[go: up one dir, main page]

WO2018136628A1 - Procédé et appareil pour l'élimination continue de vapeurs de gaz - Google Patents

Procédé et appareil pour l'élimination continue de vapeurs de gaz Download PDF

Info

Publication number
WO2018136628A1
WO2018136628A1 PCT/US2018/014230 US2018014230W WO2018136628A1 WO 2018136628 A1 WO2018136628 A1 WO 2018136628A1 US 2018014230 W US2018014230 W US 2018014230W WO 2018136628 A1 WO2018136628 A1 WO 2018136628A1
Authority
WO
WIPO (PCT)
Prior art keywords
vapor
liquid mixture
carrier gas
gas
liquid
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/US2018/014230
Other languages
English (en)
Inventor
Larry Baxter
Aaron SAYRE
Stephanie BURT
Nathan Davis
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.)
Individual
Original Assignee
Individual
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from US15/410,024 external-priority patent/US10213731B2/en
Priority claimed from US15/410,106 external-priority patent/US10307709B2/en
Application filed by Individual filed Critical Individual
Priority to CN201880019280.7A priority Critical patent/CN110678242B/zh
Priority to EP18741443.8A priority patent/EP3570950A4/fr
Publication of WO2018136628A1 publication Critical patent/WO2018136628A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D7/00—Sublimation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/40—Extractive distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • 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
    • B01D53/002—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 condensation
    • 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
    • B01D53/26—Drying gases or vapours
    • B01D53/265—Drying gases or vapours by refrigeration (condensation)
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
    • 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
    • B01D2257/00—Components to be removed
    • B01D2257/80—Water
    • 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
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • This invention relates generally to the field of purification of gases.
  • Our immediate interest is in the removal of vapors, such as water or carbon dioxide, that would be considered an impurity from a gas stream, such as combustion flue gas, natural gas, syngas, and air.
  • Chemical complexing in solids occurs by passing the gas stream through a bed of desiccants or related solids that chemically bind the vapor. Chemical complexing in liquids occurs in brine solutions, near-eutectic solutions, or other systems where the liquid has the ability to complex with the vapor.
  • Condensation occurs when the partial pressure of the vapor is reduced below the vapor's condensation point, allowing the vapor to condense into a liquid form.
  • Desublimation is considered a form of condensation, as it brings a gas to a condensed state, namely to a solid.
  • United States patent publication number 2008/7314502 to Kelley teaches a method for the separation of a single component from a multi -component gas stream. This disclosure is pertinent and could benefit from vapor removal methods disclosed herein and is hereby incorporated for reference in its entirety for all that it teaches.
  • United States patent publication number 2011/0203174 to Lackner teaches a method and apparatus for extracting carbon dioxide from air. This disclosure is pertinent and could benefit from vapor removal methods disclosed herein and is hereby incorporated for reference in its entirety for all that it teaches.
  • United States patent publication number 9067173 to Alban teaches a method and equipment for treating carbon dioxide-rich smoke. This disclosure is pertinent and could benefit from vapor removal methods disclosed herein and is hereby incorporated for reference in its entirety for all that it teaches.
  • United States patent publication number 8088197 to Wright teaches a method for removing carbon dioxide from air. This disclosure is pertinent and could benefit from vapor removal methods disclosed herein and is hereby incorporated for reference in its entirety for all that it teaches.
  • a method for continuously removing vapor, such as water or carbon dioxide from a carrier gas includes, first, causing direct contact of the carrier gas with a liquid mixture in a separation chamber, the carrier gas condensing at a lower temperature than the vapor.
  • a combination of chemical effects cause the vapor to condense, complex, or both condense and complex with the liquid mixture.
  • the liquid mixture is chosen from the group consisting of: first, a combination of components that can be maintained in a liquid phase at a temperature below the vapor's condensation point, whereby the vapor condenses into the liquid mixture; second, a combination of components where at least one component forms a chemical complex with the carbon dioxide vapor and thereby extracts at least a portion of the carbon dioxide vapor from the carrier gas; and third, a combination of components that can both be maintained in a liquid phase at a temperature below the carbon dioxide's condensation point, and wherein at least one component forms a chemical complex with the carbon dioxide vapor and thereby extracts at least a portion of the carbon dioxide vapor from the carrier gas.
  • the liquid mixture is then reconstituted after passing through the separation chamber by a chemical separation process chosen to remove an equivalent amount of the carbon dioxide vapor from the liquid mixture as was removed from the carrier gas.
  • the reconstituted liquid mixture is restored to temperature and pressure through heat exchange, compression, and expansion, as necessary, in preparation for recycling back to the separation chamber.
  • the liquid mixture is then returned to the separation chamber. In this manner, the carrier gas leaving the exchanger has between 1% and 100% of the carbon dioxide vapor removed.
  • the liquid mixture may consist of a mixture of water and a compound from either of the following two groups: i) ionic compounds including potassium carbonate, potassium formate, potassium acetate, calcium magnesium acetate, magnesium chloride, sodium chloride, lithium chloride, and calcium chloride; and, ii) soluble organic compounds including glycerol, ammonia, propylene glycol, ethylene glycol, ethanol, and methanol.
  • the carrier gas may consist of combustion flue gas, moist air, syngas, producer gas, natural gas, steam reforming gas, any hydrocarbon that has higher volatility than carbon dioxide or water, as the case may be, or light gases.
  • the separation chamber may be either a counter-current, direct-contact exchanger or a co-current, direct-contact exchanger.
  • the chemical separation process for reconstituting the liquid mixture may be distillation, pressure-swing separation, liquid extraction, solid extraction, reverse osmosis, forward osmosis, filtration, stripping, or a combination of these.
  • Figure 1 shows a general process flow diagram in accordance with an embodiment of the invention
  • Figure 2 shows a process flow diagram for dehydrating combustion flue gas, in accordance with an embodiment of the invention
  • Figure 3 shows a process flow diagram for dehydrating natural gas, in accordance with an embodiment of the invention
  • FIG. 4 shows a process flow diagram for dehydrating propane gas, in accordance with an embodiment of the invention
  • Figure 5 shows a process flow diagram for dehydrating nitrogen gas, in accordance with an embodiment of the invention
  • Figure 6 shows a phase diagram for ionic compounds that include a subset of useful compounds in accordance with some embodiments of the invention
  • Figure 7 shows a phase diagram for inorganic and organic compounds that include a subset of useful compounds in accordance with some embodiments of the invention.
  • a carrier gas 102 containing a vapor 104 to be removed, enters a separation chamber 106.
  • the vapor is one that would be considered an impurity to the carrier gas, such as water vapor or carbon dioxide vapor.
  • a cold liquid mixture 108 enters separation chamber 106 flowing counter-current to the carrier gas 102 vapor 104 combination.
  • Carrier gas 102 exits separations chamber 106 with substantially less vapor 104. In some embodiments, this can mean a removal of between 1% and 100% of vapor 104, such as carbon dioxide vapor.
  • Liquid mixture 108 and extracted vapor 104 exit separations chamber 106 and are conveyed to a separations system 110.
  • the extracted carbon dioxide vapor is transported as a combination of carbon dioxide dissolved in liquid mixture 108, carbon dioxide complexed in liquid mixture 108, and solid carbon dioxide suspended in liquid mixture 108.
  • Captured carbon dioxide vapor 104 is removed in separations system 110, and liquid mixture 108, now at the same composition as required for separation chamber 106, is sent to a heat exchanger, compressor, or expander 112 to bring liquid mixture 108 to the required temperature for separations chamber 106.
  • the chemical separation process for reconstituting the liquid mixture may be distillation, pressure-swing separation, liquid extraction, solid extraction, reverse osmosis, forward osmosis, filtration, stripping, or a combination of these.
  • the liquid mixture consists of water and a compound from either of the following two groups: i) ionic compounds including potassium carbonate, potassium formate, potassium acetate, calcium magnesium acetate, magnesium chloride, sodium chloride, lithium chloride, and calcium chloride; and, ii) soluble organic compounds including glycerol, ammonia, propylene glycol, ethylene glycol, ethanol, and methanol.
  • Carrier gas 102 may be combustion flue gas, syngas, producer gas, natural gas, steam reforming gas, any hydrocarbon that has higher volatility than carbon dioxide or water, as the case may be, or light gases.
  • Combustion flue gas consists of the exhaust gas from a fireplace, oven, furnace, boiler, steam generator, or other combustor.
  • the combustion fuel sources include coal, hydrocarbons, and biomass.
  • Combustion flue gas varies greatly in composition depending on the method of combustion and the source of fuel. Combustion in pure oxygen produces little to no nitrogen in the flue gas. Combustion using air leads to the majority of the flue gas consisting of nitrogen.
  • the non-nitrogen flue gas consists of mostly carbon dioxide, water, and sometimes unconsumed oxygen. Small amounts of carbon monoxide, nitrogen oxides, sulfur dioxide, hydrogen sulfide, and trace amounts of hundreds of other chemicals are present, depending on the source. Entrained dust and soot will also be present in all combustion flue gas streams. The method disclosed applies to any combustion flue gases.
  • Syngas consists of hydrogen, carbon monoxide, and carbon dioxide.
  • Producer gas consists of a fuel gas manufactured from materials such as coal, wood, or syngas. It consists mostly of carbon monoxide, with tars and carbon dioxide present as well.
  • Steam reforming is the process of producing hydrogen, carbon monoxide, and other compounds from hydrocarbon fuels, including natural gas.
  • the steam reforming gas referred to herein consists primarily of carbon monoxide and hydrogen, with varying amounts of carbon dioxide and water.
  • Light gases include gases with higher volatility than water or carbon dioxide, as the case may be, including hydrogen, helium, nitrogen, and oxygen. This list is for example only and should not be implied to constitute a limitation as to the viability of other gases in the process. A person of skill in the art would be able to evaluate any gas as to whether it has higher volatility than water or carbon dioxide.
  • liquid mixture 108 is conveyed from separation chamber 106 by a pump.
  • the pump chosen would preferably be a cryogenic-style pump, capable of handling temperatures below the freezing point of carbon dioxide, as well as handling solid particles.
  • the pump chosen could be a centrifugal, piston, pressure-recovery, propeller, circulator, slurry, positive-displacement, diaphragm, progressive-cavity, screw, or vane pump.
  • the internals of the pump would again be chosen based on the specifics of liquid mixture 108, but would have to be chosen to be resistant to whatever materials were conveyed. They would need to be cold resistant, but may also need to be acid or corrosive resistant.
  • the possibility of particulates, especially in cases where the carrier gas may have contaminants like soot or dust, would also indicate an erosion resistant material, such as ceramic or stainless steel.
  • a combustion flue gas 202 containing vapor 204 to be removed, enters a counter-current direct contact exchanger 206.
  • a cold liquid mixture 208 enters exchanger 206 flowing counter-current to the combustion flue gas 202/vapor 204 combination.
  • Liquid mixture 208 is chosen to consist of water and calcium and/or sodium chloride at an appropriate concentration and temperature, as per Figure 6.
  • Combustion flue gas 202 exits exchanger 206 with all vapor 204 removed.
  • the liquid mixture 208 and extracted 204 exit exchanger 206 and are conveyed to a solid- liquid separation system 210 where the captured solid carbon dioxide 204 is removed, and liquid mixture 208, now at the same composition as required for exchanger 206, is sent to a heat exchanger 212 for cooling to the required temperature for exchanger 206.
  • Liquid mixture 208 is assumed to reach an equilibrium with dissolved and complexed carbon dioxide as it recirculates, meaning the removed carbon dioxide is primarily removed as a solid.
  • FIG. 3 another embodiment of the present invention is disclosed, with a process flow diagram 300 shown.
  • natural gas 302 containing a vapor 304 to be removed, enters a co-current direct contact exchanger 306.
  • a cold liquid mixture 308 enters exchanger 306 flowing co-current to the liquefied natural gas 302/ vapor 304 combination.
  • Liquid mixture 308 is chosen to to consist of water and ethanol at an appropriate concentration and temperature, as per Figure 7.
  • Liquefied natural gas 302 exits exchanger 306 with all vapor 304 removed.
  • liquid mixture 308 and extracted 304 exit exchanger 306 and are conveyed to a solid-liquid separation system 310 where the captured solid carbon dioxide 304 is removed, and liquid mixture 308, now at the same composition as required for exchanger 306, is sent to a heat exchanger 312 for cooling to the required temperature for exchanger 306.
  • Liquid mixture 308 is assumed to reach an equilibrium with dissolved and complexed carbon dioxide as it recirculates, meaning the removed carbon dioxide is primarily removed as a solid.
  • propane gas 402 containing vapor 404 to be removed, enters a counter-current direct contact exchanger 406.
  • a cold liquid mixture 408 enters exchanger 406 flowing counter-current to the propane 402/ vapor 404 combination.
  • Liquid mixture 408 is chosen to consist of water and potassium acetate at an appropriate concentration and temperature, as per Figure 6.
  • Propane gas 402 exits exchanger 406 with all vapor 404 removed.
  • liquid mixture 408 and extracted vapor 404 exit exchanger 406 and are conveyed to a solid-liquid separation system 410 where the captured solid carbon dioxide 404 is removed, and liquid mixture 408, now at the same composition as required for exchanger 406, is sent to a heat exchanger 412 for cooling to the required temperature for exchanger 406.
  • Liquid mixture 408 is assumed to reach an equilibrium with dissolved and complexed carbon dioxide as it recirculates, meaning the removed carbon dioxide is primarily removed as a solid.
  • nitrogen gas 502 containing vapor 504 to be removed, enters a counter-current direct contact exchanger 506.
  • a cold liquid mixture 508 enters exchanger 506 flowing counter-current to the nitrogen gas 502/ vapor 504 combination.
  • Liquid mixture 508 is chosen to consist of water and potassium acetate at an appropriate concentration and temperature, as per Figure 7.
  • Nitrogen gas 502 exits exchanger 506 with all vapor 504 removed.
  • liquid mixture 508 and extracted vapor 504 exit exchanger 506 and are conveyed to a flash separation system 510 where the captured solid carbon dioxide 504 is sublimated and removed, and liquid mixture 508, now at the same composition as required for exchanger 506, is sent to a heat exchanger 512 for cooling to the required temperature for exchanger 506.
  • Liquid mixture 508 is assumed to reach an equilibrium with dissolved and complexed carbon dioxide as it recirculates, meaning the removed carbon dioxide is primarily removed as a solid.
  • FIG. 6 a phase diagram for various ionic compounds that are acceptable for use as part of liquid mixture 108, 208, or 408 with water is shown. While this list includes very useful ionic compounds in solution with water, this chart should not be interpreted as limiting the selection of compounds useful in the present invention.
  • Those of ordinary skill in the art can determine the desired concentration and temperatures for liquid mixtures 108, 208, and 408 based on reference charts and phase diagrams for different combinations of compounds. In the case of the phase diagram in Figure 6, the concentration chosen will determine the temperature that liquid mixture 108, 208, or 408 can reach. Depending on how much vapor is to be removed, different concentrations will be required.
  • liquid mixtures 108, 208, or 408 are chosen to have a combination of one or more of the following properties: (i) Liquid mixture 108, 208, or 408 are at a temperature and pressure such that the partial vapor pressure is below the condensation point of vapor 104, 204, or 404, and thus vapor 104, 204, or 404 desublimates. (ii) Liquid mixtures 108, 208, or 408 contain at least one compound that can form complexes with vapor 104, 204, or 404, the system being at such a concentration that any of vapor 104, 204, or 404 passing through will be complexed.
  • Liquid mixtures 108, 208, or 408 contain a combination of components wherein at least one component absorbs vapor 108, 208, or 408 and thereby extracts at least a portion of vapor 108, 208, or 408 from carrier gas 102, 202, or 402. iv) A combination of the above.
  • FIG. 7 a phase diagram for various inorganic and organic compounds that are acceptable for use as part of liquid mixture 108, 208, 308, 408, and 508 with water is shown.
  • This diagram is prior art. While this list includes very useful organic compounds in solution with water, this chart should not be interpreted as limiting the selection of compounds useful in the present invention.
  • Those of ordinary skill in the art can determine the desired concentration and temperatures for liquid mixtures 108, 208, 308, 408, and 508 based on reference charts and phase diagrams for different combinations of compounds. In the case of the phase diagram in Figure 7, the concentration chosen will determine the temperature that liquid mixture 108, 208, 308, 408, and 508 can reach. Depending on how much vapor is to be removed, different concentrations will be required.
  • liquid mixture 108, 208, 308, 408, and 508 are chosen to have a combination of one or more of the following properties: (i) Liquid mixture 108, 208, 308, 408, and 508 are at a temperature and pressure such that the partial vapor pressure is below the condensation point of vapor 104, 204, 304, 404, or 504, and thus vapor 104, 204, 304, 404, or 504 desublimates.
  • Liquid mixtures 108, 208, 308, 408, and 508 contain at least one compound that can form complexes with vapor 104, 204, 304, 404, or 504, the system being at such a concentration that any of vapor 104, 204, 304, 404, or 504 passing through will be complexed.
  • Liquid mixtures 108, 208, 308, 408, and 508 contain a combination of components wherein at least one component absorbs vapor 108, 208, 308, 408, and 508 and thereby extracts at least a portion of vapor 108, 208, 308, 408, and 508 from carrier gas 102, 202, 302, 402, or 502.
  • a combination of the above

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Analytical Chemistry (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Water Supply & Treatment (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

L'invention concerne un procédé pour l'élimination continue d'une vapeur, qui serait considérée comme une impureté, d'un gaz vecteur. De préférence, la vapeur est soit de la vapeur d'eau soit de la vapeur de dioxyde de carbone. Le présent procédé inclut, en premier lieu, le fait d'amener un contact direct du gaz vecteur avec un mélange liquide dans une chambre de séparation, le gaz vecteur se condensant à une plus basse température que la vapeur. Une combinaison d'effets chimiques amène la vapeur à se condenser, à complexer, ou à la fois à se condenser et à complexer avec le mélange liquide.
PCT/US2018/014230 2017-01-19 2018-01-18 Procédé et appareil pour l'élimination continue de vapeurs de gaz Ceased WO2018136628A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
CN201880019280.7A CN110678242B (zh) 2017-01-19 2018-01-18 从多种气体中连续除去蒸气的方法和装置
EP18741443.8A EP3570950A4 (fr) 2017-01-19 2018-01-18 Procédé et appareil pour l'élimination continue de vapeurs de gaz

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US15/410,024 2017-01-19
US15/410,106 2017-01-19
US15/410,024 US10213731B2 (en) 2017-01-19 2017-01-19 Method and apparatus for continuous removal of carbon dioxide vapors from gases
US15/410,106 US10307709B2 (en) 2017-01-19 2017-01-19 Method and apparatus for continuous removal of water vapors from gases

Publications (1)

Publication Number Publication Date
WO2018136628A1 true WO2018136628A1 (fr) 2018-07-26

Family

ID=62908962

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/US2018/014230 Ceased WO2018136628A1 (fr) 2017-01-19 2018-01-18 Procédé et appareil pour l'élimination continue de vapeurs de gaz

Country Status (3)

Country Link
EP (1) EP3570950A4 (fr)
CN (1) CN110678242B (fr)
WO (1) WO2018136628A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10758874B2 (en) 2016-09-15 2020-09-01 Netzsch-Gerätebau GmbH Method and device for generating a continuous carrier gas/vapour mixture stream
EP3865202A1 (fr) 2020-02-13 2021-08-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Utilisation d'effluent gazeux contenant du co2 dans la preparation du beton

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113175537B (zh) * 2021-04-24 2022-02-08 开维喜阀门集团有限公司 一种基于智慧水利工程的闸阀系统及其运行方法

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3759047A (en) * 1971-11-22 1973-09-18 Univ California Vapor condensation system and method
US4342624A (en) * 1976-04-05 1982-08-03 Eaton Corporation Vapor compression liquid treating system
US4480393A (en) * 1981-06-15 1984-11-06 Minnesota Mining And Manufacturing Company Vapor recovery method and apparatus
WO2016090357A1 (fr) * 2014-12-05 2016-06-09 Carbon Capture Scientific, Llc Procédé de séparation d'un produit gazeux présent dans un mélange gazeux
US20180071694A1 (en) * 2016-09-15 2018-03-15 Netzsch-Gerätebau GmbH Method And Device For Generating A Continuous Carrier Gas/Vapour Mixture Stream

Family Cites Families (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4832718A (en) * 1982-05-03 1989-05-23 Advanced Extraction Technologies, Inc. Processing nitrogen-rich, hydrogen-rich, and olefin-rich gases with physical solvents
FR2863910B1 (fr) * 2003-12-23 2006-01-27 Inst Francais Du Petrole Procede de capture du dioxyde de carbone contenu dans des fumees
US20070277674A1 (en) * 2004-03-02 2007-12-06 Yoshio Hirano Method And System Of Processing Exhaust Gas, And Method And Apparatus Of Separating Carbon Dioxide
FR2925954B1 (fr) * 2007-12-27 2015-03-13 Armines Ass Pour La Rech Et Le Dev Des Methodes Et Processus Ind Systeme de refroidissement d'un melange psychrometrique par couplage d'une unite de condensation et d'une unite d'evaporation
US7919064B2 (en) * 2008-02-12 2011-04-05 Michigan Technological University Capture and sequestration of carbon dioxide in flue gases
FR2957269B1 (fr) * 2010-03-15 2015-11-13 Air Liquide Procede et installation de traitement de fumees riches en co2
US8747520B2 (en) * 2010-05-03 2014-06-10 Battelle Memorial Institute Carbon dioxide capture from power or process plant gases
CN103596660B (zh) * 2010-11-19 2016-08-24 可持续能源解决方案公司 通过直接接触热交换将可冷凝蒸气与气体分离的系统和方法
CA2825143C (fr) * 2010-12-30 2019-02-26 Chevron U.S.A. Inc. Procede pour ameliorer la demande en energie totale dans un procede de capture de carbone post-combustion a l'aide d'un absorbant ionique
PL3317240T3 (pl) * 2015-05-06 2025-03-24 Sustainable Energy Solutions, Inc. Proces oczyszczania kriogenicznego i oddzielania etanu

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3759047A (en) * 1971-11-22 1973-09-18 Univ California Vapor condensation system and method
US4342624A (en) * 1976-04-05 1982-08-03 Eaton Corporation Vapor compression liquid treating system
US4480393A (en) * 1981-06-15 1984-11-06 Minnesota Mining And Manufacturing Company Vapor recovery method and apparatus
WO2016090357A1 (fr) * 2014-12-05 2016-06-09 Carbon Capture Scientific, Llc Procédé de séparation d'un produit gazeux présent dans un mélange gazeux
US20180071694A1 (en) * 2016-09-15 2018-03-15 Netzsch-Gerätebau GmbH Method And Device For Generating A Continuous Carrier Gas/Vapour Mixture Stream

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See also references of EP3570950A4 *

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US10758874B2 (en) 2016-09-15 2020-09-01 Netzsch-Gerätebau GmbH Method and device for generating a continuous carrier gas/vapour mixture stream
EP3865202A1 (fr) 2020-02-13 2021-08-18 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Utilisation d'effluent gazeux contenant du co2 dans la preparation du beton
WO2021160424A1 (fr) 2020-02-13 2021-08-19 L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Utilisation d'un effluent gazeux contenant du co2

Also Published As

Publication number Publication date
EP3570950A4 (fr) 2021-02-24
CN110678242B (zh) 2023-03-28
EP3570950A1 (fr) 2019-11-27
CN110678242A (zh) 2020-01-10

Similar Documents

Publication Publication Date Title
US10213731B2 (en) Method and apparatus for continuous removal of carbon dioxide vapors from gases
RU2534075C1 (ru) Способ отделения диоксида углерода из отработанного газа с использованием стадий мембранного разделения на основе продувки и абсорбции
RU2489197C2 (ru) Способ разделения газов с применением мембран с продувкой пермеата для удаления co2 из продуктов сжигания
Aspelund et al. Gas conditioning—The interface between CO2 capture and transport
US7459134B2 (en) Method of decarbonating a combustion fume with extraction of the solvent contained in the purified fume
CN101896246B (zh) 再生吸收剂溶液的系统和方法
US20110296868A1 (en) CO2 Recovery Method Using Cryo-Condensation
US20080127632A1 (en) Carbon dioxide capture systems and methods
US20080016868A1 (en) Integrated capture of fossil fuel gas pollutants including co2 with energy recovery
US8715605B2 (en) Method for burning carbonated fuels with combustion smoke filtration before compression
WO2011140117A2 (fr) Capture du dioxyde de carbone provenant de gaz de centrale électrique ou d'installation de traitement
CA3059059C (fr) Amelioration du traitement de gaz residuaire de claus par technologie a membrane selective au dioxyde de soufre
EP2668994A1 (fr) Changement de phase de CO2 intégré absorbant pour système de séparation de CO2
JP2001025627A (ja) 複合アミンブレンドを使用する二酸化炭素の回収
WO2012038866A1 (fr) Système et procédé pour la récupération de dioxyde de carbone
CN110678242B (zh) 从多种气体中连续除去蒸气的方法和装置
CN109310945B (zh) 用于从由多个燃烧源产生的排放气体中除去二氧化碳的基于吹扫的膜分离方法
Feron et al. Water production through CO2 capture in coal‐fired power plants
JP2015529545A (ja) 酸素燃焼プロセスから生成される酸性化合物の制御方法
US10307709B2 (en) Method and apparatus for continuous removal of water vapors from gases
Śpiewak et al. PDU-scale experimental results of CO2 removal with AMP/PZ solvent
US20110252828A1 (en) Carbon Dioxide Recovery Method Using Cryo-Condensation
CN105636672B (zh) 从烟气中去除SOx和CO2的方法和设备
CN105705217A (zh) 通过吸附净化co2的装置和方法
Pascu et al. Simulation of polymeric membrane in ASPEN Plus for CO2 post-combustion capture

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 18741443

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 2018741443

Country of ref document: EP

Effective date: 20190819