CN103566712B - A kind of smoke carbon dioxide capture technique - Google Patents
A kind of smoke carbon dioxide capture technique Download PDFInfo
- Publication number
- CN103566712B CN103566712B CN201210277347.1A CN201210277347A CN103566712B CN 103566712 B CN103566712 B CN 103566712B CN 201210277347 A CN201210277347 A CN 201210277347A CN 103566712 B CN103566712 B CN 103566712B
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- China
- Prior art keywords
- heat exchanger
- gas
- regeneration
- cfc
- reboiler
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- 238000000034 method Methods 0.000 title claims abstract description 33
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 20
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims description 9
- 239000001569 carbon dioxide Substances 0.000 title claims description 9
- 239000000779 smoke Substances 0.000 title claims description 4
- 239000007789 gas Substances 0.000 claims abstract description 29
- 238000011069 regeneration method Methods 0.000 claims abstract description 25
- 230000008929 regeneration Effects 0.000 claims abstract description 22
- 238000010438 heat treatment Methods 0.000 claims abstract description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000003546 flue gas Substances 0.000 claims abstract description 11
- 239000002918 waste heat Substances 0.000 claims abstract description 10
- 239000006227 byproduct Substances 0.000 claims abstract description 8
- 239000000428 dust Substances 0.000 claims abstract description 7
- 230000005611 electricity Effects 0.000 claims abstract description 6
- 239000002994 raw material Substances 0.000 claims abstract description 5
- 238000004140 cleaning Methods 0.000 claims abstract description 3
- 238000001556 precipitation Methods 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 12
- 238000010521 absorption reaction Methods 0.000 claims description 9
- 238000009835 boiling Methods 0.000 claims description 9
- 238000002309 gasification Methods 0.000 claims description 6
- 238000005261 decarburization Methods 0.000 claims description 2
- 229960004424 carbon dioxide Drugs 0.000 abstract description 11
- 238000005265 energy consumption Methods 0.000 abstract description 9
- 235000011089 carbon dioxide Nutrition 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 238000011084 recovery Methods 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 150000001412 amines Chemical class 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 238000010992 reflux Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000000498 cooling water Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- QZAYGJVTTNCVMB-UHFFFAOYSA-N serotonin Chemical compound C1=C(O)C=C2C(CCN)=CNC2=C1 QZAYGJVTTNCVMB-UHFFFAOYSA-N 0.000 description 2
- -1 this Chemical compound 0.000 description 2
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 description 1
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 229940076279 serotonin Drugs 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material 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
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention belongs to environmental protection and energy saving technical field, a kind of simple to operate, cheap collecting carbonic anhydride technique for process gas residual heat recovery is provided, it is characterized in that the dust adopted in the method separate raw materials gas of electric precipitation, and utilize high-temperature flue gas waste heat byproduct steam to heat for the reboiler of device; Adopt the mode of heating expansion driven turbine generating to utilize regeneration overhead gas waste heat, the dynamic equipment that can meet whole cleaning system that generates electricity power.Whole device is compared with traditional handicraft, and reboiler energy consumption reduces 15-25%, and dynamic equipment is outer for the energy without the need to other.
Description
Technical field
The invention belongs to environmental protection and energy saving technical field, relate to a kind of comprehensive utilization of industrial decarbonization process waste heat, is a kind of energy saving optimizing technology.
Background technology
CO
2trapping, utilize and seal the hot subject that (CCUS) is current international concern up for safekeeping.CO
2trapping technique be the primary link of CCUS, to control CO
2discharge has vital effect.
The organic amine range of solvents being representative with MDEA, MEA, AMP is widely used in the technological process of flue gas collecting carbonic anhydride (US4336233A, CN92113637.4).In amine method decarbonizing process, regeneration energy consumption accounts for more than 2/3rds of total operating cost, in today that greenhouse gas emission is day by day serious, how effectively to reduce regeneration energy consumption, become and reduce collecting carbonic anhydride cost, promote the key issue of large-range carbon dioxide trapping technique better.
Patent ZL01134103.3 proposes a kind of serotonin solution for reclaiming low fractional pressure carbon dioxide, uses this solution can on the basis of traditional MEA technique, steam consumption decline 12-40%, amine consumption decline 30-80%; While the lyosoption that research regeneration energy consumption is lower, by process optimization, fully utilize various heat energy, reduce overall energy consumption, also be the major issue that this Technique Popularizing faces, patent WO2007/012143 proposes the technique adopting heat pump unstripped gas for regeneration of waste liquor.
Summary of the invention
The object of the present invention is to provide a set of simple to operate, cheap collecting carbonic anhydride technique for process gas residual heat recovery, the comprehensive utilization of former process gas waste heat can be realized, the energy consumption of reduction capture operation by a relatively large margin and power consumption.
Main technical schemes of the present invention: smoke carbon dioxide capture technique, is characterized in that, adopts the dust in the method separate raw materials gas of electric precipitation, and utilizes high-temperature flue gas (180-280 DEG C) waste heat byproduct steam to heat for the reboiler of device; Adopt the mode of heating expansion driven turbine generating to utilize regeneration overhead gas waste heat, the dynamic equipment that can meet whole cleaning system that generates electricity power.Whole device is compared with traditional handicraft, and reboiler energy consumption reduces 15-25%, and except the required steam of reboiler heating, dynamic equipment is outer for the energy without the need to other.
Usually, present invention process equipment needed thereby mainly comprises electric dust-removing equipment, the heat exchanger of byproduct steam, turbine, absorption tower, regenerator, boiling device, other equipment such as heat exchanger, pump.
The carbon dioxide containing gas of described high temperature (180-280 DEG C) first enters electric dust collector, enter heat exchanger after dedusting again and produce low-pressure steam, low-pressure steam enters first order solution boiling device for heated solution, and the solution after heating enters solution second level reboiler thermal regeneration again.After the heat exchanger of byproduct steam, flue gas cool-down, to 120-140 DEG C, enters heat exchanger for heating the rich solution into regenerator, cool to 95 DEG C, enter next heat exchanger afterwards, for heating boiler water, and cool to 50 DEG C, and then enter absorption tower and carry out decarburization absorption.Take full advantage of the waste heat of raw material flue gas like this, can reboiler steam 15-25% be saved.
Describedly heat CFC from the regeneration overhead regeneration gas of 90-99 DEG C out by heat exchanger, expand after making it gasification pressurization, promotion turbine generates electricity, CFC gas temperature after acting and pressure drop, liquefy after subcooler again, be then recycled to heat exchanger through pump and reheat gasification.This regeneration gas UTILIZATION OF VESIDUAL HEAT IN process can be used for generating, and the electric energy produced can the power of lean pump in feed system and the equipment such as rich solution pump and reflux pump use.
Described CFC, what select is the Small molecular CFC of boiling point within the scope of 25-65 DEG C, as C
2h
5cl, CH
2cl
2, C
2clF
5, CCl
3f, C
2h
4f
2, CHCl
2one or more in F.
Accompanying drawing explanation
Accompanying drawing 1 is embodiment of the present invention process flow diagram.
In figure, 1-carbon dioxide, 2-electric dust collector, 3-heat exchanger, 4-rich solution preheater, 5-boiler water heater, 6-absorption tower, 7-rich solution pump, 8-poor rich liquid heat exchanger, 9-regenerator, 10-lean pump, 11-lean solution cooler, 12-regeneration gas cooler, 13-condensate return pump, 14-first order solution boiling device, 15-second level solution boiling device, 16-steam condensate (SC) is intake, 17-low-pressure steam, the water outlet of 18-steam condensate (SC), 19-steam enters, 20-condensed water goes out, 21-regeneration gas, 22-CFC pressurized vapor, 23-turbine, 24-low pressure CFC, 25-cooler, 26-liquid chlorofluorocarbons, 27-circulating pump, 28-liquid chlorofluorocarbons returns heat exchanger, 29-boiler water enters, boiler water after 30-preheating, 31-regeneration gas goes out, 32-cooling water enters, 33-cooling water goes out, 34-unstripped gas enters separator, 35-separator, 36-condensed water goes out.
Detailed description of the invention
Below in conjunction with embodiment and accompanying drawing, present invention process is described in detail.
embodiment:shown in the present embodiment process drawing 1, its process is as follows:
The carbon dioxide containing gas 1 of high temperature (250 DEG C) first enters electric dust collector 2, heat exchanger 3 is entered again after dedusting, low-pressure steam is produced after heat exchange, low-pressure steam enters first order solution boiling device 14, heated solution, the solution after heating enters solution second level reboiler 24 thermal regeneration again.After the heat exchanger of byproduct steam, flue gas cool-down, to 130 DEG C, entering heat exchanger 4 for heating the rich solution into regenerator, cooling to 95 DEG C, entering heat exchanger 5 afterwards, for heating boiler water, and cool to 50 DEG C, and then enters absorption tower 6 and absorb.Take full advantage of the waste heat of raw material flue gas like this, can reboiler steam be saved.Simultaneously few than traditional handicraft equipment such as water scrubber and water washing cycles pump, decreases equipment investment, reduces operating cost.
Eject from regenerator 9 regeneration gas of 98 DEG C come and heat CFC by heat exchanger 12, expand after making it gasification pressurization, promote turbine 23 to generate electricity, CFC gas temperature after acting and pressure drop, liquefy after subcooler 25 again, be then recycled to heat exchanger 12 through pump 27 and reheat gasification.This regeneration gas UTILIZATION OF VESIDUAL HEAT IN process can be used for generating, and the electric energy produced can the power of lean pump 10 in feed system and the equipment such as rich solution pump 7 and reflux pump 13 use.
application case
Certain device unstripped gas 250 DEG C, volume flow 43000 mark sides per hour, carbonated 12%, steam 11%, oxygen 5.3%, all the other are nitrogen, after above-mentioned PROCESS FOR TREATMENT, can byproduct steam 1.8 tons/hour, reboiler steam consumption 8.2 tons/hour; This device regeneration gas flow 6200 mark is cube per hour, and temperature 98 degree, heats CCl by heat exchanger
3f gasifies expansion, and after making it to promote the technique of turbine power generation, generating 120 kilowatt hour per hour, the power that simultaneously can meet the equipment such as the lean pump in whole system, rich solution pump and reflux pump uses.
comparative example
Certain device unstripped gas 250 DEG C, volume flow 43000 mark sides per hour, carbonated 12%, steam 11%, oxygen 5.3%, all the other are nitrogen, and unstripped gas heat energy does not utilize, directly be water-cooled to 50 DEG C through cool cycles, enter absorption tower after separating and condensing water, regeneration gas waste heat does not also utilize, and all the other operations are identical with embodiment, reboiler steam consumption 10 tons/hour under this condition, needs dynamic equipment to power 105 kilowatt hours simultaneously.
Can be found out by contrast, technique provided by the present invention can be reduced to 8.2 tons/hour steam consumption from 10 tons/hour, and reduce regeneration energy consumption 18%, generate electricity 120 kilowatt hours in addition, and meet dynamic equipment power demands, energy conservation and consumption reduction effects is obvious.
Claims (3)
1. a smoke carbon dioxide capture technique, is characterized in that, before high-temperature flue gas enters absorption tower, adopts the dust in the method separate raw materials gas of electric precipitation, and utilizes the reboiler that high-temperature flue gas waste heat byproduct steam is device to provide heat; In regeneration overhead, utilize regeneration overhead regeneration gas heating low boiling point working medium, making it heat up expand after acting drive turbine generating, the dynamic equipment meeting whole cleaning system that generates electricity power; First described high-temperature flue gas enters electric dust collector, and enter heat exchanger after dedusting again and produce low-pressure steam, low-pressure steam enters first order solution boiling device for heated solution, and the solution after heating enters solution second level reboiler thermal regeneration again; After the heat exchanger of byproduct steam, steam is used for the reboiler heating at the bottom of regenerator, flue gas cool-down is to 120-140 DEG C, enter heat exchanger for heating the rich solution into regenerator, cool to 95 DEG C, enter next heat exchanger afterwards, for heating boiler water, and cool to 50 DEG C, and then enter absorption tower and carry out decarburization absorption; CFC is heated by heat exchanger from the regeneration overhead regeneration gas of 90-99 DEG C out, expand after making it gasification pressurization, promote turbine generating, the CFC gas temperature after acting and pressure drop, liquefy after subcooler again, be then recycled to heat exchanger through pump and reheat gasification.
2. technique as claimed in claim 1, is characterized in that the Small molecular CFC that described CFC selects boiling point within the scope of 25-65 DEG C.
3. technique as claimed in claim 1, is characterized in that described CFC selects C
2h
5cl, CH
2cl
2, C
2clF
5, CCl
3f, C
2h
4f
2, CHCl
2one or more in F.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210277347.1A CN103566712B (en) | 2012-08-07 | 2012-08-07 | A kind of smoke carbon dioxide capture technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210277347.1A CN103566712B (en) | 2012-08-07 | 2012-08-07 | A kind of smoke carbon dioxide capture technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103566712A CN103566712A (en) | 2014-02-12 |
| CN103566712B true CN103566712B (en) | 2016-03-30 |
Family
ID=50039948
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210277347.1A Active CN103566712B (en) | 2012-08-07 | 2012-08-07 | A kind of smoke carbon dioxide capture technique |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106039960B (en) * | 2016-06-13 | 2018-04-24 | 大连理工大学 | A kind of collecting carbonic anhydride liquefaction process of cascade utilization fume afterheat |
| CN106122977B (en) * | 2016-09-05 | 2018-01-05 | 重庆科技学院 | CO2 recovery systems based on refuse gasification combustion gas and steam turbine cogeneration |
Citations (4)
| 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 |
| CN101634449A (en) * | 2009-09-01 | 2010-01-27 | 东南大学 | Method for reducing emission of carbon dioxide by circulating fluidized bed temperature flue gas circulation oxygen combustion |
| WO2011002198A3 (en) * | 2009-06-30 | 2011-03-31 | 한국전력공사 | System and method for absorbing and separating acid gas |
| CN102022746A (en) * | 2009-09-16 | 2011-04-20 | Bha控股公司 | Power plant emissions control using integrated organic rankine cycle |
-
2012
- 2012-08-07 CN CN201210277347.1A patent/CN103566712B/en active Active
Patent Citations (4)
| 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 |
| WO2011002198A3 (en) * | 2009-06-30 | 2011-03-31 | 한국전력공사 | System and method for absorbing and separating acid gas |
| CN101634449A (en) * | 2009-09-01 | 2010-01-27 | 东南大学 | Method for reducing emission of carbon dioxide by circulating fluidized bed temperature flue gas circulation oxygen combustion |
| CN102022746A (en) * | 2009-09-16 | 2011-04-20 | Bha控股公司 | Power plant emissions control using integrated organic rankine cycle |
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| Publication number | Publication date |
|---|---|
| CN103566712A (en) | 2014-02-12 |
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Address after: Liuhe District of Nanjing City, Jiangsu province 210048 geguan Road No. 699 Patentee after: China Petroleum & Chemical Corp. Patentee after: SINOPEC NANJING CHEMICAL RESEARCH INSTITUTE Co.,Ltd. Address before: Liuhe District of Nanjing City, Jiangsu province 210048 geguan Road No. 699 Patentee before: China Petroleum & Chemical Corp. Patentee before: Nanhua Group Research Institute |