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WO2003008071A1 - Procede et dispositif pour l'absorption du co2 dans l'eau de mer - Google Patents

Procede et dispositif pour l'absorption du co2 dans l'eau de mer Download PDF

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Publication number
WO2003008071A1
WO2003008071A1 PCT/NO2001/000308 NO0100308W WO03008071A1 WO 2003008071 A1 WO2003008071 A1 WO 2003008071A1 NO 0100308 W NO0100308 W NO 0100308W WO 03008071 A1 WO03008071 A1 WO 03008071A1
Authority
WO
WIPO (PCT)
Prior art keywords
water
gas
loops
sintered material
bubbles
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.)
Ceased
Application number
PCT/NO2001/000308
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English (en)
Inventor
Sigurd Fongen
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Individual
Original Assignee
Individual
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Filing date
Publication date
Application filed by Individual filed Critical Individual
Priority to PCT/NO2001/000308 priority Critical patent/WO2003008071A1/fr
Publication of WO2003008071A1 publication Critical patent/WO2003008071A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • 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
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • 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
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • This invention concerns method and means for absorption and conversion of CO 2 and other gas molecules into carbonates or other, inorganic compounds by reactions with minerals in water.
  • the inventor has previously the following patents in related, technological fields:
  • Both inventions concern reactions between oxidising molecules, preferably pure oxygen,
  • the present invention concerns method and means for reactions between non-oxidising gas molecules, as for example CO 2 , and inorganic matter and compounds in water, for example Ca-compounds an sea-water.
  • non-oxidising gas molecules as for example CO 2
  • inorganic matter and compounds in water for example Ca-compounds an sea-water.
  • Raschig rings are frequently used, which have a large surface and which spread out the liquid on its way down through the tower in such a manner that the surface ofthe liquid facing the gas becomes as large as possible.
  • the invention relates to method and means for a quick, efficient and relatively inexpensive absorption of CO 2 or other non-oxidising gases in mineral-containing water, which can replace to-day's slow and inefficient processes, as these for example are carried out in voluminous, space demanding and relatively expensive reaction towers.
  • the process is of particular importance for the elimination of CO -emissions to the atmosphere from boiler houses or power plants using fossil fuels as coal, oil or gas.
  • a radical increase of the accessibility between the CO -gas and mineral-containing water, made possible by a strong increase of the interface between the water and the gas, combined with strong water movements, will increase the reaction speeds as well as make the reactions more complete.
  • This invention fulfils this aim and describes a method and means for absorption and conversion of gas molecules into carbonates or other, inorganic compounds in mineral- containing water.
  • the invention also opens for the possibilities of a more comprehensive and economically more inexpensive elimination of CO -emissions to the atmosphere.
  • the method and means of the invention are described in the following for 2 alternatives, carried out on land and carried out under water respectively. Both modes of execution apply however the same, special method which is described below, and which includes a substantial increase of the interface between water and gas, combined with strong water movements, carried out under pressure and with simultaneous addition of crystallisation nuclei for mineral precipitation
  • the gas is transformed into micro bubbles, here defined as gas bubbles with diameters preferably smaller than 50 ⁇ m.
  • the size of the micro bubbles is determining for the magnitude of the interface between gas and liquid, as shown in the table below: For 1 litre of gas the following relation between bubble diameter and interface is valid:
  • micro bubbles are formed by blowing the gas into the liquid through a sintered material, composed of small particles of metal or another suitable material of such minute size that by the sintering they can form pores for gas penetration with diameters down to about 5 ⁇ m.
  • the gas bubbles are torn off from the surface before getting the opportunity to accumulate into larger bubbles.
  • the liquid stream is set into turbulent movement either by circulating the liquid within one or more loops or by conducting the liquid through pipes which at the inside are provided with static mixers of different shapes which cause strong liquid turbulence.
  • Fig. 1 shows the formation of micro bubbles.
  • the gas (1) is conducted into a pipe, whose walls consist of a sintered material, (2), below called the sintered pipe, with openings which for example have diameters of about 20 ⁇ m and whereby an initial micro gas bubble (3) of the same order of magnitude is formed.
  • Such bubble will, in stagnant, surrounding water (A), stay attached to the outer surface of the pipe due to adhesion forces, and at the same time it will grow increasingly larger because of the gas influx, until the bubbles (4) are so large that they release themselves from the surface due to buoyancy forces.
  • the water around the gas pipe (2) is set into strong movement (B) which causes the bubbles (5) to be torn off from the surface of the gas pipe before they can grow in size, for thereafter to follow the water stream with their approximate, initial size.
  • Micro gas bubbles show however a tendency to accumulate into larger bubbles when getting into touch with each other, also when being in streaming media.
  • Fig. 2 shows an example of method and means for landbased absorption of industrial CO 2 -gas in mineral-containing water, here exemplified by sea-water.
  • Sea-water has a salinity of approx. 34,3 0/00, containing several elements, of which the most important are:
  • Chlorine, CI about 19,0 g/kg
  • the CO 2 -gas (1) which shall be absorbed and bound to inorganic minerals in sea-water is conducted into one or more continuous and pressurised water loops (7).
  • the sea- water is being pumped into the loops by means of a pump (8) which causes the water to flow through the loops (7) and a gas vent (9) before it is being led back into the sea (10) at deep level (11), preferably discharging into a sea current (12) or near sea farming of shellfish, for example mussels (13).
  • the CO 2 -gas (1) is being pressed by a compressor (14) through a gas supply pipe (15) and regulating valves (16) and sintered pipe (2) into the water loops (7) which are kept in strong, circulating movements by pumps (17), situated within and being a part of the loops.
  • sea-water and not absorbed gas are being separated by spraying the water through a nozzle (22) against a wall (23) whereby the gas bubbles in the water are being released and the gas is being conducted into a chamber (24), from where through a separate pipe (25) it is conducted back to the suction side ofthe compressor (14).
  • the water (26) from the gas separator is conducted by a pipe (27) back to the suction side ofthe pump (8).
  • the water is being moved continuously from one loop (7) to the next through a transferring pipe (28) and at the end flows through the gas vent (9), in which the water forms a vortex (29) before it leaves the system through an outlet pipe (30) and a valve (31) which regulates the pressure in and the flow through this landbased gas absorption device, whereupon the water is discharged at deep water level (11) through the outlet opening ofthe pipe (32).
  • crystallisation nuclei (42) in form of washed dolomite- or calcite powder can be injected, added through an injection pump (43) from a separate washing plant (44), not shown in the figure.
  • the means can deviate from the drawing in Fig. 2.
  • the shape and position of the sintered pipe can be somewhat different from the drawing, and the loops can likewise have different design.
  • the sintered material is preferably placed in the peripheral part of the loop.
  • the circulation within the loop can be intensified by placing a pump within a branch stream of the peripheral part of the loop. Accumulating gas bubbles can be led out of the central part ofthe loop and be conducted back to the beginning ofthe process.
  • This landbased means also has equipment for addition of other chemicals or catalysts to the water, not shown on the figure.
  • the pressure within the pipe system is being regulated by an outlet valve (31) and the other regulating valves for gas addition (16) and for outlet of the gas-water mixture (19)
  • Fig. 3 shows more in detail the principle design and mode of operation of the exemplified loops (7).
  • the water is being pumped preferably tangentially into the loop through an inlet pipe (33) and leaves the loop after several circulations, preferably tangentially through an outlet pipe (28) which at the same time is inlet pipe for the next loop.
  • the circulation within the loop is maintained by a pump (17) which pumps the water stream (34) around in the loop.
  • the pump has a separate inlet channel (35) and an outlet channel (36), here shown in form of a separating wall (37) which keeps the peripheral part of the liquid stream before and after the pump separated from the other part of the loop's cross section, as shown in the figure.
  • the peripheral water stream (34) is here shown as separated from the main stream in the loop (7) before the inlet of the circulation pump (17) with the separating wall (37) and is being mixed in the pump (17) for thereafter to be rejoined with the main stream.
  • the outer, peripheral stream (34) has during the passage through the pump received new kinetic energy which draws the whole water cross section in the loop (7) around in a continuous circulation.
  • the gas is added to the loop through regulating valves (16) and pipes (2) of sintered material which are preferably placed in the peripheral part (34) ofthe loop.
  • the sintered material delivers its micro bubbles to the peripheral part of the loop which is being enriched with micro bubbles anew every time the water is passing the sintered material, at the same time as the circulation pump (17) also causes a strong mixing of the water, containing micro bubbles, by every circulation of the water stream through the pump.
  • Fig. 4 shows more in detail how the micro bubbles preferably are in the periphery of the loop after having been injected into the liquid through the sintered pipes, which preferably are placed in the outer, peripheral part of the loop. This peripheral part of the water loop which contains the micro bubbles, is being mixed within the circulation pump
  • Fig. 5 shows an example of method and means for the same abso ⁇ tion of CO 2 -gas in sea-water, carried out by means placed under water.
  • the gas (1) is conducted to a compressor (14) from where it is being pressed down through an inlet pipe (15) to the means (52) in which the gas abso ⁇ tion is being carried out.
  • the means is placed in deep waters (51), for example at a depth of 200 meters.
  • the compressed gas in the means has thereby a pressure exceeding 20 bars in order to outbalance the water pressure when it flows through the sintered material within the means.
  • Down to the same means (52) large quantities of sea-water from a water intake (53) are at the same time pumped through a pump (8) down through an inlet pipe (54) to the same means.
  • This method with appurtenant means (52) has the following, special advantages:
  • the means (52) can operate with correspondingly reduced gas volumina, which is of advantage because the area and dimensioning of the sintered material can be reduced accordingly.
  • the fact is especially advantageous when large quantities of nitrogen gas accompany the CO -gas from the combustion plant.
  • large quantities of water can be pumped trough pump (8) and inlet pipe (54) to the means with a relatively modest consumption of kW by the pump because the water column within the inlet pipe (54) between the water surface (55) and the means (52) in deep water (51) balances the water pressure around the means and whereby the power consumption of the pump mainly is used for lifting the water from the water surface (55) up to the pump, a lifting height which however is approximately balanced by the outgoing liquid column from the pump (8) and down to the water surface (55).
  • the power consumption of the pump is therefore relatively modest because the consumed power is mainly being used for overcoming the flow resistance and flow loss in the inlet pipe (54) and the means itself (52) respectively down in the deep.
  • the water (55), which comes out of the means, and which has absorbed the gas (1) is being mixed with the water in large ocean currents (56) which spread the water from the means over vast ocean areas and great depths.
  • crystallisation nuclei (42) is being injected in the form of dolomite or calcite powder, added from a separate washing plant (44), not specified in the figure.
  • the means has equipment for addition of other chemicals or catalysts to the water, not shown in the figure.
  • Fig. 2, 3, 4 and 5 show thus examples of alternative modes of execution of the means placed on land, and which are especially suited for treatment of pure CO -gas which is not mixed with nitrogen or other gases, possibly with an extra addition of crystallisation nuclei, as described above.
  • Fig. 6, 7, 8, 9 and 10 show examples of alternative modes of execution ofthe means (52) placed under water, especially suited for treatment of CO 2 -gas mixed with nitrogen or other gases.
  • dolomite or calcite powder will increase the reaction speed and extent, and the means has also equipment for addition of other chemicals or catalysts, not shown in the drawing.
  • Fig. 6 shows the gas abso ⁇ tion within a closed container (60) placed under water and which is equipped with an inner, pipe-formed core (61) where the water (62) whirls several times around the core on its way from the inlet (63) to the outlet (64) and which thereby is conducted into rotating loops, approximately like the loops which are described above for landbased plants under Fig. 2 above.
  • compressed CO 2 -gas (65) is being added to the water (62) from the supply pipe (15) through the sintered material (2) which is placed within the water stream, either as a perforated, sintered pipe placed within the water stream or as a sintered plate fitted into the wall of the container (60) and whereby the plate is becoming a part of same, as exemplified in Fig. 11 below.
  • Fig. 6 is sketch-wise indicated how the water (62) is carrying out repeated circulations in a corkscrew-formed movement around the inner core (61) within the container. Likewise is indicated that the sintered material can be placed in different positions in relation to this loop, of which only one alternative position is indicated in the figure.
  • the outlet pipe (64) can be throttled by a suitable regulation valve, not shown in the figure.
  • Fig. 7 shows another form of execution applying the same principle in regard to method and means.
  • the container (60) is without core, and the water (62) is being pumped axially into the container where separating walls (66) cover parts of the inner cross section of the container, preferably placed radially and inclined.
  • the separating walls are here current conductors which are placed in such a manner that the water (62) is being conducted in ever changing directions within the container and whereby a strong, inner turbulence in the water is developed.
  • the sintered material (2) which also here can have several embodiments as described under Fig. 6 above, is being overflushed by the turbulent water which at high velocity exercises the same effect as described in Fig. 1 above.
  • Fig. 8 shows the sintered material (2) formed as several pipes placed cross-wise and preferably radially within a container (60) without core, and through which the gas (65) is being added to the water (62) as described for Fig. 6 and 7.
  • Fig. 9 shows another embodiment where the water (62) is being pumped into a spirally formed pipe (68) whereby the water is set into a corkscrew-formed circulation movement, similar to the water movement described in Fig. 6, and with approximately the same effect.
  • the gas (65) is being added to the water (62) through the sintered material (2) as described in Fig. 6.
  • static mixers can also be placed within the pipe (68).
  • Fig. 10 shows another, alternative embodiment where the water (65) is being pumped through the container (60) and over the sintered material (2) which is placed within the container, by a pump (69) which works under water and which is connected to the container (60) in a suitable form, as indicated principally on the figure, and which causes a similar flushing of sea-water over the sintered material (2) within the container with approximately the same effect as described above for Fig. 1, 6, 7, 8 and 9.
  • FIG. 2 above shows example of method and means for carrying out gas abso ⁇ tion on land.
  • Fig. 6, 7, 8 and 9 show the same method and means carried out under water, which also can be executed at deep water, with the advantages described above.
  • static mixers can also be applied for further intensification of the inner water turbulence of the means, not shown in the figures.
  • Fig. 11 shows an example of the sintered material (2) affixed as a part of the wall in the container (60) described in Fig. 6, 7 and 10 or the pipe (68) described in Fig. 9 above.
  • the sintered material is here formed according to the shapes of the container (60) or pipe (68), and is affixed to the container or the pipe by a flange or other fastening devise

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Environmental & Geological Engineering (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

Cette invention se rapporte à un procédé et à un moyen servant à l'absorption de gaz dans de l'eau et à la réaction de ces gaz avec les minéraux contenus dans l'eau. Dans ce procédé, le gaz est transformé en microbulles, lesquelles sont ajoutées à l'eau renfermant des minéraux, cette eau étant déplacée à des vitesses élevées à l'intérieur d'un ou de plusieurs systèmes tubulaires et pressurisés à mouvement tourbillonnaire, qui peuvent être placés sur terre ou sous l'eau. Ce procédé et ce moyen s'appliquent en particulier à l'absorption du CO2 dans l'eau de mer. Auxdits systèmes à mouvement tourbillonnaire on ajoute des noyaux de cristallisation destinés à augmenter la vitesse et l'amplitude de la réaction.
PCT/NO2001/000308 2001-07-17 2001-07-17 Procede et dispositif pour l'absorption du co2 dans l'eau de mer Ceased WO2003008071A1 (fr)

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Application Number Priority Date Filing Date Title
PCT/NO2001/000308 WO2003008071A1 (fr) 2001-07-17 2001-07-17 Procede et dispositif pour l'absorption du co2 dans l'eau de mer

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PCT/NO2001/000308 WO2003008071A1 (fr) 2001-07-17 2001-07-17 Procede et dispositif pour l'absorption du co2 dans l'eau de mer

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Cited By (25)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7735274B2 (en) 2007-05-24 2010-06-15 Calera Corporation Hydraulic cements comprising carbonate compound compositions
US7744761B2 (en) 2007-06-28 2010-06-29 Calera Corporation Desalination methods and systems that include carbonate compound precipitation
US7749476B2 (en) 2007-12-28 2010-07-06 Calera Corporation Production of carbonate-containing compositions from material comprising metal silicates
US7754169B2 (en) 2007-12-28 2010-07-13 Calera Corporation Methods and systems for utilizing waste sources of metal oxides
US7753618B2 (en) 2007-06-28 2010-07-13 Calera Corporation Rocks and aggregate, and methods of making and using the same
US7771684B2 (en) 2008-09-30 2010-08-10 Calera Corporation CO2-sequestering formed building materials
US7790012B2 (en) 2008-12-23 2010-09-07 Calera Corporation Low energy electrochemical hydroxide system and method
US7815880B2 (en) 2008-09-30 2010-10-19 Calera Corporation Reduced-carbon footprint concrete compositions
US7829053B2 (en) 2008-10-31 2010-11-09 Calera Corporation Non-cementitious compositions comprising CO2 sequestering additives
US7875163B2 (en) 2008-07-16 2011-01-25 Calera Corporation Low energy 4-cell electrochemical system with carbon dioxide gas
US7887694B2 (en) 2007-12-28 2011-02-15 Calera Corporation Methods of sequestering CO2
US7939336B2 (en) 2008-09-30 2011-05-10 Calera Corporation Compositions and methods using substances containing carbon
US7966250B2 (en) 2008-09-11 2011-06-21 Calera Corporation CO2 commodity trading system and method
US7993500B2 (en) 2008-07-16 2011-08-09 Calera Corporation Gas diffusion anode and CO2 cathode electrolyte system
US7993511B2 (en) 2009-07-15 2011-08-09 Calera Corporation Electrochemical production of an alkaline solution using CO2
US8137444B2 (en) 2009-03-10 2012-03-20 Calera Corporation Systems and methods for processing CO2
US8357270B2 (en) 2008-07-16 2013-01-22 Calera Corporation CO2 utilization in electrochemical systems
US8491858B2 (en) 2009-03-02 2013-07-23 Calera Corporation Gas stream multi-pollutants control systems and methods
CN103556599A (zh) * 2013-11-22 2014-02-05 马瑞志 大气碳吸收的仿地学方法
US8834688B2 (en) 2009-02-10 2014-09-16 Calera Corporation Low-voltage alkaline production using hydrogen and electrocatalytic electrodes
US8869477B2 (en) 2008-09-30 2014-10-28 Calera Corporation Formed building materials
US9133581B2 (en) 2008-10-31 2015-09-15 Calera Corporation Non-cementitious compositions comprising vaterite and methods thereof
US9260314B2 (en) 2007-12-28 2016-02-16 Calera Corporation Methods and systems for utilizing waste sources of metal oxides
US10589214B2 (en) 2016-02-02 2020-03-17 University Of Kentucky Research Foundation CO2 mass transfer enhancement of aqueous amine solvents by particle additives
WO2025225138A1 (fr) * 2024-04-24 2025-10-30 住友電気工業株式会社 Dispositif de récupération de dioxyde de carbone

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EP0429154A1 (fr) * 1989-11-21 1991-05-29 Mitsubishi Jukogyo Kabushiki Kaisha Procédé pour la fixation de l anhydride carbonique et dispositif pour traiter de l anhydride carbonique
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US8857118B2 (en) 2007-05-24 2014-10-14 Calera Corporation Hydraulic cements comprising carbonate compound compositions
US7735274B2 (en) 2007-05-24 2010-06-15 Calera Corporation Hydraulic cements comprising carbonate compound compositions
US7906028B2 (en) 2007-05-24 2011-03-15 Calera Corporation Hydraulic cements comprising carbonate compound compositions
US7914685B2 (en) 2007-06-28 2011-03-29 Calera Corporation Rocks and aggregate, and methods of making and using the same
US7753618B2 (en) 2007-06-28 2010-07-13 Calera Corporation Rocks and aggregate, and methods of making and using the same
US7931809B2 (en) 2007-06-28 2011-04-26 Calera Corporation Desalination methods and systems that include carbonate compound precipitation
US7744761B2 (en) 2007-06-28 2010-06-29 Calera Corporation Desalination methods and systems that include carbonate compound precipitation
US7754169B2 (en) 2007-12-28 2010-07-13 Calera Corporation Methods and systems for utilizing waste sources of metal oxides
US7887694B2 (en) 2007-12-28 2011-02-15 Calera Corporation Methods of sequestering CO2
US7749476B2 (en) 2007-12-28 2010-07-06 Calera Corporation Production of carbonate-containing compositions from material comprising metal silicates
US9260314B2 (en) 2007-12-28 2016-02-16 Calera Corporation Methods and systems for utilizing waste sources of metal oxides
US8333944B2 (en) 2007-12-28 2012-12-18 Calera Corporation Methods of sequestering CO2
US8357270B2 (en) 2008-07-16 2013-01-22 Calera Corporation CO2 utilization in electrochemical systems
US7875163B2 (en) 2008-07-16 2011-01-25 Calera Corporation Low energy 4-cell electrochemical system with carbon dioxide gas
US8894830B2 (en) 2008-07-16 2014-11-25 Celera Corporation CO2 utilization in electrochemical systems
US7993500B2 (en) 2008-07-16 2011-08-09 Calera Corporation Gas diffusion anode and CO2 cathode electrolyte system
US7966250B2 (en) 2008-09-11 2011-06-21 Calera Corporation CO2 commodity trading system and method
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US7815880B2 (en) 2008-09-30 2010-10-19 Calera Corporation Reduced-carbon footprint concrete compositions
US7771684B2 (en) 2008-09-30 2010-08-10 Calera Corporation CO2-sequestering formed building materials
US7939336B2 (en) 2008-09-30 2011-05-10 Calera Corporation Compositions and methods using substances containing carbon
US8869477B2 (en) 2008-09-30 2014-10-28 Calera Corporation Formed building materials
US8431100B2 (en) 2008-09-30 2013-04-30 Calera Corporation CO2-sequestering formed building materials
US8470275B2 (en) 2008-09-30 2013-06-25 Calera Corporation Reduced-carbon footprint concrete compositions
US8603424B2 (en) 2008-09-30 2013-12-10 Calera Corporation CO2-sequestering formed building materials
US7829053B2 (en) 2008-10-31 2010-11-09 Calera Corporation Non-cementitious compositions comprising CO2 sequestering additives
US9133581B2 (en) 2008-10-31 2015-09-15 Calera Corporation Non-cementitious compositions comprising vaterite and methods thereof
US7790012B2 (en) 2008-12-23 2010-09-07 Calera Corporation Low energy electrochemical hydroxide system and method
US9267211B2 (en) 2009-02-10 2016-02-23 Calera Corporation Low-voltage alkaline production using hydrogen and electrocatalytic electrodes
US8834688B2 (en) 2009-02-10 2014-09-16 Calera Corporation Low-voltage alkaline production using hydrogen and electrocatalytic electrodes
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