CN108404612A - A kind of rich solution multi-stage heat exchanger type carbon dioxide capture system and technique - Google Patents
A kind of rich solution multi-stage heat exchanger type carbon dioxide capture system and technique Download PDFInfo
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- CN108404612A CN108404612A CN201810378266.8A CN201810378266A CN108404612A CN 108404612 A CN108404612 A CN 108404612A CN 201810378266 A CN201810378266 A CN 201810378266A CN 108404612 A CN108404612 A CN 108404612A
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- liquid
- carbon dioxide
- absorption tower
- regenerator
- heat exchanger
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 127
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 81
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 44
- 238000000034 method Methods 0.000 title claims abstract description 40
- 239000007788 liquid Substances 0.000 claims abstract description 171
- 238000010521 absorption reaction Methods 0.000 claims abstract description 71
- 238000000926 separation method Methods 0.000 claims abstract description 62
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 46
- 230000005532 trapping Effects 0.000 claims abstract description 17
- 238000011069 regeneration method Methods 0.000 claims abstract description 16
- 230000008929 regeneration Effects 0.000 claims abstract description 15
- 239000006260 foam Substances 0.000 claims abstract description 11
- 239000002250 absorbent Substances 0.000 claims abstract description 7
- 230000002745 absorbent Effects 0.000 claims abstract description 7
- 238000010438 heat treatment Methods 0.000 claims abstract description 4
- 239000000463 material Substances 0.000 claims abstract description 4
- 239000000779 smoke Substances 0.000 claims abstract description 4
- 230000008016 vaporization Effects 0.000 claims abstract description 4
- 229960004424 carbon dioxide Drugs 0.000 claims description 52
- 239000007789 gas Substances 0.000 claims description 30
- 235000011089 carbon dioxide Nutrition 0.000 claims description 22
- 239000003546 flue gas Substances 0.000 claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 15
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 claims description 12
- XTUVJUMINZSXGF-UHFFFAOYSA-N N-methylcyclohexylamine Chemical compound CNC1CCCCC1 XTUVJUMINZSXGF-UHFFFAOYSA-N 0.000 claims description 8
- PAMIQIKDUOTOBW-UHFFFAOYSA-N N-methylcyclohexylamine Natural products CN1CCCCC1 PAMIQIKDUOTOBW-UHFFFAOYSA-N 0.000 claims description 8
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 5
- 230000009471 action Effects 0.000 claims description 3
- QVYARBLCAHCSFJ-UHFFFAOYSA-N butane-1,1-diamine Chemical compound CCCC(N)N QVYARBLCAHCSFJ-UHFFFAOYSA-N 0.000 claims description 3
- 238000005119 centrifugation Methods 0.000 claims description 3
- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 238000005261 decarburization Methods 0.000 claims description 3
- DYUWTXWIYMHBQS-UHFFFAOYSA-N n-prop-2-enylprop-2-en-1-amine Chemical compound C=CCNCC=C DYUWTXWIYMHBQS-UHFFFAOYSA-N 0.000 claims description 3
- 230000000630 rising effect Effects 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 2
- 239000000243 solution Substances 0.000 claims 20
- -1 alcohol Amine Chemical class 0.000 claims 1
- 239000007864 aqueous solution Substances 0.000 claims 1
- 230000018044 dehydration Effects 0.000 claims 1
- 238000006297 dehydration reaction Methods 0.000 claims 1
- 238000000746 purification Methods 0.000 claims 1
- 238000005516 engineering process Methods 0.000 abstract description 19
- 238000005265 energy consumption Methods 0.000 abstract description 14
- 238000002485 combustion reaction Methods 0.000 abstract description 13
- 239000000498 cooling water Substances 0.000 abstract description 9
- 230000000694 effects Effects 0.000 abstract description 2
- 239000012071 phase Substances 0.000 description 15
- 230000008569 process Effects 0.000 description 8
- 239000007791 liquid phase Substances 0.000 description 7
- 239000002904 solvent Substances 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 238000003795 desorption Methods 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 3
- 229910002090 carbon oxide Inorganic materials 0.000 description 3
- 239000002803 fossil fuel Substances 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000006210 lotion Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- WGYKZJWCGVVSQN-UHFFFAOYSA-N propylamine Chemical compound CCCN WGYKZJWCGVVSQN-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- 101001039157 Homo sapiens Leucine-rich repeat-containing protein 25 Proteins 0.000 description 1
- 102100040695 Leucine-rich repeat-containing protein 25 Human genes 0.000 description 1
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 1
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 150000001993 dienes Chemical class 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- QHJABUZHRJTCAR-UHFFFAOYSA-N n'-methylpropane-1,3-diamine Chemical compound CNCCCN QHJABUZHRJTCAR-UHFFFAOYSA-N 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 239000012074 organic phase Substances 0.000 description 1
- 238000005504 petroleum refining Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000005303 weighing Methods 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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/50—Combinations of absorbents
- B01D2252/504—Mixtures of two or more absorbents
-
- 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
The invention discloses a kind of rich solution multi-stage heat exchanger type carbon dioxide capture system and techniques, it solves post-combustion capture CO in the prior art2Technology has that regeneration energy consumption is high, the big investment of regenerator volume is high, has the effect of reducing steam consumption and cooling water flow, the trapping cost for reducing carbon dioxide；Its technical solution is：Including absorption tower, water scrubber, regenerator, alkanolamine solution of the absorption tower inner containment as absorbent, absorption tower connects multistage Liquid liquid Separation device by rich solution pump, and forming circuit is connect with absorption tower per level-one Liquid liquid Separation device；Water scrubber is used to absorb the purifying smoke being discharged at the top of water scrubber and carries out foam removal；Regenerator is connected by heat exchanger with multistage Liquid liquid Separation device, and the bottom connection reboiler of regenerator, material in reboiler expanded by heating to vaporizing and be back in regenerator；The top of regenerator connects gas-liquid separator by heat exchanger, and gas-liquid separator connect forming circuit with regenerator by water cooler.
Description
Technical field
The present invention relates to object gas technical field more particularly to a kind of rich solution multi-stage heat exchanger type two are removed from source gas
Carbonoxide trapping system and technique.
Background technology
Global climate change is the problem of current international community is concerned, combustion of fossil fuel power generation process generate two
Carbonoxide is the main reason for causing atmospheric carbon dioxide levels to increase.Since fossil energy production technology is reliable, at low cost,
Current is more than that 80% energy demand both is from fossil fuel in the world.Therefore, one of international community's response environment crisis
Main striving direction is exactly that the discharge of carbon dioxide is reduced while ensuring that global economy is maintained to increase.It is great to cope with this
Challenge, the technology that CO2 emission is controlled from fuel combustion source are just of increasing concern.
The discharge of carbon dioxide in world wide is reduced, and meets the energy demands such as fossil fuel simultaneously, it is meant that carbon
It is highly desirable to capture and seal up for safekeeping (CCS) technology.With the development of technology, the factory that will look for novelty of legislative branch is ready for carbon
Trapping, and a determining date, new CCS equipment need to be equipped.Once CCS technologies are feasible, existing works by full proof
The CCS equipment of factory very likely needs to be renovated.Emission trading and CO2Capturing also will be as in existing and new factory's peace
Fill the most important driving force of CCS equipment.
Collecting carbonic anhydride and Plugging Technology Applied (CCS) are then to reduce the most direct effective method of greenhouse gas emission, at present
It can be used for power plant CO there are three types of main Trapping ways2Trapping, is pre-combustion capture, post-combustion capture and oxygen-enriched combusting respectively.
Pre-combustion capture is mainly used in IGCC system, the high-pressure oxygen-enriched gasification of coal is become coal gas, after Water gas shift/WGS
Generate CO2And H2, wherein gas pressure and CO2Concentration is all very high, it is easy to CO2It is trapped.The advantages of technology is trapping
System is small, low energy consumption, has prodigious potentiality in efficiency and to the control aspect of pollutant, therefore receive significant attention.However,
IGCC generation technologies are still faced with the problems such as cost of investment is too high, reliability need to be improved.Oxygen-enriched combusting is coal-fired using tradition
The techniqueflow in power station, but by oxygenerating technology, oxygen is isolated from air, the oxygen using high concentration and the part drawn back
The mixed gas of flue gas substitutes air, there is the CO of high concentration in the flue gas obtained in this way2Gas can be handled directly
With seal up for safekeeping.The biggest problem that the technology path faces be oxygenerating technology investment and energy consumption it is too high, be much to seek now a kind of honest and clean
The active technology of valence low consumption.Post-combustion capture traps CO in the flue gas of burning and exhausting2, post-combustion capture technology is suitable for appointing
A kind of what thermal power plant, can be applied to new power plant can also be to original power plant's upgrading.Technique also relative maturity,
It is technology most potential in the following emission reduction market.
Post-combustion capture CO 2 technology is the most suitable commercialization skill that carbon dioxide is trapped from fuel power plant
Art has fabulous application in natural gas processing and petroleum refining industry at present.Currently, common chemical absorption solvents are organic
Amine, but the features such as its energy consumption is big, of high cost seriously limit its large-scale application.In order to reduce energy consumption, make post-combustion capture skill
Art obtains commercial applications in the power plant of different scales, it is also necessary to develop the combustion of high reliability, low input and low running cost
Trapping technique after burning.
Invention content
For overcome the deficiencies in the prior art, the present invention provides a kind of rich solution multi-stage heat exchanger type carbon dioxide capture systems
And technique, have the effect of reducing steam consumption and cooling water flow, the trapping cost for reducing carbon dioxide.
The present invention uses following technical proposals：
A kind of rich solution multi-stage heat exchanger type carbon dioxide capture system, including：
Absorption tower, alkanolamine solution of the inner containment as absorbent；Absorption tower connects multistage liquid liquid point by rich solution pump
From device, forming circuit is connect with absorption tower per level-one Liquid liquid Separation device；
Water scrubber, for absorbing the purifying smoke being discharged at the top of water scrubber and carrying out foam removal；
Regenerator is connected by heat exchanger with multistage Liquid liquid Separation device, and the bottom connection of the regenerator is boiled again
Device, material in reboiler expanded by heating to vaporizing and be back in regenerator；
The top of the regenerator connects gas-liquid separator by heat exchanger, and gas-liquid separator passes through water cooler and regeneration
Tower connection forming circuit.
Further, the multistage Liquid liquid Separation device includes sequentially connected level-one Liquid liquid Separation device, two level liquid liquid
Separator and three-level Liquid liquid Separation device.
Further, the level-one Liquid liquid Separation device and absorption tower side middle and lower part entrance, two level Liquid liquid Separation device
With absorption tower side centre entrance, three-level Liquid liquid Separation device and absorption tower side surface upper part entrance.
A kind of rich solution multi-stage heat exchanger type collecting carbonic anhydride technique, process are：
The rich solution flowed out from absorb the bottom of the tower flows into level-one Liquid liquid Separation device, and level-one separation is realized by standing, wherein
A carbon dioxide loaded amount low phase in upper layer is sent into absorption tower by absorption tower middle and lower part entrance and is recycled, and lower layer's carbon dioxide is negative
The high phase of carrying capacity enters two level Liquid liquid Separation device and carries out standing separation；
The low phase of carbon dioxide loaded amount is sent into absorption to two level Liquid liquid Separation device by absorption tower centre entrance at the middle and upper levels
Tower recycles, and the high phase of lower layer's carbon dioxide loaded amount enters three-level Liquid liquid Separation device, and is carried out by centrifugation
Separation；
The low phase of carbon dioxide loaded amount is sent into absorption to three-level Liquid liquid Separation device by absorption tower upper entrance at the middle and upper levels
Tower recycles, and the high phase of lower layer's carbon dioxide loaded amount enters regenerator and carries out carbon dioxide.
Further, the flue gas after dehydrated cooled flows under fan action into absorption tower from bottom to top, from absorption
The flue gas of tower top infeed absorbing liquid, the absorbing liquid and rising forms counter current contacting by carbon dioxide eliminating.
Further, purified decarburization flue gas is discharged at the top of absorption tower, foam removal is carried out into water scrubber, after foam removal
Purified gas empties.
Further, the alkanolamine solution includes N, N- dimethyl cyclohexyl amines, N-methylcyclohexylamine, triethylamine, diene
Propyl amine, N, N- diethyl ethylene diamines, Isosorbide-5-Nitrae butanediamine, N- methyl-1s, 3- propane diamine, N-methylcyclohexylamine, piperazine.
Further, into the rich liquid stream of regenerator rich or poor liquid is carried out in heat exchanger and the lean solution of regeneration tower bottom outflow
Heat exchange carries out rich solution using the waste heat of lean solution after regeneration to be heated to set temperature.
Further, after the water cooled device of lean solution after heat exchange is cooled to set temperature, and through gas-liquid separator separates two
After the excessive water that liquid water after carbonoxide, the part from water scrubber recycle collects at current divider, it is pumped into absorption tower, follows
Ring is as absorbing liquid.
Further, the carbon dioxide and steam mixture being discharged at the top of regenerator imported into water cooling in water cooler, temperature
It spends to import in gas-liquid separator after being reduced to set temperature and carries out gas-liquid separation；The carbon dioxide gas isolated enters subsequent
Compression processing program.
Further, tower bottom is being regenerated by low-pressure steam after reboiler and the heat exchange of regenerator bottom rich solution, rich solution is added
Carbon dioxide gas is resolved out after heat to set temperature, is discharged via at the top of regenerator, parses the lean solution after carbon dioxide
Via regeneration tower bottom discharge.
Compared with prior art, the beneficial effects of the invention are as follows：
(1) present invention uses chemical solvent absorption method, being capable of selective absorbing mixing using alkanolamine solution as absorbent
CO in flue gas2, absorb CO2Rich solution afterwards enters separator, and the separation for realizing liquid-liquid diphase, wherein CO are stood by three-level2It is negative
The low phase of carrying capacity is sent back to absorption tower and recycles, CO2The high phase of load capacity is admitted to regenerator and carries out parsing regeneration；With
Common process is compared, which can reduce the capacity of stripping liquid, and the sensible heat of water temperature evaporation and gasification are latent when reducing desorption and regeneration
Heat effectively reduces parsing energy consumption；Meanwhile reducing lyosoption and being recycled in whole system, reduce the power consumption of pump；
(2) present invention increases liquid phase separating device, compares traditional CO2Trapping technique can reduce steam consumption, drop
Low cooling water flow, makes CO2Trapping cost is greatly reduced.
Description of the drawings
The accompanying drawings which form a part of this application are used for providing further understanding of the present application, and the application's shows
Meaning property embodiment and its explanation do not constitute the improper restriction to the application for explaining the application.
Fig. 1 is carbon dioxide capture system figure of the present invention；
Wherein, the absorption towers 1-, 2- water scrubbers, 3- rich solution pumps, 4- level-one Liquid liquid Separation devices, 5- heat exchangers I, 6- boil again
Device, 7- regenerators, 8- heat exchangers II, 9- gas-liquid separator, 10- two level Liquid liquid Separation devices, 11- three-level Liquid liquid Separations dress
It sets.
Specific implementation mode
It is noted that following detailed description is all illustrative, it is intended to provide further instruction to the application.Unless another
It indicates, all technical and scientific terms used herein has usual with the application person of an ordinary skill in the technical field
The identical meanings of understanding.
It should be noted that term used herein above is merely to describe specific implementation mode, and be not intended to restricted root
According to the illustrative embodiments of the application.As used herein, unless the context clearly indicates otherwise, otherwise singulative
It is also intended to include plural form, additionally, it should be understood that, when in the present specification using term "comprising" and/or " packet
Include " when, indicate existing characteristics, step, operation, device, component and/or combination thereof.
In the present invention, unless otherwise instructed, " rich solution ", " rich solvent " refer to the CO for absorbing a large amount of targets2Gas
Liquid." lean solution ", " lean solvent " refer to having parsed largely or entirely CO2The liquid of gas.
As background technology is introduced, post-combustion capture CO exists in the prior art2Regeneration energy consumption height existing for technology,
The high deficiency of the big investment of regenerator volume, in order to solve technical problem as above, present applicant proposes a kind of rich solution multi-stage heat exchangers
Type carbon dioxide capture system and technique.
In a kind of typical embodiment of the application, as shown in Figure 1, providing a kind of rich solution multi-stage heat exchanger type titanium dioxide
Carbon trapping system, including absorption tower 1, water scrubber 2, regenerator 7, multistage Liquid liquid Separation device, gas-liquid separator 9, reboiler 6,
Heat exchanger I5, heat exchanger II8.
The multistage Liquid liquid Separation device includes three-level, i.e. level-one Liquid liquid Separation device 4, two level Liquid liquid Separation device 10 altogether
With three-level Liquid liquid Separation device 11.
Absorption tower 1, alkanolamine solution of the inner containment as absorbent, alkanolamine solution include N, N- dimethyl cyclohexyl amines
(DMCA), N-methylcyclohexylamine (MCA), triethylamine (TEA), diallylamine (DAA), N, N- diethyl ethylene diamines
(DEEA), Isosorbide-5-Nitrae butanediamine (BDA), N- methyl-1,3- propane diamine (MAPA), N-methylcyclohexylamine (MCA), piperazine (PZ).
Absorption tower 1 can use plate column, bubble absorbing tower, the stirring bubbling of gas in the liquid phase with bubble shape dispersion
Absorption tower；Or liquid disperses injector, Venturi tube, spray tower in the gas phase with droplet-like；Or liquid is with membranaceous movement
The packed absorber and film-falling absorption tower contacted with gas phase.
In absorption tower 1 type of flow of gas-liquid two-phase can adverse current also can cocurrent, preferably reflux type, i.e., absorbent with
Tower top addition flows from above to below, and is contacted with the source gas flowed from bottom to top, and the liquid for absorbing absorbent is discharged from bottom of tower,
Purified gas is discharged from tower top.
Absorption tower 1 connects multistage Liquid liquid Separation device by rich solution pump, is connect with absorption tower 1 per level-one Liquid liquid Separation device
Forming circuit；The level-one Liquid liquid Separation device 4 and 1 side middle and lower part entrance of absorption tower, two level Liquid liquid Separation device 10 and suction
Receive 1 side centre entrance of tower, three-level Liquid liquid Separation device 11 and 1 side surface upper part entrance of absorption tower.
Water scrubber 2 is used to carry out foam removal to the purifying smoke that absorption tower top row goes out, since absorbing liquid has higher steam
Pressure, in order to reduce absorbing liquid with flue gas take out of and cause absorbing liquid lose and atmosphere pollution, water scrubber 2 can have both cycle washing
With demisting, the function of foam removal.Meanwhile the water lotion used in water scrubber 2 is usually clean water, can recycle, also may be used
It is supplied to after absorption tower is collected as absorbing liquid or with the part of rich liquid stream using to isolate a part and is supplied to regeneration overhead, the shunting
A part of water lotion out can be used for adjusting the flow distribution in whole system.
Regenerator 7 is the device for making CO2 parse wherein by high-temperature vapour the rich solvent for absorbing CO2, is introduced again
It is 130~150 DEG C that steam stripped low-pressure steam temperature is carried out in raw tower 7；Regenerator 7 passes through heat exchanger I5 and multistage Liquid liquid Separation
Device is connected, and the bottom of the regenerator 7 connects reboiler 6, material in reboiler 6 expanded by heating to vaporizing and be back to
In regenerator 7.
By heat exchanger II8 connections gas-liquid separator 9, gas-liquid separator 9 mainly will again at the top of the regenerator 7
The high-temperature vapour mixture cooling that 7 top of raw tower generates, makes water condensation get off, with CO2Gas detaches；Gas-liquid separator 9 passes through
Water cooler connect forming circuit with regenerator 7.
Use the technical process of rich solution multi-stage heat exchanger type carbon dioxide capture system for：
The trapping technique can be applied to the CO in the flue gas of thermal power plant burning and exhausting2Trapping；This is from flue gas
Unstripped gas temperature is 50 DEG C, and raw gas pressure 0.03MPa, unstripped gas group becomes：CO2For 51.95v/v%, H2For 19.74v/
V%, CO 9.71v/v%, CH4For 16.09v/v%, H2O is 0.87v/v%, N2It is with volume basis for 1.64v/v%
Content meter.
Under the action of wind turbine, above-mentioned raw materials gas after dehydrated cooled (35 DEG C of temperature) by absorption tower reservoir liquid level on
Into absorption tower, flow from bottom to top.Absorbing liquid (flow 84m is fed from 1 top of absorption tower3/ h, 40 DEG C of temperature, at being grouped as：
CO2The 30wt% liquid liquid phases that load capacity is 0.16mol/mol become solution), counter current contacting is formed with the flue gas of rising, makes CO2It is able to
Removing；Purified decarburization flue gas goes out from absorption tower top row, and foam removal is carried out into water scrubber 2, the purified gas emptying after foam removal.
1 middle part of absorption tower is gas-liquid contact part, this part mainly strengthens gas-liquid contact by filler, reinforces absorbing liquid
To CO2Absorption, generally arrange gas-liquid distributor in tower, enable absorbing liquid evenly into filler；1 bottom of absorption tower is to absorb
Liquid storage tank, absorbs CO2Liquid (be known as rich solution) be stored in the region.
The rich solution of 1 bottom of absorption tower outflow first realizes level-one separation by level-one Liquid liquid Separation device 4 by standing, at the middle and upper levels
The low phase of CO2 load capacity by absorption tower middle and lower part entrance be sent into absorption tower recycled, lower layer's CO2 load capacity it is high one
Mutually enter two level Liquid liquid Separation device 10 carry out standing separation, two level Liquid liquid Separation device 10 at the middle and upper levels CO2 load capacity it is low one
It is mutually sent into absorption tower 1 by 1 centre entrance of absorption tower to be recycled, the high phase of lower layer's CO2 load capacity enters three-level liquid liquid
Separator 11, is detached by centrifugation.
The low phase of CO2 load capacity is sent into absorption tower 1 to three-level Liquid liquid Separation device 11 by 1 upper entrance of absorption tower at the middle and upper levels
It is recycled, the high phase of lower layer's CO2 load capacity enters through rich or poor liquid heat exchanger I5 and enters the progress of regenerator 7 CO2
Desorption；Become separation 11 by three-level liquid liquid phase, the rich solution CO2 load capacity for eventually entering into regenerator 7 is big, and flow is reduced, energy saving
Regenerate vapor volume, while also power saving consumption and cooling water amount.
Into rich liquid stream (the flow 58m of regenerator 73/ h, 58 DEG C, CO2Load capacity is the solvent of 0.63mol/mol) in heat
The lean solution of exchanger I5 and 7 bottom of regenerator outflow carries out rich or poor liquid heat exchange, using the lean solution after regeneration waste heat to rich solution into
Row is heated to 83 DEG C, to reduce steam consumption when rich solution regeneration, while also reaching the mesh of cooling regeneration lean solution (to 67 DEG C)
's.
After the water cooled device of lean solution after heat exchange is cooled to 40 DEG C, CO is detached with from gas-liquid separator 92Liquid afterwards
After the excessive water that water, the part from water scrubber 2 recycle collects at current divider, it is pumped into absorption tower 1, cycle is as absorption
Liquid.Absorbing liquid cyclic constitutes continuous absorption and parsing CO2Technical process.
The CO gone out from 7 top row of regenerator2And steam mixture (123 DEG C of temperature, 4.32 ton hour of flow) imported into water cooling
Device water cooling, temperature are further decreased to 85 DEG C, are then directed into gas-liquid separator 9, carry out gas-liquid separation, the CO isolated2
Gas enters subsequent compression processing program.
At 7 bottom of regenerator by low-pressure steam (135 DEG C of low-pressure steam, 215.1 ton hours) through reboiler 6 and 7 bottom of regenerator
After rich solution heat exchange, rich solution is heated to 122 DEG C, CO2Gas is resolved out to be gone out via 7 top row of regenerator, and CO is parsed2Afterwards poor
Liquid (flow 76m3/ h, 122 DEG C) via regenerator bottom be discharged.
Cooling water flow, power consumption, steam consumption that present embodiment uses are counted, the method for statistics is to survey
Cooling water always makes in the complete technological process of amount one (absorb how many cubes of flue gas or carry out absorption how long)
The supply amount of dosage, motor (pump) power consumption, regenerator bottom low-pressure steam.
The result of statistics is listed in the table below respectively in 1~table 3.
Table 1：The comparison of difference trapping technique steam energy consumption
Table 2：Comparison of the Different Optimization process to cooling water flow
| Inlet temperature (DEG C) | Outlet temperature (DEG C) | Flow (ton hour) | |
| Tradition trapping mold technique | 30 | 40 | 68.86 |
| Liquid liquid phase becomes technique | 30 | 40 | 49.42 |
Table 3：Comparison of the Different Optimization process to wind turbine and pump power consumption
As it can be seen from table 1 the CO of the application2Trap technique and traditional CO2Trapping technique is compared, and is regenerated to solution
The consumption of steam has and significantly reduces, and reaches as high as 41.3%.
From table 2 it can be seen that the CO of the application2Trap technique and traditional CO2Trapping technique is compared, cooling water flow
Also having significantly reduces, and reaches as high as 28.2%.
From table 3 it can be seen that the CO of the application2Trapping technique increasingly complex is due to being detached by multistage centrifugal etc.
System, power consumption slightly improve, and increase by 14.7%.But consider, liquid liquid phase becomes CO2Trap total energy consumption, object of the technique to system
Consumption is optimized, and reduces CO2Trap cost.
In traditional post combustion carbon dioxide trapping system, main energy consumption comes from the stripping of production supply regenerator
The energy consumption of steam wherein regenerator is discharged in the steam mixture entrainment heat after stripping, and has been resolved the poor molten of CO2 gases
Agent be also required to it is cooling after can just be supplied to absorption tower, present in a large amount of heat waste.
The application increases liquid phase separating device, compares traditional CO2 trappings technique, can reduce steam consumption, reduce
Cooling water flow makes CO2 trappings cost be greatly reduced.
The application mainly utilizes multi-stage heat exchanger technique, so that system thermal is comprehensively utilized, greatly reduces system energy consumption；
And using systems such as washing tail gas, gas-liquid separations, the solution in tail gas is fully recycled；And keep the water of entire trapping system flat
Weighing apparatus reduces the consumption of solution and water, to solve CO after existing burning2The problem of high energy consumption and high cost of trapping.With it is normal
Rule technique is compared, which can reduce the capacity of stripping liquid, the sensible heat and gasification latent heat of water temperature evaporation when reducing desorption and regeneration,
Effectively reduce parsing energy consumption；Meanwhile reducing lyosoption and being recycled in whole system, reduce the power consumption of pump.
Since the organic phase desorbed can further extract the organic amine in rich solution, desorption reaction balance is promoted to move to right,
Make CO2More quick release comes out, and reduces desorption temperature.
The foregoing is merely the preferred embodiments of the application, are not intended to limit this application, for the skill of this field
For art personnel, the application can have various modifications and variations.Within the spirit and principles of this application, any made by repair
Change, equivalent replacement, improvement etc., should be included within the protection domain of the application.
Claims (10)
1. a kind of rich solution multi-stage heat exchanger type carbon dioxide capture system, which is characterized in that including：
Absorption tower, alkanolamine solution of the inner containment as absorbent；Absorption tower connects multistage Liquid liquid Separation dress by rich solution pump
It sets, forming circuit is connect with absorption tower per level-one Liquid liquid Separation device；
Water scrubber, for absorbing the purifying smoke being discharged at the top of water scrubber and carrying out foam removal；
Regenerator is connected by heat exchanger with multistage Liquid liquid Separation device, and the bottom of the regenerator connects reboiler, object
Material in reboiler expanded by heating to vaporizing and be back in regenerator；
The top of the regenerator connects gas-liquid separator by heat exchanger, and gas-liquid separator is connected by water cooler and regenerator
Connect forming circuit.
2. a kind of rich solution multi-stage heat exchanger type carbon dioxide capture system according to claim 1, which is characterized in that described more
Grade Liquid liquid Separation device includes sequentially connected level-one Liquid liquid Separation device, two level Liquid liquid Separation device and three-level Liquid liquid Separation dress
It sets.
3. a kind of rich solution multi-stage heat exchanger type carbon dioxide capture system according to claim 2, which is characterized in that described one
Grade Liquid liquid Separation device and absorption tower side middle and lower part entrance, two level Liquid liquid Separation device and absorption tower side centre entrance, three
Grade Liquid liquid Separation device and absorption tower side surface upper part entrance.
4. a kind of rich solution multi-stage heat exchanger type carbon dioxide capture system according to claim 1, which is characterized in that the alcohol
Amine aqueous solution includes N, N- dimethyl cyclohexyl amines, N-methylcyclohexylamine, triethylamine, diallylamine, N, N- diethyl ethylene diamines,
Isosorbide-5-Nitrae butanediamine, N- methyl-1s, 3- propane diamine, N-methylcyclohexylamine, piperazine.
5. a kind of rich solution multi-stage heat exchanger type collecting carbonic anhydride technique, which is characterized in that using as described in claim 1-3 is any
Trapping system, from absorb the bottom of the tower flow out rich solution flow into level-one Liquid liquid Separation device, by standing realize level-one separation,
The low phase of carbon dioxide loaded amount is sent into absorption tower by absorption tower middle and lower part entrance and is recycled at the middle and upper levels, lower layer's carbon dioxide
The high phase of load capacity enters two level Liquid liquid Separation device and carries out standing separation；
Two level Liquid liquid Separation device at the middle and upper levels by absorption tower centre entrance feeding absorption tower followed by the low phase of carbon dioxide loaded amount
Ring utilizes, and the high phase of lower layer's carbon dioxide loaded amount enters three-level Liquid liquid Separation device, and is detached by centrifugation；
Three-level Liquid liquid Separation device at the middle and upper levels by absorption tower upper entrance feeding absorption tower followed by the low phase of carbon dioxide loaded amount
Ring utilize, lower layer's carbon dioxide loaded amount it is high one communicate over-heat-exchanger enter regenerator carry out carbon dioxide.
6. a kind of rich solution multi-stage heat exchanger type collecting carbonic anhydride technique according to claim 5, which is characterized in that through dehydration
Flue gas after cooling flows under fan action into absorption tower from bottom to top, and absorbing liquid, the suction are fed from absorption tower top
The flue gas for receiving liquid and rising forms counter current contacting by carbon dioxide eliminating.
7. a kind of rich solution multi-stage heat exchanger type collecting carbonic anhydride technique according to claim 6, which is characterized in that after purification
Decarburization flue gas be discharged at the top of the absorption tower, carry out foam removal into water scrubber, the purified gas emptying after foam removal.
8. a kind of rich solution multi-stage heat exchanger type collecting carbonic anhydride technique according to claim 5, which is characterized in that enter again
The rich liquid stream of raw tower carries out rich or poor liquid heat exchange in heat exchanger and the lean solution of regeneration tower bottom outflow, utilizes lean solution after regeneration
Waste heat carries out rich solution to be heated to set temperature.
9. a kind of rich solution multi-stage heat exchanger type collecting carbonic anhydride technique according to claim 8, which is characterized in that heat exchange
After the water cooled device of lean solution afterwards is cooled to set temperature, with after gas-liquid separator separates carbon dioxide liquid water, come from water
Wash tower part cycle excessive water collect at current divider after, be pumped into absorption tower, cycle be used as absorbing liquid.
10. a kind of rich solution multi-stage heat exchanger type collecting carbonic anhydride technique according to claim 8, which is characterized in that from again
The carbon dioxide and steam mixture of raw top of tower discharge imported into water cooling in water cooler, and temperature imports after being reduced to set temperature
Gas-liquid separation is carried out in gas-liquid separator；The carbon dioxide gas isolated enters subsequent compression processing program；
Tower bottom is being regenerated by low-pressure steam after reboiler and the heat exchange of regenerator bottom rich solution, after rich solution is heated to set temperature
Carbon dioxide gas is resolved out, is discharged via at the top of regenerator, parses the lean solution after carbon dioxide via regeneration tower bottom
Discharge.
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Application publication date: 20180817 |