CN105268283B - It is a kind of to combine the collecting carbonic anhydride and compression handling process for absorbing - Google Patents
It is a kind of to combine the collecting carbonic anhydride and compression handling process for absorbing Download PDFInfo
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- CN105268283B CN105268283B CN201510628118.3A CN201510628118A CN105268283B CN 105268283 B CN105268283 B CN 105268283B CN 201510628118 A CN201510628118 A CN 201510628118A CN 105268283 B CN105268283 B CN 105268283B
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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
- 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
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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
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
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Abstract
Combine the collecting carbonic anhydride for absorbing and compression handling process the present invention relates to a kind of, belong to decarburization and carbon dioxide discharge-reduction field.Combine two methods of Physical Absorption and chemical absorbing in technique, high pressure presses desorption in absorbing, it is intended to tackle high efficiency low energy consumption decarburization technique problem.The technique is：After carbon containing air-flow enters physics trapping technique desulfurization, first through Physical Absorption tower and the most of carbon dioxide of attached technique removing；Enter back into chemistry trapping technique removing residual carbon dioxide.After sulfur-bearing rich solution regenerates through desulfurization regeneration, carbon containing physical absorbent rich solution through multistage flash evaporation, Physical Absorption tower is returned respectively.Chemical absorbent rich solution returns to chemical absorbing tower through thermal desorption regeneration.The carbon dioxide that flash tank is discharged with desorber is through multi-stage compression to the condition of burying.In process system, heat is reclaimed using heat exchanger, and work(is reclaimed using expanding machine.Carbon capture rate of the present invention is high, energy consumption is low, carbon trapping and the compression treatment of the carbon dioxide enriched air-flow of suitable extensive high pressure.
Description
Technical field
The invention belongs to decarburization and carbon dioxide discharge-reduction technical field, it is adaptable to which the mesohigh of industrial flow is carbon dioxide enriched
The carbonization treatment or collecting carbonic anhydride of air-flow and the carbon dioxide compression treatment to reach storage condition, and in particular to one
Plant collecting carbonic anhydride and compression handling process that joint absorbs.
Background technology
Energy resource structure of the China based on coal will also be continued for an extended period of time, and rapid economic development causes a large amount of titanium dioxides
Carbon (CO2) discharge.Sustainable economic development is realized, propulsion CO is needed badly2Trapping and the exploitation of Plugging Technology Applied and application.
Carbon Trapping ways mainly have three kinds：Carbon trapping, oxygen-enriched combusting and post combustion carbon capture before burning.From technological investment,
For the aspects such as carbon trapping energy consumption and efficiency, carbon trapping is preferably to select before burning, is especially suitable for cleaning coal utilization technology, example
Such as integrated gasification combined cycle plants (IGCC) power plant.It is characterized in containing CO2The pressure and CO of air-flow2Concentration is all very high, easily implements
Carbon is trapped.This high pressure richness CO2Air-flow, is also common in Chemical Manufacture, for example, synthesize ammonia and synthesizing methanol.
Absorption process is most ripe at present, and wide variety of extensive CO2Isolation technics.According to principle of absorption and absorbent
Difference, absorption process can be divided into Physical Absorption method, chemical absorption method.Physical absorbent is to CO2Pressure is more sensitive, is adapted to high pressure high
Concentration C O2The absorption and separation of air-flow, and chemical absorbent is then adapted to low pressure low concentration CO2The absorption and separation of air-flow.It is currently based on thing
The mainstream technology of reason absorption exploitation has Rectisol techniques (absorbent is methyl alcohol), Purisol techniques, and (absorbent is N- methyl pyrroles
Pyrrolidone, NMP), (absorbent is polyethylene glycol two for Fluor techniques (absorbent is propene carbonate, PC) and Selexol techniques
Methyl ether, DEPG).Chemical absorbing is mainly hydramine method, and conventional absorbent has MEA (MEA), 2- amido -2- methyl isophthalic acids-the third
Alcohol (AMP), diethanol amine (DEA) and N methyldiethanol amine (MDEA) etc.；Ammonia absorption is also used.
For high pressure richness CO2The carbon trapping of air-flow, it is current main using Physical Absorption method.Although CO under high pressure2Inhaled in physics
Solubility is higher in receiving agent, but needs than relatively low absorption temperature, and carbon-drop rate requirement it is higher when need substantial amounts of absorbent.
CO2Desorption by vacuum flashing realize, CO after flash distillation2Pressure often for normal pressure is even lower, causes CO2The loss of pressure, and
After trapping, CO2Pressure need to be improved through multi-stage compression can be only achieved storage condition.Therefore excessively decompression means to compress energy consumption
Be substantially improved.This is little blind spot considered in current application and research, because CO2Seal up for safekeeping and do not closed extensively also
Note.
Chemical absorption method is usually used in the carbon trapping in flue gas and carbon-drop rate is high, but the regeneration energy consumption of thermal desorption is big.It is many
Researcher is devoted to the improvement of traditional process, and patent CN103961979A proposes a kind of chemical method CO of multi-stage diffluence regeneration2
Trapping technique, rich solution is divided into multiply, and the diverse location of desorber is entered after recovery lean solution heat energy, and regeneration is improve to a certain extent
Spend, reduce reboiler.Patent CN103463955A is based on tradition CO2Trapping technological process, integrates shunting desorption and heat
Pump rectification process, effectively utilizes and desorbs tower top steam latent heat.Patent CN103566712A is then driven using regeneration overhead gas waste heat
The mode that turbine generates electricity, reduces the energy consumption of reboiler.These corrective measures can to a certain extent reduce the energy of carbon trapping
Consumption, but because the original overall energy consumption of chemical absorption method is just high, work as CO2It is bigger needed for regeneration energy consumption when treating capacity is especially big, because
And the technique after improving can not also meet the extensive high pressure richness CO for the treatment of2The need for air-flow.
Therefore, the characteristics of present invention combines physics absorption process and chemical absorption method each, the two is combined and is caught in same carbon
Collection and compression handling process, play its advantage, avoid its shortcoming, by the recovery of heat energy and work(, realize the big rule of low energy consumption treatment
Mould high pressure richness CO2The effect of air-flow.By retrieval, not yet find and present patent application identical publication or other phases
Close document.
The content of the invention
It is an object of the invention to provide a kind of collecting carbonic anhydride and compression handling process, the process integration combined and absorb
Traditional Physical Absorption method and chemical absorption method CO2Trapping technique, mainly takes the strategy of high pressure absorption-middle pressure desorption, will
High pressure richness CO2The carbon trapping of air-flow is divided into two stages：The high-pressure high-concentration CO of starting2Physical Absorption and it is follow-up in force down
Concentration C O2Chemical absorbing, physics trapping technique and chemical trapping technique are corresponded to respectively.By process integration, and reclaim heat energy
And work(, reduce CO2Trapping and the energy consumption of compression, acquisition reach the CO of storage condition2(the usually liquid of 11MPa to 15MPa
CO2).Present invention process carbon capture rate is high, energy consumption is low, at the carbon trapping and compression of the carbon dioxide enriched air-flow of suitable extensive high pressure
Reason.
To achieve the above object, the technical solution of present invention use is：
It is a kind of to combine the collecting carbonic anhydride and compression treatment device for absorbing, it is characterised in that including desulfurizer, physics
Capturing device, chemical capturing device and carbon dioxide compression cooling device；The desulfurizer includes desulfurizing tower (1), first cold
But device (10), the first solution pump (9), first circulation air compressor (4), heater (2), the first flash tank (3) and hydrogen sulfide divide
From device (5), the tower top import of the desulfurizing tower (1) connects the outlet of the first cooler (10), the import of the first cooler (10)
Connect the outlet of the first solution pump (9), the bottom of towe import of tower top outlet connection physics absorption tower (7) of desulfurizing tower (1), desulfurizing tower
(1) outlet of bottom of towe import connection first circulation air compressor (4), bottom of towe outlet connection heater (2) of desulfurizing tower (1)
Import, the outlet of heater (2) connects the import of the first flash tank (3), and the top exit connection first of the first flash tank (3) is followed
The import of ring air compressor (4), the import of outlet at bottom connection hydrogen sulphide separator (5) of the first flash tank (3), hydrogen sulfide point
From the import of outlet at bottom connection First Heat Exchanger (6) of device (5)；The physics capturing device includes Physical Absorption tower (7), the
One heat exchanger (6), current divider (8), the first expanding machine (11), the second flash tank (12), the second expanding machine (16), the 3rd flash tank
(17), the second solution pump (18) and the second cooler (19), the tower top outlet connection First Heat Exchanger of the Physical Absorption tower (7)
(6) import, the import of bottom of towe outlet connection current divider (8) of Physical Absorption tower (7), the outlet of current divider (8) is divided into two-way,
Connect the import of the first solution pump (9) all the way, another road connects the import of the first expanding machine (11), the first expanding machine (11) go out
The import of mouth the second flash tank of connection (12), the top exit pipeline of the second flash tank (12) sets at least one cycle compressor
Machine and at least one cooler are connected with the bottom of towe import of Physical Absorption tower (7), the outlet at bottom connection of the second flash tank (12)
The import of the second expanding machine (16), the outlet of the second expanding machine (16) connects the import of the 3rd flash tank (17), the 3rd flash tank
(17) outlet at bottom connects the import of the second solution pump (18), and the outlet of the second solution pump (18) connects the second cooler (19)
Import, the second cooler (19) outlet connection physics absorption tower (7) tower top import, the hot logistics of First Heat Exchanger (6)
The centre inlet of outlet connection physics absorption tower (7)；The chemical capturing device includes chemical absorbing tower (24), the second heat exchanger
(25), desorber (26), the 4th flash tank (27), the 3rd solution pump (28), the 4th cooler (29), other at least one heat exchange
Device and at least one expanding machine, the cold stream outlet of First Heat Exchanger (6) connect at least one heat exchanger and at least one expansion
The bottom of towe inlet ductwork of machine (first heat exchanger, rear expanding machine are alternately placed) again with chemical absorbing tower (24) is connected, chemical absorbing tower
(24) import of bottom of towe outlet the second heat exchanger of connection (25), the cold stream outlet connection desorber of the second heat exchanger (25)
(26) tower top import, the tower top outlet of desorber (26) connects the import of the 4th flash tank (27), the bottom of towe of desorber (26)
The import of outlet the 3rd solution pump (28) of connection, the outlet of the 3rd solution pump (28) connects the import of the second heat exchanger (25), the
The hot stream outlet pipeline of two heat exchangers (25) connects import of at least one heat exchanger again with the 4th cooler (29) and is connected, the
The tower top import of outlet connection chemical absorbing tower (24) of four coolers (29)；The carbon dioxide compression cooling device is included extremely
Few four compressors and at least four coolers, the top exit of the 4th flash tank (27) connect at least one compressor and at least
One top exit of the cooler (first compressor, aftercooler are alternately placed) again with the 3rd flash tank (17) merges, after merging
Pipeline connect at least three compressors and three coolers (first compressor, aftercooler are alternately placed).
A kind of to combine the collecting carbonic anhydride and compression handling process for absorbing, system traps technique, chemistry trapping by physics
Technique and compression cooling technique joint are constituted, and associated form is：
1) physics trapping, desulfurization.Pretreated carbon dioxide containing air flow initially enters physics trapping technique, from desulfurizing tower
(1) bottom of towe charging, from bottom to top with Physical Absorption liquid counter current contacting, the hydrogen sulfide in air-flow is absorbed；The bottom of towe of desulfurizing tower (1)
After the heated device of discharge liquor (2) heating gas-liquid separation, the top discharge of the first flash tank (3) are carried out into the first flash tank (3)
Gas sends desulfurizing tower (1) bottom back to after being compressed through first circulation compressor (4)；The bottom discharge liquor of the first flash tank (3) enters sulphur
Change hydrogen separator (5), hydrogen sulfide is separated and leaves system from hydrogen sulphide separator (5)；The bottom row of hydrogen sulphide separator (5)
After going out liquid through First Heat Exchanger (6) recovery heat energy, Physical Absorption tower (7) is entered as absorbing liquid.
2) physics trapping, decarburization.Air-flow after desulfurization enters Physical Absorption tower (7) bottom of towe by desulfurizing tower (1) tower top, under
And upper and Physical Absorption liquid counter current contacting, more than 60% CO in air-flow2Absorbed, residual gas is from Physical Absorption tower (7) tower
Top row goes out, and chemical trapping technique is entered after being heated through First Heat Exchanger (6)；The bottom of towe discharge liquor of Physical Absorption tower (7) is through shunting
Device (8) is divided into two strands, and a stock-traders' know-how the first solution pump (9) and the first cooler (10) enter desulfurizing tower (1) tower top as physics afterwards
Absorbing liquid desulfurization, the desulfurization needed for this strand of uninterrupted of discharge liquor should be able to make the actual condition of desulfurizing tower (1) reach regulation will
Ask, another burst of discharge liquor enters after the first expanding machine (11) reclaims expansion work done delivers to the second flash tank (12)；Second dodges
The top discharge gas of steaming pot (12) passes sequentially through at least one recycle gas compressor and at least one cooler (first cycle compressor
Machine, aftercooler is alternately placed) after send Physical Absorption tower (7) bottom of towe back to, the bottom discharge liquor of the second flash tank (12) enters the
Two expanding machines (16), the 3rd flash tank (17) is delivered to after reclaiming expansion work done, is regenerated Physical Absorption liquid and is obtained CO2Gas
Body, CO2Gas is discharged from the 3rd flash tank (17) top, into carbon dioxide compression cooling device；3rd flash tank (17)
After bottom discharge liquor improves pressure and the second cooler (19) reduction temperature through the second solution pump (18), sent as Physical Absorption liquid
Return Physical Absorption tower (7) tower top.
3) chemistry trapping, decarburization.After the tower top discharge gas of Physical Absorption tower (7) is heated through First Heat Exchanger (6), then through extremely
After few heat exchanger recovery heat energy and at least one expanding machine recovery expansion work done (first heat exchanger, rear expanding machine, alternately
Place), deliver to the charging of chemical absorbing tower (24) bottom of towe, the chemical absorbing liquid counter current contacting for entering with tower top from bottom to top；Removing
CO2Purified gas chemically absorption tower (24) tower top discharge system；The bottom of towe discharge liquor of chemical absorbing tower (24) is through the second heat exchange
Regenerate chemical absorbing liquid and obtain CO into desorber (26) tower top after device (25) heating2Gas, the tower top of desorber (26)
Discharge gas enters the 4th flash tank (27), and the 4th flash tank (27) bottom discharge aqueous water simultaneously leaves system；4th flash tank
(27) top discharge CO2Gas, into carbon dioxide compression cooling device；The bottom of towe discharge liquor of desorber (26) flows through successively
Three solution pumps (28) improve pressure and the second heat exchanger (25) and reclaim heat energy, then with the exit flow of First Heat Exchanger (6) through extremely
A few heat exchanger reclaims heat energy, then by after the cooling of the 4th cooler (29), chemical absorbing being delivered to as chemical absorbing liquid
Tower (24) tower top.
4)CO2Compression cooling.The CO of the 4th flash tank (27) top discharge2Gas, through at least one compressor and at least one
After individual cooler (first compressor, aftercooler are alternately placed), CO2The temperature and pressure of gas and the 3rd flash tank (17) are pushed up
The CO of portion's discharge2Gas phase is same, two gangs of CO2After gas converges, pressure and at least three coolers are improved through at least three compressors
After reducing temperature (first compressor, aftercooler are alternately placed), discharge system.
The collecting carbonic anhydride that present invention joint absorbs and compression handling process, use multiple internal flows in process system
Heat exchanger reclaims heat energy, and work(is reclaimed using multiple expanding machines, and way of recycling is：
1) energy recovery.The tower top discharge gas of Physical Absorption tower (7) reclaims hydrogen sulphide separator by First Heat Exchanger (6)
(5) heat energy of bottom of towe discharge liquor；The bottom of towe discharge liquor of chemical absorbing tower (24) reclaims desorber by the second heat exchanger (25)
(26) heat energy of bottom of towe discharge liquor；Then the tower top of Physical Absorption tower (7) discharges qi leel not by least one heat exchanger to solution
The heat energy for inhaling tower (26) bottom of towe discharge liquor is further reclaimed.
2) work(is reclaimed.Larger one rich solution of flow of Physical Absorption tower (7) bottom of towe discharge, returns into the first expanding machine (11)
The second flash tank (12) is delivered to after receiving expansion work done, the bottom discharge liquor of the second flash tank (12) enters back into the second expanding machine
(16) expansion work done is reclaimed；After the tower top discharge gas of Physical Absorption tower (7) is heated continuously, at least one expanding machine
Reclaim expansion work done.
Physical absorbent described in present invention process can be any conventional absorbent, including but not limited to：
1-METHYLPYRROLIDONE (NMP), propene carbonate (PC) and NHD (DEPG) etc.；Described chemical absorbent can
To be the mixture of any conventional absorbents or various conventional absorbents, described conventional absorbents include but do not limit
In：MEA (MEA), 2- amidos -2- methyl isophthalic acids-propyl alcohol (AMP), diethanol amine (DEA) and N methyldiethanol amine
(MDEA) etc..Therefore the absorbent group of the selection comprising diversified forms of physical absorbent Yu chemical absorbent involved in the present invention
Conjunction mode.
The technique of physics trapping described in present invention process takes the mode of high pressure absorption-middle pressure desorption, i.e. CO2Physical Absorption
The operating pressure of tower (7) is 2~7MPa, the CO of the 3rd flash tank (17) outlet2Pressure is 0.5~1.5MPa；Chemistry trapping work
Skill take the mode that middle pressure absorptions-normal pressure is desorbed, i.e. the feed stream pressure of chemical absorbing tower (24) bottom of towe for 0.8~
1.5MPa, the operating pressure of desorber (26) is 0.1~0.3MPa.
Above is the main technical schemes of present invention process, are now explained further and are described as follows：
The bottom of towe discharge liquor of Physical Absorption tower (7) is divided into first strand of rich solution and second strand of rich solution, first strand through current divider (8)
Rich solution is used from tower top as hydrogen sulfide absorption liquid into desulfurizing tower (1), and its consumption should be less, and vulcanization in feeding gas is absorbed enough
Hydrogen (the desulfurization requirement needed for making the actual condition of desulfurizing tower (1) reach regulation), it is follow-up again to reduce physical absorbent
Raw energy consumption, cooling energy consumption and pump work.
Second flash tank (12) is set it is the non-CO in order to be carried in the tower bottom liquid of Physical Absorption tower (7)2Gas is separated,
Recycled back Physical Absorption tower (7) bottom of towe, therefore compression cooling circulating air (i.e. the top discharge gas of the second flash tank (12)) institute
The recycle gas compressor of use and the number of cooler should regard the pressure differential and temperature of the second flash tank (12) and Physical Absorption tower (7)
Degree is differed from and reasonable set.
Similarly, in the work(recovery scheme, the tower top of Physical Absorption tower (7) is discharged gas and is returned at least one expanding machine
Expansion work done is received, heat exchanger is set between each two expanding machine, reclaim the heat energy of the bottom of towe discharge liquor of desorber (25).Institute
The heat exchanger of use and the number of expanding machine should also set depending on the pressure differential between Physical Absorption tower (7) and chemical absorbing tower (24)
It is fixed.
Similarly, in CO2In compression cooling scheme, the CO of the 4th flash tank (27) top discharge in chemistry trapping technique2Gas
CO of the pressure less than the 3rd flash tank (17) top discharge in physics trapping technique2Gas, therefore by two gangs of CO2Gas mixing
Before, need that lowpressure stream stock first is compressed into the condition that cooling reaches high-pressure spray stock, the compressor for being used and cooler
Number should also regard two gangs of CO2The pressure and temperature difference of gas and set.Additionally, two gangs of CO2Gas enters compression bosher after converging
Skill, the compressor and the number of cooler for being used should also regard pressure and temperature of the 3rd flash tank (17) and storage condition between
Difference and set.
In chemistry trapping process portion, should also equip the supplement tank of chemical absorbent, including pure water supplement tank and alcohol
Chemical absorbent lean solution after the supplement tank of amine, with regeneration together enters chemical absorbing tower (24), to make up what thermal desorption was caused
Absorbent loses, and maintains the liquid-gas ratio in tower, ensures that operating mode is stable.
Brief description of the drawings
Accompanying drawing is a kind of process flow diagram for combining the collecting carbonic anhydride and compression handling process for absorbing of the present invention
Wherein, 1 is desulfurizing tower；2 is heater；3 is the first flash tank；4 is first circulation air compressor；5 is hydrogen sulfide
Separator；6 is First Heat Exchanger；7 is Physical Absorption tower；8 is current divider；9 is the first solution pump；10 is the first cooler；11
It is the first expanding machine；12 is the second flash tank；13 is second circulation air compressor；14 is the 3rd cooler；15 is the 3rd circulation
Air compressor；16 is the second expanding machine；17 is the 3rd flash tank；18 is the second solution pump；19 is the second cooler；20 is the 3rd
Heat exchanger；21 is the 3rd expanding machine；22 is the 4th heat exchanger；23 is the 4th expanding machine；24 is chemical absorbing tower；25 is second to change
Hot device；26 is desorber；27 is the 4th flash tank；28 is the 3rd solution pump；29 is the 4th cooler.
Specific embodiment
In order to the technical scheme for preferably illustrating feasibility of the invention, being taken can realize predetermined goal of the invention, knot
Accompanying drawing is closed, technique proposed by the present invention and specific embodiment are described in detail.It is to be understood that, following case study on implementation
It is illustrative and not restrictive, it is impossible to limit protection scope of the present invention with following case study on implementation.
Application field (the high pressure richness CO of present invention process2The carbon trapping of air-flow), set the bar of pretreated feeding gas
Part is：Pressure 4.0MPa, 38.0 DEG C of temperature, percentage by volume composition is hydrogen 58.4%, CO241.0%, hydrogen sulfide 0.6%,
Molar flow rate 1000kmol/h.Flow as shown in drawings is set up, present invention process trapping compression CO is calculated2Required energy consumption.Institute
It is NHD (DEPG) with physical absorbent, chemical absorbent is MEA (MEA).
First it is the desulfurized step of physics trapping technique.As shown in drawings, feeding gas initially enter desulfurizing tower (1) bottom of towe,
From bottom to top with absorb CO2DEPG counter current contactings, tower pressure be 4.0MPa, hydrogen sulfide by whole (more than 99.99%) absorb,
Sulfur-bearing rich solution is discharged from desulfurizing tower (1) bottom of towe, and heated device (2) is depressured after being warming up to 56 DEG C into the first flash tank (3)
0.2MPa gas-liquid separations, the whole hydrogen and a small amount of CO carried in sulfur-bearing rich solution2Discharged from the first flash tank (3) top, by the
Send desulfurizing tower (1) bottom of towe after one recycle gas compressor (4) compression back to, the first flash tank (3) bottom discharge liquor is divided into hydrogen sulfide
It is totally separated hydrogen sulfide and leaves system from device (5)；Hydrogen sulphide separator (5) bottom discharge liquor is cold through First Heat Exchanger (6)
But to 24 DEG C, into the middle part column plate charging of Physical Absorption tower (7).
Present invention process is made up of physics trapping technique and chemistry trapping process integration, and accordingly, two trap technique
CO2The total CO for adding and be technique of amount of collected2Amount of collected.Physics trapping technique herein is related to be caught respectively with chemistry trapping technique
How many CO collected2Allocation proportion problem, in the implementation case, the ratio is set as 4:1.It is noted, that because physics is inhaled
Receive and be adapted to high-pressure high-concentration CO2Separation, chemical absorbing is adapted to low pressure low concentration CO2Separation, so physics trapping process allocation
CO2Amount of collected should be greater than chemical trapping technique.In practical operation, 4:1 not necessarily optimal ratio, can be as needed
Adjustment.Additionally, the total carbon capture rate requirement of setting technique is more than 90%, then in the implementation case, physics trapping technique and change
Learning trapping technique need to trap the CO of acquisition2Molar flow respectively may be about 295kmol/h and 74kmol/h.
Enter Physical Absorption-desorption procedure after charging desulfurization.CO in the tower top discharge gas of desulfurizing tower (1)2Concentration is decreased slightly as
As little as about 40%, enter horizontal high voltage into physics trapping technique and absorb：From Physical Absorption tower (7) bottom of towe charging from bottom to top with DEPG
Solution counter current contacting, most of CO2Absorbed, Physical Absorption tower (7) tower pressure is 3.8MPa.The tower top row of Physical Absorption tower (7)
CO in outlet2Concentration about 17%, enters chemical trapping technique after being warming up to 20 DEG C through First Heat Exchanger (6).Physical Absorption tower (7)
Bottom of towe discharge liquor be divided into first strand of rich solution and second strand of rich solution through current divider (8), its mass flow ratio is 0.85：0.15, the
One rich solution temperature after the first solution pump (9) and the first cooler (10) is reduced to 0 DEG C, into the tower top conduct of desulfurizing tower (1)
Absorbing liquid desulfurization.Second strand of rich solution then carries out middle pressure desorption into physics trapping technique：The first expanding machine (11) is initially entered (to adopt
Use hydraulic turbine device) acting, pressure is reduced to 1.3MPa, then delivers to the second flash tank (12) and carry out constant pressure adiabatic flash, flows stock
The Hydrogen Separation of middle carrying is discharged from the second flash tank (12) top, successively through second circulation air compressor (13), the 3rd cooling
Send the bottom of towe of Physical Absorption tower (7) after device (14) and the compression of the 3rd recycle gas compressor (15) back to；Second flash tank (12) bottom
After discharge liquor enters the second expanding machine (16) (using hydraulic turbine device) acting, pressure is reduced to 0.54MPa, delivers to the 3rd flash distillation
Tank (17) constant pressure adiabatic flash, isolates the CO of 0.54MPa2Air-flow, molar flow about 295kmol/h, from the 3rd flash tank
(17) carbon dioxide compression cooling device is delivered at top.3rd flash tank (17) bottom discharge liquor is through the second solution pump (18) and
Two coolers (19) temperature is down to -4 DEG C, sends the tower top of Physical Absorption tower (7) back to as absorbing liquid.
Major part CO in feeding gas2After by Physical Absorption, physics trapping technique, air-flow pressure are left from First Heat Exchanger (6)
Power is 3.8MPa, into before chemical absorbing tower (24) (tower pressure is set as 1.0MPa), by two heat exchangers and two for setting
Individual expanding machine, reclaims the heat energy of the bottom of towe discharge liquor of desorber (26), and by expansion work.By the 3rd heat exchanger (20) and
After 3rd expanding machine (21), stream pressure is reduced to 1.8MPa, and after the 4th heat exchanger (22) and the 4th expanding machine (23), pressure
1.0MPa is reduced to, temperature is 20 DEG C.
Air-flow after acting enters chemical absorbing-desorption procedure.The characteristics of chemical absorbing is that middle pressure absorbs：1.0MPa's enters
Chemically absorption tower (24) bottom of towe charging of material gas, the MEA aqueous absorbents for entering with tower top from bottom to top (the wherein matter of MEA
Amount fraction reaches the requirement of carbon capture rate and (the total carbon capture rate of technique is set in the implementation case to set 32.5%) counter current contacting
>90%) purified gas temperature is 30 DEG C, chemically the tower top discharge system of absorption tower (24).The bottom of towe of chemical absorbing tower (24)
Discharge liquor is 52 DEG C, and desorber (26) tower top is entered after being heated to 86 DEG C through the second heat exchanger (25).Chemistry desorption the characteristics of be
Normal pressure is desorbed：The tower pressure that desorber (26) is set in the implementation case is 0.1MPa, tower top row's air outlet temperature of desorber (26)
It it is 20 DEG C, into the 4th flash tank (27).4th flash tank (27) bottom of towe separates water outlet and leaves system, the 4th flash tank (27)
Tower top discharges CO2The molar flow of air-flow about 74kmol/h, makes present invention process reach 90% CO2Capture rate level, should
CO2Air-flow leaves chemical trapping technique, delivers to carbon dioxide compression cooling device.The bottom of towe discharge liquor temperature of desorber (26) is
103 DEG C, pressure is improved to 1.0MPa through the 3rd solution pump (28), then through the second heat exchanger (25), the 3rd heat exchanger (20) and the
Four heat exchangers (22) reclaim heat energy, and after being cooled down through the 4th cooler (29), temperature is down to 20 DEG C, and entering chemistry as absorbing liquid inhales
Receive tower (24) tower top and absorb CO2。
The CO trapped in present invention process2For sealing up for safekeeping, storage condition need to be reached through multi-stage compression and cascade EDFA：It is logical
It is often the liquid CO of 11.0~15.0MPa2.Compression cooling technique is set the need for meet various sealing up for safekeeping, in the implementation case
Outlet CO2Pressure is 15.0MPa.The CO of chemistry trapping process outlet2Stream pressure about 0.1MPa, need to compress it to thing
The CO of reason trapping process outlet2After stream pressure 0.54MPa, two gangs of CO of outlet are remixed2Air-flow, compresses and cools down through level Four,
The condition of outlets at different levels be respectively 1.2MPa, 20 DEG C；2.7MPa、20℃；6.0MPa, 20 DEG C and 15.0MPa, 20 DEG C, reaching can
The condition sealed up for safekeeping, leaves process system.
Implementation result
On the basis of marking coal, energy consumption conversion is carried out to the cold and heat needed for whole technique, needed for being corresponded to
Mark consumption of coal amount, then be electricity by mark consumption of coal amount conversion, then plus electricity (including the pump work, compression consumed in technique
Work(, and offset the work(that expanding machine is produced), the as total power consumption of present invention process, its value is 0.165MWh/tCO2。
The carbon trapping estimated in the world at present and the cost for compressing, from CO2The total energy consumption for being compressed to 15.0MPa is trapped,
It is commonly considered as 0.2MWh/tCO2(Gary T.Rochelle, et al., Science 325,1652,2009).By contrast,
Present invention process reduces 17.5% carbon trapping and compression energy consumption.Therefore, according to the result of the implementation case, present invention process
The low energy consumption CO of the carbon dioxide enriched air-flow of extensive high pressure under high-carbon capture rate can be realized2Trapping and compression treatment.
The above case study on implementation is only that one embodiment of the present invention is described, not to the scope of the present invention
It is defined, on the premise of design spirit of the present invention is not departed from, this area engineers and technicians are to technical scheme
The various forms of deformations and improvement made, all should fall into the protection domain that claim of the invention determines.
Claims (4)
1. it is a kind of to combine the collecting carbonic anhydride and compression treatment device for absorbing, it is characterised in that to be caught including desulfurizer, physics
Acquisition means, chemical capturing device and carbon dioxide compression cooling device；The desulfurizer includes desulfurizing tower (1), the first cooling
Device (10), the first solution pump (9), first circulation air compressor (4), heater (2), the first flash tank (3) are separated with hydrogen sulfide
Device (5), the tower top import of the desulfurizing tower (1) connects the outlet of the first cooler (10), and the import of the first cooler (10) connects
Connect the outlet of the first solution pump (9), the bottom of towe import of tower top outlet connection physics absorption tower (7) of desulfurizing tower (1), desulfurizing tower
(1) outlet of bottom of towe import connection first circulation air compressor (4), bottom of towe outlet connection heater (2) of desulfurizing tower (1)
Import, the outlet of heater (2) connects the import of the first flash tank (3), and the top exit connection first of the first flash tank (3) is followed
The import of ring air compressor (4), the import of outlet at bottom connection hydrogen sulphide separator (5) of the first flash tank (3), hydrogen sulfide point
From the import of outlet at bottom connection First Heat Exchanger (6) of device (5)；The physics capturing device includes Physical Absorption tower (7), the
One heat exchanger (6), current divider (8), the first expanding machine (11), the second flash tank (12), the second expanding machine (16), the 3rd flash tank
(17), the second solution pump (18) and the second cooler (19), the tower top outlet connection First Heat Exchanger of the Physical Absorption tower (7)
(6) import, the import of bottom of towe outlet connection current divider (8) of Physical Absorption tower (7), the outlet of current divider (8) is divided into two-way,
Connect the import of the first solution pump (9) all the way, another road connects the import of the first expanding machine (11), the first expanding machine (11) go out
The import of mouth the second flash tank of connection (12), the top exit pipeline of the second flash tank (12) sets at least one cycle compressor
Machine and at least one cooler are connected with the bottom of towe import of Physical Absorption tower (7), the outlet at bottom connection of the second flash tank (12)
The import of the second expanding machine (16), the outlet of the second expanding machine (16) connects the import of the 3rd flash tank (17), the 3rd flash tank
(17) outlet at bottom connects the import of the second solution pump (18), and the outlet of the second solution pump (18) connects the second cooler (19)
Import, the second cooler (19) outlet connection physics absorption tower (7) tower top import, the hot logistics of First Heat Exchanger (6)
The centre inlet of outlet connection physics absorption tower (7)；The chemical capturing device includes chemical absorbing tower (24), the second heat exchanger
(25), desorber (26), the 4th flash tank (27), the 3rd solution pump (28), the 4th cooler (29), other at least one heat exchange
Device and at least one expanding machine, the cold stream outlet of First Heat Exchanger (6) connect at least one heat exchanger and at least one expansion
Machine, heat exchanger expanding machine is alternately placed；The bottom of towe inlet ductwork with chemical absorbing tower (24) is connected again, chemical absorbing tower (24)
The import of bottom of towe outlet the second heat exchanger of connection (25), the tower of cold stream outlet connection desorber (26) of the second heat exchanger (25)
Jacking mouthful, the tower top outlet of desorber (26) connects the import of the 4th flash tank (27), the bottom of towe outlet connection of desorber (26)
The import of the 3rd solution pump (28), the outlet of the 3rd solution pump (28) connects the import of the second heat exchanger (25), the second heat exchanger
(25) hot stream outlet pipeline connects at least one heat exchanger, then is connected with the import of the 4th cooler (29), the 4th cooling
The tower top import of outlet connection chemical absorbing tower (24) of device (29)；The carbon dioxide compression cooling device includes at least four
Compressor and at least four coolers, the top exit of the 4th flash tank (27) connect at least one compressor and at least one cold
But top exit of the device again with the 3rd flash tank (17) merges, and the pipeline after merging connects at least three compressors and three coolings
Device, compressor cooler is alternately placed.
2. the collecting carbonic anhydride that a kind of joint of application device as claimed in claim 1 absorbs and compression handling process, it is special
Levy and be, described technique is trapped technique, chemistry trapping technique and compression handling process by physics and combines and constitute, associated form
For：
1) pretreated carbon dioxide containing air flow initially enters physics trapping technique, from the charging of desulfurizing tower (1) bottom of towe, from lower
Upper and Physical Absorption liquid counter current contacting, the hydrogen sulfide in air-flow is absorbed；The heated device of the bottom of towe discharge liquor (2) of desulfurizing tower (1)
Gas-liquid separation is carried out into the first flash tank (3) after heating, gas is discharged through first circulation compressor in the top of the first flash tank (3)
(4) desulfurizing tower (1) bottom is sent back to after compressing；The bottom discharge liquor of the first flash tank (3) enters hydrogen sulphide separator (5), vulcanization
Hydrogen is separated and is left system from hydrogen sulphide separator (5) top；The bottom discharge liquor of hydrogen sulphide separator (5) is through the first heat exchange
After device (6) reclaims heat energy, Physical Absorption tower (7) is entered as absorbing liquid；
2) air-flow after desulfurization enters Physical Absorption tower (7) bottom of towe by desulfurizing tower (1) tower top, inverse with Physical Absorption liquid from bottom to top
Stream contact, more than 60% CO in air-flow2Absorbed, residual gas is discharged from Physical Absorption tower (7) tower top, through First Heat Exchanger
(6) chemical trapping technique is entered after heating；The bottom of towe discharge liquor of Physical Absorption tower (7) is divided into two strands, a stock-traders' know-how through current divider (8)
First solution pump (9) and the first cooler (10) enter desulfurizing tower (1) tower top as Physical Absorption liquid desulfurization, another burst of discharge afterwards
Liquid enters after the first expanding machine (11) reclaims expansion work done delivers to the second flash tank (12)；The top of the second flash tank (12)
Discharge gas sends Physical Absorption tower (7) bottom of towe back to after flowing through at least one recycle gas compressor and at least one cooler successively, the
The bottom discharge liquor of two flash tanks (12) enters the second expanding machine (16), and the 3rd flash tank is delivered to after reclaiming expansion work done
(17), CO2Gas is discharged from the 3rd flash tank (17) top, into CO2Compression handling process；Arrange 3rd flash tank (17) bottom
Go out the Physical Absorption liquid of regeneration, after improving pressure and the second cooler (19) reduction temperature through the second solution pump (18), as thing
Reason absorbing liquid enters Physical Absorption tower (7) tower top；
3) exit flow of First Heat Exchanger (6) reclaims heat energy through at least one heat exchanger and at least one expanding machine reclaims expansion
After work done, the charging of chemical absorbing tower (24) bottom of towe is delivered to, from bottom to top with chemical absorbing liquid counter current contacting；Removing CO2's
Purified gas chemically absorption tower (24) tower top discharge system, the bottom of towe discharge liquor of chemical absorbing tower (24) is through the second heat exchanger (25)
Enter desorber (26) tower top after heating；The tower top discharge CO of desorber (26)2Gas enters the 4th flash tank (27), and the 4th dodges
Discharge aqueous water, the 4th flash tank (27) top discharge CO in steaming pot (27) bottom2Gas, into CO2Compression handling process；Desorption
The chemical absorbing liquid of tower (26) bottom of towe discharge regeneration, improves pressure and the second heat exchanger (25) reclaims heat through the 3rd solution pump (28)
Can, then after reclaiming heat energy through at least one heat exchanger with the exit flow of First Heat Exchanger (6), as chemical absorbing liquid entranceization
Learn absorption tower (24) tower top；
4) CO of the 4th flash tank (27) top discharge2Gas, after at least one compressor and at least one cooler, CO2Gas
The temperature and pressure of body and the CO of the 3rd flash tank (17) top discharge2Gas phase is same, two gangs of CO2After gas converges, through at least three
After individual compressor improves pressure and at least three coolers reduction temperature, discharge system.
3. a kind of joint as claimed in claim 2 absorbs collecting carbonic anhydride and compression handling process, it is characterised in that institute
The Physical Absorption liquid stated is：It is a certain or various in 1-METHYLPYRROLIDONE, propene carbonate or NHD
Mixture；Described chemical absorbing liquid is：MEA, 2- amidos -2- methyl isophthalic acids-propyl alcohol, diethanol amine or N- methyl two
A certain or various mixture in monoethanolamine.
4. a kind of joint as claimed in claim 2 absorbs collecting carbonic anhydride and compression handling process, it is characterised in that thing
Reason trapping technique takes the mode of high pressure absorption-middle pressure desorption, and the tower pressure of Physical Absorption tower (7) is 2~7MPa, the 3rd flash tank
(17) CO of outlet2Pressure is 0.5~1MPa；Chemical trapping technique takes the mode that middle pressure absorption-normal pressure is desorbed, chemical absorbing
The feed stream pressure of tower (24) bottom of towe is 0.8~1.5MPa, and the tower pressure of desorber (26) is 0.1~0.3MPa.
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| CN115388616B (en) * | 2022-08-25 | 2023-06-16 | 北京航天试验技术研究所 | Mars surface carbon dioxide continuous capturing system adopting pressurizing liquefaction and method thereof |
| CN116492816B (en) * | 2023-03-23 | 2024-03-12 | 中国能源建设集团广东省电力设计研究院有限公司 | High CO 2 Loaded absorbent carbon capture desorption system and method |
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