CN104511228A - Process system and method for flue gas combined desulfurization and decarburization - Google Patents
Process system and method for flue gas combined desulfurization and decarburization Download PDFInfo
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- CN104511228A CN104511228A CN201410766487.4A CN201410766487A CN104511228A CN 104511228 A CN104511228 A CN 104511228A CN 201410766487 A CN201410766487 A CN 201410766487A CN 104511228 A CN104511228 A CN 104511228A
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- 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
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- 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
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- 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
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Abstract
A process system and method for flue gas combined desulfurization and decarburization. The system includes an absorption tower, a SO2 regenerator, a CO2 regeneration tower, a CO2 separator, a SO2 separator, a desulfurization and decarburization solution heat exchanger, a desulfurization poor and rich liquid heat exchanger, a decarburization poor and rich liquid heat exchanger, a desulfurization liquid cooler, a desulphurization liquid cooler and a CO2 cooler. The inside of the absorption tower from the bottom to the top is divided into a desulfurization region, a decarburization region and a tail gas washing region. The invention also provides a desulfurization and decarburization method for the system. The system can be used in collection of acidic gas containing SO2 and CO2 flue gas in power plant boiler and chemical industry, and has function of simultaneous removal of SO2 and CO2. The process system and method use the temperature difference in the SO2 and CO2 regeneration process to realize temperature cascade utilization within the system, and at the same time use waste heat from CO2 regeneration process as a heat source for SO2 regeneration; and liquid water after regeneration and separation of CO2 is used as a cold source for gas-liquid separation after SO2 regeneration. The system finally obtains high purity SO2 and CO2 gas.
Description
Technical field
The present invention relates to flue gas desulfurization and Technology of Reducing Greenhouse Gas Emissions field, be specifically related to a kind of process system and method for flue gas combined desulfurization decarburization.
Background technology
At present, coal-burning boiler all requires to install flue gas desulfurization facilities additional, and the overwhelming majority adopts Wet Limestone Desulfurization technology, and desulfuration efficiency can reach more than 90%, SO
2discharge is generally 50 ~ 100mg/Nm
3.Along with improving constantly and the appearance of recent National Development and Reform Committee about " coal electricity energy-saving and emission-reduction upgrading and transformation action plan (2014-2020) " of environmental protection standard, require the newly-built coal unit SO in east China area
2concentration of emission reaches gas turbine group emission limit substantially, and (namely under benchmark oxygen content 6% condition, SO2 concentration of emission is not higher than 35mg/Nm
3), middle part also will reach or in principle close to this limit value.For reaching this index, desulfurizer more efficiently must be adopted, can implement capacity-increasing transformation in existing Wet Limestone Desulfurization technical foundation on the one hand, adopt single tower Two-way Cycle or the bicirculating mode of double tower, be then adopt other more efficient desulfur technology on the one hand.
Improve constantly environmental protection standard at traditional pollutant, while pollutant control system is extensively applied, the reduction of discharging of main greenhouse gas CO2 is also paid attention in recent years day by day.A lot of western countries have started to promote the decarburization work of substantial power plant.But because fire coal boiler fume has broad-minded feature, and the content of its CO2 is more than the decades of times of SO2 content, make the trapping system investment of CO2 large.Because CO2 and SO2 is all sour gas, possess the genetic prerequisite adopting similar removing sulfuldioxide, can realize combining removing.
Summary of the invention
In order to overcome above-mentioned prior art Problems existing, the object of the present invention is to provide a kind of process system and method for flue gas combined desulfurization decarburization, removing of SO2 and CO2 can be realized in a system unit, and respective subtractive process dependent but complement one another, finally realize a kind of decarbonization desulfurization system of fully-integratedization.
In order to realize foregoing invention object, the technical scheme that the present invention takes is:
A kind of process system of flue gas combined desulfurization decarburization, comprise absorption tower 1, inside, described absorption tower 1 is divided into desulfurization zone 1A, decarburization region 1B and washing tail gas region 1C from bottom to top successively, be communicated with the top of SO2 regenerator 2 with the rich or poor heat exchanger 7 of doctor solution by desulfurization and decarburization solution heat exchanger 6 successively bottom described desulfurization zone 1A, be communicated with the top of CO2 regenerator 3 by the rich or poor heat exchanger 8 of decarbonizing liquid bottom described decarburization region 1B, the top of described washing tail gas region 1C is communicated with air; Be communicated with 1B top, decarburization region with decarbonizing liquid cooler 9 by the rich or poor heat exchanger 8 of decarbonizing liquid, desulfurization and decarburization solution heat exchanger 6 bottom described CO2 regenerator 3; The bottom of described SO2 regenerator 2 is communicated with the top of CO2 regenerator 3, be communicated with the top of doctor solution cooler 10 with desulfurization zone 1A by the rich or poor heat exchanger 7 of doctor solution simultaneously, also be communicated with CO2 separator 4 top by CO2 cooler 11, the top of described SO2 regenerator 2 is communicated with the top of SO2 separator 5; Be communicated with the top of SO2 regenerator 2 with CO2 regenerator 3 respectively bottom described SO2 separator 5; Be communicated with the top of SO2 separator 5 bottom described CO2 separator 4.
The process system of flue gas combined desulfurization decarburization described above carries out the method for desulfurization and decarburization, flue gas containing SO2 and CO2 enters from the bottom on absorption tower 1, first in the desulfurization zone 1A on absorption tower 1 Yu from 1A top, desulfurization zone, the doctor solution counter current contacting entered is sprayed, the doctor solution and the sulfur removing pregnant solution that absorb SO2 are discharged bottom the 1A of desulfurization zone, sulfur removing pregnant solution is first by desulfurization and decarburization solution heat exchanger 6, again by the rich or poor heat exchanger 7 of doctor solution after the heat of recovery section decarburization regenerated liquid, reclaim the heat after doctor solution autosynthesis, finally enter SO2 regenerator 2 from the top of SO2 regenerator 2,
Flue gas in absorption tower 1 is by entering decarburization region 1B immediately after the 1A of desulfurization zone, with spray the decarbonizing liquid counter current contacting entered from 1B top, decarburization region, the decarbonizing liquid and the decarburization rich solution that absorb CO2 are discharged bottom the 1B of decarburization region, decarburization rich solution is through the rich or poor heat exchanger 8 of decarbonizing liquid, reclaim the heat after decarburization rich solution autosynthesis, finally enter CO2 regenerator 3 from the top of CO2 regenerator 3;
Flue gas in absorption tower 1 is by entering washing tail gas region 1C immediately after the 1B of decarburization region, and in the 1C of washing tail gas region, flue gas is by entering air from top, absorption tower 1 and washing tail gas region 1C after the washings washing of circulation;
The decarburization rich solution entered from CO2 regenerator 3 top sprays from top to bottom, by external heat source heating decarburization rich solution, flow out bottom CO2 regenerator 3 after making the regeneration of decarburization rich solution isolate CO2, the decarburization regenerated liquid flowed out and decarburization lean solution are through the rich or poor heat exchanger 8 of decarbonizing liquid, desulfurization and decarburization solution heat exchanger 6 is passed through again with after the heat exchange of decarburization rich solution, utilize the heat heating sulfur removing pregnant solution of decarburization lean solution further, decarburization lean solution after cooling is lowered the temperature by decarbonizing liquid cooler 9, finally enter absorption tower 1 from 1B top, decarburization region, start the CO2 absorption process of a new round;
From the sulfur removing pregnant solution that SO2 regenerator 2 top enters, there is provided thermal source to heat by the CO2 mist introduced from CO2 regenerator 3, flow out bottom SO2 regenerator 2 after making desulfurization regeneration isolate SO2, the desulfurization regeneration liquid flowed out and desulfurization lean solution are through the rich or poor heat exchanger 7 of doctor solution, lower the temperature with sulfur removing pregnant solution heat exchange, desulfurization lean solution after cooling is lowered the temperature by doctor solution cooler 10, finally enters absorption tower 1 from 1A top, desulfurization zone, starts the SO2 absorption process of a new round;
The CO2 mist that the decarbonizing liquid of discharging from CO2 regenerator 3 top bears again, enter in SO2 regenerator 2, as the thermal source of desulfurization regeneration, CO2 mist after heat exchange cooling flows out bottom SO2 regenerator 2, cooled by CO2 cooler 11, then enter in CO2 separator 4, CO2 after separation discharges from CO2 separator 4 top and enters follow-up workshop section, isolated aqueous water imports SO2 separator 5 and sprays bottom CO2 separator 4, to leave from SO2 regenerator 2 top and the SO2 regeneration gas entered in SO2 separator 5 directly cools, thus realize being separated of SO2 gas and moisture in SO2 regeneration gas, SO2 after separation discharges from SO2 separator 5 top and enters follow-up workshop section, isolated aqueous water is divided into two-way, SO2 regenerator 2 and CO2 regenerator 3 top is injected respectively by flow-control, maintain the water balance in SO2 absorption and regeneration and CO2 absorption and regeneration loop respectively.
Compared to the prior art, tool has the following advantages in the present invention:
1) owing to achieving removing of SO2 and CO2 in absorption tower 1, save and need to build the absorption that SO2 and CO2 is carried out on two absorption towers respectively respectively, utilize the temperature difference of SO2 and CO2 regenerative process simultaneously, the cascade utilization of temperature is realized in internal system, utilize the waste heat of CO2 regenerative process as the regeneration thermal source of SO2 simultaneously, utilize CO2 to regenerate the aqueous water after being separated as the gas-liquid separation low-temperature receiver after SO2 regeneration, this system finally obtains highly purified SO2 and CO2 gas respectively.
2) utilize doctor solution and decarbonizing liquid in the temperature difference (decarbonizing liquid is than desulfurization regeneration temperature height about 20 DEG C) of regeneration stage, the doctor solution of the desulfurization zone 1A outlet at bottom on absorption tower 1 is first through desulfurization and decarburization solution heat exchanger 6, again by the rich or poor heat exchanger 7 of doctor solution after the heat of recovery section decarburization regenerated liquid, reclaim the heat after doctor solution autosynthesis, achieve the cascade utilization of temperature.
3) temperature difference considering desulfurization and decarburization regeneration stage and the amount of SO2 and CO2 born again poor, the CO2 mist born again by the decarbonizing liquid of discharging from CO2 regenerator 3 top imports in SO2 regenerator 2, as desulfurization regeneration thermal source, both meet desulfurization regeneration heat, also reduce the cooling water amount needed in CO2 cooler 11 simultaneously.
4) after CO2 regeneration gas in CO2 separator 4 being separated, low temperature liquid water imports spray in SO2 separator 5, to leave from SO2 regenerator 2 top and the SO2 regeneration gas entered in SO2 separator 5 directly cools, thus realize being separated of SO2 gas and moisture in SO2 regeneration gas.
Accompanying drawing explanation
Accompanying drawing is structural representation of the present invention.
Detailed description of the invention
Below in conjunction with drawings and the specific embodiments, the present invention is described in further detail.
As shown in drawings, the process system of a kind of flue gas combined desulfurization decarburization of the present invention, comprise absorption tower 1, inside, described absorption tower 1 is divided into desulfurization zone 1A, decarburization region 1B and washing tail gas region 1C from bottom to top successively, be communicated with the top of SO2 regenerator 2 with the rich or poor heat exchanger 7 of doctor solution by desulfurization and decarburization solution heat exchanger 6 successively bottom described desulfurization zone 1A, be communicated with the top of CO2 regenerator 3 by the rich or poor heat exchanger 8 of decarbonizing liquid bottom described decarburization region 1B, the top of described washing tail gas region 1C is communicated with air; Be communicated with 1B top, decarburization region with decarbonizing liquid cooler 9 by the rich or poor heat exchanger 8 of decarbonizing liquid, desulfurization and decarburization solution heat exchanger 6 bottom described CO2 regenerator 3; The bottom of described SO2 regenerator 2 is communicated with the top of CO2 regenerator 3, be communicated with the top of doctor solution cooler 10 with desulfurization zone 1A by the rich or poor heat exchanger 7 of doctor solution simultaneously, also be communicated with CO2 separator 4 top by CO2 cooler 11, the top of described SO2 regenerator 2 is communicated with the top of SO2 separator 5; Be communicated with the top of SO2 regenerator 2 with CO2 regenerator 3 respectively bottom described SO2 separator 5; Be communicated with the top of SO2 separator 5 bottom described CO2 separator 4.
As shown in drawings, the process system of flue gas combined desulfurization decarburization of the present invention carries out the method for desulfurization and decarburization, flue gas containing SO2 and CO2 enters from the bottom on absorption tower 1, first in the desulfurization zone 1A on absorption tower 1 Yu from 1A top, desulfurization zone, the doctor solution counter current contacting entered is sprayed, the doctor solution and the sulfur removing pregnant solution that absorb SO2 are discharged bottom the 1A of desulfurization zone, sulfur removing pregnant solution is first by desulfurization and decarburization solution heat exchanger 6, again by the rich or poor heat exchanger 7 of doctor solution after the heat of recovery section decarburization regenerated liquid, reclaim the heat after doctor solution autosynthesis, finally enter SO2 regenerator 2 from the top of SO2 regenerator 2, flue gas in absorption tower 1 is by entering decarburization region 1B immediately after the 1A of desulfurization zone, with spray the decarbonizing liquid counter current contacting entered from 1B top, decarburization region, the decarbonizing liquid and the decarburization rich solution that absorb CO2 are discharged bottom the 1B of decarburization region, decarburization rich solution is through the rich or poor heat exchanger 8 of decarbonizing liquid, reclaim the heat after decarburization rich solution autosynthesis, finally enter CO2 regenerator 3 from the top of CO2 regenerator 3, flue gas in absorption tower 1 is by entering washing tail gas region 1C immediately after the 1B of decarburization region, and in the 1C of washing tail gas region, flue gas is by entering air from top, absorption tower 1 and washing tail gas region 1C after the washings washing of circulation, the decarburization rich solution entered from CO2 regenerator 3 top sprays from top to bottom, by external heat source heating decarburization rich solution, flow out bottom CO2 regenerator 3 after making the regeneration of decarburization rich solution isolate CO2, the decarburization regenerated liquid flowed out and decarburization lean solution are through the rich or poor heat exchanger 8 of decarbonizing liquid, desulfurization and decarburization solution heat exchanger 6 is passed through again with after the heat exchange of decarburization rich solution, utilize the heat heating sulfur removing pregnant solution of decarburization lean solution further, decarburization lean solution after cooling is lowered the temperature by decarbonizing liquid cooler 9, finally enter absorption tower 1 from 1B top, decarburization region, start the CO2 absorption process of a new round, from the sulfur removing pregnant solution that SO2 regenerator 2 top enters, there is provided thermal source to heat by the CO2 mist introduced from CO2 regenerator 3, flow out bottom SO2 regenerator 2 after making desulfurization regeneration isolate SO2, the desulfurization regeneration liquid flowed out and desulfurization lean solution are through the rich or poor heat exchanger 7 of doctor solution, lower the temperature with sulfur removing pregnant solution heat exchange, desulfurization lean solution after cooling is lowered the temperature by doctor solution cooler 10, finally enters absorption tower 1 from 1A top, desulfurization zone, starts the SO2 absorption process of a new round, the CO2 mist that the decarbonizing liquid of discharging from CO2 regenerator 3 top bears again, enter in SO2 regenerator 2, as the thermal source of desulfurization regeneration, CO2 mist (water containing gas-liquid mixed phase) after heat exchange cooling flows out bottom SO2 regenerator 2, cooled by CO2 cooler 11, then enter in CO2 separator 4, CO2 after separation discharges from CO2 separator 4 top and enters follow-up workshop section, isolated aqueous water imports SO2 separator 5 and sprays bottom CO2 separator 4, to leave from SO2 regenerator 2 top and the SO2 regeneration gas entered in SO2 separator 5 directly cools, thus realize being separated of SO2 gas and moisture in SO2 regeneration gas, SO2 after separation discharges from SO2 separator 5 top and enters follow-up workshop section, isolated aqueous water is divided into two-way, SO2 regenerator 2 and CO2 regenerator 3 top is injected respectively by flow-control, maintain the water balance in SO2 absorption and regeneration and CO2 absorption and regeneration loop respectively.
Claims (2)
1. the process system of a flue gas combined desulfurization decarburization, it is characterized in that: comprise absorption tower (1), described absorption tower (1) inside is divided into desulfurization zone (1A) from bottom to top successively, decarburization region (1B) and washing tail gas region (1C), bottom, described desulfurization zone (1A) is communicated with the top of the rich or poor heat exchanger of doctor solution (7) with SO2 regenerator (2) by desulfurization and decarburization solution heat exchanger (6) successively, described decarburization region (1B) bottom is communicated with the top of CO2 regenerator (3) by the rich or poor heat exchanger of decarbonizing liquid (8), the top of described washing tail gas region (1C) is communicated with air, described CO2 regenerator (3) bottom is communicated with decarburization region (1B) top with decarbonizing liquid cooler (9) by the rich or poor heat exchanger of decarbonizing liquid (8), desulfurization and decarburization solution heat exchanger (6), the bottom of described SO2 regenerator (2) is communicated with the top of CO2 regenerator (3), be communicated with the top of doctor solution cooler (10) with desulfurization zone (1A) by the rich or poor heat exchanger of doctor solution (7) simultaneously, also be communicated with CO2 separator (4) top by CO2 cooler (11), the top of described SO2 regenerator (2) is communicated with the top of SO2 separator (5), described SO2 separator (5) bottom is communicated with the top of SO2 regenerator (2) with CO2 regenerator (3) respectively, described CO2 separator (4) bottom is communicated with the top of SO2 separator (5).
2. the process system of flue gas combined desulfurization decarburization described in claim 1 carries out the method for desulfurization and decarburization, it is characterized in that: the flue gas containing SO2 and CO2 enters from the bottom of absorption tower (1), first in the desulfurization zone (1A) of absorption tower (1) with spray from desulfurization zone (1A) top the doctor solution counter current contacting entered, the doctor solution and the sulfur removing pregnant solution that absorb SO2 are discharged from desulfurization zone (1A) bottom, sulfur removing pregnant solution is first by desulfurization and decarburization solution heat exchanger (6), again by the rich or poor heat exchanger of doctor solution (7) after the heat of recovery section decarburization regenerated liquid, reclaim the heat after doctor solution autosynthesis, finally enter SO2 regenerator (2) from the top of SO2 regenerator (2),
Flue gas in absorption tower (1) enters decarburization region (1B) immediately by behind desulfurization zone (1A), with spray the decarbonizing liquid counter current contacting entered from decarburization region (1B) top, the decarbonizing liquid and the decarburization rich solution that absorb CO2 are discharged from decarburization region (1B) bottom, decarburization rich solution is through the rich or poor heat exchanger of decarbonizing liquid (8), reclaim the heat after decarburization rich solution autosynthesis, finally enter CO2 regenerator (3) from the top of CO2 regenerator (3);
Flue gas in absorption tower (1) enters washing tail gas region (1C) immediately by behind decarburization region (1B), and in washing tail gas region (1C), flue gas is by entering air from (1) top, absorption tower and washing tail gas region (1C) after the washings washing of circulation;
The decarburization rich solution entered from CO2 regenerator (3) top sprays from top to bottom, by external heat source heating decarburization rich solution, flow out from CO2 regenerator (3) bottom after making the regeneration of decarburization rich solution isolate CO2, the decarburization regenerated liquid flowed out and decarburization lean solution are through the rich or poor heat exchanger of decarbonizing liquid (8), desulfurization and decarburization solution heat exchanger (6) is passed through again with after the heat exchange of decarburization rich solution, utilize the heat heating sulfur removing pregnant solution of decarburization lean solution further, decarburization lean solution after cooling is by decarbonizing liquid cooler (9) cooling, finally enter absorption tower (1) from decarburization region (1B) top, start the CO2 absorption process of a new round,
From the sulfur removing pregnant solution that SO2 regenerator (2) top enters, there is provided thermal source to heat by the CO2 mist introduced from CO2 regenerator (3), flow out from SO2 regenerator (2) bottom after making desulfurization regeneration isolate SO2, the desulfurization regeneration liquid flowed out and desulfurization lean solution are through the rich or poor heat exchanger of doctor solution (7), lower the temperature with sulfur removing pregnant solution heat exchange, desulfurization lean solution after cooling is by doctor solution cooler (10) cooling, finally enter absorption tower (1) from desulfurization zone (1A) top, start the SO2 absorption process of a new round;
The CO2 mist that the decarbonizing liquid of discharging from CO2 regenerator (3) top bears again, enter in SO2 regenerator (2), as the thermal source of desulfurization regeneration, CO2 mist after heat exchange cooling flows out from SO2 regenerator (2) bottom, cooled by CO2 cooler (11), then enter in CO2 separator (4), CO2 after separation discharges from CO2 separator (4) top and enters follow-up workshop section, isolated aqueous water imports spray SO2 separator (5) from CO2 separator (4) bottom, to leave from SO2 regenerator (2) top and the SO2 regeneration gas entered SO2 separator (5) directly cools, thus realize being separated of SO2 gas and moisture in SO2 regeneration gas, SO2 after separation discharges from SO2 separator (5) top and enters follow-up workshop section, isolated aqueous water is divided into two-way, SO2 regenerator (2) and CO2 regenerator (3) top is injected respectively by flow-control, maintain the water balance in SO2 absorption and regeneration and CO2 absorption and regeneration loop respectively.
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| CN105688603A (en) * | 2016-03-08 | 2016-06-22 | 长沙有色冶金设计研究院有限公司 | Regenerative desulfurization system adopting mechanical steam supercharging |
| CN107349759A (en) * | 2017-07-19 | 2017-11-17 | 哈尔滨工程大学 | A kind of ship tail gas combined desulfurization carbonization treatment device |
| WO2023221696A1 (en) * | 2022-05-16 | 2023-11-23 | 江南环境科技公司 | Method and apparatus for waste heat recovery in ammonia-based desulfurization and decarbonization system |
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| CN104511228B (en) | 2016-05-04 |
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