WO2010110939A1 - Gas stream processing - Google Patents
Gas stream processing Download PDFInfo
- Publication number
- WO2010110939A1 WO2010110939A1 PCT/US2010/022710 US2010022710W WO2010110939A1 WO 2010110939 A1 WO2010110939 A1 WO 2010110939A1 US 2010022710 W US2010022710 W US 2010022710W WO 2010110939 A1 WO2010110939 A1 WO 2010110939A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- flue gas
- ammonia solution
- gas stream
- water
- capture system
- Prior art date
Links
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
- B01D53/34—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
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
- B01D2251/2062—Ammonia
-
- 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
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- 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 technology relates to systems and methods for removing carbon dioxide from gas streams including carbon dioxide and sulfur dioxide.
- a process gas or flue gas is generated in the combustion of a fuel, such as coal, oil, peat, waste, etc.
- a flue gas will often contain, among other things, carbon dioxide (CO 2 ) and sulfur dioxide (SO 2 ).
- CO 2 carbon dioxide
- SO 2 sulfur dioxide
- Known systems include chilled ammonia based systems. Chilled ammonia based systems can capture and/or remove CO 2 from a gas stream. For example, absorption of CO 2 from a gas stream can be achieved by contacting a chilled ionic ammonia solution (or slurry) with a flue gas stream that contains CO 2 .
- These systems can include strippers for removing ammonia from water and returning the water to the process. The strippers operate at predetermined temperatures. The operating temperature affects energy efficiency.
- a CO 2 capture system for removing carbon dioxide from a flue gas stream
- the CO 2 capture system comprising an absorber vessel configured to introduce both a lean ionic ammonia solution from a regeneration system and the flue gas stream from a cooling system and configured to provide a rich ionic ammonia solution to the regeneration system, wherein the introduction of the lean ionic ammonia solution and the flue gas stream reacts to produce a flue gas substantially devoid of CO 2 .
- a water wash vessel is configured to receive flue gas from the absorber and produce ammoniated water.
- a stripper is configured to receive the ammoniated water and is configured to remove ammonia from the ammoniated water thereby producing a cleaned flue gas stream, the stripper being operable in at least partial vacuum conditions.
- a power generation plant comprising a CO 2 capture system for removing carbon dioxide from a flue gas stream, the CO 2 capture system comprising an absorber vessel configured to introduce a lean ionic ammonia solution from a regeneration system and the flue gas stream from a cooling system. The ammonia solution and the flue gas react in the absorber vessel.
- the absorber vessel is further configured to discharge a rich ionic ammonia solution to the regeneration system, wherein the interaction of the lean ionic ammonia solution with the flue gas stream produces an absorber flue gas stream substantially devoid of CO 2 .
- a water wash vessel is configured to receive the absorber flue gas. It introduces water, mixing the two, producing ammoniated water.
- a stripper is configured to receive the ammoniated water and remove ammonia from the ammoniated water, thereby producing a cleaned flue gas stream, the stripper being operable in at least partial vacuum conditions.
- the cooling system reduces the temperature of the flue gas stream, then provides the flue gas stream to the CO 2 capture system, and then receives the cleaned flue gas stream from the CO 2 capture system after CO 2 removal.
- the regeneration system is configured to receive the rich ionic ammonia solution from the CO 2 capture system, remove ammonia, and provide the lean ionic ammonia solution to the CO 2 capture system, wherein the lean ionic ammonia solution is an absorbent ionic ammonia solution.
- the absorbent ionic ammonia solution is an aqueous solution comprising water, ammonium ions, bicarbonate ions, carbonate ions, and carbamate ions, and wherein heat for operating the stripper is provided by a reject water stream from a power plant, the reject water stream being provided at a temperature of about 90° F.
- a method for removing carbon dioxide from flue gas streams comprising in an absorber vessel, reacting a lean ionic ammonia solution from a regeneration system and a flue gas stream from a cooling system.
- a rich ionic ammonia solution resulting from the reaction in the absorber vessel is provided to the regeneration system.
- the introduction of the lean ionic ammonia solution to the flue gas stream in the absorber vessel produces an absorber flue gas stream substantially devoid of CO 2 .
- the absorber flue gas is introduced in the water wash vessel and intermixed with water thereby producing ammoniated water. Discharged water may be returned to the water wash vessel or otherwise recycled.
- the ammoniated water is then transported from the water wash vessel to a stripper, where ammonia is removed from the ammoniated water thereby producing a cleaned flue gas stream, the stripper being operable in at least partial vacuum conditions.
- FIG. 1 is a schematic representation of a power generation plant including a system for removing CO 2 from a flue gas stream;
- FIG. 2 is a schematic representation of a CO 2 capture system in a system for removing CO 2 from a flue gas stream
- FIG. 3 is a schematic representation of a CO 2 removal system including a cooling system, a CO 2 capture system, and a regeneration system.
- a method and system permitting the reduction of the operational temperature for strippers and the removal of carbon dioxide in gas stream processing is provided.
- a flue gas processing system 102 can remove pollutants (for example, CO 2 104) from a flue gas stream 106 emitted by a combustion chamber 108 of a boiler system 110.
- System 102 can be used in a power generation plant 112.
- System 102 can include a CO 2 removal system 114 configured to remove CO 2 from flue gas stream 106 prior to emitting a cleaned flue gas stream 116 (for example, to an exhaust stack 118 or for additional processing).
- CO 2 removal system 114 can transport CO 2 removed from flue gas stream 106 for storage, collection, or other use.
- CO 2 removal system 114 can include a cooling system 120 for cooling flue gas stream 106 entering an additional cooling system (not shown), a CO 2 capture system 122 for capturing/removing CO 2 from flue gas stream 106, and/or a regeneration system 124 for regenerating an ionic ammonia solution used to remove CO 2 from flue gas stream 106.
- Cooling system 120 can be any suitable cooling system configured to provide flue gas stream 106 to CO 2 capture system 122 and receive a cleaned flue gas stream 116 from CO 2 capture system 122.
- system 102 may further include a dust removal system 126.
- Dust removal system 126 can receive flue gas stream 106 emitted by combustion chamber 108. Dust removal system 126 can remove dust, ash, and other particulate matter from flue gas stream 106 prior to flue gas stream 106 being processed by CO 2 removal system 114.
- system 102 may further include suitable processing systems.
- system 102 may include a scrubber 128 configured to further process flue gas stream 106 prior to flue gas stream 106 being processed by CO 2 removal system 114.
- CO 2 capture system 122 can include an absorber vessel 202 configured to apply an absorbent ionic ammonia solution (for example, a lean ionic ammonia solution 204) from regeneration system 124 to flue gas stream 106 coming from cooling system 120.
- an absorbent ionic ammonia solution for example, a lean ionic ammonia solution 204
- the absorbent ionic ammonia solution can be aqueous and can include water and ammonium ions, bicarbonate ions, carbonate ions, and/or carbamate ions.
- Regeneration system 124 can be any suitable system configured to receive a rich ionic ammonia solution 206 from CO 2 capture system 122 and provide lean ionic ammonia solution 204 to CO 2 capture system 122.
- the phrase "rich ionic ammonia solution” refers to ionic ammonia solution having an increased concentration of CO 2 .
- the rich ionic ammonia solution 206 includes a ratio of ammonia : CO 2 , which may be from about 1.5 : 1 to about 1.9 : 1.
- the phrase “lean ionic ammonia solution” refers to ionic ammonia solution having a decreased concentration of CO 2 as compared to the rich ionic ammonia solution.
- the lean ionic ammonia solution 204 includes a ratio of ammonia : CO 2 , which may be from about 2.3 : 1 to about 3.5 : 1.
- Absorber vessel 202 can receive the lean ionic ammonia solution 204 from regeneration system 124.
- a liquid distribution system (not shown) can introduce lean ionic ammonia solution 204 into absorber vessel 202 while flue gas stream 106 is being received by absorber vessel 202.
- a gas-liquid contacting device 205 (for example, a mass transfer device) can introduce absorbent ionic ammonia solution 204 into device 205 to contact and/or co-mix solution 204 with flue gas stream 106.
- the gas-liquid contacting device 205 can be a predetermined structure and/or random packing materials.
- the gas-liquid contacting device 205 can include valve trays, sieve trays, structured packing, random packing or other suitable packing materials, or a combination thereof.
- Device 205 increases surface area of ionic ammonia solution 204, thereby increasing gas-liquid interface.
- the gas- liquid contacting device 205 can be located in absorber vessel 202 and within a path of flue gas stream 106.
- Lean ionic ammonia solution 204 can absorb CO 2 from flue gas stream 106, thus increasing the concentration of CO 2 in a solution derived from lean ionic ammonia solution 204 being contacted and/or co-mixed with flue gas stream 106.
- This solution derived from lean ionic ammonia solution 204 can be rich ionic ammonia solution 206. Rich ionic ammonia solution 206 can flow toward gas-liquid contacting device 205 and then be collected. For example, solution 206 can be collected in absorber vessel 202.
- Rich ionic ammonia solution 206 can then flow to regeneration system 124.
- rich ionic ammonia solution 206 can release CO 2 absorbed by lean ionic ammonia solution 204.
- the released CO 2 can be collected and/or transported for storage and/or use.
- the resulting ionic ammonia solution has a lower concentration of CO 2 and thereby can be recycled as lean ionic ammonia solution 204.
- the recycled lean ionic ammonia solution 204 can be reused to absorb CO 2 from flue gas stream 106 or an additional flue gas stream.
- the flue gas stream 106 containing ammonia leaving absorber vessel 202 after interaction with lean ionic ammonia solution 204 can be directed to water wash vessel 210 where it interacts with water.
- Water wash vessel 210 can remove ammonia 216 that may be present in flue gas substantially devoid CO 2 224 thereby producing ammoniated water 212.
- ammoniated water 212 may be provided by regeneration system 124.
- the source of ammoniated water 212 may be water wash vessel 210, lean ionic ammonia solution 204, regeneration system 124, or combinations thereof.
- Ammoniated water 212 can be directed to stripper 214.
- Stripper 214 can remove ammonia 216 from ammoniated water 212 and return water 218 back to water wash vessel 210. Ammonia 216 removed from water wash vessel 210 can be returned to absorber vessel 202.
- Stripper 214 can operate at a predetermined temperature.
- the predetermined temperature is a boiling point of water at a given operating pressure. Decreasing the boiling point of water can improve efficiency of stripper 214 by decreasing the predetermined temperature. Such a reduction in the predetermined temperature permits additional sources of heat to be effective.
- the predetermined temperature may be about 90° F when the source is at a pressure of about 0.70 pounds-force per square inch absolute (“psia").
- psia pounds-force per square inch absolute
- stripper 214 can be heated by any suitable source with a lower temperature under lower pressure.
- Stripper 214 can be part of CO 2 capture system 122 within CO 2 removal system 114.
- Stripper 214 can include a stripper vessel 222 and a vacuum pump 220.
- Stripper vessel 222 can be any suitable vessel (for example, a generally cylindrically-shaped vessel (for example, a steel vessel) configured to operate within a predetermined pressure range).
- Stripper vessel 222 can include one or more suitable gas-liquid contacting devices 205 (for example, a mass transfer device) as described above.
- Stripper vessel 222 can include a heater (not shown) for providing temperature control of liquid collected in stripper vessel 222.
- the heater can heat the liquid collected in the bottom of stripper vessel 222.
- Vacuum pump 220 can generate at least partial vacuum conditions for stripper vessel 222.
- the at least partial vacuum conditions can be generated by a vacuum pump (not shown) or steam jet injector.
- stripper 214 can be operated as a vacuum stripper. Operating the vacuum stripper under at least partial vacuum conditions can permit use of a water source within lower temperature ranges.
- the at least partial vacuum conditions are known and can be found in available steam tables. As stripper 214 approaches full evacuation, the source used can be of a lower temperature. Thus, the desired amount of heat for stripper 214 can be reduced by increased evacuation.
- the at least partial vacuum conditions of stripper 214 include a pressure of less than about 10 psia. In other exemplary embodiments, the at least partial vacuum conditions of stripper 214 include a pressure of less than about 1 psia.
- FIG. 3 shows a further exemplary embodiment of power generation plant 112 including cooling system 120, CO 2 capture system 122, and regeneration system 124.
- cooling system 120 can include a first vessel 302 configured to cool cleaned flue gas stream 116 prior to cleaned flue gas stream 116 being sent to exhaust stack 118.
- First vessel 302 can receive water 218 from a water source. Heat from the gas stream is exchanged with the water and water is sent to a cooling tower 304.
- a cooling tower 304 In an open system, water is circulated through the cooling tower, some of which evaporates, the remainder being returned to the first vessel and supplemented with water from the water source, such as a river, lake, or stream.
- a closed loop system water is circulated though the cooling tower and is returned to the first vessel.
- Cooling tower 304 can be any suitable cooling mechanism.
- cooling tower 304 receives air 306 and cools heated water 218 prior to air 306 being released into the atmosphere, into another process, or stored.
- second vessel 308 may receive flue gas stream 106 from another system (for example, boiler system 110). Second vessel 308 is configured to provide ammonia scrubbing of SO 2 by reacting flue gas stream 106 with chilled water 218 from first vessel 302 to form ammonium sulfate. A portion of the flue gas stream 106 can then form a bleed 310, which may be used in another process or stored. The remaining portion of flue gas stream 106 can flow to CO 2 capture system 122.
- CO 2 capture system 122 in FIG. 3 can include features identified above with reference to FIG. 2.
- CO 2 capture system 122 can include one or more buffer tanks 312 for providing flow control and/or a volume for storage of lean ionic ammonia solution 204 and/or rich ionic ammonia solution 206.
- CO 2 capture system 122 can include cooling tower 304 and chiller arrangement 322 for cooling water 218 to be used in water wash vessel 210.
- additional heat exchangers, pumps, flow control devices, and other process control systems/apparatus may be included for further regulating the flow of flue gas stream 106, lean ionic ammonia solution 204, rich ionic ammonia solution 206, water 218, ammoniated water 212, ammonia 216, flue gas substantially devoid of CO 2 224, or other suitable process fluids.
- Regeneration system 124 can receive rich ionic ammonia solution 206 from CO 2 capture system 122.
- Regeneration system 124 can include a heat exchanger 314 for transferring heat from lean ionic ammonia solution 204 directed toward CO 2 capture system 122 to rich ionic ammonia solution 206 heading toward a main column 316 of regeneration system 124.
- Regeneration system 124 can further include a direct contact cooler 318 and a treatment system 320 for purifying CO 2 104 prior to its release, storage, or use.
- Operation of an embodiment including the vacuum stripper 222 according to the embodiments disclosed herein can increase energy efficiency by permitting use of a source to drive the vacuum stripper within lower temperature ranges. Such operation can clean gas being emitted by industrial processes. Additionally or alternatively, such operation can permit sequestration of CO 2 to be more efficient.
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (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)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP10703582A EP2411120A1 (en) | 2009-03-27 | 2010-02-01 | Gas stream processing |
RU2011143323/05A RU2011143323A (en) | 2009-03-27 | 2010-02-01 | GAS FLOW PROCESSING |
MA34276A MA33215B1 (en) | 2009-03-27 | 2010-02-01 | TREATMENT OF A GAS CURRENT |
BRPI1010274A BRPI1010274A2 (en) | 2009-03-27 | 2010-02-01 | gas stream processing |
MX2011010135A MX2011010135A (en) | 2009-03-27 | 2010-02-01 | Gas stream processing. |
IL215347A IL215347A0 (en) | 2009-03-27 | 2011-09-25 | Gas stream processing |
ZA2011/07046A ZA201107046B (en) | 2009-03-27 | 2011-09-27 | Gas stream processing |
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US16418509P | 2009-03-27 | 2009-03-27 | |
US61/164,185 | 2009-03-27 | ||
US12/609,076 | 2009-10-30 | ||
US12/609,076 US8292989B2 (en) | 2009-10-30 | 2009-10-30 | Gas stream processing |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2010110939A1 true WO2010110939A1 (en) | 2010-09-30 |
Family
ID=41832826
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US2010/022710 WO2010110939A1 (en) | 2009-03-27 | 2010-02-01 | Gas stream processing |
Country Status (8)
Country | Link |
---|---|
EP (1) | EP2411120A1 (en) |
BR (1) | BRPI1010274A2 (en) |
IL (1) | IL215347A0 (en) |
MA (1) | MA33215B1 (en) |
MX (1) | MX2011010135A (en) |
RU (1) | RU2011143323A (en) |
WO (1) | WO2010110939A1 (en) |
ZA (1) | ZA201107046B (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102225311A (en) * | 2011-05-05 | 2011-10-26 | 北京化工大学 | Method for absorbing carbon dioxide in exhaust gas from power plant |
WO2013144877A1 (en) * | 2012-03-30 | 2013-10-03 | Alstom Technology Ltd | A system for recovery of ammonia from lean solution in a chilled ammonia process utilizing residual flue gas |
EP2754481A1 (en) * | 2013-01-11 | 2014-07-16 | Alstom Technology Ltd | Heat integration of a chilled ammonia process |
CN104039423A (en) * | 2012-01-18 | 2014-09-10 | 阿尔斯通技术有限公司 | Control of a chilled ammonia process for co2 removal from a flue gas |
US8887510B2 (en) | 2010-10-28 | 2014-11-18 | Sargas As | Heat integration in CO2 capture |
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US2533992A (en) * | 1947-09-26 | 1950-12-12 | Lummus Co | Ammonia recovery unit |
US4093544A (en) * | 1975-02-05 | 1978-06-06 | Sterling Drug, Inc. | Method and apparatus for ammonia-nitrogen removal by vacuum desorption |
EP0202600A2 (en) * | 1985-05-22 | 1986-11-26 | BASF Aktiengesellschaft | Process for eliminating carbon dioxide and/or hydrogen sulfide from gases |
WO2006022885A1 (en) * | 2004-08-06 | 2006-03-02 | Eig, Inc. | Ultra cleaning of combustion gas including the removal of co2 |
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US20080307968A1 (en) * | 2007-06-04 | 2008-12-18 | Posco | Apparatus and Method for Recovering Carbon Dioxide from Flue Gas Using Ammonia Water |
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DE4041379A1 (en) * | 1990-12-21 | 1992-07-02 | Martin Umwelt & Energietech | METHOD FOR RECOVERY OR RECOVERY FOR DISPOSAL OF AMMONIAK OR AMMONIUM COMPOUNDS OF MIXTURES AND WASHING WATER |
-
2010
- 2010-02-01 BR BRPI1010274A patent/BRPI1010274A2/en not_active IP Right Cessation
- 2010-02-01 RU RU2011143323/05A patent/RU2011143323A/en not_active Application Discontinuation
- 2010-02-01 EP EP10703582A patent/EP2411120A1/en not_active Withdrawn
- 2010-02-01 WO PCT/US2010/022710 patent/WO2010110939A1/en active Application Filing
- 2010-02-01 MX MX2011010135A patent/MX2011010135A/en not_active Application Discontinuation
- 2010-02-01 MA MA34276A patent/MA33215B1/en unknown
-
2011
- 2011-09-25 IL IL215347A patent/IL215347A0/en unknown
- 2011-09-27 ZA ZA2011/07046A patent/ZA201107046B/en unknown
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US2533992A (en) * | 1947-09-26 | 1950-12-12 | Lummus Co | Ammonia recovery unit |
US4093544A (en) * | 1975-02-05 | 1978-06-06 | Sterling Drug, Inc. | Method and apparatus for ammonia-nitrogen removal by vacuum desorption |
EP0202600A2 (en) * | 1985-05-22 | 1986-11-26 | BASF Aktiengesellschaft | Process for eliminating carbon dioxide and/or hydrogen sulfide from gases |
WO2006022885A1 (en) * | 2004-08-06 | 2006-03-02 | Eig, Inc. | Ultra cleaning of combustion gas including the removal of co2 |
DE102004053167A1 (en) * | 2004-11-01 | 2006-05-04 | Degussa Ag | Polymeric absorbent for gas absorption and absorption process |
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Cited By (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US8887510B2 (en) | 2010-10-28 | 2014-11-18 | Sargas As | Heat integration in CO2 capture |
CN102225311A (en) * | 2011-05-05 | 2011-10-26 | 北京化工大学 | Method for absorbing carbon dioxide in exhaust gas from power plant |
CN104039423A (en) * | 2012-01-18 | 2014-09-10 | 阿尔斯通技术有限公司 | Control of a chilled ammonia process for co2 removal from a flue gas |
CN104039423B (en) * | 2012-01-18 | 2019-01-01 | 通用电器技术有限公司 | Control freezing ammonia process is used to remove CO from flue gas2 |
WO2013144877A1 (en) * | 2012-03-30 | 2013-10-03 | Alstom Technology Ltd | A system for recovery of ammonia from lean solution in a chilled ammonia process utilizing residual flue gas |
US8864879B2 (en) | 2012-03-30 | 2014-10-21 | Jalal Askander | System for recovery of ammonia from lean solution in a chilled ammonia process utilizing residual flue gas |
AU2013239162B2 (en) * | 2012-03-30 | 2014-11-06 | General Electric Technology Gmbh | A system for recovery of ammonia from lean solution in a chilled ammonia process utilizing residual flue gas |
CN104185500A (en) * | 2012-03-30 | 2014-12-03 | 阿尔斯通技术有限公司 | A system for recovery of ammonia from lean solution in a chilled ammonia process utilizing residual flue gas |
EP2754481A1 (en) * | 2013-01-11 | 2014-07-16 | Alstom Technology Ltd | Heat integration of a chilled ammonia process |
Also Published As
Publication number | Publication date |
---|---|
MA33215B1 (en) | 2012-04-02 |
MX2011010135A (en) | 2011-12-08 |
IL215347A0 (en) | 2011-12-29 |
EP2411120A1 (en) | 2012-02-01 |
BRPI1010274A2 (en) | 2016-03-22 |
ZA201107046B (en) | 2012-12-27 |
RU2011143323A (en) | 2013-05-10 |
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