US20220274063A1 - Wind-Powered Direct Air Carbon Dioxide Capture Device for Ocean Sequestration - Google Patents
Wind-Powered Direct Air Carbon Dioxide Capture Device for Ocean Sequestration Download PDFInfo
- Publication number
- US20220274063A1 US20220274063A1 US17/665,459 US202217665459A US2022274063A1 US 20220274063 A1 US20220274063 A1 US 20220274063A1 US 202217665459 A US202217665459 A US 202217665459A US 2022274063 A1 US2022274063 A1 US 2022274063A1
- Authority
- US
- United States
- Prior art keywords
- brine
- naoh
- wind turbine
- alkaline solution
- desalination
- Prior art date
- Legal status (The legal status 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 status listed.)
- Abandoned
Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims description 75
- 239000001569 carbon dioxide Substances 0.000 title claims description 57
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims description 57
- 230000009919 sequestration Effects 0.000 title abstract description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 246
- 239000012267 brine Substances 0.000 claims abstract description 59
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 59
- 238000010612 desalination reaction Methods 0.000 claims abstract description 24
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 21
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 14
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 22
- 239000012670 alkaline solution Substances 0.000 claims description 19
- 238000005868 electrolysis reaction Methods 0.000 claims description 15
- 238000000746 purification Methods 0.000 claims description 7
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 35
- 238000000034 method Methods 0.000 abstract description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 21
- 230000008569 process Effects 0.000 abstract description 15
- 239000001257 hydrogen Substances 0.000 abstract description 11
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 11
- 239000013505 freshwater Substances 0.000 abstract description 6
- 239000007788 liquid Substances 0.000 abstract description 4
- 238000007599 discharging Methods 0.000 abstract description 2
- 239000003570 air Substances 0.000 description 32
- 239000000243 solution Substances 0.000 description 19
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 14
- UIIMBOGNXHQVGW-UHFFFAOYSA-M Sodium bicarbonate Chemical compound [Na+].OC([O-])=O UIIMBOGNXHQVGW-UHFFFAOYSA-M 0.000 description 10
- 238000010521 absorption reaction Methods 0.000 description 9
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 8
- 239000011780 sodium chloride Substances 0.000 description 7
- 239000007921 spray Substances 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 238000003843 chloralkali process Methods 0.000 description 5
- 239000012530 fluid Substances 0.000 description 5
- 238000012545 processing Methods 0.000 description 5
- 235000017557 sodium bicarbonate Nutrition 0.000 description 5
- 229910000030 sodium bicarbonate Inorganic materials 0.000 description 5
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 4
- 239000003513 alkali Substances 0.000 description 4
- 239000012080 ambient air Substances 0.000 description 4
- 239000000460 chlorine Substances 0.000 description 4
- 229910052801 chlorine Inorganic materials 0.000 description 4
- 238000000909 electrodialysis Methods 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 239000002803 fossil fuel Substances 0.000 description 4
- 150000003839 salts Chemical class 0.000 description 4
- 239000013535 sea water Substances 0.000 description 4
- 229910000029 sodium carbonate Inorganic materials 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 230000006835 compression Effects 0.000 description 3
- 238000007906 compression Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 230000014759 maintenance of location Effects 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 230000000630 rising effect Effects 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 2
- 238000004581 coalescence Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 150000002500 ions Chemical class 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 238000001728 nano-filtration Methods 0.000 description 2
- 239000012466 permeate Substances 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000007704 transition Effects 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical compound OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000004177 carbon cycle Methods 0.000 description 1
- 150000004649 carbonic acid derivatives Chemical class 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- XTEGARKTQYYJKE-UHFFFAOYSA-N chloric acid Chemical compound OCl(=O)=O XTEGARKTQYYJKE-UHFFFAOYSA-N 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000000502 dialysis Methods 0.000 description 1
- 230000003292 diminished effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000004146 energy storage Methods 0.000 description 1
- 239000012527 feed solution Substances 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hcl hcl Chemical compound Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- -1 hydroxide ions Chemical class 0.000 description 1
- 238000010348 incorporation Methods 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000005342 ion exchange Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000010801 machine learning Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 230000037361 pathway Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000012465 retentate Substances 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000002344 surface layer Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Images
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/08—Apparatus therefor
- B01D61/081—Apparatus therefor used at home, e.g. kitchen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/08—Apparatus therefor
-
- B01D61/022—
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
- B01D61/026—Reverse osmosis; Hyperfiltration comprising multiple reverse osmosis steps
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/10—Accessories; Auxiliary operations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D63/00—Apparatus in general for separation processes using semi-permeable membranes
- B01D63/06—Tubular membrane modules
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B1/00—Hydrodynamic or hydrostatic features of hulls or of hydrofoils
- B63B1/02—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement
- B63B1/04—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement with single hull
- B63B1/048—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement with single hull with hull extending principally vertically
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B43/00—Improving safety of vessels, e.g. damage control, not otherwise provided for
- B63B43/02—Improving safety of vessels, e.g. damage control, not otherwise provided for reducing risk of capsizing or sinking
- B63B43/04—Improving safety of vessels, e.g. damage control, not otherwise provided for reducing risk of capsizing or sinking by improving stability
- B63B43/06—Improving safety of vessels, e.g. damage control, not otherwise provided for reducing risk of capsizing or sinking by improving stability using ballast tanks
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B43/00—Improving safety of vessels, e.g. damage control, not otherwise provided for
- B63B43/02—Improving safety of vessels, e.g. damage control, not otherwise provided for reducing risk of capsizing or sinking
- B63B43/10—Improving safety of vessels, e.g. damage control, not otherwise provided for reducing risk of capsizing or sinking by improving buoyancy
- B63B43/14—Improving safety of vessels, e.g. damage control, not otherwise provided for reducing risk of capsizing or sinking by improving buoyancy using outboard floating members
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B77/00—Transporting or installing offshore structures on site using buoyancy forces, e.g. using semi-submersible barges, ballasting the structure or transporting of oil-and-gas platforms
-
- 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/06—External membrane module supporting or fixing means
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/20—Specific housing
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/20—Specific housing
- B01D2313/206—Specific housing characterised by the material
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/36—Energy sources
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/36—Energy sources
- B01D2313/367—Renewable energy sources, e.g. wind or solar sources
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/54—Modularity of membrane module elements
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/56—Specific mechanisms for loading the membrane in a module
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2313/00—Details relating to membrane modules or apparatus
- B01D2313/57—Tools used for removal of membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/06—Submerged-type; Immersion type
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/04—Elements in parallel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/06—Use of membrane modules of the same kind
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B1/00—Hydrodynamic or hydrostatic features of hulls or of hydrofoils
- B63B1/02—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement
- B63B1/10—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement with multiple hulls
- B63B1/107—Semi-submersibles; Small waterline area multiple hull vessels and the like, e.g. SWATH
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B1/00—Hydrodynamic or hydrostatic features of hulls or of hydrofoils
- B63B1/02—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement
- B63B1/04—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement with single hull
- B63B2001/044—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement with single hull with a small waterline area compared to total displacement, e.g. of semi-submersible type
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B1/00—Hydrodynamic or hydrostatic features of hulls or of hydrofoils
- B63B1/02—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement
- B63B1/10—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement with multiple hulls
- B63B1/14—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement with multiple hulls the hulls being interconnected resiliently or having means for actively varying hull shape or configuration
- B63B2001/145—Hydrodynamic or hydrostatic features of hulls or of hydrofoils deriving lift mainly from water displacement with multiple hulls the hulls being interconnected resiliently or having means for actively varying hull shape or configuration having means for actively varying hull shape or configuration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B35/00—Vessels or similar floating structures specially adapted for specific purposes and not otherwise provided for
- B63B35/44—Floating buildings, stores, drilling platforms, or workshops, e.g. carrying water-oil separating devices
- B63B2035/442—Spar-type semi-submersible structures, i.e. shaped as single slender, e.g. substantially cylindrical or trussed vertical bodies
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B35/00—Vessels or similar floating structures specially adapted for specific purposes and not otherwise provided for
- B63B35/44—Floating buildings, stores, drilling platforms, or workshops, e.g. carrying water-oil separating devices
- B63B2035/4433—Floating structures carrying electric power plants
- B63B2035/446—Floating structures carrying electric power plants for converting wind energy into electric energy
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B43/00—Improving safety of vessels, e.g. damage control, not otherwise provided for
- B63B43/02—Improving safety of vessels, e.g. damage control, not otherwise provided for reducing risk of capsizing or sinking
- B63B43/04—Improving safety of vessels, e.g. damage control, not otherwise provided for reducing risk of capsizing or sinking by improving stability
- B63B2043/047—Improving safety of vessels, e.g. damage control, not otherwise provided for reducing risk of capsizing or sinking by improving stability by means of hull shapes comprising a wide hull portion near the design water line, and a slender, buoyancy providing, main hull portion extending towards the bottom
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
- B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING
- B63B39/00—Equipment to decrease pitch, roll, or like unwanted vessel movements; Apparatus for indicating vessel attitude
- B63B39/02—Equipment to decrease pitch, roll, or like unwanted vessel movements; Apparatus for indicating vessel attitude to decrease vessel movements by displacement of masses
- B63B39/03—Equipment to decrease pitch, roll, or like unwanted vessel movements; Apparatus for indicating vessel attitude to decrease vessel movements by displacement of masses by transferring liquids
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/08—Seawater, e.g. for desalination
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/002—Construction details of the apparatus
- C02F2201/007—Modular design
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/008—Mobile apparatus and plants, e.g. mounted on a vehicle
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/009—Apparatus with independent power supply, e.g. solar cells, windpower, fuel cells
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/10—Energy recovery
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2307/00—Location of water treatment or water treatment device
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
- Y02A20/138—Water desalination using renewable energy
- Y02A20/144—Wave energy
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/20—Controlling water pollution; Waste water treatment
- Y02A20/208—Off-grid powered water treatment
- Y02A20/212—Solar-powered wastewater sewage treatment, e.g. spray evaporation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/30—Wastewater or sewage treatment systems using renewable energies
- Y02W10/33—Wastewater or sewage treatment systems using renewable energies using wind energy
Definitions
- This invention relates to the sequestration of atmospheric carbon dioxide.
- CO 2 carbon dioxide
- Carbon dioxide is a greenhouse gas that absorbs and radiates heat from the sun. CO 2 concentrations are rising primarily because fossil fuels are burned for power production, the CO 2 trapping additional heat and raising Earth's average temperature. The scale needed to transform the world's primary energy sources from carbon-emitting fossil fuels to renewable energy is vast. It requires an alarming transition rate, indicating that carbon dioxide capture and storage are imperative to achieving the level of future CO 2 reduction needed to combat global warming and climate change.
- CO 2 is separated from flue gas, compressed, and transported to be sequestered underground.
- Direct ambient air capture (DAC) of CO 2 occurs when ambient air passes across an alkaline solution, such as sodium hydroxide.
- alkaline solution such as sodium hydroxide.
- various DAC methods have proved costly due to the energy needed to process sufficient amounts of air to capture dilute ( ⁇ 419 ppm) atmospheric CO 2 , the cost and delivery of the alkaline feedstock, the transfer and containment of the CO 2 to be sequestered, and the large land area and structures needed for the air processing system.
- Water loss may be substantial in an air capture system as the relatively low concentration of CO 2 in the atmosphere requires a large amount of interaction between the gaseous and the liquid phases. Fresh water availability is a significant problem in many parts of the world. As rising atmospheric temperatures drive changes in the hydrological cycle, water availability for DAC is often limited. In a typical DAC system, water loss is about 20 moles for every mole of CO 2 absorbed (at 15 degrees C. and 65% RH). However, it can be lowered significantly by appropriate design and operating parameters.
- the present invention overcomes these and other deficiencies of the prior art by utilizing an offshore wind turbine for an efficient DAC process.
- Power generated by a wind turbine is applied to drive reverse osmosis (RO) desalination.
- RO reverse osmosis
- NaOH sodium hydroxide
- Direct air capture of CO 2 occurs when liquid NaOH, extracted from the RO desalination brine, is conveyed to the rotor hub and emitted from the wind turbine blades to react with CO 2 in the atmosphere.
- the power of an offshore wind turbine is used for the onboard production of fresh water to supply shoreside water needs while adding the vital process of CO 2 sequestration to the ocean.
- brine processed by electrolysis produces NaOH, chlorine gas (Ch), and hydrogen gas (H 2 ).
- the hydrogen can be captured as fuel for power generation by a fuel cell or by thermal combustion, as needed during times of diminished power from the wind turbine due to low-windspeeds or turbine outage for servicing.
- Hydrogen is also an essential part of the transition away from fossil fuels, particularly for transportation. Offshore wind turbines producing hydrogen can serve the fueling needs of new fuel cell electric marine vessels, trending toward powering by non-fossil fuels. Hydrogen production by electrolysis is energy-intensive, consuming about 55 MWh/tonne of hydrogen. Wind turbine power used for RO desalination must be balanced against the power used for the brine purification, concentration, and electrolysis to yield hydrogen, chlorine, and the sodium hydroxide used for carbon dioxide sequestration.
- the present invention provides significant benefits compared to offshore turbines delivering only electric power and desalinated water to shore. It reduces, if not eliminates, brine discharge into the ocean and provides an additional yield of desalinated water.
- Sodium hydroxide produced from brine and subsequent CO 2 sequestration is achieved with low capital cost and wind energy.
- the present invention produces chlorine, and hydrochloric acid, valued commodities, which can be used in seawater reverse osmosis and NaOH production processes.
- the hydrogen can serve as energy storage for power generation during periods of low production by the wind turbine or sold as higher value “green hydrogen.”
- a direct air carbon dioxide capture device comprises a wind turbine generator comprising one or more blades; a desalination system, wherein the desalination produces brine; means for producing an alkaline solution from the brine; and means for emitting the alkaline solution into an air stream passing through the one or more blades.
- the means for emitting the alkaline solution comprises a plurality of nozzles disposed on the one or more blades.
- the desalination system comprises a reverse osmosis system or an evaporator and condenser. The reverse osmosis system is powered by energy generated by the wind turbine generator.
- the means for producing the alkaline solution comprises a brine purification system and a brine concentration system.
- the brine purification system and the brine concentration system are powered by energy generated by the wind turbine generator.
- the device further comprises an electrolysis system, storage for hydrogen gas, and storage for chlorine gas, wherein the electrolysis system is powered by energy generated by the wind turbine generator.
- the device further comprises a direct electrosynthesis system, wherein the direct electrosynthesis system produces the alkaline solution and hydrochloric acid, the alkaline solution comprising sodium hydroxide.
- the means for producing the alkaline solution comprises a heater using heat from the wind turbine generator.
- the device further comprises a pump for conveying the alkaline solution to the means for emitting the alkaline solution into an air stream passing through the one or more blades, wherein the pump uses centrifugal force induced by the one or more blades.
- a method of capturing atmospheric carbon dioxide for ocean sequestration comprises the steps of generating electric power via a wind turbine generator located in a saltwater environment; desalinating salt water from the saltwater environment, using the electric power generated via the wind turbine generator, to produce brine; processing the brine, using the electric power generated via the wind turbine generator, to produce sodium hydroxide; and emitting the sodium hydroxide solution into an air stream passing through a rotor of the wind turbine generator.
- the step of desalinating saltwater produces fresh water.
- the step of processing the brine comprises the steps of purifying the brine to produce purified brine; increasing salt concentration of the purified brine to produce concentrated brine; and performing electrolysis on the concentrated brine to produce the sodium hydroxide solution, hydrogen gas, and chlorine gas.
- the method further comprises the steps of compressing and storing the hydrogen gas and converting the chlorine gas into a chlorine-based chemical.
- the step of processing the brine comprises the steps of direct electrosynthesis of the sodium hydroxide solution and hydrochloric acid through electrodialysis.
- the step of emitting the sodium hydroxide solution comprises spraying the sodium hydroxide solution via a plurality of nozzles disposed on one or more blades of the wind turbine generator.
- the step of desalinating salt water comprises reverse osmosis or evaporation and condensation.
- the step of processing the brine comprises electrosynthesizing the brine to form the sodium hydroxide solution and hydrochloric acid.
- the method further comprises the step of reacting the emitted sodium hydroxide solution with atmospheric carbon dioxide to form sodium carbonate or sodium bicarbonate.
- the method further comprises the steps of mixing the sodium carbonate or sodium bicarbonate into the saltwater environment and sequestering the sodium carbonate or sodium bicarbonate into the saltwater environment.
- FIG. 1 illustrates a side view of a direct air carbon dioxide capture device according to an embodiment of the invention.
- FIG. 2 illustrates a chlor-alkali NaOH production process implemented on the direct air carbon dioxide capture system shown in FIG. 1 , according to an embodiment of the invention.
- FIG. 3 illustrates a system of direct air carbon dioxide capture devices according to an embodiment of the invention.
- FIGS. 1-3 Preferred embodiments of the present invention and their advantages may be understood by referring to FIGS. 1-3 , wherein like reference numerals refer to like elements.
- the present invention may be deployed in any water environment, preferably where renewable wind energy is available. It can also be configured to use a range of alkaline CO 2 absorbents apart from NaOH.
- the present invention employs an offshore wind turbine system that powers onboard reverse osmosis, producing desalinated water and brine, as disclosed in U.S. patent application Ser. No. 17/163,295, entitled “Wind and Wave Desalination Vessel,” the entire disclosure of which is incorporated by reference herein. There, the brine is dispersed directly back into the ocean. This system is primarily for water supply to land but can also supply marine vessels.
- the present invention advances the utility of an offshore wind turbine powering an onboard desalination plant. Rather than returning the brine to the ocean, it uses a portion of the power generated for on-site brine purification, concentration, and electrolysis. These are essential steps in producing sodium hydroxide for direct ambient air CO 2 absorption for ocean sequestration. Economical and clean wind energy directly powers the mechanical, thermal, and electrochemical process of using the brine recovered from seawater reverse osmosis (SWRO) desalination to produce streams of Na OH, chlorine (Ch), and hydrogen (H 2 ) through the chloralkali process while also increasing the delivery of desalinated water to shore by ⁇ 16%.
- An alternative process involving the direct electrosynthesis of NaOH and hydrochloric acid (HCl) from SWRO brine (through electrodialysis) can also be used depending on the required outputs.
- the direct ambient air capture (DAC) system of the present invention is added to a wind turbine platform designed for reverse osmosis (RO) desalination. There are added costs for the equipment used to process the otherwise discharged brine, and a fraction of the power generated by the turbine is needed to produce NaOH, H 2 . Ch and HCl.
- FIG. 1 illustrates a side view of a direct air carbon dioxide capture device 100 according to an embodiment of the invention.
- System 100 comprises a wind turbine generator (WTG) 110 with rotor blades 112 , a tower (mast) 120 , a spar buoy 130 including a main buoyancy section 132 , a cylindrical section 134 , and a ballast section 136 .
- WTG wind turbine generator
- mast tower
- spar buoy 130 including a main buoyancy section 132 , a cylindrical section 134 , and a ballast section 136 .
- deck 133 of the buoyancy chamber 132 joins the mast 120 on which mounts the tower base of the WTG 110 .
- a reverse osmosis system 140 Housed within the buoyancy chamber 132 and the cylindrical section 134 or a portion thereof.
- a NaOH solution is piped (as shown by dotted line) to the wind turbine's blades 112 , which serve as a “rotator contactor,” emitting the solution through nozzles 114 as a fine mist 116 , into the wind 118 streaming through the rotor disc.
- Atmospheric CO 2 is absorbed by the NaOH mist, forming sodium carbonate and sodium hydrogen carbonate (“sodium bicarbonate”).
- the carbonate droplets are drawn by gravity to the surface layer of the ocean, where mixing by the orbital action of waves leads to increased levels of dissolved carbonates and gradual capture by marine organisms and incorporation into the natural carbon cycle.
- the reaction solution drops landing on the ocean are mildly alkaline, comprising a mixture of carbonate, bicarbonate, and unreacted hydroxide ions.
- the present invention therefore, has the potential to locally reduce ocean acidity with the associated benefits to marine ecosystems.
- the component of the present invention that enables the NaOH to absorb atmospheric CO 2 is termed the “contactor.”
- the turbine rotor contactor disperses the NaOH produced onboard through nozzles 114 on the turbine blades 112 to react with the dilute, ⁇ 419 ppm atmospheric CO 2 . Since CO 2 is so dilute in air, the contactor must have a large crosssectional area and sufficient airflow to process the large volumes of air required for CO 2 absorption.
- Wind turbine rotors provide an ideal means of exposure to large volumes of air. For example, a 10 MW wind turbine with a 220 m rotor has a swept area of 38,000 m2 (about 9.4 acres).
- the volume of air passing through the rotor in one hour is about 1 billion m3, with an air stream run of 29 km and an air mass transport of air of 1.37 million tons.
- a rotor of this size operates at about 8 to 10 rpm with blade tip speeds typically exceeding 150 mph (240 kmph).
- the NaOH misting from the blade nozzles 114 interacts with the surrounding air stream 118 , dispersing through the air mass flowing across the rotor, forming a spiraling wake from the turbine blades and mixing the NaOH droplets and CO 2 by the vortices and wind shear.
- the selected blades determine optimization for the number of nozzles, fluid pressure, flow rate, and spray density. Control of droplet size is critical for efficient CO 2 absorption, with the ideal droplet diameter being 50 to 100 microns.
- the nozzles operate within this droplet size range, on pressures ranging from 100 to 620 kPa, producing various flow rates and spray patterns.
- Nozzle selection is based upon the desired NaOH concentration, which is expected to be in the range of 0.35 and 5 molar (M) solution.
- the lower end of the range represents a dilute state, with viscosity and vapor pressure about the same as water.
- a 5M solution, with about a 20 wt. % sodium hydroxide represents the high end of the range with a solution viscosity about three times that of water.
- blade nozzle emitters are placed at points on the airfoil that minimally impact the aerodynamic efficiency of the blade. Diligent design of the nozzle array and spray patterns will optimize NaOH concentration in the air stream, spray patterns, and drop size—minimizing unfavorable drop coalescence.
- Efficient absorption of ambient atmospheric CO 2 requires large volumes of air flowing through the rotor contactor.
- the design of the blade-contactor ensures a spray pattern where the NaOH has sufficient air retention time for absorption before drop coalescence, which sharply reduces CO 2 absorption capacity.
- the preferred embodiment uses a turbine tower height of greater than 80 meters to provide sufficient droplet air retention time and promote maximum CO 2 absorption before reaching the ocean surface.
- the present invention includes integrating wind turbine power production with desalination and NaOH production, balancing the processes to optimize sodium hydroxide delivery to combine with diffuse atmospheric carbon dioxide.
- a system controller uses machine learning to optimize the complete process of wind turbine variable power for NaOH production and maximize the efficiency of each step of the process chain with automated control of flow paths, flow rates, and solution concentrations, and chemical ratios.
- RO reverse osmosis
- FIG. 2 illustrates a chlor-alkali NaOH production process 200 implemented by the direct air carbon dioxide capture device 100 , according to an embodiment of the invention.
- Brine from seawater reverse osmosis is passed through nano-filters (Step 210 ) to reduce harmful concentrations of ions such as Ca++ and Mg++.
- the brine permeate from this step has ⁇ 5 wt. % NaCl. The retentate is discarded.
- the brine from nanofiltration is passed through electrodialysis (ED, Step 220 ) to increase the salt concentration to ⁇ 20% where the solution is saturated, mainly with sodium chloride (NaCl).
- the brine from ED is concentrated further to about 26% using either evaporation or mechanical vapor compression (MVC, Step 230 ).
- MVC mechanical vapor compression
- Step 240 the remaining hardness ions in the brine are removed by chemical softening (Step 240 ) and ion exchange (Step 250 ).
- HCl is added (Step 260 ) to lower pH, which along with system losses of MVC (or the evaporator) accounts for about 10% of the energy used internally, a small amount of energy use compared with Steps 210 , 220 , and 230 .
- Electrolysis uses an electric current to drive a chemical reaction that otherwise would not occur spontaneously.
- Electrolysis (Step 270 ) of the concentrated brine produces aqueous NaOH and gaseous Ch and H 2 .
- the NaOH solution sprayed from nozzles of the rotorcontactor reacts with the CO 2 in the airstream, initiating sequestration.
- the efficiency of step 270 can be improved by using turbine generator heat transferred through a heat exchanger for preheating the concentrated brine before passing it to the electrolyzer.
- One kilogram of 26 wt % brine entering the electrolyzer contains 260 g or 4.45 moles of NaCl. For every mole of NaCl consumed, a mole of NaOH is produced, therefore maximum production from electrolysis will be 4.45 moles or 0.178 kg of NaOH per kg of brine.
- Step 270 uses direct electrosynthesis (DE) of sodium hydroxide and hydrochloric acid produced from the brine stream.
- DE direct electrosynthesis
- This technique produces NaOH without the costly purification and concentration of the chlor-alkali process.
- Electrosynthesis of NaOH and HCl uses less energy than electrolysis, at 1.8 MWh per tonne of NaOH, but it produces a much lower concentration of NaOH ( ⁇ 2 M), or about 44 g of HCl per kilogram of brine (7 wt. %).
- Hydrochloric acid is a valuable by-product of DE that is fed back into the SWRO and NaOH production processes to lower the pH of the feed solution.
- the power generated by the selected wind turbine must balance between the amount of energy consumed by RO desalination and the amount needed for NaOH production and spray emission.
- Energy consumption estimates for onboard NaOH production include the more costly evaporation method of the chlor-alkali process as an upper reference point.
- mechanical vapor compression (MVC) is used to concentrate brine from 20% to 26%, as it consumes less than 10% of the energy needed by evaporative concentration.
- Optimizing NaOH production involves maximizing the efficiency of each step using automated control of flow paths, flow rates, solution concentrations, and chemical ratios.
- the maximum stoichiometric yield of NaOH (dry equivalent) is 48 g per kilogram of 7 wt. % brine. Losses in yield can result from equipment voltage losses, loss of membrane efficiency, and the need to divert and purge parts of the waste stream.
- Input brine (7 wt. % NaCl) fed through the chlor-alkali process produces a maximum of 48 g of NaOH, yielding 42 g of chlorine gas and 1.2 g of hydrogen gas.
- the energy needed for NaOH conveyance to the contactor and NaOH solution misting includes pumping the NaOH fluid to tower height and for the fluid nozzle pressure over the number of nozzles used.
- the centrifugal force of the fluid reduces this pumping energy load in the blade pipes as the rotor spins.
- the 10 MW turbine, with a 220 m rotor at 10 rpm has blade tip nozzle pressure of 880 psi or 6,067 kPa, well above the pumping pressure needed for lifting the fluid 100 m (979 kPa or 142 psi) and nozzle pressure (100 kPa to 620 kPa).
- the efficiency of NaOH production and the emission from the rotor contactor are factors in sizing the NaOH production chain along with the turbine output related to windspeed distribution and variability at the specific operating site.
- the amount of electric power consumed for desalination is balanced against the power needed for Na OH production. More production of NaOH requires more energy; then less energy is available for desalination, reducing the amount of brine feedstock, thus limiting the capacity of NaOH production.
- a 10 MW turbine operating at 50% of net rated capacity generates ⁇ 44,000 MW hours of power per year.
- the 20% of power generated a balance of 8,800 MWh, is available for NaOH production through the chlor-alkali process.
- the primary energy load is the membrane electrolyzer, consuming about three-quarters of the total operating energy load, which amounts to ⁇ 6,600 MWh of the 8,800 MWh available.
- Energy consumption is based on a process model for NaOH with a production rate of 64.8 kg/h (dry) or about 570 tonnes/MW per year.
- Example 10 MW turbine, using 20% of its power, or 8,800 MWh for NaOH production, consumes 3.17 MWh/tonne, thereby yielding 2,776 tonnes of NaOH per year.
- To capture one ton of CO 2 requires at least 0.9 ton of NaOH.
- the blade contactor emitting a solution containing 2,776 tonnes of NaOH (dry equivalent), would capture 3,084 tonnes of CO 2 per year.
- the DAC device controller is programmed to ensure optimal air to liquid (NaOH) mass flow ratios at selected NaOH concentrations.
- NaOH air to liquid
- Using this data for the 10 MW turbine with a rotor contactor area of 38,000 m2 indicates CO 2 capture could reach 15,200 tons of CO 2 per year if sufficient NaOH is available.
- NaOH production is limited by turbine power production and the allocation of available energy between SWRO desalination and NaOH production.
- FIG. 3 illustrates a system of direct air carbon dioxide capture devices 100 according to an embodiment of the invention.
Abstract
Description
- The present application claims priority to and is a divisional application of U.S. patent application Ser. No. 17/391,884, filed on Aug. 2, 2021, and entitled “Wind-Powered Direct Air Carbon Dioxide Capture For Ocean Sequestration,” which is a continuation of U.S. patent application Ser. No. 17/163,295, entitled “Wind and Wave Desalination Vessel,” and filed on Jan. 29, 2021, which is a continuation-in-part of U.S. patent application Ser. No. 17/087,309, entitled “Reverse Osmosis Water Production Apparatus,” and filed on Nov. 2, 2020, which claims priority to U.S. patent application Ser. No. 16/129,783, entitled “Reverse Osmosis Water Production Apparatus,” and filed on Sep. 12, 2018, the entire disclosures of which hare all incorporated by reference herein.
- This invention relates to the sequestration of atmospheric carbon dioxide.
- To mitigate global heating, deep reductions in carbon dioxide (CO2) emissions are required to reduce atmospheric CO2 concentration. Carbon dioxide is a greenhouse gas that absorbs and radiates heat from the sun. CO2 concentrations are rising primarily because fossil fuels are burned for power production, the CO2 trapping additional heat and raising Earth's average temperature. The scale needed to transform the world's primary energy sources from carbon-emitting fossil fuels to renewable energy is vast. It requires an alarming transition rate, indicating that carbon dioxide capture and storage are imperative to achieving the level of future CO2 reduction needed to combat global warming and climate change.
- Current techniques for carbon capture are directed at capturing CO2 from large stationary sources, such as power plants. Typically, CO2 is separated from flue gas, compressed, and transported to be sequestered underground.
- Direct ambient air capture (DAC) of CO2 occurs when ambient air passes across an alkaline solution, such as sodium hydroxide. However, various DAC methods have proved costly due to the energy needed to process sufficient amounts of air to capture dilute (−419 ppm) atmospheric CO2, the cost and delivery of the alkaline feedstock, the transfer and containment of the CO2 to be sequestered, and the large land area and structures needed for the air processing system.
- Water loss may be substantial in an air capture system as the relatively low concentration of CO2 in the atmosphere requires a large amount of interaction between the gaseous and the liquid phases. Fresh water availability is a significant problem in many parts of the world. As rising atmospheric temperatures drive changes in the hydrological cycle, water availability for DAC is often limited. In a typical DAC system, water loss is about 20 moles for every mole of CO2 absorbed (at 15 degrees C. and 65% RH). However, it can be lowered significantly by appropriate design and operating parameters.
- It is compelling to look beyond land-based CO2 sequestration to the oceans, for both process water availability and the sequestration of CO2, mimicking parts of the natural cycle of ocean CO2 absorption and helping to reduce the acidification of the oceans. Rising atmospheric CO2 has led to more CO2 dissolving into the sea and a drop in average pH (now about 8.1).
- The present invention overcomes these and other deficiencies of the prior art by utilizing an offshore wind turbine for an efficient DAC process. Power generated by a wind turbine is applied to drive reverse osmosis (RO) desalination. Rather than discharging the resulting brine back into the ocean, it is concentrated and modified through industrial-scale processes to produce sodium hydroxide (NaOH). Direct air capture of CO2 occurs when liquid NaOH, extracted from the RO desalination brine, is conveyed to the rotor hub and emitted from the wind turbine blades to react with CO2 in the atmosphere. The power of an offshore wind turbine is used for the onboard production of fresh water to supply shoreside water needs while adding the vital process of CO2 sequestration to the ocean.
- In addition to delivering fresh water to shore, brine processed by electrolysis produces NaOH, chlorine gas (Ch), and hydrogen gas (H2). The hydrogen can be captured as fuel for power generation by a fuel cell or by thermal combustion, as needed during times of diminished power from the wind turbine due to low-windspeeds or turbine outage for servicing.
- Hydrogen is also an essential part of the transition away from fossil fuels, particularly for transportation. Offshore wind turbines producing hydrogen can serve the fueling needs of new fuel cell electric marine vessels, trending toward powering by non-fossil fuels. Hydrogen production by electrolysis is energy-intensive, consuming about 55 MWh/tonne of hydrogen. Wind turbine power used for RO desalination must be balanced against the power used for the brine purification, concentration, and electrolysis to yield hydrogen, chlorine, and the sodium hydroxide used for carbon dioxide sequestration.
- The present invention provides significant benefits compared to offshore turbines delivering only electric power and desalinated water to shore. It reduces, if not eliminates, brine discharge into the ocean and provides an additional yield of desalinated water. Sodium hydroxide produced from brine and subsequent CO2 sequestration is achieved with low capital cost and wind energy. In addition to hydrogen, the present invention produces chlorine, and hydrochloric acid, valued commodities, which can be used in seawater reverse osmosis and NaOH production processes. The hydrogen can serve as energy storage for power generation during periods of low production by the wind turbine or sold as higher value “green hydrogen.”
- In an embodiment of the invention, a direct air carbon dioxide capture device comprises a wind turbine generator comprising one or more blades; a desalination system, wherein the desalination produces brine; means for producing an alkaline solution from the brine; and means for emitting the alkaline solution into an air stream passing through the one or more blades. The means for emitting the alkaline solution comprises a plurality of nozzles disposed on the one or more blades. The desalination system comprises a reverse osmosis system or an evaporator and condenser. The reverse osmosis system is powered by energy generated by the wind turbine generator. The means for producing the alkaline solution comprises a brine purification system and a brine concentration system. The brine purification system and the brine concentration system are powered by energy generated by the wind turbine generator. The device further comprises an electrolysis system, storage for hydrogen gas, and storage for chlorine gas, wherein the electrolysis system is powered by energy generated by the wind turbine generator. The device further comprises a direct electrosynthesis system, wherein the direct electrosynthesis system produces the alkaline solution and hydrochloric acid, the alkaline solution comprising sodium hydroxide. The means for producing the alkaline solution comprises a heater using heat from the wind turbine generator. The device further comprises a pump for conveying the alkaline solution to the means for emitting the alkaline solution into an air stream passing through the one or more blades, wherein the pump uses centrifugal force induced by the one or more blades.
- In another embodiment of the invention, a method of capturing atmospheric carbon dioxide for ocean sequestration comprises the steps of generating electric power via a wind turbine generator located in a saltwater environment; desalinating salt water from the saltwater environment, using the electric power generated via the wind turbine generator, to produce brine; processing the brine, using the electric power generated via the wind turbine generator, to produce sodium hydroxide; and emitting the sodium hydroxide solution into an air stream passing through a rotor of the wind turbine generator. The step of desalinating saltwater produces fresh water. The step of processing the brine comprises the steps of purifying the brine to produce purified brine; increasing salt concentration of the purified brine to produce concentrated brine; and performing electrolysis on the concentrated brine to produce the sodium hydroxide solution, hydrogen gas, and chlorine gas. The method further comprises the steps of compressing and storing the hydrogen gas and converting the chlorine gas into a chlorine-based chemical. The step of processing the brine comprises the steps of direct electrosynthesis of the sodium hydroxide solution and hydrochloric acid through electrodialysis. The step of emitting the sodium hydroxide solution comprises spraying the sodium hydroxide solution via a plurality of nozzles disposed on one or more blades of the wind turbine generator. The step of desalinating salt water comprises reverse osmosis or evaporation and condensation. The step of processing the brine comprises electrosynthesizing the brine to form the sodium hydroxide solution and hydrochloric acid. The method further comprises the step of reacting the emitted sodium hydroxide solution with atmospheric carbon dioxide to form sodium carbonate or sodium bicarbonate. The method further comprises the steps of mixing the sodium carbonate or sodium bicarbonate into the saltwater environment and sequestering the sodium carbonate or sodium bicarbonate into the saltwater environment.
- The foregoing and other features and advantages of the invention will be apparent from the following, more particular description of the invention's preferred embodiments, as shown in the accompanying drawings and the claims.
- For a complete understanding of the present invention and its advantages, reference is now made to the ensuing descriptions taken in connection with the accompanying drawings briefly described as follows.
-
FIG. 1 illustrates a side view of a direct air carbon dioxide capture device according to an embodiment of the invention. -
FIG. 2 illustrates a chlor-alkali NaOH production process implemented on the direct air carbon dioxide capture system shown inFIG. 1 , according to an embodiment of the invention. -
FIG. 3 illustrates a system of direct air carbon dioxide capture devices according to an embodiment of the invention. - Preferred embodiments of the present invention and their advantages may be understood by referring to
FIGS. 1-3 , wherein like reference numerals refer to like elements. The present invention may be deployed in any water environment, preferably where renewable wind energy is available. It can also be configured to use a range of alkaline CO2 absorbents apart from NaOH. - The present invention employs an offshore wind turbine system that powers onboard reverse osmosis, producing desalinated water and brine, as disclosed in U.S. patent application Ser. No. 17/163,295, entitled “Wind and Wave Desalination Vessel,” the entire disclosure of which is incorporated by reference herein. There, the brine is dispersed directly back into the ocean. This system is primarily for water supply to land but can also supply marine vessels.
- The present invention advances the utility of an offshore wind turbine powering an onboard desalination plant. Rather than returning the brine to the ocean, it uses a portion of the power generated for on-site brine purification, concentration, and electrolysis. These are essential steps in producing sodium hydroxide for direct ambient air CO2 absorption for ocean sequestration. Economical and clean wind energy directly powers the mechanical, thermal, and electrochemical process of using the brine recovered from seawater reverse osmosis (SWRO) desalination to produce streams of Na OH, chlorine (Ch), and hydrogen (H2) through the chloralkali process while also increasing the delivery of desalinated water to shore by −16%. An alternative process involving the direct electrosynthesis of NaOH and hydrochloric acid (HCl) from SWRO brine (through electrodialysis) can also be used depending on the required outputs.
- The direct ambient air capture (DAC) system of the present invention is added to a wind turbine platform designed for reverse osmosis (RO) desalination. There are added costs for the equipment used to process the otherwise discharged brine, and a fraction of the power generated by the turbine is needed to produce NaOH, H2. Ch and HCl.
-
FIG. 1 illustrates a side view of a direct air carbondioxide capture device 100 according to an embodiment of the invention.System 100 comprises a wind turbine generator (WTG) 110 withrotor blades 112, a tower (mast) 120, aspar buoy 130 including amain buoyancy section 132, acylindrical section 134, and aballast section 136. Above the ocean surface,deck 133 of thebuoyancy chamber 132 joins themast 120 on which mounts the tower base of theWTG 110. Housed within thebuoyancy chamber 132 and thecylindrical section 134 or a portion thereof is areverse osmosis system 140. - A NaOH solution is piped (as shown by dotted line) to the wind turbine's
blades 112, which serve as a “rotator contactor,” emitting the solution throughnozzles 114 as afine mist 116, into thewind 118 streaming through the rotor disc. Atmospheric CO2 is absorbed by the NaOH mist, forming sodium carbonate and sodium hydrogen carbonate (“sodium bicarbonate”). The carbonate droplets are drawn by gravity to the surface layer of the ocean, where mixing by the orbital action of waves leads to increased levels of dissolved carbonates and gradual capture by marine organisms and incorporation into the natural carbon cycle. - The reaction solution drops landing on the ocean are mildly alkaline, comprising a mixture of carbonate, bicarbonate, and unreacted hydroxide ions. The present invention, therefore, has the potential to locally reduce ocean acidity with the associated benefits to marine ecosystems.
- The component of the present invention that enables the NaOH to absorb atmospheric CO2 is termed the “contactor.” The turbine rotor contactor disperses the NaOH produced onboard through
nozzles 114 on theturbine blades 112 to react with the dilute, −419 ppm atmospheric CO2. Since CO2 is so dilute in air, the contactor must have a large crosssectional area and sufficient airflow to process the large volumes of air required for CO2 absorption. Wind turbine rotors provide an ideal means of exposure to large volumes of air. For example, a 10 MW wind turbine with a 220 m rotor has a swept area of 38,000 m2 (about 9.4 acres). In an 8 m/s wind regime, the volume of air passing through the rotor in one hour is about 1 billion m3, with an air stream run of 29 km and an air mass transport of air of 1.37 million tons. A rotor of this size operates at about 8 to 10 rpm with blade tip speeds typically exceeding 150 mph (240 kmph). The NaOH misting from theblade nozzles 114 interacts with the surroundingair stream 118, dispersing through the air mass flowing across the rotor, forming a spiraling wake from the turbine blades and mixing the NaOH droplets and CO2 by the vortices and wind shear. - The selected blades determine optimization for the number of nozzles, fluid pressure, flow rate, and spray density. Control of droplet size is critical for efficient CO2 absorption, with the ideal droplet diameter being 50 to 100 microns. The nozzles operate within this droplet size range, on pressures ranging from 100 to 620 kPa, producing various flow rates and spray patterns.
- Nozzle selection is based upon the desired NaOH concentration, which is expected to be in the range of 0.35 and 5 molar (M) solution. The lower end of the range represents a dilute state, with viscosity and vapor pressure about the same as water. A 5M solution, with about a 20 wt. % sodium hydroxide represents the high end of the range with a solution viscosity about three times that of water.
- In an embodiment of the invention, blade nozzle emitters are placed at points on the airfoil that minimally impact the aerodynamic efficiency of the blade. Diligent design of the nozzle array and spray patterns will optimize NaOH concentration in the air stream, spray patterns, and drop size—minimizing unfavorable drop coalescence.
- Efficient absorption of ambient atmospheric CO2 requires large volumes of air flowing through the rotor contactor. The design of the blade-contactor ensures a spray pattern where the NaOH has sufficient air retention time for absorption before drop coalescence, which sharply reduces CO2 absorption capacity. The preferred embodiment uses a turbine tower height of greater than 80 meters to provide sufficient droplet air retention time and promote maximum CO2 absorption before reaching the ocean surface.
- The present invention includes integrating wind turbine power production with desalination and NaOH production, balancing the processes to optimize sodium hydroxide delivery to combine with diffuse atmospheric carbon dioxide. In an embodiment of the invention, a system controller uses machine learning to optimize the complete process of wind turbine variable power for NaOH production and maximize the efficiency of each step of the process chain with automated control of flow paths, flow rates, and solution concentrations, and chemical ratios.
- Desalination by reverse osmosis (RO) increases seawater salinity of 3.5 wt. % to 7 wt. % and requires 3.0-4.5 kilowatt-hours per cubic meter of permeate (product water). The energy consumed in NaOH production ranges from 3.17 MWh to 6.00 MWh per tonne, depending on the method of brine concentration used (as shown in Table 1).
- The power generated by
WTG 110 determines the amount of desalinated water produced, which is about the same volume as the brine available for NaOH production.FIG. 2 illustrates a chlor-alkali NaOH production process 200 implemented by the direct air carbondioxide capture device 100, according to an embodiment of the invention. Brine from seawater reverse osmosis is passed through nano-filters (Step 210) to reduce harmful concentrations of ions such as Ca++ and Mg++. The brine permeate from this step has −5 wt. % NaCl. The retentate is discarded. The brine from nanofiltration is passed through electrodialysis (ED, Step 220) to increase the salt concentration to −20% where the solution is saturated, mainly with sodium chloride (NaCl). The brine from ED is concentrated further to about 26% using either evaporation or mechanical vapor compression (MVC, Step 230). Prior to electrolysis, the remaining hardness ions in the brine are removed by chemical softening (Step 240) and ion exchange (Step 250). HCl is added (Step 260) to lower pH, which along with system losses of MVC (or the evaporator) accounts for about 10% of the energy used internally, a small amount of energy use compared withSteps - Electrolysis uses an electric current to drive a chemical reaction that otherwise would not occur spontaneously. Electrolysis (Step 270) of the concentrated brine produces aqueous NaOH and gaseous Ch and H2. The NaOH solution sprayed from nozzles of the rotorcontactor reacts with the CO2 in the airstream, initiating sequestration. The efficiency of
step 270 can be improved by using turbine generator heat transferred through a heat exchanger for preheating the concentrated brine before passing it to the electrolyzer. - One kilogram of 26 wt % brine entering the electrolyzer contains 260 g or 4.45 moles of NaCl. For every mole of NaCl consumed, a mole of NaOH is produced, therefore maximum production from electrolysis will be 4.45 moles or 0.178 kg of NaOH per kg of brine.
- An alternative or additional pathway to that described in
Step 270 uses direct electrosynthesis (DE) of sodium hydroxide and hydrochloric acid produced from the brine stream. This technique produces NaOH without the costly purification and concentration of the chlor-alkali process. Electrosynthesis of NaOH and HCl uses less energy than electrolysis, at 1.8 MWh per tonne of NaOH, but it produces a much lower concentration of NaOH (−2 M), or about 44 g of HCl per kilogram of brine (7 wt. %). Hydrochloric acid is a valuable by-product of DE that is fed back into the SWRO and NaOH production processes to lower the pH of the feed solution. - The power generated by the selected wind turbine must balance between the amount of energy consumed by RO desalination and the amount needed for NaOH production and spray emission. Energy consumption estimates for onboard NaOH production (Table 1) include the more costly evaporation method of the chlor-alkali process as an upper reference point. In the preferred embodiment of the invention, mechanical vapor compression (MVC) is used to concentrate brine from 20% to 26%, as it consumes less than 10% of the energy needed by evaporative concentration.
-
TABLE 1 Energy use estimates for chlor-alkali production of NaOH from RO desalination brine are shown per tonne dry weight of NaOH. Energy use NaCl wt. % MWh/t NaOH Process step Input Output MVC Evap. 210 Nanofiltration 7 7 0.17 220 Electrodialysis 7 20 0.41 230 MVC/(Evaporation) 20 26 0.24 (3.07) 270 Electrolysis 26 2.35 Total MWhr/t of NaOH 3.17 (6.00) - A minimum energy of 3.17 megawatt-hours per tonne of NaOH produced is required to bring about the chlor-alkali reactions. Optimizing NaOH production involves maximizing the efficiency of each step using automated control of flow paths, flow rates, solution concentrations, and chemical ratios.
- The maximum stoichiometric yield of NaOH (dry equivalent) is 48 g per kilogram of 7 wt. % brine. Losses in yield can result from equipment voltage losses, loss of membrane efficiency, and the need to divert and purge parts of the waste stream. Input brine (7 wt. % NaCl) fed through the chlor-alkali process produces a maximum of 48 g of NaOH, yielding 42 g of chlorine gas and 1.2 g of hydrogen gas.
- The energy needed for NaOH conveyance to the contactor and NaOH solution misting includes pumping the NaOH fluid to tower height and for the fluid nozzle pressure over the number of nozzles used. The centrifugal force of the fluid reduces this pumping energy load in the blade pipes as the rotor spins. For example, the 10 MW turbine, with a 220 m rotor at 10 rpm has blade tip nozzle pressure of 880 psi or 6,067 kPa, well above the pumping pressure needed for lifting the fluid 100 m (979 kPa or 142 psi) and nozzle pressure (100 kPa to 620 kPa).
- The efficiency of NaOH production and the emission from the rotor contactor are factors in sizing the NaOH production chain along with the turbine output related to windspeed distribution and variability at the specific operating site. The amount of electric power consumed for desalination is balanced against the power needed for Na OH production. More production of NaOH requires more energy; then less energy is available for desalination, reducing the amount of brine feedstock, thus limiting the capacity of NaOH production.
- For example, a 10 MW turbine operating at 50% of net rated capacity generates ˜44,000 MW hours of power per year.
- By using 80% of the power −35,200 MWh and consuming 3.5 kWh per m3 for SWRO desalination, the annual production of brine is 10.06 million m3. By adding brine dialysis in
Step 220, freshwater production is increased 16% to 11.7 million m3. In the preferred embodiment of the present invention, mechanical vapor compression (MVC) is used forStep 230, where brine concentration increases from 20% to 26%. Using MVC in NaOH production consumes 3.17 MWh per ton of Na OH (Table 1). - The 20% of power generated, a balance of 8,800 MWh, is available for NaOH production through the chlor-alkali process. Here, the primary energy load is the membrane electrolyzer, consuming about three-quarters of the total operating energy load, which amounts to −6,600 MWh of the 8,800 MWh available. Energy consumption is based on a process model for NaOH with a production rate of 64.8 kg/h (dry) or about 570 tonnes/MW per year.
- The Example 10 MW turbine, using 20% of its power, or 8,800 MWh for NaOH production, consumes 3.17 MWh/tonne, thereby yielding 2,776 tonnes of NaOH per year. To capture one ton of CO2 requires at least 0.9 ton of NaOH. Thus the blade contactor, emitting a solution containing 2,776 tonnes of NaOH (dry equivalent), would capture 3,084 tonnes of CO2 per year.
- The DAC device controller is programmed to ensure optimal air to liquid (NaOH) mass flow ratios at selected NaOH concentrations. Studies based on air tunnel-type tests using an open air flow, sprayed with NaOH with an air/liquid mass flow ratio of 8.3 and a drop residence of 3 meters, indicated an absorption rate of 0.4 tonne of CO2 per m2 contactor area. Using this data for the 10 MW turbine with a rotor contactor area of 38,000 m2 indicates CO2 capture could reach 15,200 tons of CO2 per year if sufficient NaOH is available. However, NaOH production is limited by turbine power production and the allocation of available energy between SWRO desalination and NaOH production.
-
FIG. 3 illustrates a system of direct air carbondioxide capture devices 100 according to an embodiment of the invention. - The invention has been described herein using specific embodiments for illustration only. However, it will be readily apparent to one of ordinary skill in the art that the invention's principles can be embodied in other ways. Therefore, the invention should not be regarded as limited in scope to the specific embodiments disclosed herein; it should be fully commensurate in scope with the following claims.
Claims (10)
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US17/665,459 US20220274063A1 (en) | 2017-09-22 | 2022-02-04 | Wind-Powered Direct Air Carbon Dioxide Capture Device for Ocean Sequestration |
Applications Claiming Priority (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
NZ735748 | 2017-09-22 | ||
NZ735748A NZ735748A (en) | 2017-09-22 | 2017-09-22 | Reverse osmosis water production apparatus |
US16/129,783 US20190091629A1 (en) | 2017-09-22 | 2018-09-12 | Reverse osmosis water production apparatus |
US17/087,309 US20210046422A1 (en) | 2017-09-22 | 2020-11-02 | Reverse osmosis water production apparatus |
US17/163,295 US11660572B2 (en) | 2017-09-22 | 2021-01-29 | Wind and wave desalination vessel |
US17/391,884 US20210362094A1 (en) | 2017-09-22 | 2021-08-02 | Wind-Powered Direct Air Carbon Dioxide Capture for Ocean Sequestration |
US17/665,459 US20220274063A1 (en) | 2017-09-22 | 2022-02-04 | Wind-Powered Direct Air Carbon Dioxide Capture Device for Ocean Sequestration |
Related Parent Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US17/391,884 Division US20210362094A1 (en) | 2017-09-22 | 2021-08-02 | Wind-Powered Direct Air Carbon Dioxide Capture for Ocean Sequestration |
Publications (1)
Publication Number | Publication Date |
---|---|
US20220274063A1 true US20220274063A1 (en) | 2022-09-01 |
Family
ID=75909762
Family Applications (3)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US17/163,295 Active US11660572B2 (en) | 2017-09-22 | 2021-01-29 | Wind and wave desalination vessel |
US17/391,884 Abandoned US20210362094A1 (en) | 2017-09-22 | 2021-08-02 | Wind-Powered Direct Air Carbon Dioxide Capture for Ocean Sequestration |
US17/665,459 Abandoned US20220274063A1 (en) | 2017-09-22 | 2022-02-04 | Wind-Powered Direct Air Carbon Dioxide Capture Device for Ocean Sequestration |
Family Applications Before (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US17/163,295 Active US11660572B2 (en) | 2017-09-22 | 2021-01-29 | Wind and wave desalination vessel |
US17/391,884 Abandoned US20210362094A1 (en) | 2017-09-22 | 2021-08-02 | Wind-Powered Direct Air Carbon Dioxide Capture for Ocean Sequestration |
Country Status (1)
Country | Link |
---|---|
US (3) | US11660572B2 (en) |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20190219026A1 (en) * | 2018-01-17 | 2019-07-18 | Lone Gull Holdings, Ltd. | Self-powered, self-propelled computer grid with loop topology |
JP2021079315A (en) * | 2019-11-15 | 2021-05-27 | 株式会社東芝 | Water treatment apparatus and water treatment method |
DE102021113385B4 (en) * | 2021-05-25 | 2023-02-23 | Aerodyn Consulting Singapore Pte Ltd | Floating wind turbine |
US11685679B2 (en) * | 2021-06-20 | 2023-06-27 | Jianchao Shu | 100 % renewably -powered desalination /water purification station |
US11465925B1 (en) * | 2022-01-13 | 2022-10-11 | Heimdal Limited | Carbon capture method and system |
NO347215B1 (en) * | 2021-10-08 | 2023-07-10 | Niels Christian Olsen | Floating foundation for wind turbine generators and a method for instalment |
CN113955859B (en) * | 2021-11-15 | 2022-07-01 | 中建中环工程有限公司 | Automatically regulated ecological landscape body with sewage purification function |
CN114031154A (en) * | 2021-11-19 | 2022-02-11 | 东北电力大学 | Offshore wind power delivery method utilizing seawater desalination technology |
US20230286845A1 (en) * | 2022-03-08 | 2023-09-14 | Jianchao Shu | Fully renewably -powered desalination /water purification station |
CN115848574A (en) * | 2022-11-23 | 2023-03-28 | 华南理工大学 | Wave energy-wind power generation hydrogen production integrated system based on semi-submersible platform |
Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AU2007231797A1 (en) * | 2006-11-08 | 2008-05-29 | Jolyon Emmanuel Nove | Desalination and power generation plant |
WO2008115662A2 (en) * | 2007-02-25 | 2008-09-25 | Puregeneration (Uk) Ltd. | Carbon dioxide sequestering fuel synthesis system and use thereof |
US20090212560A1 (en) * | 2006-11-03 | 2009-08-27 | Vestas Wind Systems A/S | Heating System, Wind Turbine Or Wind Park, Method For Utilizing Surplus Heat Of One Or More Wind Turbine Components And Use Hereof |
US20110103950A1 (en) * | 2009-11-04 | 2011-05-05 | General Electric Company | System and method for providing a controlled flow of fluid to or from a wind turbine blade surface |
CN102726336A (en) * | 2011-03-30 | 2012-10-17 | 国立成功大学 | Mechanism for increasing dissolved oxygen in water by wind power |
US20150251924A1 (en) * | 2012-08-16 | 2015-09-10 | University Of South Florida | Systems and methods for water desalination and power generation |
US20160296881A1 (en) * | 2013-11-21 | 2016-10-13 | Ruth Muffett | Absorption of atmospheric carbon dioxide |
GB2546251A (en) * | 2016-01-06 | 2017-07-19 | Statoil Petroleum As | Offshore wind turbine |
CN206366465U (en) * | 2016-06-15 | 2017-08-01 | 陆英豪 | Planetary water spray windmill |
Family Cites Families (18)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5371686A (en) | 1976-12-09 | 1978-06-26 | Efu Konerii Robaato | Tubular molecule filtering apparatus |
WO2003087569A1 (en) | 2002-04-04 | 2003-10-23 | Lunatech, Llc | Barge-mounted tidal-powered desalinization system |
US7453164B2 (en) * | 2003-06-16 | 2008-11-18 | Polestar, Ltd. | Wind power system |
JP4484635B2 (en) | 2004-09-02 | 2010-06-16 | 日東電工株式会社 | Spiral type reverse osmosis membrane element and manufacturing method thereof |
WO2010059209A2 (en) | 2008-11-21 | 2010-05-27 | Ocean Power Technologies, Inc. | Float for wave energy converter (wec) |
GB0900982D0 (en) * | 2009-01-22 | 2009-03-04 | Green Ocean Energy Ltd | Method and apparatus for energy generation |
US8282823B2 (en) | 2010-03-04 | 2012-10-09 | Terragroup Corporation | Lightweight modular water purification system with reconfigurable pump power options |
US20100314238A1 (en) | 2010-04-30 | 2010-12-16 | Sunlight Photonics Inc. | Hybrid solar desalination system |
US9334849B2 (en) | 2014-03-17 | 2016-05-10 | Aquantis, Inc. | Floating tower frame for ocean current turbine system |
US20150290589A1 (en) | 2014-04-11 | 2015-10-15 | Parker-Hannifin Corporation | Encapsulating outer shell for membrane elements |
US10513446B2 (en) | 2014-10-10 | 2019-12-24 | EcoDesal, LLC | Depth exposed membrane for water extraction |
US9878265B2 (en) * | 2015-06-16 | 2018-01-30 | Glen Truett Hendrix | System for producing fresh water and electricity using cold ocean water in combination with wind power |
US10077540B2 (en) | 2016-02-16 | 2018-09-18 | Hyperloop Technologies, Inc. | Corrosion-resistant fluid membrane |
JP2019509217A (en) * | 2016-03-15 | 2019-04-04 | スティーズダル オフショアー テクノロジーズ アクティーゼルスカブ | Floating wind turbine and method for installing such a floating wind turbine |
US10479706B2 (en) | 2016-06-03 | 2019-11-19 | Katz Water Tech, Llc | Apparatus, method and system for desalinating water |
WO2017212086A1 (en) * | 2016-06-08 | 2017-12-14 | González Pérez Adolfo | Autonomous sustainable wind unit, multi-blade reticular rotor, energy accumulator and energy converter and uses |
WO2020010285A1 (en) * | 2018-07-03 | 2020-01-09 | Excipio Energy, Inc. | Integrated offshore renewable energy floating platform |
US10982654B1 (en) * | 2019-08-01 | 2021-04-20 | Dehlsen Associates, Llc | Yawing buoy mast for floating offshore wind turbines |
-
2021
- 2021-01-29 US US17/163,295 patent/US11660572B2/en active Active
- 2021-08-02 US US17/391,884 patent/US20210362094A1/en not_active Abandoned
-
2022
- 2022-02-04 US US17/665,459 patent/US20220274063A1/en not_active Abandoned
Patent Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US20090212560A1 (en) * | 2006-11-03 | 2009-08-27 | Vestas Wind Systems A/S | Heating System, Wind Turbine Or Wind Park, Method For Utilizing Surplus Heat Of One Or More Wind Turbine Components And Use Hereof |
AU2007231797A1 (en) * | 2006-11-08 | 2008-05-29 | Jolyon Emmanuel Nove | Desalination and power generation plant |
WO2008115662A2 (en) * | 2007-02-25 | 2008-09-25 | Puregeneration (Uk) Ltd. | Carbon dioxide sequestering fuel synthesis system and use thereof |
US20110103950A1 (en) * | 2009-11-04 | 2011-05-05 | General Electric Company | System and method for providing a controlled flow of fluid to or from a wind turbine blade surface |
CN102726336A (en) * | 2011-03-30 | 2012-10-17 | 国立成功大学 | Mechanism for increasing dissolved oxygen in water by wind power |
US20150251924A1 (en) * | 2012-08-16 | 2015-09-10 | University Of South Florida | Systems and methods for water desalination and power generation |
US20160296881A1 (en) * | 2013-11-21 | 2016-10-13 | Ruth Muffett | Absorption of atmospheric carbon dioxide |
GB2546251A (en) * | 2016-01-06 | 2017-07-19 | Statoil Petroleum As | Offshore wind turbine |
CN206366465U (en) * | 2016-06-15 | 2017-08-01 | 陆英豪 | Planetary water spray windmill |
Non-Patent Citations (2)
Title |
---|
English language machine translation of CN102726336, 6 pages, NO DATE. * |
Thiel et al, ACS Sustainable Chem. Eng. 2017, 5, 11147−11162. (Year: 2017) * |
Also Published As
Publication number | Publication date |
---|---|
US20210146307A1 (en) | 2021-05-20 |
US20210362094A1 (en) | 2021-11-25 |
US11660572B2 (en) | 2023-05-30 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20220274063A1 (en) | Wind-Powered Direct Air Carbon Dioxide Capture Device for Ocean Sequestration | |
Morgan | Techno-economic feasibility study of ammonia plants powered by offshore wind | |
US8795525B2 (en) | Utility scale osmotic grid storage | |
ES2671195T3 (en) | Method and system for recovery of carbon dioxide from gas | |
US4568522A (en) | Synfuel production ship | |
AU2017276466B2 (en) | Ocean carbon capture and storage method and device | |
US4282187A (en) | Production of synthetic hydrocarbons from air, water and low cost electrical power | |
WO2008115662A2 (en) | Carbon dioxide sequestering fuel synthesis system and use thereof | |
MX2007002019A (en) | Removal of carbon dioxide from air. | |
US11452949B2 (en) | Apparatus and process for removal of carbon dioxide from a gas flow and treatment of brine/waste water from oil fields | |
US20110204841A9 (en) | System for storing electrical energy | |
EP3895785A1 (en) | Unit for desalination and greenhouse gas sequestration | |
KR102470189B1 (en) | Carbon dioxide and sulfur oxide capture and carbon resource conversion system for onshore | |
WO2014007032A1 (en) | Method and device for treating saline wastewater | |
US20230191322A1 (en) | Systems and methods for direct air carbon dioxide capture | |
CN109689184A (en) | The method of osmotic drive membrane process and system and recycling driving solute | |
CN116328510A (en) | Self-sufficient carbon dioxide capture and sequestration system | |
US11701616B2 (en) | Sorbent emitter for direct air capture of carbon dioxide | |
KR101489642B1 (en) | Complex fresh water production system using fuel cell apparatus | |
CN116940404A (en) | Apparatus and method for reducing carbon dioxide content in atmosphere | |
CN116685387A (en) | Apparatus and method for maintaining a predetermined carbon dioxide/oxygen ratio in the atmosphere | |
JP2005087821A (en) | Desalination apparatus | |
US20110086250A1 (en) | Method and apparatus for storing electrical power by evaporating water | |
CN220802672U (en) | Forward osmosis membrane separation equipment for high-pressure gas-driven negative pressure separation | |
TW202406622A (en) | Self-sufficient systems for carbon dioxide removal and sequestration and method thereof |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
AS | Assignment |
Owner name: DEHLSEN ASSOCIATES OF THE PACIFIC LIMITED, NEW ZEALAND Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNOR:DEHLSEN, JAMES;REEL/FRAME:059977/0226 Effective date: 20220314 |
|
STPP | Information on status: patent application and granting procedure in general |
Free format text: NON FINAL ACTION MAILED |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |
|
STPP | Information on status: patent application and granting procedure in general |
Free format text: RESPONSE TO NON-FINAL OFFICE ACTION ENTERED AND FORWARDED TO EXAMINER |
|
STPP | Information on status: patent application and granting procedure in general |
Free format text: FINAL REJECTION MAILED |
|
STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |