GB2623575A - Exhaust gas treatment system and method - Google Patents

Exhaust gas treatment system and method Download PDF

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Publication number
GB2623575A
GB2623575A GB2215603.8A GB202215603A GB2623575A GB 2623575 A GB2623575 A GB 2623575A GB 202215603 A GB202215603 A GB 202215603A GB 2623575 A GB2623575 A GB 2623575A
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GB
United Kingdom
Prior art keywords
absorbent
scrubber
carbon dioxide
reformer
exhaust gas
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.)
Pending
Application number
GB2215603.8A
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GB202215603D0 (en
Inventor
Alan Burns Michael
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Clean Thermodynamic Energy Conversion Ltd
Original Assignee
Clean Thermodynamic Energy Conversion Ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Clean Thermodynamic Energy Conversion Ltd filed Critical Clean Thermodynamic Energy Conversion Ltd
Priority to GB2215603.8A priority Critical patent/GB2623575A/en
Publication of GB202215603D0 publication Critical patent/GB202215603D0/en
Priority to PCT/EP2023/079229 priority patent/WO2024084021A1/en
Publication of GB2623575A publication Critical patent/GB2623575A/en
Pending 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
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/10—Inorganic absorbents
    • B01D2252/103—Water
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
    • B01D2252/20—Organic absorbents
    • B01D2252/204—Amines
    • B01D2252/20478—Alkanolamines
    • B01D2252/20484—Alkanolamines with one hydroxyl group
    • 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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1425—Regeneration of liquid absorbents
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • 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
    • 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

Landscapes

  • 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)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

A gas treatment system comprising: a carbon dioxide scrubber, 101, an absorbent supply ,103, and an absorbent reformer, 105. The absorbent scrubs carbon dioxide (CO2) and residual pollutants from the gas, and the reformer,105, receives the carbon dioxide-rich absorbent from the scrubber 101 and regenerates it for re-use. The gas source may be a waste processing system, the scrubber may be a cyclonic scrubber, the absorbent may be an aqueous amine solution, and the regeneration step may utilise steam from the waste processing system. The absorbent may be filtered, 109, as part of the recycling process to remove further potential pollutants.

Description

EXHAUST GAS TREATMENT SYSTEM AND METHOD
The present invention relates to an exhaust gas treatment system for and method of treating exhaust gas, in particular from a waste treatment system for processing waste product, such as municipal solid waste (MSW) and processed waste, for example, refuse-derived waste (RDF), including human waste, waste which contains organofluorines, such as perfluorocarbons (PFCs), including perfluoroalkyl and polyfluoroalkyl substances (PFAS), such as perfluorooctanoic acid (PFOA), perfluorooctanesulfonic acid (PFOS) and perfluorohexane sulfonic acid (PFHxS), and also fluorinated gases (F-gases). The waste product can be a solid, liquid or gas, or combinations thereof, and can be supplied in many forms, for example, sludge, plastic and biomass, and includes tires and flooring material and tiles.
PFAS are substances having a chain of linked carbon and fluorine atoms, and, because the carbon-fluorine bond is one of the strongest, these substances are recalcitrant and not easily degraded.
Waste product typically contains a significant percentage of water, which gives rise to problems in processing, especially in systems using high-temperature combustion. The present inventors have, however, recognized that this contained water can advantageously be employed in processing of the waste product itself, in that, if the contained water is extracted to generate supercritical water, this supercritical water can be utilized for supercritical water oxidation (SCWO), which has been found to reduce the PFAS content by greater than 99% (Krause et al, Supercritical Water Oxidation as an Innovative Technology for PFAS Destruction, Journal of Environmental Engineering, 148, 10.1061/(ASCE)EE.1943-7870.0001957), The PFAS content of the waste product would otherwise have to be converted thermally at high temperature, typically above 1200 C, and moisture arising from water in the waste product would have to be carefully regulated. -2 -
In one aspect the present invention provides an exhaust gas treatment system, comprising: a carbon dioxide scrubber which receives an exhaust gas, optionally from a waste processing system; an absorbent supply which supplies absorbent to the scrubber, wherein the absorbent acts to remove carbon dioxide and residual pollutants from the exhaust gas; and an absorbent reformer which receives the carbon dioxide-rich absorbent from the scrubber and reforms the absorbent for re-use.
In another aspect the present invention provides a method of treating an exhaust gas, comprising: delivering an exhaust gas, optionally from a waste processing system, to a carbon dioxide scrubber; supplying absorbent to the scrubber from an absorbent supply, wherein the absorbent acts to remove carbon dioxide and residual pollutants from the exhaust gas; and reforming the absorbent from the carbon dioxide-rich absorbent which is received from the scrubber using an absorbent reformer for re-use.
Preferred embodiments of the present invention will now be described hereinbelow by way of example only with reference to the accompanying drawings, in which: Figure 1 illustrates a waste processing system in accordance with one embodiment of the present invention; Figure 2 illustrates a horizontal sectional view (along section I-I in Figure 1) of the system of Figure 1; Figure 3 illustrates an exhaust gas treatment system in accordance with one embodiment of the present invention; and Figure 4 represents the reduction in carbon dioxide emission to the atmosphere using the exhaust gas treatment system of Figure 3. -3 -
Figures 1 and 2 illustrate a waste processing system in accordance with one embodiment of the present invention.
The system comprises a primary waste product supply 3 for supplying waste product, a secondary waste product supply 5 for supplying waste product, a drying chamber 7 which is supplied with the waste product from the primary waste product supply 3 and heats the waste product to dry the waste product and generate steam, a gasification chamber 9 which receives the waste product from the drying chamber 7 and in which the waste product is heated to generate synthetic gas or syngas, a treatment unit 11 for treating steam vented from the drying chamber 7, and a thermal converter 12 for generating a stream of heated gas for energy conversion.
In one embodiment the waste product is municipal solid waste (MSW) or processed waste, for example, refuse-derived waste (RDF), including human waste.
In one embodiment the waste product contains organofluorines, such as perfluorocarbons (PFCs), including perfluoroalkyl and polyfluoroalkyl substances (PFAS), for example, perfluorooctanoic acid (PFOA), perfluorooctanesulfonic acid (PFOS) and perfluorohexane sulfonic acid (PFHxS).
In one embodiment the waste product contains fluorinated gases (F-gases).
In one embodiment the waste product comprises a solid, liquid or gas, or combinations thereof.
In one embodiment the waste product is supplied in many forms, for example, sludge, plastic and biomass, and includes tires and flooring material and tiles.
In this embodiment the primary waste product supply 3 comprises a container 15, here in the form of a hopper, which contains waste product, in one -4 -embodiment in the form of a solid or sludge or mixtures thereof, and a waste feed 17 which feeds waste product from the container 15 to the drying chamber 7.
In this embodiment the waste feed 17 comprises a ram 19 which is actuated reciprocally between a first, material-receiving position, in which waste product can fall from the container 15 in front of the ram 19, and a second, feed position, in which the waste product ahead of the ram 19 is fed, here pushed, into an upstream end of the drying chamber 7. With this action of the ram 19, the feeding of fresh waste product into the drying chamber 7 causes waste product at a downstream end of the drying chamber 7 to be fed into an upstream end of the gasification chamber 9.
In this embodiment the drying chamber 7 comprises an elongate cavity 21 along which waste product is displaced with operation of the waste feed 17.
In this embodiment the drying chamber 7 includes a heated gas source 23 which supplies a heated gas into the cavity 21 thereof, which heated gas can be a recirculated exhaust gas, and an outlet 24, here including a plurality of vents 26, through which steam, in this embodiment flash steam, is vented from the drying chamber 7. With this configuration, the heated gas supplied to the drying chamber 7 and heat from the gasification chamber 9 acts to heat the waste product within the cavity 21 of the drying chamber 7.
In this embodiment the temperature of the drying chamber 7 is controlled such that the upstream end of the cavity 21 is maintained at a temperature of less than 600 C, which is sufficient to yield steam from the moisture within the waste product.
In this embodiment the treatment unit 11 heats the steam which is received from the drying chamber 7 to a temperature above 374 C and a pressure above 22.1 MPa, which represents the critical point, in order to generate supercritical water.
In this embodiment the treatment unit 11 includes an inlet 27 which is fluidly connected to the outlet 24 of the drying chamber? and an outlet 28 which is fluidly connected to the thermal converter 12.
In this embodiment the treatment unit 11 includes a heated gas source 29 which supplies a heated gas to the treatment unit 11 to heat the received steam, which heated gas can be a recirculated exhaust gas.
In this embodiment the treatment unit 11 includes a reactor 30, which generates supercritical water from the received steam.
In this embodiment the treatment unit 11 includes an oxidant supply 31 which supplies an oxidant, here air, to the generated supercritical water. With the addition of oxidant, the supercritical water provides for supercritical water oxidation of material, here in the thermal converter 12, which, as noted above, has been found to reduce the PFAS content by greater than 99%.
In this embodiment the gasification chamber 9 comprises a cavity 33 having an outlet 34, here in an upper section thereof, and a floor assembly 35, here at lower section thereof, over which waste product is transferred.
In this embodiment the floor assembly 35 comprises a transfer mechanism 39 which provides a grate at the floor of the gasification chamber 9 and transfers waste product which is received from the drying chamber 7 through a gasification zone GZ.
In this embodiment the transfer mechanism 39 comprises a stepped assembly 45 over which waste product is transferred.
In this embodiment the stepped assembly 45 comprises a plurality of steps 47, here of fixed position, which are arranged in staggered downward relation, and a plurality of movable members 49 which are movable -6 -reciprocally in relation to the steps 47 to transfer waste product along and over the steps 47.
In this embodiment the steps 47 are arranged substantially in spaced, parallel relation, and the movable members 49 are configured such that upper and lower surfaces of the movable members 49 are in close relation to adjacent surfaces of the steps 47, whereby the action of withdrawing the movable members 49 acts to scrape material therefrom.
In this embodiment ones or groups of ones of the movable members 49 are movable independently of one another, so as to enable control of an amount of waste product in the gasification zone GZ. This manner of control allows readily for use with different kinds of waste product, with the rate of transfer being controlled accordingly.
In this embodiment the gasification chamber 9 includes a heated gas source 51 which supplies a heated gas to the gasification chamber 9, which heated gas can be a recirculated exhaust gas, and heats the waste product to generate synthetic gas or syngas, with the temperature within the gasification zone GZ being controlled so as to prevent combustion, here to a temperature of less than 600 C. In this embodiment the heated gas source 51 supplies the heated gas to the gasification chamber 9 through the transfer mechanism 39.
In this embodiment the gasification chamber 9 includes a combustion zone CZ at a downstream region thereof, at which a temperature is maintained to provide for starved combustion of the waste product thereat, which waste product has passed through the gasification zone GZ and from which syngas has been extracted.
In this embodiment the gasification chamber 9 includes a flow restrictor 55, here in the form of an apertured refractory member, at the outlet 34 thereof -7 -through which the flow of the generated syngas and heated gas is restricted, in order to provide for controlled generation and supply of syngas from the gasification chamber 9.
In this embodiment the thermal converter 12 is fluidly connected to the outlets 28, 34 of the treatment unit 11 and the gasification chamber 9.
In this embodiment the outlet 28 of the treatment unit 11 is fluidly connected to the thermal converter 12 downstream of the outlet 34 of the gasification chamber 9.
In this embodiment the thermal converter 12 includes an elongate cavity 71, with the outlet 34 of the gasification chamber 9 being located at an upstream region of the cavity 71.
In this embodiment the thermal converter 12 includes a flow accelerator 73 which is fluidly connected to the outlet 34 of the gasification chamber 9 and acts to provide a flow of syngas of increased velocity from the gasification chamber 9.
In this embodiment the thermal converter 12 includes a burner 75 which acts to ignite and provide for burning of the syngas as delivered from the gasification chamber 9, and a suction fan 77 which acts to draw the syngas into the cavity 71 of the thermal converter 12.
In this embodiment the suction fan 77 is regulated to control temperature and residence time within the thermal converter 12.
In this embodiment the thermal converter 12 is controlled such that a temperature of at least 1000 C, in one embodiment at least 1100 C, is maintained in the cavity 71 thereof. In this embodiment the temperature within the cavity 71 of the thermal regulator 12 is maintained at a temperature of less than 1400 C. In this embodiment the secondary waste product supply 5 comprises a container 81, here in the form of a chamber, which contains waste product, in one embodiment in the form of a particulate, liquid or gas or mixtures thereof, and a waste feed 83 which feeds waste product from the container 81 into the cavity 71 of the thermal converter 12.
In one embodiment the container 81 is adapted separately to contain particulate, liquid and gas or mixtures thereof.
In one embodiment the waste feed 83 comprises one or more injectors 85.
With this configuration, the thermal converter 12, in addition to generating a stream of heated gas for energy conversion, acts further to destroy substances which are delivered in the gas flow from the gasification chamber 9, including residual hydrocarbons, organofluorines and fluorinated gases, and also waste product which is delivered directly by the secondary waste product supply 5 into the cavity 71 of the thermal converter 12.
Figure 3 illustrates an exhaust gas treatment system in accordance with one embodiment of the present invention.
The exhaust gas treatment system comprises a carbon dioxide scrubber 101 which receives an exhaust gas, in this embodiment from the waste treatment system of the above-described embodiment, and an absorbent, which acts to remove carbon dioxide and residual pollutants from the exhaust gas, an absorbent supply 103 for supplying absorbent to the scrubber 101, and a carbon dioxide reformer 105 which receives the carbon dioxide-rich absorbent from the scrubber 101 and reforms the absorbent and yields carbon dioxide for capture.
In this embodiment the scrubber 101 is a cyclone scrubber. -9 -
In one embodiment the absorbent is provided as a spray.
In this embodiment the absorbent is an aqueous absorbent. In one embodiment the absorbent is an amine.
In this embodiment the absorbent is monoethanolamine (MEA).
In this embodiment the reformer 105 reforms the carbon-dioxide absorbent by steam reforming to boil the absorbent, here with steam supplied from the waste treatment system, and yields carbon dioxide for capture, with the lean, reformed absorbent being recirculated to the absorbent supply 103.
In this embodiment the system further comprises a carbon dioxide extraction unit 107, which extracts carbon dioxide from the reformer 105 under vacuum and compresses the extracted carbon dioxide for recycling.
In this embodiment the system further comprises a filtration unit 109, which receives the residual water from the reformer 105 and filters residual pollutants therefrom.
With this configuration, the present inventors have recognized that, by utilizing steam, as an available by-product of the waste processing system, much reduced consumption of the absorbent can be achieved and the captured carbon dioxide can be recycled to provide a usable source of carbon dioxide.
Use of the embodied exhaust gas treatment system in the above-described waste processing system avoids significant carbon dioxide emission to the atmosphere as compared to incineration, with the present embodiment typically yielding a reduction in the atmospheric carbon dioxide emission of greater than 80%, as represented in Figure 4.
-10 -Finally, it will be understood that the present invention will be described in its preferred embodiments and can be modified in many different ways without departing from the scope of the present invention as defined by the appended claims.
For example, in the above-described waste processing system, the secondary waste product supply 5 could be omitted.

Claims (18)

  1. CLAIMS1. An exhaust gas treatment system, comprising: a carbon dioxide scrubber (101) which receives an exhaust gas, optionally from a waste processing system; an absorbent supply (103) which supplies absorbent to the scrubber (101), wherein the absorbent acts to remove carbon dioxide and residual pollutants from the exhaust gas; and an absorbent reformer (105) which receives the absorbent from the scrubber (101) and reforms the absorbent for re-use.
  2. 2. The system of claim 1, wherein the scrubber (101) is a cyclone scrubber.
  3. 3. The system of claim 1 or 2, wherein the absorbent is an aqueous absorbent.
  4. 4. The system of any of claims 1 to 3, wherein the absorbent is an amine.
  5. 5. The system of claim 4, wherein the absorbent is monoethanolamine (MEA).
  6. 6. The system of any of claims 1 to 5, wherein the reformer (105) supplies the reformed absorbent to the absorbent supply (103).
  7. 7. The system of any of claims 1 to 6, wherein the reformer (105) reforms the absorbent by steam reforming, optionally with steam supplied from the waste treatment system.
  8. 8. The system of any of claims 1 to 7, further comprising: a carbon dioxide extraction unit (107) which extracts carbon dioxide from the reformer (105).
  9. -12 - 9. The system of any of claims 1 to 8, further comprising: a filtration unit (109) which receives residue from the reformer (105) and filters pollutants therefrom.
  10. 10. A method of treating an exhaust gas, comprising: delivering an exhaust gas, optionally from a waste processing system, to a carbon dioxide scrubber (101); supplying absorbent to the scrubber (101) from an absorbent supply (103), wherein the absorbent acts to remove carbon dioxide and residual pollutants from the exhaust gas; and reforming the absorbent from the absorbent which is received from the scrubber (101) using an absorbent reformer (105) for re-use.
  11. 11. The method of claim 10, wherein the scrubber (101) is a cyclone scrubber.
  12. 12. The method of claim 10 or 11, wherein the absorbent is an aqueous absorbent.
  13. 13. The method of any of claims 10 to 12, wherein the absorbent is an amine.
  14. 14. The method of claim 13, wherein the absorbent is monoethanolamine (MEA).
  15. 15. The method of any of claims 10 to 14, further comprising: supplying the reformed absorbent to the absorbent supply (103).
  16. 16. The method of any of claims 10 to 15, wherein the absorbent is reformed by steam reforming, optionally with steam supplied from the waste treatment system.
  17. 17. The method of any of claims 10 to 16, further comprising: -13 -extracting carbon dioxide from the absorbent reformer (105).
  18. 18. The method of any of claims 10 to 17, further comprising: filtering pollutants from residue which is received from the reformer (105) using a filtration unit (109).
GB2215603.8A 2022-10-21 2022-10-21 Exhaust gas treatment system and method Pending GB2623575A (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
GB2215603.8A GB2623575A (en) 2022-10-21 2022-10-21 Exhaust gas treatment system and method
PCT/EP2023/079229 WO2024084021A1 (en) 2022-10-21 2023-10-20 Exhaust gas treatment system and method

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
GB2215603.8A GB2623575A (en) 2022-10-21 2022-10-21 Exhaust gas treatment system and method

Publications (2)

Publication Number Publication Date
GB202215603D0 GB202215603D0 (en) 2022-12-07
GB2623575A true GB2623575A (en) 2024-04-24

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WO (1) WO2024084021A1 (en)

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20040118126A1 (en) * 2002-12-19 2004-06-24 Ong James O.Y. Use of a chemical solvent to separate CO2 from a H2S-rich stream
WO2016160612A1 (en) * 2015-03-27 2016-10-06 Blue Planet, Ltd. Modular co2 sequestration units and systems, and methods for using the same
WO2017136728A1 (en) * 2016-02-03 2017-08-10 Novek Ethan Integrated process for capturing carbon dioxide
US20190128603A1 (en) * 2017-10-27 2019-05-02 Larry Baxter Vapor Stripping by Desublimation and Dissolution
US20190217248A1 (en) * 2018-01-16 2019-07-18 Nuorganics LLC Systems and methods for concentrating a substance recovered from a gas stream
CN212548975U (en) * 2020-12-23 2021-02-19 天津环科环境咨询有限公司 Flue gas desulfurization denitration washing system

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9631284B2 (en) * 2013-03-15 2017-04-25 Colorado School Of Mines Electrochemical device for syngas and liquid fuels production

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20040118126A1 (en) * 2002-12-19 2004-06-24 Ong James O.Y. Use of a chemical solvent to separate CO2 from a H2S-rich stream
WO2016160612A1 (en) * 2015-03-27 2016-10-06 Blue Planet, Ltd. Modular co2 sequestration units and systems, and methods for using the same
WO2017136728A1 (en) * 2016-02-03 2017-08-10 Novek Ethan Integrated process for capturing carbon dioxide
US20190128603A1 (en) * 2017-10-27 2019-05-02 Larry Baxter Vapor Stripping by Desublimation and Dissolution
US20190217248A1 (en) * 2018-01-16 2019-07-18 Nuorganics LLC Systems and methods for concentrating a substance recovered from a gas stream
CN212548975U (en) * 2020-12-23 2021-02-19 天津环科环境咨询有限公司 Flue gas desulfurization denitration washing system

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WO2024084021A1 (en) 2024-04-25
GB202215603D0 (en) 2022-12-07

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