CN102059037A - Process for purifying carbon dioxide from tail gas of natural gas - Google Patents
Process for purifying carbon dioxide from tail gas of natural gas Download PDFInfo
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- CN102059037A CN102059037A CN2010105523638A CN201010552363A CN102059037A CN 102059037 A CN102059037 A CN 102059037A CN 2010105523638 A CN2010105523638 A CN 2010105523638A CN 201010552363 A CN201010552363 A CN 201010552363A CN 102059037 A CN102059037 A CN 102059037A
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- carbon dioxide
- tail gas
- mea
- temperature
- solution
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 151
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 75
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 75
- 239000007789 gas Substances 0.000 title claims abstract description 63
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 16
- 239000003345 natural gas Substances 0.000 title claims abstract description 15
- 239000007788 liquid Substances 0.000 claims abstract description 14
- 230000000694 effects Effects 0.000 claims abstract description 10
- 238000001035 drying Methods 0.000 claims description 14
- 238000005516 engineering process Methods 0.000 claims description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 229910001868 water Inorganic materials 0.000 claims description 12
- 238000010521 absorption reaction Methods 0.000 claims description 10
- 238000005406 washing Methods 0.000 claims description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 239000006096 absorbing agent Substances 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 6
- 238000006243 chemical reaction Methods 0.000 claims description 5
- 230000008676 import Effects 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 230000006837 decompression Effects 0.000 claims description 3
- 239000000428 dust Substances 0.000 claims description 3
- 230000008929 regeneration Effects 0.000 claims description 3
- 238000011069 regeneration method Methods 0.000 claims description 3
- 238000005201 scrubbing Methods 0.000 claims description 3
- FGUUSXIOTUKUDN-IBGZPJMESA-N C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 Chemical compound C1(=CC=CC=C1)N1C2=C(NC([C@H](C1)NC=1OC(=NN=1)C1=CC=CC=C1)=O)C=CC=C2 FGUUSXIOTUKUDN-IBGZPJMESA-N 0.000 claims description 2
- 238000000746 purification Methods 0.000 claims description 2
- 238000009776 industrial production Methods 0.000 abstract description 2
- 150000001412 amines Chemical class 0.000 abstract 1
- 238000005265 energy consumption Methods 0.000 abstract 1
- 238000004064 recycling Methods 0.000 abstract 1
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 1
- 240000004859 Gamochaeta purpurea Species 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 229910000004 White lead Inorganic materials 0.000 description 1
- 230000008033 biological extinction Effects 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 239000002075 main ingredient Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000011430 maximum method Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
Classifications
-
- 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
-
- 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
Landscapes
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a process for purifying carbon dioxide from tail gas of natural gas. In the process, mono etobaccool amine (MEA) barren liquor is utilized to absorb carbon dioxide in the tail gas; the carbon dioxide is released; the carbon dioxide in the tail gas is converted into liquid carbon dioxide which is applied to industrial production, thus reaching an environment-friendly effect, recycling the wastes, and saving energy resources; and in addition, in the process, the heat of the tail gas is sufficiently utilized, thus reducing energy consumption in the running process of a system.
Description
Technical field
The present invention relates to the technology that carbon dioxide is purified in a kind of tail gas, the technology that the carbon dioxide behind especially a kind of combustion of natural gas in the tail gas is purified.
Background technology
Mainly contain nitrogen, carbon dioxide and water in the tail gas that natural gas discharges after burning, at present, most enterprise directly discharges tail gas, cause the content of carbon dioxide in the atmosphere to raise, because carbon dioxide has the effect of insulation, therefore cause global temperature to raise, the member of this little army is more and more now, elevate the temperature, nearly 100 years, global temperature raise 0.6 ℃, goes down after this manner, expect mid-21st Century, global temperature will raise 1.5-4.5 ℃.Because the rising of global temperatures, melt in the glacier, causes sea-level rise, nearly 100 years, sea level rise 14 centimetres, to mid-21st Century, will rise 25-140 centimetres in the sea level, the rising on sea level, the Amazon rainforest will disappear, and the ice cube of ocean, the two poles of the earth also will all melt.All these variations are tantamount to extinction to wild animal.
On the other hand, carbon dioxide also is very widely in industrial application, and atmospheric carbon dioxide can be used for basic industry, sugar industry, and is used for the quenching of steel casting and the manufacturing of white lead etc.; Carbon dioxide is used also very extensive at welding field. as: carbon dioxide gas arc welding is to use maximum methods in producing at present.Solid carbon dioxide is commonly called as dry ice, can absorb big calorimetric during distillation, thereby as cold-producing medium, as rain making, is used to make smog in the stage of also being everlasting.
Therefore the emission of carbon-dioxide contaminated air causes greenhouse effects, and also very extensive in industrial application, seeks a kind of method that is used for commercial Application after carbon dioxide in the tail gas is purified and presses for.
Summary of the invention
Technical problem to be solved by this invention is to provide the technology that the carbon dioxide in the tail gas is purified behind kind of the combustion of natural gas, the carbon dioxide in the natural gas tail gas can be purified, and reach the purpose of energy-saving and emission-reduction, and can be with the carbon dioxide recovery utilization.
The object of the present invention is achieved like this, a kind of from natural gas tail gas the technology of purifying carbon dioxide, finish by following steps:
A, release heat: the high-temperature tail gas after will burning is introduced in the tail gas energy absorber, about 80 ℃ the MEA rich solution that obtains with steps d carries out the heat that heat exchange discharges tail gas, this moment, the temperature of tail gas was reduced to 70-90 ℃, and the temperature of MEA rich solution then is increased to about 113 ℃;
B, washing: the tail gas after will lowering the temperature imports in the scrubbing tower, and water is incited somebody to action dust flush away wherein, and simultaneously, the temperature of tail gas further is reduced to 30-50 ℃ after washing;
C, absorption: the tail gas after washing imports in the absorption tower, with the temperature that obtains in the steps d be MEA lean solution reaction about 40 ℃, at this moment, most carbon dioxide is absorbed by the MEA lean solution in the tail gas, the MEA lean solution that has absorbed carbon dioxide becomes the MEA rich solution, and temperature is increased to about 55 ℃;
The rich or poor liquid heat exchange of d, MEA: the MEA rich solution that obtains among the step c pumps in the rich or poor liquid interchanger, carry out heat exchange with the MEA lean solution that obtains among the step e, make the temperature of MEA rich solution be increased to about 80 ℃ by about 55 ℃, the temperature of MEA lean solution is reduced to about 75 ℃; At this moment, the MEA lean solution enters in the lean solution cooler to be cooled off, and enters the carbon dioxide reaction in c circulation and the tail gas after making temperature reduce to about 40 ℃; The MEA rich solution then enters a circulation and carries out heat exchange with high-temperature tail gas;
E, release of carbon dioxide: about 113 ℃ the MEA rich solution that obtains among the step a enters regenerator, in this regenerator, after dilatation, decompression, the carbon dioxide in the MEA rich solution is discharged, the carbon dioxide that discharges enters surge tank, the MEA rich solution that has discharged carbon dioxide becomes the MEA lean solution, and temperature is reduced to about 95 ℃, this moment, the MEA lean solution entered in the d circulation, carried out heat exchange with the MEA rich solution that obtains among the step c;
F, purification and liquefaction: the compression of the compressed machine of the carbon dioxide in the described surge tank is laggard goes into the moisture of telling in the water segregator wherein, enter in the liquefier after the further drying of drying device, absorber purify again and liquefy, obtain carbon dioxide liquid, at last the carbon dioxide liquid tinning is obtained canned carbon dioxide.
The present invention absorbs carbon dioxide in the tail gas with the MEA lean solution, then carbon dioxide is discharged, and the carbon dioxide in the tail gas is changed into liquid carbon dioxide be used for industrial production, has reached the effect of environmental protection, with refuse reclamation, has saved the energy; On the other hand, the present invention makes full use of the heat of tail gas, has reduced the consumption of energy in system's running.
In technique scheme: the temperature of described high-temperature tail gas is about 220 ℃, wherein contains 71% the nitrogen of having an appointment, 18% steam and 9.4% carbon dioxide.
In technique scheme: the stable of tail gas among the step b after washing reduced to 40 ℃.
In technique scheme: unabsorbed gases is got rid of from the top on absorption tower among the step c.
In step f, dry process is made by two driers exchanges and is used for finishing, and the drier in drier wherein when causing drying effect to reduce, carries out drying by another drier because of absorbing water too much; In the process of carbon dioxide liquefaction and storage tank, be not liquefied or the tail gas of storage tank after being heated above 100 ℃, feed in the drier after absorbing water, the moisture in the drier is taken away, allow the drier regeneration.
Technology of the present invention is simple, and equipment is less demanding, and the present invention not only the carbon dioxide in the tail gas is purified after utilization again, also make full use of the heat energy of tail gas, the consumption of the energy when having reduced system's operation has reached the effect of energy-saving and emission-reduction.
Description of drawings
Fig. 1 is a flow chart of the present invention.
The specific embodiment
MEA is the abbreviation of Monoethanolamine in the present invention, refers to monoethanolamine, and molecular weight is 61.
Embodiment 1, the discharge tail gas temperature is about behind natural gas kiln and the natural gas boiler gas-firing: about 220 ℃, under the effect of air-introduced machine, at first pass through the tail gas energy absorber, release heat in the tail gas energy absorber, temperature is reduced to about 80 ℃ from about 220 ℃, through the scrubbing tower washing, remove the dust in the tail gas, and be cooled to about 40 ℃ then; Tail gas after washing enters the absorption tower then, in the absorption tower, be MEA lean solution reaction about 40 ℃ with temperature, carbon dioxide is absorbed back MEA lean solution by the MEA lean solution and becomes the MEA rich solution, and unabsorbed gases (Main Ingredients and Appearance is a nitrogen) is discharged by the top, absorption tower.The process that carbon dioxide is absorbed by the MEA lean solution is an exothermic process, and temperature will raise behind the MEA lean solution absorbing carbon dioxide, rises to about 55 ℃ by former 40 ℃.Under the effect of pump, the MEA lean solution heat exchange that the MEA rich solution at first comes out in rich or poor liquid interchanger and regenerator, temperature is increased to about 80 ℃ by about 55 ℃, enter tail gas energy absorber and high-temperature tail gas heat exchange then, temperature is increased to about 113 ℃ by about 80 ℃, reach the temperature of technological requirement, enter regenerator at last; In regenerator, the MEA rich solution is through dilatation, decompression, and carbon dioxide will discharge from the MEA rich solution, and the solution after the release of carbon dioxide is called the MEA lean solution; Carbon dioxide will be discharged from the top of regenerator, and concentration of carbon dioxide will reach 99% this moment; MEA rich solution release of carbon dioxide becomes in the process of MEA lean solution, temperature will be reduced to about 95 ℃ from about 113 ℃, at this moment, the MEA lean solution enters rich or poor liquid interchanger and carries out heat exchange with the MEA rich solution that has just absorbed carbon dioxide, temperature through MEA lean solution after the heat exchange is reduced to about 75 ℃ by about 95 ℃, MEA lean solution after the cooling enters and further is cooled in the lean solution cooler about 40 ℃, and the MEA lean solution that obtain this moment enters in the absorption tower, absorbs the carbon dioxide in the tail gas again.
The carbon dioxide of being got rid of by the regenerator cat head enters in the surge tank, the compression of the compressed machine of carbon dioxide in the surge tank is laggard goes into the moisture of telling in the water segregator wherein, enter in the liquefier after the further drying of drying device, absorber purify again and liquefy, obtain carbon dioxide liquid, at last the carbon dioxide liquid tinning is obtained canned carbon dioxide; Wherein Gan Zao process is made by the exchange of two driers and is used for finishing, and the drier in drier wherein when causing drying effect to reduce, carries out drying by another drier because of absorbing water too much; In the process of carbon dioxide liquefaction and storage tank, be not liquefied or the tail gas of storage tank after being heated above 100 ℃, feed in the drier after absorbing water, the moisture in the drier is taken away, allow the drier regeneration.
Claims (5)
1. the technology of a purifying carbon dioxide from natural gas tail gas, finish by following steps:
A, release heat: the high-temperature tail gas after will burning is introduced in the tail gas energy absorber, about 80 ℃ the MEA rich solution that obtains with steps d carries out the heat that heat exchange discharges tail gas, this moment, the temperature of tail gas was reduced to 70-90 ℃, and the temperature of MEA rich solution then is increased to about 113 ℃;
B, washing: the tail gas after will lowering the temperature imports in the scrubbing tower, and water is incited somebody to action dust flush away wherein, and simultaneously, the temperature of tail gas further is reduced to 30-50 ℃ after washing;
C, absorption: the tail gas after washing imports in the absorption tower, with the temperature that obtains in the steps d be MEA lean solution reaction about 40 ℃, at this moment, most carbon dioxide is absorbed by the MEA lean solution in the tail gas, the MEA lean solution that has absorbed carbon dioxide becomes the MEA rich solution, and temperature is increased to about 55 ℃;
The rich or poor liquid heat exchange of d, MEA: with the MEA rich solution that obtains among the step c pump in the rich or poor liquid interchanger with step e in the MEA lean solution that obtains carry out heat exchange, make the temperature of MEA rich solution be increased to about 80 ℃ by about 55 ℃, the temperature of MEA lean solution is reduced to about 75 ℃; At this moment, the MEA lean solution enters in the lean solution cooler to be cooled off, and enters the carbon dioxide reaction in c circulation and the tail gas after making temperature reduce to about 40 ℃; The MEA rich solution then enters a circulation and carries out heat exchange with high-temperature tail gas;
E, release of carbon dioxide: about 113 ℃ the MEA rich solution that obtains among the step a enters regenerator, in this regenerator, after dilatation, decompression, the carbon dioxide in the MEA rich solution is discharged, the carbon dioxide that discharges enters surge tank, the MEA rich solution that has discharged carbon dioxide becomes the MEA lean solution, and temperature is reduced to about 95 ℃, this moment, the MEA lean solution entered in the d circulation, carried out heat exchange with the MEA rich solution that obtains among the step c;
F, purification and liquefaction: the compression of the compressed machine of the carbon dioxide in the described surge tank is laggard goes into the moisture of telling in the water segregator wherein, enter in the liquefier after the further drying of drying device, absorber purify again and liquefy, obtain carbon dioxide liquid, at last the carbon dioxide liquid tinning is obtained canned carbon dioxide.
According to claim 1 described from natural gas tail gas the technology of purifying carbon dioxide, it is characterized in that: the temperature of described high-temperature tail gas is about 220 ℃, wherein contains 71% the nitrogen of having an appointment, 18% steam and 9.4% carbon dioxide.
According to claim 1 described from natural gas tail gas the technology of purifying carbon dioxide, it is characterized in that: the stable of tail gas among the step b after washing reduced to 40 ℃.
According to claim 1 described from natural gas tail gas the technology of purifying carbon dioxide, it is characterized in that: unabsorbed gases is got rid of from the top on absorption tower among the step c.
According to claim 1 described from natural gas tail gas the technology of purifying carbon dioxide, it is characterized in that: in step f, dry process is made by two drier exchanges and is used for finishing, drier in drier wherein is because of absorbing water too much, when causing drying effect to reduce, carry out drying by another drier; In the process of carbon dioxide liquefaction and storage tank, be not liquefied or the tail gas of storage tank after being heated above 100 ℃, feed in the drier after absorbing water, the moisture in the drier is taken away, allow the drier regeneration.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010105523638A CN102059037A (en) | 2010-11-22 | 2010-11-22 | Process for purifying carbon dioxide from tail gas of natural gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010105523638A CN102059037A (en) | 2010-11-22 | 2010-11-22 | Process for purifying carbon dioxide from tail gas of natural gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102059037A true CN102059037A (en) | 2011-05-18 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2010105523638A Pending CN102059037A (en) | 2010-11-22 | 2010-11-22 | Process for purifying carbon dioxide from tail gas of natural gas |
Country Status (1)
| Country | Link |
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| CN (1) | CN102059037A (en) |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4160810A (en) * | 1978-03-07 | 1979-07-10 | Benfield Corporation | Removal of acid gases from hot gas mixtures |
| CN1261545A (en) * | 1999-12-06 | 2000-08-02 | 重庆理想科技有限公司 | Method for recovering CO2 from mixed gas |
| CN1300635A (en) * | 2000-12-19 | 2001-06-27 | 中国冶金建设集团鞍山焦化耐火材料设计研究总院 | Process for removing CO2 and H2S from biological gas |
| US20050169825A1 (en) * | 2003-12-23 | 2005-08-04 | Renaud Cadours | Method of collecting carbon dioxide contained in fumes |
| CN1668364A (en) * | 2002-09-17 | 2005-09-14 | 弗劳尔公司 | Configuration and method for acid gas removal |
| CN1795039A (en) * | 2003-03-26 | 2006-06-28 | 犹德有限公司 | Method for the selective removal of hydrogen sulphide and co2 from crude gas |
| CN1887405A (en) * | 2005-06-27 | 2007-01-03 | 成都华西化工研究所 | Process of removing and recovering CO2 from fume |
| CN101325995A (en) * | 2005-08-16 | 2008-12-17 | Co2Crc技术股份有限公司 | Apparatus and method for removing carbon dioxide from a gas stream |
| WO2010039785A1 (en) * | 2008-10-02 | 2010-04-08 | Fluor Technologies Corporation | Configurations and methods of high pressure acid gas removal |
| CN101703880A (en) * | 2009-11-02 | 2010-05-12 | 西安交通大学 | Power plant flue gas desulphurization and decarbonization integrated purification system |
| US20100236408A1 (en) * | 2007-11-15 | 2010-09-23 | Basf Se | Method for removing carbon dioxide from fluid flows, in particular combustion exhaust gases |
| US20100282074A1 (en) * | 2007-10-09 | 2010-11-11 | Dge Dr.-Ing. Günther Engineering Gmbh | Method And System For Regenerating An Amine-Containing Scrubbing Solution Obtained During Gas Purification |
-
2010
- 2010-11-22 CN CN2010105523638A patent/CN102059037A/en active Pending
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4160810A (en) * | 1978-03-07 | 1979-07-10 | Benfield Corporation | Removal of acid gases from hot gas mixtures |
| CN1261545A (en) * | 1999-12-06 | 2000-08-02 | 重庆理想科技有限公司 | Method for recovering CO2 from mixed gas |
| CN1300635A (en) * | 2000-12-19 | 2001-06-27 | 中国冶金建设集团鞍山焦化耐火材料设计研究总院 | Process for removing CO2 and H2S from biological gas |
| CN1668364A (en) * | 2002-09-17 | 2005-09-14 | 弗劳尔公司 | Configuration and method for acid gas removal |
| CN1795039A (en) * | 2003-03-26 | 2006-06-28 | 犹德有限公司 | Method for the selective removal of hydrogen sulphide and co2 from crude gas |
| US20050169825A1 (en) * | 2003-12-23 | 2005-08-04 | Renaud Cadours | Method of collecting carbon dioxide contained in fumes |
| CN1887405A (en) * | 2005-06-27 | 2007-01-03 | 成都华西化工研究所 | Process of removing and recovering CO2 from fume |
| CN101325995A (en) * | 2005-08-16 | 2008-12-17 | Co2Crc技术股份有限公司 | Apparatus and method for removing carbon dioxide from a gas stream |
| US20100282074A1 (en) * | 2007-10-09 | 2010-11-11 | Dge Dr.-Ing. Günther Engineering Gmbh | Method And System For Regenerating An Amine-Containing Scrubbing Solution Obtained During Gas Purification |
| US20100236408A1 (en) * | 2007-11-15 | 2010-09-23 | Basf Se | Method for removing carbon dioxide from fluid flows, in particular combustion exhaust gases |
| WO2010039785A1 (en) * | 2008-10-02 | 2010-04-08 | Fluor Technologies Corporation | Configurations and methods of high pressure acid gas removal |
| CN101703880A (en) * | 2009-11-02 | 2010-05-12 | 西安交通大学 | Power plant flue gas desulphurization and decarbonization integrated purification system |
Non-Patent Citations (2)
| Title |
|---|
| 《医药工程设计》 20000228 钱嘉兴 烟道气二氧化碳回收装置设计实施探讨 2-6 第21卷, 第1期 * |
| 《大氮肥》 20021231 杨虹,吴丹,张述伟,王长英,俞裕国 制氢尾气二氧化碳回收装置设计 377-379 第25卷, 第6期 * |
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Application publication date: 20110518 |