CN110115910A - A kind of energy-saving carbon dioxide capture system and method - Google Patents
A kind of energy-saving carbon dioxide capture system and method Download PDFInfo
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- CN110115910A CN110115910A CN201910538286.1A CN201910538286A CN110115910A CN 110115910 A CN110115910 A CN 110115910A CN 201910538286 A CN201910538286 A CN 201910538286A CN 110115910 A CN110115910 A CN 110115910A
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 60
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 29
- 229960004424 carbon dioxide Drugs 0.000 claims abstract description 66
- 238000010521 absorption reaction Methods 0.000 claims abstract description 51
- 239000007788 liquid Substances 0.000 claims abstract description 42
- 230000008929 regeneration Effects 0.000 claims abstract description 29
- 238000011069 regeneration method Methods 0.000 claims abstract description 29
- 239000003546 flue gas Substances 0.000 claims abstract description 24
- 230000002745 absorbent Effects 0.000 claims abstract description 23
- 239000002250 absorbent Substances 0.000 claims abstract description 23
- 238000005406 washing Methods 0.000 claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 230000008569 process Effects 0.000 claims abstract description 14
- 235000011089 carbon dioxide Nutrition 0.000 claims abstract description 10
- 239000000243 solution Substances 0.000 claims description 131
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 26
- 239000007789 gas Substances 0.000 claims description 14
- 238000005261 decarburization Methods 0.000 claims description 8
- 238000010992 reflux Methods 0.000 claims description 8
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonium chloride Substances [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 claims description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 229910017053 inorganic salt Inorganic materials 0.000 claims description 4
- 239000012266 salt solution Substances 0.000 claims description 4
- 125000004122 cyclic group Chemical group 0.000 claims description 2
- 230000001172 regenerating effect Effects 0.000 claims description 2
- 125000003277 amino group Chemical group 0.000 claims 1
- 125000002924 primary amino group Chemical group [H]N([H])* 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 8
- 239000000126 substance Substances 0.000 abstract description 8
- 238000009833 condensation Methods 0.000 abstract description 6
- 230000005494 condensation Effects 0.000 abstract description 6
- 230000003247 decreasing effect Effects 0.000 abstract description 5
- 238000004134 energy conservation Methods 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 238000012423 maintenance Methods 0.000 abstract description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract description 3
- 238000000746 purification Methods 0.000 abstract description 2
- 230000009467 reduction Effects 0.000 abstract description 2
- 230000000052 comparative effect Effects 0.000 description 5
- 150000001412 amines Chemical class 0.000 description 4
- -1 amino-acid salt Chemical class 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 2
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 238000010612 desalination reaction Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 230000008439 repair process Effects 0.000 description 2
- 230000026676 system process Effects 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005262 decarbonization Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- SOQBVABWOPYFQZ-UHFFFAOYSA-N oxygen(2-);titanium(4+) Chemical class [O-2].[O-2].[Ti+4] SOQBVABWOPYFQZ-UHFFFAOYSA-N 0.000 description 1
- 230000007115 recruitment Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N titanium dioxide Inorganic materials O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 1
- 235000010215 titanium dioxide Nutrition 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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
- B01D53/1425—Regeneration of liquid absorbents
-
- 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
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- 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
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
A kind of energy-saving carbon dioxide capture system and method disclosed by the invention, belong to flue gases purification field.By the way that Separate System of Water-jet is arranged, rich solution is set first to carry out partial regeneration before entering regenerator, enter regenerator after carbon dioxide separation is discharged, reduce the thermic load of regenerator, regenerator can be made to be maintained at higher temperature, compared with conventional chemical absorption process carries out the system of collecting carbonic anhydride, the size of regeneration energy consumption, reduction regenerator can be greatly lowered.It is re-used in addition, the partial condensation liquid of regenerator upper section return tank is sent into absorption tower wash mill, the consumption of demineralized water can be made to be greatly decreased, the purpose of washing is to prevent absorbent steam from spreading.Reasonable, energy conservation and environmental protection is designed, and the cost of device fabrication and system maintenance can be significantly reduced.
Description
Technical field
The invention belongs to flue gases purification fields, and in particular to a kind of energy-saving carbon dioxide capture system and method.
Background technique
In recent years, by the trapping of carbon dioxide and seal up for safekeeping CCS realize reduction of greenhouse gas discharge technology path become the world
Cope with one of the important measure of climate change.To realize this target, develop in succession both at home and abroad such as chemical absorbing, absorption,
The various methods such as UF membrane, deep cooling carry out the trapping of carbon dioxide.Wherein, it is produced using absorbent removing coal-fired power plant etc.
The chemical absorption process of raw sour gas carbon dioxide is one of most common method, is had efficiently and consistent excellent
Gesture.Capture process based on alcohol ammonia absorbent is a kind of chemical absorbing technical examples of technically reliable, which is successfully used for
In petrochemical industry decarbonization process.Nevertheless, the isolation technics could be used to handle boiler combustion there is still a need for process modification is carried out
The flue gas of discharge.
Fig. 1 show the work flow diagram that collecting carbonic anhydride is carried out using conventional chemical absorption process.Flue gas 1 after cooling
Generally it is in contact under the conditions of 40~60 DEG C of temperature with absorbent；Carbon dioxide in flue gas is absorbed after agent absorbs from absorption
The discharge of 9 bottom of tower, decarburization flue gas 4 are discharged from the top on absorption tower 9.Circulation washing water in circulation washing water pipeline 3 plays back
Receive the effect of the absorbent spread with flue gas.The absorbent for absorbing carbon dioxide is referred to as rich solution, the rich solution in rich solution pipeline 5
11 filler upper end of regenerator is sent to after the heating of rich or poor heat exchanger 10.Pressure of the rich solution at 110-140 DEG C and 150-200kPa
It is regenerated under power, parses carbon dioxide gas.Regenerator regenerative process will consume thermal energy, be provided by reboiler 12.Regeneration
Gas 6 is mainly made of carbon dioxide and steam, contains a small amount of absorbent steam.The regeneration gas in feed channel 6 is regenerated by condensation
Device 13 cools down, and the condensate liquid isolated by return tank 7 is re-delivered to regenerator 11 through condensate liquid pipeline 8, two isolated
Carbonoxide is discharged through the CO2 emission pipeline on return tank 7.Absorbent after regeneration is known as lean solution, lean solution pipeline 2
Interior lean solution is transported to absorption tower 9 with pump after rich or poor heat exchanger 10 recycles heat.
In above-mentioned process flow, carbon dioxide regenerative process will consume big energy, and rich solution leads to before entering regenerator
It crosses rich or poor heat exchanger to be heated, forms gas-liquid two-phase medium and enter regenerator, result in heat exchange efficiency in tower and decline, increase
Regeneration energy consumption.In addition, regeneration gas condensation and separation of condensate liquid be not used as absorption tower cleaning solution re-use, increase washing section
Demineralized water magnitude of recruitment.
Summary of the invention
In order to solve above-mentioned defect existing in the prior art, the purpose of the present invention is to provide a kind of energy-saving titanium dioxides
Carbon capture system and method, can be greatly lowered the consumption and regeneration energy consumption of demineralized water, and reduce the size of regenerator.It should
System design is reasonable, building is simple, energy conservation and environmental protection, and can significantly reduce the cost of device fabrication and system maintenance.
The present invention is achieved through the following technical solutions:
The invention discloses a kind of energy-saving carbon dioxide capture system, including absorption tower, rich or poor heat exchanger, regenerator,
Return tank and flash tank；Absorb the bottom of the tower is connected to by rich solution pipeline with flash tank, on the liquid outlet and regenerator of flash tank
Rich solution entrance connection, rich solution pipeline be equipped with rich solution pump；The washing section on absorption tower is equipped with circulation washing water pipeline；In flue gas
Carbon dioxide becomes decarburization flue gas after the absorption of absorption tower inner absorbent and absorption tower is discharged；
The lean solution outlet of regeneration tower bottom is connected to by lean solution pipeline with the lean solution entrance on absorption tower, is set on lean solution pipeline
There are lean pump and lean solution cooler；Lean solution pipeline is exchanged heat with rich solution pipeline by rich or poor heat exchanger；Regenerator is connected with reboiler；
Regeneration gas outlet on regenerator is connect by regenerating feed channel with return tank, and regeneration feed channel is equipped with condenser, return tank
Liquid outlet be connected to the condensate inlet of regenerator by condensate liquid pipeline；Condensate liquid pipeline passes through condensate liquid reflux line
It is connected to circulation washing water pipeline.
Preferably, the lean solution pipeline between lean solution outlet and rich or poor heat exchanger is equipped with semi lean solution-lean solution heat exchanger, regeneration
Tower is equipped with semi lean solution circulating line, and semi lean solution circulating line is connected to semi lean solution-lean solution heat exchanger, in semi lean solution circulating line
Semi lean solution in semi lean solution-lean solution heat exchanger in lean solution pipeline lean solution heat exchange after return to regenerator.
It is further preferred that semi lean solution-lean solution heat exchanger is shell-and-tube heat exchanger.
Preferably, condenser is panel cooler or chimney cooler.
Preferably, lean solution cooler is panel cooler or chimney cooler
Preferably, absorbent is one or more of amine liquid, amino-acid salt, inorganic salt solution and ammonia solution.
Preferably, the gas vent of flash tank is connected to return tank.
The invention discloses the method for carrying out collecting carbonic anhydride using above-mentioned energy-saving carbon dioxide capture system, packets
Include: after flue gas enters absorption tower, the carbon dioxide in flue gas is absorbed agent absorption, becomes decarburization flue gas and is discharged after washing section
Absorption tower；The absorbent i.e. rich solution for absorbing carbon dioxide is pumped into flash distillation through rich solution pump by rich solution pipeline from absorb the bottom of the tower
Tank, rich solution is isolated in flash tank enters regenerator from rich solution entrance after carbon dioxide, heats through reboiler, isolates dioxy
Change carbon, carbon dioxide enters return tank through condenser by regeneration feed channel, and the condensate liquid a part generated in return tank passes through cold
Lime set pipeline enters regenerator, and another part enters circulation washing water pipeline by condensate liquid reflux line；Carbon dioxide removal
Absorbent, that is, lean solution, by lean solution pipeline after lean pump is pumped into lean solution cooler enter absorption tower, start it is next absorb/again
Raw circulation, in cyclic process, rich solution pipeline and lean solution pipeline pass through the progress heat exchange of rich or poor heat exchanger.
Preferably, it is externally provided with semi lean solution-lean solution heat-exchange system in regenerator, the semi lean solution in regenerator is poor in semi lean solution-
Regenerator is returned with after the lean solution heat exchange in lean solution pipeline in liquid heat-exchange system.
Compared with prior art, the invention has the following beneficial technical effects:
A kind of energy-saving carbon dioxide capture system disclosed by the invention is entering rich solution again by the way that flash tank is arranged
Partial regeneration is first carried out before raw tower, regenerator is entered after carbon dioxide separation is discharged, reduces the thermic load of regenerator, it can
Regenerator is set to be maintained at higher temperature, it, can be significantly compared with conventional chemical absorption process carries out the system of collecting carbonic anhydride
The size for reducing regeneration energy consumption, reducing regenerator.In addition, the partial condensation liquid of regenerator upper section return tank is passed through circulation
Washing water pipeline is sent into absorption tower wash mill and is re-used, and the consumption of demineralized water can be made to be greatly decreased, the purpose of washing is anti-
Only absorbent steam is spread.System design rationally, energy conservation and environmental protection, and can significantly reduce device fabrication and system maintenance at
This.
Further, it by the way that semi lean solution-lean solution heat exchanger is arranged, make lean solution and regenerates the semi lean solution heat exchange of midsection, fills
Divide heat contained in the lean solution for being utilized and being discharged from regenerator, further reduces the steam consumption of reboiler.
Further, semi lean solution-lean solution heat exchanger uses shell-and-tube heat exchanger, and structure is simple, low cost, can be in high temperature
It is used under high pressure operating condition.
Further, condenser and lean solution cooler use panel cooler or chimney cooler, and heat exchange efficiency is high, heat waste
Lose small, structure is compact, long service life.
Further, absorbent is using one of amine liquid, amino-acid salt, inorganic salt solution and ammonia solution or multiple combinations
It uses, to the good absorption effect of carbon dioxide.
Further, the gas vent of flash tank is connected to return tank, and carbon dioxide is collected in return tank discharge, is convenient for
Unified Collection utilization, while decreasing because collecting device being respectively set and bring cost.
The method disclosed by the invention that collecting carbonic anhydride is carried out using above-mentioned energy-saving carbon dioxide capture system, sufficiently
The heat of each link product is utilized, reduces the consumption of energy；The partial condensation liquid of regenerator upper section return tank is sent into and is inhaled
It receives tower wash mill to re-use, the consumption of demineralized water can be made to be greatly decreased.The technological operation is simple, energy conservation and environmental protection.
Further, semi lean solution-lean solution heat-exchange system takes full advantage of heat contained in lean solution, needs semi lean solution
Heat is reduced, and further reduces the steam consumption of reboiler.
Detailed description of the invention
Fig. 1 is the process flow chart that collecting carbonic anhydride is carried out using conventional chemical absorption process；
Fig. 2 is the system process figure of the embodiment of the present invention 1；
Fig. 3 is the system process figure of the embodiment of the present invention 2.
In figure: 1- flue gas, 2- lean solution pipeline, 3- recycle washing water pipeline, 4- decarburization flue gas, 5- rich solution pipeline, 6- regeneration
Feed channel, 7- return tank, 8- condensate liquid pipeline, the absorption tower 9-, the rich or poor heat exchanger of 10-, 11- regenerator, 12- reboiler, 13- are cold
Condenser, 14- lean solution cooler, 15- flash tank, 16- condensate liquid reflux line, 17- semi lean solution-lean solution heat exchanger.
Specific embodiment
The invention will be described in further detail in the following with reference to the drawings and specific embodiments, and content is to solution of the invention
It releases rather than limits:
Embodiment 1
Such as Fig. 2, energy-saving carbon dioxide capture system of the invention, including absorption tower 9, rich or poor heat exchanger 10, regenerator
11, return tank 7 and flash tank 15；9 bottom of absorption tower is connected to by rich solution pipeline 5 with flash tank 15, the liquid discharge of flash tank 15
Mouth is connected to the rich solution entrance on regenerator 11, the gas vent of flash tank 15 can be connected to return tank 7；Rich solution pipeline 5
It is equipped with rich solution pump；The washing section on absorption tower 9 is equipped with circulation washing water pipeline 3；Carbon dioxide in flue gas 1 is through in absorption tower 9
Absorbent absorb after become decarburization flue gas 4 be discharged absorption tower 9, absorbent can using amine liquid, amino-acid salt, inorganic salt solution and
One or more of ammonia solution；The lean solution outlet of 11 bottom of regenerator passes through the lean solution entrance on lean solution pipeline 2 and absorption tower 9
Connection, lean solution pipeline 2 are equipped with lean pump and lean solution cooler 14；Lean solution pipeline 2 and rich solution pipeline 5 pass through rich or poor heat exchanger 10
Heat exchange；Regenerator 11 is connected with reboiler 12；Regeneration gas outlet on regenerator 11 is connected by regeneration feed channel 6 and return tank 7
It connects, regeneration feed channel 6 is equipped with condenser 13, and the liquid outlet of return tank 7 passes through the condensation of condensate liquid pipeline 8 and regenerator 11
The connection of liquid entrance；Condensate liquid pipeline 8 is connected to by condensate liquid reflux line 16 with circulation washing water pipeline 3.
The absorbent (rich solution) that carbon dioxide is absorbed in absorption tower 9 exchanged heat with high temperature (110~130 DEG C) lean solution
It is heated in journey, then send flash tank 15, the carbon dioxide gas flashed off send return tank 7, and liquid is sent into 11 upper section of regenerator.
A part of the condensate liquid generated in return tank 7 is sent into regenerator by condensate liquid pipeline 8, and another part is flowed back by condensate liquid
Pipeline 16 is sent into 9 wash mill of absorption tower.
Condenser 13 and lean solution cooler 14 can use panel cooler or chimney cooler；
Embodiment 2
Such as Fig. 3, on the basis of 1 system of embodiment, on the lean solution pipeline 2 between lean solution outlet and rich or poor heat exchanger 10
Semi lean solution-lean solution heat exchanger 17 is set, and regenerator 11 is equipped with semi lean solution circulating line, the semi lean solution in semi lean solution circulating line
Regenerator 11 is returned with after the lean solution heat exchange in lean solution pipeline 2 in semi lean solution-lean solution heat exchanger 17.Semi lean solution-lean solution heat exchange
Device 17 can use shell-and-tube heat exchanger.
Comparative example
As Fig. 1 does not include flash tank 15, semi lean solution-lean solution using the carbon dioxide capture system of conventional chemical absorption process
Heat exchanger 17 and condensate liquid reflux line 16.
Compliance test result
By the flue gas that temperature is 40 DEG C, carbon dioxide volume fraction is 15%, by 2.0m3The flow of/hour is respectively fed to
9 bottom of system absorption tower of embodiment 1, embodiment 2 and comparative example, using 30wt% ethanolamine solutions as carbon dioxide absorption
Agent, internal circulating load are set as 100ml/ minutes, and the absorbent temperature for being sent into absorption tower is set in 40 DEG C.9 inlet flue gas of absorption tower, 1 He
Gas concentration lwevel in decarburization flue gas 4 is measured with gas analyzer, is calculated reboiler by 90% carbon dioxide eliminating rate and is being caught
The heat consumption in carbon dioxide per ton is obtained, the results are shown in Table 1.
The comparison of the regeneration energy consumption of 1 embodiment 1,2 of table and comparative example
As shown in Table 1, when capturing equal amount carbon dioxide under the conditions of identical carbon dioxide eliminating efficiency (90%), implement
Example 1 and the cooling water of embodiment 2 and reboiler heat consumption are lower than comparative example.Should the result shows that, in identical carbon dioxide
Under removal efficiency, the negative of desalination water consumption and regenerator can be reduced with energy-saving carbon dioxide capture system of the invention and technique
Lotus, and steam consumption is greatly lowered.
The invention proposes pass through two kinds of energy-saving recycling techniques of heating and method among rich solution partial regeneration and regenerator, drop
Low regenerator thermic load, can allow regenerator to be maintained at higher temperature, with conventional amine liquid absorbent carbon dioxide capture system phase
Than regeneration energy consumption and regenerator size can be greatly lowered.In addition, because the condensate liquid of regenerator upper section return tank is sent
Enter the re-using of absorption tower wash mill, desalination water consumption can be greatly decreased.Therefore, regeneration energy can be reduced and water disappears
Consumption, this is most important factor in collecting carbonic anhydride technique.
With the system of the embodiment of the present invention 2 compared with conventional system (comparative example), regeneration energy consumption 0.45GJ/ can be reduced
Ton CO2.According to the carbon dioxide treatment status of the coal-burning power plant 500MW, 10,000 ton of carbon dioxide is about generated daily, 90%
Under the conditions of removal efficiency, energy consumption can decline about 4,500GJ.
It should be noted that the foregoing is merely one of embodiment of the present invention, system institute having thus described the invention
The equivalence changes done, are included in protection scope of the present invention.Those skilled in the art can be to institute
The specific example of description does similar mode and substitutes, and without departing from structure of the invention or surmounts the claims and determines
The range of justice, all belongs to the scope of protection of the present invention.
Claims (9)
1. a kind of energy-saving carbon dioxide capture system, which is characterized in that including lean solution pipeline (2), rich solution pipeline (5), reflux
Tank (7), absorption tower (9), rich or poor heat exchanger (10), regenerator (11) and flash tank (15)；Absorption tower (9) bottom passes through rich solution pipe
Road (5) is connected to flash tank (15), and the liquid outlet of flash tank (15) is connected to the rich solution entrance on regenerator (11), rich solution pipe
Road (5) is equipped with rich solution pump；The washing section on absorption tower (9) is equipped with circulation washing water pipeline (3)；Carbon dioxide in flue gas (1)
Become decarburization flue gas (4) discharge absorption tower (9) after the absorption of absorption tower (9) inner absorbent；
The lean solution outlet of regenerator (11) bottom is connected to by lean solution pipeline (2) with the lean solution entrance on absorption tower (9), lean solution pipe
Road (2) is equipped with lean pump and lean solution cooler (14)；Lean solution pipeline (2) and rich solution pipeline (5) pass through rich or poor heat exchanger (10)
Heat exchange；Regenerator (11) is connected with reboiler (12)；Regeneration gas outlet on regenerator (11) by regeneration feed channel (6) and is returned
Tank (7) connection is flowed, regeneration feed channel (6) is equipped with condenser (13), and the liquid outlet of return tank (7) passes through condensate liquid pipeline
(8) it is connected to the condensate inlet of regenerator (11)；Condensate liquid pipeline (8) is washed by condensate liquid reflux line (16) and circulation
Waterpipe (3) connection.
2. energy-saving carbon dioxide capture system according to claim 1, which is characterized in that lean solution outlet and rich or poor heat exchange
Lean solution pipeline (2) between device (10) is equipped with semi lean solution-lean solution heat exchanger (17), and regenerator (11) is recycled equipped with semi lean solution
Pipeline, semi lean solution circulating line are connected to semi lean solution-lean solution heat exchanger (17), and the semi lean solution in semi lean solution circulating line is poor half
Regenerator (11) are returned with after the lean solution heat exchange in lean solution pipeline (2) in liquid-lean solution heat exchanger (17).
3. energy-saving carbon dioxide capture system according to claim 2, which is characterized in that semi lean solution-lean solution heat exchanger
It (17) is shell-and-tube heat exchanger.
4. energy-saving carbon dioxide capture system according to claim 1, which is characterized in that condenser (13) is board-like cold
But device or chimney cooler.
5. energy-saving carbon dioxide capture system according to claim 1, which is characterized in that lean solution cooler (14) is plate
Formula cooler or chimney cooler.
6. energy-saving carbon dioxide capture system according to claim 1, which is characterized in that absorbent is amine liquid, amino
One or more of hydrochlorate, inorganic salt solution and ammonia solution.
7. energy-saving carbon dioxide capture system according to claim 1, which is characterized in that the gas of flash tank (15) goes out
Mouth is connected to return tank (7).
8. a kind of carry out collecting carbonic anhydride using energy-saving carbon dioxide capture system described in claim 1~7 any one
Method, comprising:
After flue gas (1) enters absorption tower (9), the carbon dioxide in flue gas (1) is absorbed agent absorption, becomes decarburization flue gas (4) warp
Absorption tower (9) are discharged after crossing washing section；The absorbent i.e. rich solution for absorbing carbon dioxide passes through rich solution pipe from absorption tower (9) bottom
Road (5) is pumped into flash tank (15) through rich solution pump, and rich solution enters after isolating carbon dioxide in flash tank (15) from rich solution entrance
Regenerator (11) heats through reboiler (12), isolates carbon dioxide, carbon dioxide is by regeneration feed channel (6) through condenser
(13) enter return tank (7), the condensate liquid a part generated in return tank (7) enters regenerator by condensate liquid pipeline (8)
(11), another part enters circulation washing water pipeline (3) by condensate liquid reflux line (16)；The absorbent of carbon dioxide removal
That is lean solution enters absorption tower (9) after lean pump is pumped into lean solution cooler (14) by lean solution pipeline (2), and the next absorption of beginning/
Regeneration cycle, in cyclic process, rich solution pipeline (5) and lean solution pipeline (2) pass through rich or poor heat exchanger (10) progress heat exchange.
9. energy-saving carbon dioxide capture system according to claim 8 cleans burning process, which is characterized in that regenerating
Tower (11) is externally provided with semi lean solution-lean solution heat-exchange system, the semi lean solution in regenerator (11) in semi lean solution-lean solution heat-exchange system with
Regenerator (11) are returned after lean solution heat exchange in lean solution pipeline (2).
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| CN110538544A (en) * | 2019-09-25 | 2019-12-06 | 成都赛普瑞兴科技有限公司 | decarbonization device |
| CN112742174A (en) * | 2019-10-29 | 2021-05-04 | 中国石油化工股份有限公司 | Method for removing alcohol from decarbonization unit of ethylene oxide/ethylene glycol device |
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| CN112774401A (en) * | 2021-01-05 | 2021-05-11 | 中国神华能源股份有限公司国华电力分公司 | Novel flue gas CO2Regeneration process of trapping system |
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| CN113926302A (en) * | 2021-09-10 | 2022-01-14 | 中国石油化工股份有限公司 | Low partial pressure carbon dioxide entrapment system |
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| CN115400569A (en) * | 2022-05-31 | 2022-11-29 | 江苏景宏新材料科技有限公司 | Carbon dioxide capture system and working method thereof |
| CN115400569B (en) * | 2022-05-31 | 2024-04-02 | 江苏景宏新材料科技有限公司 | Carbon dioxide capturing system and working method thereof |
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Application publication date: 20190813 |