WO2022130380A1 - Procédé et appareil de production de bicarbonates alcalins et de carbonates alcalin - Google Patents

Procédé et appareil de production de bicarbonates alcalins et de carbonates alcalin Download PDF

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Publication number
WO2022130380A1
WO2022130380A1 PCT/IL2021/051488 IL2021051488W WO2022130380A1 WO 2022130380 A1 WO2022130380 A1 WO 2022130380A1 IL 2021051488 W IL2021051488 W IL 2021051488W WO 2022130380 A1 WO2022130380 A1 WO 2022130380A1
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WO
WIPO (PCT)
Prior art keywords
gas
liquid
liquid contactor
sparging
bicarbonate
Prior art date
Application number
PCT/IL2021/051488
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English (en)
Inventor
Marat MAAYAN
Uri STOIN
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Airovation Technologies Ltd.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Application filed by Airovation Technologies Ltd. filed Critical Airovation Technologies Ltd.
Priority to JP2023537542A priority Critical patent/JP2024500840A/ja
Publication of WO2022130380A1 publication Critical patent/WO2022130380A1/fr
Priority to US18/335,092 priority patent/US20230322569A1/en

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B32/00—Carbon; Compounds thereof
    • C01B32/60—Preparation of carbonates or bicarbonates in general
    • 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
    • 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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/79—Injecting reactants
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D7/00—Carbonates of sodium, potassium or alkali metals in general
    • C01D7/07—Preparation from the hydroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/10—Oxidants
    • B01D2251/106—Peroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/306—Alkali metal compounds of potassium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B01D2258/0291—Flue gases from waste incineration plants

Definitions

  • Alkali bicarbonates and carbonates can be prepared by passing carbon dioxide through an aqueous solution of alkali hydroxide.
  • a useful source of carbon dioxide is found in industrial CCh-bearing gas streams.
  • carbon dioxide emitted by fossil-fired power plants, or present in other industrial gas streams can be captured by scrubbing the gas with an aqueous solution of alkali hydroxide. This could serve a twofold purpose: reduction of CO2 emission to the atmosphere and its direct, on-site conversion to commercially useful chemical reagents.
  • NaHCOs sodium bicarbonate
  • baking powders it is also known as "baking soda”
  • textile, paper and ceramics industries are also known as "baking soda”.
  • the invention is primarily directed to a process for preparing alkali carbonate and/or bicarbonate salts, comprising : continuously feeding alkali hydroxide into a gas-liquid contactor; forcing incoming C0 2 -containing gas stream through a sparging device submerged in the gas-liquid contactor below the surface level of the aqueous alkali hydroxide solution, to generate bubbles and/or microbubbles; adding hydrogen peroxide in proximity to orifices of the sparging device, from which the bubbles/microbubbles evolve, wherein the supply of hydrogen peroxide is adjusted to decrease alkali carbonate formation and increase alkali bicarbonate formation; and continuously discharging an effluent from the gas-liquid contactor and recovering therefrom carbonate/bicarbonate alkali salts predominated by the bicarbonate component.
  • C02-containing gases drawn from industrial facilities can serve as a source of carbon dioxide in the production of the carbonates/bicarbonates .
  • CO2 level in the incoming gas stream is not less than 380 ppm, e.g., vary in the range from 10,000 to 200, 000 ppm (from 1 to 20%, e.g., from 1 to 18%, e.g., from 1 to 15%, e.g., from 7 to 14% CO2) .
  • the chemical absorption of CO2 by the alkaline solution to produce the bicarbonate/carbonate salts takes place in a reactor designed as a gas-liquid contactor (hereinafter the terms “reactor” and “gas-liquid contactor” are used interchangeably) .
  • the NOx and SO x -free flue gas is passed through a heat exchanger (to cool the gas stream to about 40-50°C) .
  • the heat released by the flue gas can be recovered using a stream of fresh air, which may be guided to serve downstream operations, i.e., the separation of the bicarbonate/carbonate salts from the reaction mixture as described below.
  • the gas stream is now directed to the gas-liquid contactor, where the salts formation reactions occurs.
  • the aqueous MOH solution e.g., NaOH or KOH
  • the concentration of the solution fed to the gas/liquid contactor is > 10% by weight and up to saturation (48%) , e.g. in the range of 25 to 35%, usually ⁇ 30% by weight.
  • the aqueous solution can be prepared on-site, either by dilution of commercial saturated solutions with water, or by dissolution of solid alkali hydroxide (available in the marketplace in the form of granules, pellets or flakes) in water.
  • MOH production units may be provided.
  • Each MOH production unit consists of a mixing tank in which solid MOH and water (i.e., fresh water and water recovered from downstream operations) are mixed and a pump to deliver the MOH solution to the gas-liquid contactor.
  • Suitable pumps are made of stainless steel, and operate, for example, at capacity in the range of 10 to 120 m 3 /hour, or any other range, to meet the demand of the plant emitting the CO2 gas.
  • Such a set-up consisting of alternately operating MOH production and supply units, enables one unit to be active in supplying a preprepared MOH solution as a feed stream to the gas-liquid contactor (MOH charge phase) , and the other to produce and store MOH solution (MOH production phase) , with the bicarbonate/carbonate preparation process of the invention switching from one unit to another.
  • MOH charge phase gas-liquid contactor
  • MOH production phase MOH solution
  • the sparging device mounted in the gasliquid contactor to convert the incoming C02-containing streams into microbubbles, may be configured in different geometries, e.g., flat geometry (perforated plates, horizontally positioned membranes) and tubular configuration.
  • one preferred process design is based on forcing incoming C02-containing gas stream through an array of tunnelshaped sparging units submerged in the gas-liquid contactor below the surface level of the aqueous alkali hydroxide solution, wherein a sparging unit is bounded, at least in part, by a curved surface.
  • a sparging unit operative in the process of the invention may be in the shape of a semi-cylinder. The orifices of the sparging unit are distributed on its curved surface, as explained below.
  • the size of orifices, through which the air/CO2 gas mixture is forced to create the microbubbles is less than 700 pm, e.g., less than 500 pm, e.g., diameter ranging from 50 to 300 pm, e.g., 100 to 200 pm.
  • H2O2 addition to the gas-liquid contactor preferably takes place by injecting a plurality of individual H2O2 streams in proximity to the orifices provided on the curved surface of the tunnel-shaped sparging units. This can be achieved with the aid of pipes positioned adjacent to, and parallel with, the sparging units, as described below.
  • a purified (CCh-free) air stream is released through gas outlet opening (18) , which is centrally positioned in the top section (16) of the reactor (the design illustrated for top section (16) , consisting of inclined trapezoidal plates 16a and 16b and inclined triangular plates (16c, 16d) , creating a sloping roof design, is not mandatory) ) .
  • the level of the alkali hydroxide solution 32 is designed to ensure sufficient scrubbing of the gas (in the form of microbubbles) with the aqueous alkali hydroxide solution, thereby removing carbon dioxide from the flue gas to produce the salts.
  • Numeral (21) indicates a discharge pipe, through which the reaction mixture is continuously discharged (and treated to recover the crystalline bicarbonate/carbonate salts, as shown in Figures 6 to 8) .
  • the cross-section of a tunnel-shaped sparging unit corresponds to a circle or a segment of a circle with radius in the range from 10 mm to 300 mm i.e., a part of a circle bounded by an arc and its chord, wherein the corresponding central angle a that lies on the chord is preferably in the range from 90° ⁇ a ⁇ 360°.
  • a tunnel-shaped sparging unit is bounded by a longitudinally extending flat base (34) (e.g., rectangularly shaped base, which is attached to, or is part of, the floor of the gas/liquid contactor) , wherein the opposite longitudinal sides of the base (34) are joined by a curved surface (35) , defining an interior space into which a gas stream is directed from pipe (14 n ) of manifold (14) .
  • curved surface (35) defining a tunnel-shaped sparging unit is the lateral surface of a semi-cylinder.
  • Orifices (29) are distributed densely along the length of the curved surface of the tunnel-shaped sparging unit, preferably in a uniform manner, e.g., creating a pattern consisting of orifices arranged in transverse rows along the length of the curved surface, or more precisely, in arcs (36) (owing to the curvatures of the surface) .
  • Adjacent arcs are spaced 0.5 to 10 mm apart.
  • Each arc consists of a plurality of orifices; the center-to-center distance between adjacent orifices is from 0.5 mm to 5 mm.
  • the diameter of the orifice is between 50 and 700pm, to ensure the creation of microbubbles of a desired size within the aqueous solution.
  • Manifold (26) comprises a plurality of H2O2 tubes (26i, 262, . . . , 26 m ; m>n) . At least one peroxide tube (26i) is disposed in a space between two adjacent sparging units, that is, parallel to the sparging units.
  • the H2O2 tubes and the sparging units are approximately equal in length, but the H2O2 tubes are smaller in diameter, e.g., H2O2 tube typically has a diameter of between 3 mm and 30 mm.
  • Nozzles (23) are disposed along the length of the H2O2 tube, having a diameter between 0.1 mm and 2 mm, with the nozzle tips being directed towards one of the two adjacent sparging units.
  • the nozzles are preferably evenly spaced along the H2O2 tube, the distance between adjacent nozzles being, for example, between 1 cm and 10 cm.
  • each of the nozzles injects a pressurized stream at a small inclined angle of 1 deg to 90 deg relative to the horizontal.
  • a gas-liquid contactor comprising : a longitudinal horizontal housing bounded by a bottom surface, a top section and lateral faces; an array of tunnel-shaped sparging units (28i) , (282) , ..., (28 n ) , placed horizontally and parallel to each other in the interior of the housing, wherein a sparging unit is bounded by an upward facing curved surface, with orifices distributed on said curved surface; an array of tubes (26i, 262, . . .
  • the flow rate of the alkali hydroxide solution fed continuously to the gas-liquid contactor is from 10 to 120 m 3 /hour.
  • the flow rate of the H2O2 supplied to the gas-liquid contactor is adjusted, e.g., within the range of 1 to 20 m 3 /hour such that carbonate formation is minimized and bicarbonate formation is maximized, e.g., the molar concentration of the bicarbonate in the product recovered is not less than 70%, e.g. >90%, >95%, >99%.
  • the feed rate of aqueous H2O2 may be determined by trial and error, based on the load of CO2 in the incoming gas stream, the concentration and purity of the alkali hydroxide solution and the specific design of the sparging units and H2O2 tubes, reaction and outside temperature, to achieve a steady flow of a pumpable slurry discharged from the gas-liquid contactor, with CO2 conversion rates, on industrial scale, >80%-90%.
  • Experimental work conducted in support of this invention in the lab suggests that an appropriate feed rate of aqueous H2O2 to achieve prolonged salt formation reaction is one that reaches high CO2 conversion neither too slowly nor too rapidly.
  • the flow rate of aqueous H2O2 may also be increased or decreased in response to analysis of the distribution of bicarbonate/carbonate salts in the product mixture.
  • Figure 6 illustrates the first step.
  • Effluent stream from the reactor (10) flows to a first gas-liquid separator (61) , where the gas dissolved in the effluent is removed to join the main purified (CO2-free) gas stream (62) , which is being released from the reactor (10) by the action of blower (63 B-03) .
  • the solution/slurry stream (64) which exits from the bottom of first gas-liquid separator is pumped (65 P06, e.g., capacity 75 m3/h; head 20 m water) and divided into two streams, one that is recirculated via recycle line (66) and returned to the reactor (10) , and another stream (67) which proceeds to the next separation steps needed to recover the salts.
  • Recycle line (66) is provided with a cooler (68 C-04) , e.g., in the form of spiral heat exchanger, to facilitate heat removal from reactor (10) .
  • the salt formation reaction taking place in reactor (10) is exothermic; heat released by this reaction is recovered from the effluent of reactor (10) in cooler (68) , thereby keeping a stable temperature in reactor (10) .
  • Figure 7 illustrates the second step, i.e., concentration of the solution/slurry .
  • Stream (67) undergoes partial evaporation, e.g., in a flash drum (71 F-03) , such that water vapors are removed under vacuum of 10 to 100 millibar (P-09) , to force precipitation of solubilized salts.
  • Water vapors undergo condensation (C-05, e.g., a flash condenser) , to produce a water stream which can be supplied to the process, e.g., for the preparation of alkali hydroxide solution fed to a reactor (10) .
  • a pumpable slurry withdrawn from the bottom of flash drum (71) flows (pump 72 P-07) to an agitated tank (73 T-05) , from which it is delivered by pump (74 P-08) to a solid/liquid separation unit.
  • Figure 8 illustrates the third step, i.e., isolation of the bicarbonate/carbonate salts.
  • Separation of the solids from the stream delivered from tank (73) is achieved, for example, with the aid of continuous equipment for liquid/solid separation, such as one or more centrifuges, e.g., a continuous centrifuge or two or more switchable batch centrifuges (75a, 75b) operating alternately, such that a first batch centrifuge separates the liquid-solid mixture introduced thereinto, whereas the second batch centrifuge delivers the aqueous supernatant and wet cake produced: the aqueous supernatant (76) can be recycled and used in earlier steps of the process, e.g., to supply water to dissolve alkali hydroxide, as mentioned above.
  • the aqueous supernatant 76
  • the aqueous supernatant can be recycled and used in earlier steps of the process, e.g., to supply water to dissolve alkali hydroxide, as mentioned above.
  • the wet salt particles are transferred, e.g., via conveyer screw (77) to a drier to remove residual moisture, e.g., by thermal drying.
  • a drier is a fucidized-bed drier (78) , because heat consumed by recovery from elsewhere in the process can be used, i.e., the air stream which absorbed heat from the incoming stream of flue gas at the very beginning of the process.
  • the alkali carbonate/bicarbonate particles are preferably dried at a temperature not higher than 50°C.
  • S-04 is bag filter, to further separate solids and release dust-free air using exhaust fan (B-02) .
  • Another aspect of the invention is an apparatus for producing alkali bicarbonate/carbonate, to be placed at the vicinity of CO2-emitting plant (e.g., a power plant, an incineration plant and SMR plant) , comprising: a gas-liquid contactor as described above; a first blower forcing air/CO2 stream through said gas-liquid contactor; a set of pumps to deliver liquids and slurries; upstream processing units, including: one or more tanks accommodating an aqueous alkali hydroxide solution, connected to the first liquid feed line of said gas-liquid contactor; one or more tanks accommodating hydrogen peroxide, connected to the second liquid feed line of said gas-liquid contactor, a first heat exchanger using ambient air driven by a second blower for heat transfer, said heat exchanger is provided with a feed line to receive air/CO2 stream from a chimney stack of said plant, wherein the outlet of said heat exchanger is connected to a first gas-liquid separator, equipped with a gas discharge line and a liquid discharge line, to withdraw
  • the process of the invention utilizes di f ferent C02-containg gases as a feedstock .
  • it may be used to convert CO2 produced by steam methane reforming ( SMR) into carbonate/bicarbonate salts .
  • SMR steam methane reforming
  • SMR generates hydrogen and CO2 as by-product ; so CO2 capture/removal technologies are integrated into SMR .
  • the invention is well suited for this purpose , i . e . , to receive C02-containing gas from a steam methane reforming plant , to benefit from the relatively large concentration ( ⁇ 17 % ) of CO2 and absence of impurities in streams emitted by SMR .
  • With such a feedstock high purity grades of carbonates/bicarbonate salts can be obtained .
  • Figures 1 and 2 show a perspective view of a gas-liquid contactor which is generally parallelepiped in shape , bounded by a bottom surface , a top section and four lateral faces .
  • Figures 3 to 5 show a perspective view of the interior of the gas-liquid contactor, with sparging units installed and an array of tubes deployed inside the gas-liquid contactor .
  • Figure 7 schematically shows a vacuum flash separation unit .
  • Figure 8 schematically shows a centri fuge and a drying unit .
  • Figure 9 shows the experimental set-up used in Examples 1 to 4 .
  • Reactor (100) is tubular in shape (inner diameter: 9 cm; height: 40 cm) .
  • 5mm thick stainless steel membrane (101) is mounted horizontally inside the reactor, about 2.5 cm from the bottom the reactor.
  • the pore size of the membrane was 147 pm; center to center distance between adjacent pores is ⁇ 50 pm.
  • the reactor was charged with 250 ml aqueous NaOH (30% by weight solution) , such that the liquid level in the reactor was 7 cm, i.e., the membrane (101) was submerged about 4.5 cm below the surface level of the solution .
  • the CO2 source was a commercial 100% CO2 held in a gas cylinder. Pumps made CO2 and air to flow into, and mix in, gas mixer (102) to create a mixed stream of 1000 ppm-CO2 bearing air, which was directed by pump (103) to reactor (101) at a flow rate of 13 L/min (gas inlet rotameter (104) ) .
  • Hydrogen peroxide solution (10% solution) is continuously added to reactor (100) at different flow rates (1 ml/h, 2 ml/h and 10 ml/h; reference experiment with no addition at all) using peristaltic pump “B” .
  • H2O2 stream is fed below the surface level of the sodium hydroxide solution in the reactor, in proximity to membrane (101) .
  • a pair of CO2 detectors (105in and 105out - BGA-EDG-MA, Emproco Ltd., Israel) connected to the incoming (1000 ppm-CO2 bearing air and outgoing (purified) streams (106 and 107, respectively) were used to measure the concentration of CO2, respectively .
  • the incoming air/CO2 mixed gas stream (106) entered reactor (100) through the bottom of the reactor and was forced to flow through the membrane (101) to create bubbles.
  • CO2 was chemically absorbed by the sodium hydroxide medium.
  • CO2 levels in the incoming and outgoing gas streams were recorded continuously over the test period.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Materials Engineering (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

L'invention concerne un procédé de préparation de sels de carbonate/bicarbonate alcalin, consistant à : introduire de manière continue une solution aqueuse d'hydroxyde alcalin dans un contacteur gaz-liquide ; forcer le flux gazeux entrant contenant du CO2 à traverser un dispositif de barbotage immergé dans le contacteur gaz-liquide sous le niveau de surface de la solution aqueuse d'hydroxyde alcalin pour générer des bulles et/ou des microbulles ; ajouter du peroxyde d'hydrogène à proximité des orifices du dispositif de barbotage, à partir desquels les bulles et/ou les microbulles évoluent, l'apport de peroxyde d'hydrogène étant ajusté pour diminuer la formation de carbonate alcalin et augmenter la formation de bicarbonate alcalin ; et évacuer en continu un effluent à partir du contacteur gaz-liquide et récupérer, à partir de celui-ci, de sels de carbonate et de bicarbonate alcalin dont le constituant de bicarbonate est prédominant. L'invention concerne également un contacteur gaz-liquide et un appareil.
PCT/IL2021/051488 2020-12-15 2021-12-14 Procédé et appareil de production de bicarbonates alcalins et de carbonates alcalin WO2022130380A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
JP2023537542A JP2024500840A (ja) 2020-12-15 2021-12-14 重炭酸アルカリ及び炭酸アルカリを生成するための方法及び装置
US18/335,092 US20230322569A1 (en) 2020-12-15 2023-06-14 Process and apparatus for producing alkali bicarbonates and alkali carbonates

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US202063125553P 2020-12-15 2020-12-15
US63/125,553 2020-12-15

Related Child Applications (1)

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Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100320294A1 (en) * 2005-02-14 2010-12-23 Neumann Systems Group, Inc. Gas liquid contactor and effluent cleaning system and method
US20120049114A1 (en) * 2009-03-02 2012-03-01 William Randall Seeker Gas stream multi-pollutants control systems and methods
US20200171431A1 (en) * 2016-06-28 2020-06-04 Salamandra Zone Ltd. Air treatment systems and methods

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100320294A1 (en) * 2005-02-14 2010-12-23 Neumann Systems Group, Inc. Gas liquid contactor and effluent cleaning system and method
US20120049114A1 (en) * 2009-03-02 2012-03-01 William Randall Seeker Gas stream multi-pollutants control systems and methods
US20200171431A1 (en) * 2016-06-28 2020-06-04 Salamandra Zone Ltd. Air treatment systems and methods

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
STOIN URI, BARNEA ZACH, SASSON YOEL: "New technology for post-combustion abatement of carbon dioxide via an in situ generated superoxide anion-radical", RSC ADV., vol. 4, no. 69, 1 January 2014 (2014-01-01), pages 36544 - 36552, XP055943098, DOI: 10.1039/C4RA03844D *
STOIN URI, SHAMES ALEXANDER I., MALKA ITAMAR, BAR ILANA, SASSON YOEL: "In situ Generation of Superoxide Anion Radical in Aqueous Medium under Ambient Conditions", CHEMPHYSCHEM, vol. 14, no. 18, 16 December 2013 (2013-12-16), DE , pages 4158 - 4164, XP055943103, ISSN: 1439-4235, DOI: 10.1002/cphc.201300707 *

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