENCE AND TECHNOLOGY FOR SUSTAINABLE ENERGY AND ENVIRONMENTAL APPLICATIONS, 2011, pages 184 - 213

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