CN116492816B - High CO 2 Loaded absorbent carbon capture desorption system and method - Google Patents
High CO 2 Loaded absorbent carbon capture desorption system and method Download PDFInfo
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- 239000002250 absorbent Substances 0.000 title claims abstract description 121
- 230000002745 absorbent Effects 0.000 title claims abstract description 121
- 238000003795 desorption Methods 0.000 title claims abstract description 101
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 68
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 66
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000010521 absorption reaction Methods 0.000 claims abstract description 55
- 239000007788 liquid Substances 0.000 claims description 135
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 19
- 239000003546 flue gas Substances 0.000 claims description 19
- 239000007789 gas Substances 0.000 claims description 16
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 5
- 239000001569 carbon dioxide Substances 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims 1
- 230000015556 catabolic process Effects 0.000 abstract description 5
- 238000006731 degradation reaction Methods 0.000 abstract description 5
- 238000012423 maintenance Methods 0.000 abstract description 2
- 239000012071 phase Substances 0.000 description 43
- 238000012546 transfer Methods 0.000 description 19
- 238000005265 energy consumption Methods 0.000 description 6
- 230000008569 process Effects 0.000 description 6
- 239000007791 liquid phase Substances 0.000 description 5
- 239000006096 absorbing agent Substances 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 238000005191 phase separation Methods 0.000 description 3
- 239000002594 sorbent Substances 0.000 description 3
- 230000002411 adverse Effects 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 239000000110 cooling liquid Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- -1 amine salt Chemical class 0.000 description 1
- 238000003556 assay Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000004568 cement Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
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- 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
- B01D53/1418—Recovery of products
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- 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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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a carbon capture system and a method. The carbon capture system includes: the device comprises an absorption tower, a first heat exchanger, a first cooler, an absorbent storage tank, a flash tank, a second heat exchanger, a desorption tower, a reboiler and a third heat exchanger. The carbon trapping and desorbing system of the invention can be suitable for high CO such as novel two-phase absorbent, non-aqueous absorbent and the like 2 Carbon capture of the loaded absorbent can reduce high CO 2 The high viscosity and easy degradation of the absorbent caused by the load can improve the operation stability of the novel absorbent and reduce the operation and maintenance cost.
Description
Technical Field
The invention relates to the technical field of waste gas treatment, in particular to a high CO 2 Loaded absorbent carbon capture desorption systems and methods.
Background
Low CO for coal-fired power plant, steel, cement, etc 2 Carbon dioxide emission reduction is carried out on the concentrated flue gas, and carbon dioxide trapping can be carried out by adopting a post-combustion chemical absorption method. Carbon capture processes using organic amines as the absorption liquid are currently the most mature and most commercially available technology. The MEA is the earliest commercial carbon capture absorbent, has the advantages of good absorption effect and low cost, but has the problems of high energy consumption, easy degradation, large corrosiveness and the like. The development of a novel absorbent with high and stable absorption performance and low running cost plays an important role in the application of carbon trapping technology and the realization of the peak-assisting carbon and carbon neutralization strategic targets.
In recent years, various types of novel absorbents including two-phase absorbents, nonaqueous absorbents, and the like have been proposed by many researchers to reduce the carbon capture energy consumption and running cost. Wherein the two-phase absorbent refers to absorption liquid for absorbing CO 2 After that, two immiscible lean COs are formed 2 Liquid phase (CO) 2 Low content) and rich in CO 2 Liquid phase (CO) 2 High content), separating the two, and then only enriching the CO 2 The liquid phase circulates to the desorption tower to be desorbed, the process can improve the efficiency of the absorption process and the desorption process, and simultaneously can effectively reduce the consumption of sensible heat and vaporization latent heat in the regeneration process, thereby reducing the cost of energy consumption. The nonaqueous absorbent is obtained by replacing or partially replacing water in the conventional absorbent with other organic solvents, so that the process energy consumption is reduced, and the absorbent does not contain water or has low water content and is not a solvent, so that the nonaqueous absorbent is called as the nonaqueous absorbent. The absorption load of two-phase and nonaqueous absorbents is significantly greater than that of conventional absorbents such as MEAHigh, this reduces the amount of absorbent used, but the high absorption load causes other problems, firstly an increase in viscosity, the two-phase absorbent being rich in CO 2 The rich phase of the phase and the nonaqueous absorbent can reach more than 50cp and even more than 100cp which is tens times that of the conventional absorbent, the mass transfer of the flow is easy to be adversely affected, and in addition, the amine absorbent absorbs CO 2 The degradation rate of the post-formed ionized amine salt is concentration dependent, CO 2 The higher the load of absorption, the more significantly the degradation rate, which has an adverse effect on the application of two new types of absorbent, two-phase absorbent and non-aqueous absorbent, for which there is a need to develop a new type of absorbent that is suitable for both types of high CO 2 A carbon capture desorption system of a novel loaded absorbent.
Disclosure of Invention
To overcome the existing high CO 2 Problems with the disadvantages of the carbon capture systems with loaded sorbents, one of the objectives of the present invention is to provide a high CO 2 The second object of the present invention is to provide a high CO content carbon capture and desorption system 2 A loaded absorbent carbon capture desorption method.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
the first aspect of the invention provides a high CO 2 A loaded absorbent carbon capture desorption system comprising:
an absorption tower;
the first heat exchanger is connected with the absorption tower;
the first cooler is respectively connected with the first heat exchanger and the absorption tower;
an absorbent storage tank connected to the first cooler and the absorption tower, respectively;
the flash tank is connected with the first heat exchanger;
the second heat exchanger is respectively connected with the flash tank and the first cooler;
the desorption tower is respectively connected with the flash tank, the first heat exchanger and the second heat exchanger;
a reboiler connected with the desorption tower;
and the third heat exchanger is respectively connected with the second heat exchanger, the desorption tower and the reboiler.
Preferably, such high CO 2 In the loaded absorbent carbon capture desorption system, when the absorbent is a two-phase absorbent, the carbon capture desorption system further comprises a phase separator and a second cooler, wherein the phase separator is respectively connected with the absorption tower and the first heat exchanger, and the second cooler is respectively connected with the phase separator and the absorbent storage tank; the phase separator is a gravity phase separator, and by arranging the phase separator, the carbon trapping system is particularly suitable for a two-phase absorbent carbon trapping system, and by phase separation, CO is lean 2 The liquid enters an absorbent storage tank through a second cooler, and is rich in CO 2 The liquid enters the following desorption system after being heated by the first heat exchanger, and phase separation is carried out at the desorption front section, so that the whole operation cost can be further saved.
Preferably, such high CO 2 In the carbon capture and desorption system of the load absorbent, the carbon capture and desorption system further comprises a condenser and a gas-liquid separator, wherein the condenser is connected with the desorption tower, and the gas-liquid separator is connected with the condenser; further preferably, the gas-liquid separator is further connected with a desorption tower, the gas at the top of the desorption tower is cooled by the condenser and then enters the gas-liquid separator to separate out liquid, and the liquid at the bottom of the gas-liquid separator enters the desorption tower again.
In a second aspect the invention provides a high CO 2 The carbon capture and desorption method of the load absorbent adopts the carbon capture and desorption system to recycle carbon dioxide, and specifically comprises the following steps:
containing CO 2 The flue gas and the absorbent in the absorbent storage tank respectively enter the absorption tower, and the absorbent is used for absorbing CO in the flue gas 2 Absorbing; CO is absorbed at the bottom of the absorption tower 2 The liquid in the first heat exchanger is heated and then enters a flash tank for treatment to obtain flash gas and flash liquid; flash gas enters a desorption tower, and flash liquid is divided into semi-rich liquid1 and semi-rich liquid 2, wherein the semi-rich liquid 2 is directly conveyed to a desorption tower, and the semi-rich liquid 1 is heated by a second heat exchanger and a third heat exchanger in sequence and then enters the desorption tower; CO is discharged from the top of the desorption tower 2 A gas;
heating desorption liquid at the bottom of the desorption tower through a reboiler, and heating semi-rich liquid 2 through a third heat exchanger by steam condensate formed after heat exchange of the reboiler;
and the desorption liquid at the bottom of the desorption tower is subjected to heat exchange through a first heat exchanger and a second heat exchanger respectively, cooled through a first cooler and enters an absorbent storage tank.
Preferably, such high CO 2 In the carbon capture desorption method of the load absorbent, the carbon dioxide containing CO 2 CO in flue gas of (C) 2 The concentration is 3-18vol%.
High CO in the present invention 2 In the loaded absorbent carbon capture desorption method, the absorbent includes a two-phase absorbent and a nonaqueous absorbent.
Preferably, such high CO 2 In the carbon capture desorption method of the load absorbent, the CO is absorbed 2 The temperature of the liquid heated by the first heat exchanger is 85-105 ℃; further preferably, the absorbing CO 2 The temperature of the liquid after being heated by the first heat exchanger is 90-100 ℃.
Preferably, such high CO 2 In the carbon capture desorption method of the load absorbent, the CO is absorbed 2 The pressure of the liquid heated by the first heat exchanger is 5-7.5bar; further preferably, the absorbing CO 2 The pressure of the liquid heated by the first heat exchanger is 5.5-7bar; still further preferably, the absorbing CO 2 The pressure of the liquid after heating by the first heat exchanger is 6-6.5bar.
Preferably, such high CO 2 In the carbon capturing and desorbing method of the load absorbent, CO is absorbed in the flash tank in a controlled manner 2 The temperature of the liquid of (2) is 58-70 ℃; further preferably, the flash tank is internally provided with a control device for absorbing CO 2 The temperature of the liquid of (2) is 60-68 ℃.
Preferably, such high CO 2 In the carbon capture desorption method of the load absorbent, the flash tankInternal control of CO absorption 2 The pressure of the liquid is 0.8-1.5bar; further preferably, the flash tank is internally provided with a control device for absorbing CO 2 The pressure of the liquid is 1-1.2bar.
Preferably, such high CO 2 In the carbon capturing and desorbing method of the load absorbent, the proportion of the semi-rich liquid 1 is 85-95wt%, and the proportion of the semi-rich liquid 2 is 5-15wt%; further preferably, the semi-rich liquid 1 accounts for 86-92wt% and the semi-rich liquid 2 accounts for 8-14wt%.
Preferably, such high CO 2 In the carbon capturing and desorbing method of the load absorbent, the temperature of the desorption liquid at the bottom of the desorber is 105-120 ℃; further preferably, the temperature of desorption liquid at the bottom of the desorption tower is 110-115 ℃.
Preferably, such high CO 2 In the carbon capturing and desorbing method of the load absorbent, the volume ratio of the desorption liquid at the bottom of the desorber to the desorption liquid passing through the first heat exchanger and the second heat exchanger is (1-3): 1.
preferably, such high CO 2 In the carbon capturing and desorbing method of the load absorbent, the bottom of the absorption tower absorbs CO 2 CO in a liquid of (a) 2 Load is more than or equal to 2.5mol CO 2 Preferably, the bottom of the absorption tower absorbs CO 2 CO in a liquid of (a) 2 Load is more than or equal to 3mol CO 2 /kg。
Preferably, such high CO 2 In the carbon capturing and desorbing method of the load absorbent, CO of flash liquid obtained from the flash tank 2 The load is 2 to 2.5mol CO 2 /kg。
The beneficial effects of the invention are as follows:
the carbon trapping and desorbing system of the invention can be suitable for high CO such as novel two-phase absorbent, non-aqueous absorbent and the like 2 Carbon capture of the loaded absorbent can reduce high CO 2 The high viscosity and easy degradation of the absorbent caused by the load can improve the operation stability of the novel absorbent and reduce the operation and maintenance cost.
The carbon capturing and desorbing system of the invention is provided with a first heat exchanger, the absorption liquid at the bottom of the absorption tower is heated by the desorption liquid at the bottom of the desorption tower, and a flash tank is arranged at the same time,reducing absorbent CO 2 The load and viscosity, the energy consumption of the system and the loss of the absorbent are respectively 3-10% and 5-12%.
The carbon trapping and desorbing system of the invention is used for distributing the flash liquid after the flash treatment, and part of the flash liquid is heated by the second heat exchanger and the third heat exchanger, so that the heat of the steam condensate of the reboiler is recovered; the residual flash liquid is sent to stripping section of the desorption tower, and the CO at the outlet is improved 2 And the system energy consumption is reduced by more than 35 percent.
Drawings
FIG. 1 is a CO of the present invention 2 A high load absorbent carbon capture system;
FIG. 2 is a CO of the present invention 2 A high load two-phase absorbent carbon capture system;
FIG. 3 is a CO of an embodiment of the invention 2 High load single phase absorber carbon capture system embodiment diagram;
FIG. 4 is a schematic diagram of CO according to an embodiment of the present invention 2 High load two-phase absorbent carbon capture system embodiments are shown.
Fig. 1-4 are labeled:
100-absorption tower, 200-first heat exchanger, 300-first cooler, 400-absorber storage tank, 500-flash tank, 600-second heat exchanger, 700-desorption tower, 800-reboiler, 900-third heat exchanger, 1000-phase separator, 1100-second cooler, 1200-first transfer pump, 1300-second transfer pump, 1400-third transfer pump, 1500-fourth transfer pump, 1600-condenser, 1700-gas-liquid separator.
Detailed Description
The following detailed description of embodiments of the invention is exemplary, and the examples described by reference to the drawings are only for the purpose of illustrating the invention and are not to be construed as limiting the invention.
The present invention will be described in further detail with reference to specific examples.
In the description of the present invention, it should be noted that, unless explicitly specified and limited otherwise, the terms "connected," "connected," and "connected" are to be construed broadly, and may be either fixedly connected, detachably connected, or integrally connected, for example; can be mechanically or electrically connected; may be directly connected, indirectly connected through an intermediate medium, or may be communication between two elements. The specific meaning of the above terms in the present invention can be understood by those of ordinary skill in the art according to the specific circumstances.
The starting materials, reagents or apparatus used in the examples are all commercially available from conventional sources or may be obtained by methods known in the art unless otherwise specified. Unless otherwise indicated, assays or testing methods are routine in the art.
As shown in fig. 1, a high CO 2 A loaded absorbent carbon capture desorption system comprising:
the system comprises an absorption tower 100, a first heat exchanger 200, a first cooler 300, an absorbent storage tank 400, a flash tank 500, a second heat exchanger 600, a desorption tower 700, a reboiler 800 and a third heat exchanger 900;
the first heat exchanger 200 is connected with the absorption tower 100, the first cooler 300 is connected with the first heat exchanger 200, and the first cooler 300, the absorbent storage tank 400 and the absorption tower 100 are connected in sequence; the flash tank 500 is connected to the first heat exchanger 200; the second heat exchangers 600 are respectively connected with the flash tank 500 and the first cooler 300; the desorption tower 700 is respectively connected with the flash tank 500, the first heat exchanger 200 and the second heat exchanger 600; reboiler 800 is connected to desorber 700; the third heat exchanger 900 is connected to the second heat exchanger 600, the desorption column 700, and the reboiler 800, respectively.
High CO 2 The carbon trapping and desorbing method for the load absorbent adopts a system shown in figure 1, and specifically comprises the following steps:
containing CO 2 The flue gas in the (a) and the absorbent in the absorbent storage tank 400 respectively enter the absorption tower 100, and the absorbent is used for absorbing CO in the flue gas 2 Absorbing; CO is absorbed at the bottom of the absorption tower 100 2 The liquid in the first heat exchanger 200 is heated and then enters the flash tank 500 for treatment to obtain flash gas and flash liquid; the flash gas enters a desorption tower 700, the flash liquid is divided into semi-rich liquid 1 and semi-rich liquid 2, the semi-rich liquid 2 is directly conveyed to the desorption tower 700, and the semi-rich liquid 1 is heated by a second heat exchanger 600 and a third heat exchanger 900 in sequenceEnters a desorption tower 700, and CO is discharged from the top of the desorption tower 700 2 A gas; the desorption liquid at the bottom of the desorption tower 700 is heated by a reboiler 800, and the steam condensate formed after heat exchange of the reboiler 800 is heated by a third heat exchanger 900 to semi-rich liquid 2; the desorption liquid at the bottom of the desorption tower 700 is subjected to heat exchange through the first heat exchanger 200 and the second heat exchanger 600 respectively, cooled through the first cooler 300 and enters the absorbent storage tank 400.
As shown in fig. 2, a high CO 2 A loaded sorbent carbon capture system, suitable for a two-phase sorbent carbon capture system, comprising:
100-absorption tower, 200-first heat exchanger, 300-first cooler, 400-absorber storage tank, 500-flash tank, 600-second heat exchanger, 700-desorption tower, 800-reboiler, 900-third heat exchanger, 1000-phase separator, 1100-second cooler.
The phase separator 1000 is connected with the absorption tower 100, the first heat exchanger 200 is connected with the phase separator 1000, and the first cooler 300 is respectively connected with the first heat exchanger 200 and the absorption tower 100; the absorbent storage tank 400 is connected to the first cooler 300 and the absorption tower 100, respectively; the flash tank 500 is connected to the first heat exchanger 200; the second heat exchangers 600 are respectively connected with the flash tank 500 and the first cooler 300; the desorption tower 700 is respectively connected with the flash tank 500, the first heat exchanger 200 and the second heat exchanger 600; reboiler 800 is connected to desorber 700; the third heat exchanger 900 is respectively connected with the second heat exchanger 600, the desorption tower 700 and the reboiler 800; the second cooler 1100 is connected to the phase separator 1000 and the absorbent tank 400, respectively.
A two-phase carbon capture desorption method, employing a system as shown in fig. 2, comprising the steps of:
containing CO 2 The flue gas in the (a) and the absorbent in the absorbent storage tank 400 respectively enter the absorption tower 100, and the absorbent is used for absorbing CO in the flue gas 2 Absorbing; CO is absorbed at the bottom of the absorption tower 100 2 The liquid of (2) enters the phase separator 1000 for phase separation and is separated into lean CO 2 Liquid and rich CO 2 Liquid, lean CO 2 The liquid is cooled by the second cooler 1100 and then enters the absorbent storage tank 400, and is rich in CO 2 The liquid is heated by the first heat exchanger 200 and then enters the following desorption systemAnd (5) unifying.
The CO of the embodiment is described below with reference to FIG. 3 2 A high load single phase absorber carbon capture system. As shown in fig. 3, includes: the absorption tower 100, the first heat exchanger 200, the first cooler 300, the absorbent storage tank 400, the flash tank 500, the second heat exchanger 600, the desorption tower 700, the reboiler 800, the third heat exchanger 900, the first transfer pump 1200, the second transfer pump 1300, the third transfer pump 1400, the fourth transfer pump 1500, the condenser 1600, and the gas-liquid separator 1700.
As shown in FIG. 3, in some embodiments of the invention, the flue gas from the coal-fired power plant enters the absorption tower 100 from the lower end of the tower after pretreatment, the flue gas temperature is 40 ℃, and the CO in the flue gas 2 The concentration is 10-12vol%, the absorbent is non-aqueous absorbent such as AEP-NMP-water, and the temperature is 40deg.C; the absorbent in the absorbent storage tank 400 is introduced into the absorption tower 100 from the upper end thereof by the second transfer pump 1300, and the absorbent absorbs CO 2 Then forming rich solution, the temperature of the rich solution is 48-53 ℃, and the CO of the rich solution 2 The load reaches 3.4mol CO 2 Kg, viscosity 50-80cp; the rich liquid at the bottom of the absorption tower 100 is conveyed to the first heat exchanger 200 by the first conveying pump 1200 to be heated to 90-98 ℃ and the pressure is 5-6.5bar; and then enters a flash tank 500 where the flash tank 500 is enriched in CO 2 The temperature and pressure of the phase solution are reduced to 58-65 ℃ and 1-1.3bar, the formed flash steam is discharged from a gas phase outlet at the top of the flash tank 500 and enters a desorption tower 700, the formed semi-rich liquid is discharged from a liquid phase outlet at the bottom of the flash tank 500, and the semi-rich liquid load is reduced to 2-2.4mol CO 2 The viscosity of the semi-rich liquid is 5-9cp, the semi-rich liquid is divided into two parts by a third delivery pump 1400, namely, the semi-rich liquid 1 and the semi-rich liquid 2, the proportion of the semi-rich liquid 1 is 88 percent, the proportion of the semi-rich liquid 2 is 12 percent, wherein the semi-rich liquid 1 is delivered to a second heat exchanger 600 and a third heat exchanger 900 to be heated to 103 ℃, and then delivered to a stripping section in a stripping tower 700 to strip CO 2 The method comprises the steps of carrying out a first treatment on the surface of the The semi-rich liquid is desorbed in the desorber 700 by heat provided by the reboiler 800, and the desorbed CO is discharged from the top of the desorber 700 2 ，CO 2 The gas sequentially passes through a condenser 1600 and a gas-liquid separator 1700 to obtain product gas, and the cooling liquid of the gas-liquid separator 1700 returns to the desorption tower 700; the desorption liquid temperature at the bottom of the desorption tower 700 is controlled between 108 and 115 ℃ and CO 2 Loaded with 0.7-1.2mol CO 2 /kg；The desorption liquid is respectively delivered to the first heat exchanger 200 and the second heat exchanger 600 through the fourth delivery pump 1500 to recycle heat, and the temperature is respectively reduced to 52-56 ℃ and 63-68 ℃, and then cooled to 40 ℃ by the first cooler 300 to be delivered to the absorbent storage tank 400.
The CO of the embodiment is described below with reference to FIG. 4 2 A high load two-phase absorbent carbon capture system. As shown in fig. 4, includes: the absorption tower 100, the first heat exchanger 200, the first cooler 300, the absorbent storage tank 400, the flash tank 500, the second heat exchanger 600, the desorption tower 700, the reboiler 800, the third heat exchanger 900, the phase separator 1000, the second cooler 1100, the first transfer pump 1200, the second transfer pump 1300, the third transfer pump 1400, the fourth transfer pump 1500, the condenser 1600, and the gas-liquid separator 1700.
As shown in FIG. 4, in some embodiments of the invention, the flue gas from the coal-fired power plant enters the absorption tower 100 from the lower end of the tower after pretreatment, the flue gas temperature is 40 ℃, and the CO in the flue gas 2 The concentration is 10-12vol%, the absorbent is two-phase absorbent such as MEA-sulfolane-water, and the temperature is 40 ℃; the absorbent in the absorbent storage tank 400 is introduced into the absorption tower 100 from the upper end thereof by the second transfer pump 1300, and the absorbent absorbs CO 2 After that, a rich solution is formed, the temperature of the rich solution is 48-54 ℃, and the rich solution is conveyed to the phase separator 1000 by the first conveying pump 1200 to be separated into lean CO 2 Phase solution and rich CO 2 The volume ratio of the phase solution is 52-54% and 46-48%, and the phase solution is lean in CO 2 The phase solution is cooled to 40 c by the second cooler 1100 and then sent to the absorbent storage tank 400. Rich in CO 2 The temperature of the phase solution is 48-54 ℃, CO 2 The load reaches 3.0 to 3.3mol CO 2 Per kg, viscosity 20-30cp, CO-rich 2 The phase solution is heated to 88-92 ℃ by a first heat exchanger 200 at a pressure of 5.5-6.5bar and then enters a flash tank 500, where the flash tank 500 is rich in CO 2 The temperature and pressure of the phase solution are reduced to 62-65 ℃ and 1-1.2bar, flash steam is formed and discharged from a gas phase outlet at the top of the flash tank 500, the formed semi-rich liquid is discharged from a liquid phase outlet at the bottom of the flash tank 500, and the semi-rich liquid load is reduced to 2-2.4mol CO 2 Per kg, viscosity 3-5cp, half rich liquid is divided into two parts by a third delivery pump 1400, the half rich liquid 1 accounts for 90 percent, the half rich liquid 2 accounts for 10 percent, wherein the half rich liquid 1 is delivered to a second heat exchanger 600 and a third heat exchangerThe heat exchanger 900 is heated to 105 ℃ and then sent to the stripping section of the desorption tower 700 to desorb CO 2 . The semi-rich liquid 2 is directly conveyed to a rectifying section of the desorption tower 700 to recycle heat, the semi-rich liquid is desorbed in the desorption tower 700 by the heat provided by the reboiler 800, and the desorption CO is discharged from the top of the desorption tower 700 2 ，CO 2 The gas sequentially passes through a condenser 1600 and a gas-liquid separator 1700 to obtain product gas, and the cooling liquid of the gas-liquid separator 1700 returns to the desorption tower 700; the temperature of the bottom of the desorption tower 700 is controlled to be 113-118 ℃, the temperature of the generated desorption liquid is 113-118 ℃, and the temperature of CO is controlled to be 2 Loaded with 1.2-1.6mol CO 2 /kg. The desorption liquid is respectively delivered to the first heat exchanger 200 and the second heat exchanger 600 through the fourth delivery pump 1500 to recover heat, and the temperature is respectively reduced to 50-55 ℃ and 65-70 ℃, and then the temperature is cooled to 40 ℃ by the first cooler 300 to be delivered to an absorbent storage tank.
As shown in fig. 3 and 4, in the aspect of the control method, after the carbon capture system is started, the flue gas flow, the CO of the inlet flue gas monitoring point and the flue gas monitoring point of the outlet of the absorption tower are processed according to the target carbon capture rate (such as 90 percent) 2 The concentration signal controls the outlet flow of the second transfer pump 1300, when the liquid level of the liquid level measuring point at the bottom of the absorption tower 100 rises to the design range, the first transfer pump 1200 is started, if the liquid level of the liquid level measuring point at the bottom of the absorption tower 100 is lower than the lower limit warning value, the first transfer pump 1200 stops, and if the liquid level of the liquid level measuring point at the bottom of the absorption tower 100 is higher than the upper limit warning value, the first transfer pump 1200 increases the flow output. The rich liquid at the bottom of the absorption tower 100 is conveyed through the first conveying pump 1200 to be preheated by the first heat exchanger 200, the temperature after preheating is 90-100 ℃, and the opening degree of a valve between the fourth conveying pump 1500 and the first heat exchanger 200 is controlled by a signal of a temperature measuring point at the outlet of the first heat exchanger 200. After preheating, the liquid enters the flash tank 500, the liquid level of the liquid level measuring point of the flash tank 500 rises to the design range, the third conveying pump 1400 is started, and if the liquid level of the liquid level measuring point at the bottom of the flash tank 500 is lower than the lower limit warning value, the third conveying pump 1400 is stopped. The pressure of the flash tank 500 is regulated by controlling the opening of a valve through a pressure measuring point at the top outlet of the flash tank 500. The flash liquid formed by the flash tank 500 is delivered by the third delivery pump 1400, and the delivery pipeline is divided into two paths, and respectively passed through the valvesThe DCS system performs flow control. The semi-rich liquid 1 enters the desorption tower 700 after passing through the second heat exchanger 600 and the third heat exchanger 900, the temperature of the second heat exchanger 600 and the third heat exchanger 900 after heating is controlled to be 100-110 ℃, and valves arranged on connecting pipelines of the reboiler 800 and the third heat exchanger 900 are controlled and regulated by signals of temperature measuring points of the third heat exchanger 900. The reboiler 800 provides heat through steam heating, a temperature measuring point is arranged at a liquid outlet at the cold end of the reboiler 800, a valve at the saturated steam inlet end is controlled through the temperature measuring point, when the temperature is lower than 110 ℃, the valve opening of the steam inlet end is increased, and when the temperature is higher than 120 ℃, the valve opening of the steam inlet end is reduced; the upper part of the desorption tower 700 is provided with a temperature measuring point as a supplementary control signal, when the temperature is lower than 90 ℃, the valve opening of the steam inlet end of the reboiler 800 is increased, and when the temperature is higher than 105 ℃, the valve opening of the steam inlet end of the reboiler 800 is reduced. When the liquid level of the liquid level measuring point at the bottom of the desorption tower 700 rises to the design range, the fourth delivery pump 1500 is started, if the liquid level of the liquid level measuring point at the bottom of the desorption tower 700 is lower than the lower limit warning value, the fourth delivery pump 1500 is stopped, and if the liquid level of the liquid level measuring point at the bottom of the desorption tower is higher than the upper limit warning value, the fourth delivery pump 1500 increases the flow output. The desorption solution conveyed by the fourth conveying pump 1500 enters the absorbent storage tank 400 after passing through the first heat exchanger 200, the second heat exchanger 600 and the first cooler 300, when the liquid level of the liquid level measuring point at the bottom of the absorbent storage tank 400 rises to the design range, the second conveying pump 1300 is started, and if the liquid level of the liquid level measuring point at the bottom of the absorbent storage tank 400 is lower than the lower limit warning value, the second conveying pump 1300 is stopped.
While the above description has been made in connection with the accompanying drawings, it is not intended to limit the scope of the invention, but it is to be understood that any modification, equivalent replacement, improvement or the like which comes within the spirit and principles of the present invention are included.
Claims (8)
1. High CO 2 The carbon trapping and desorbing method for the loaded absorbent is characterized by adopting a high CO 2 Carbon dioxide with loaded absorbent carbon capture desorption systemThe recovery specifically comprises the following steps:
containing CO 2 The flue gas and the absorbent in the absorbent storage tank respectively enter the absorption tower, and the absorbent is used for absorbing CO in the flue gas 2 Absorbing; CO is absorbed at the bottom of the absorption tower 2 The liquid in the first heat exchanger is heated and then enters a flash tank for treatment to obtain flash gas and flash liquid; the flash gas enters a desorption tower, the flash liquid is divided into semi-rich liquid 1 and semi-rich liquid 2, the semi-rich liquid 2 is directly conveyed to the desorption tower, and the semi-rich liquid 1 is heated by a second heat exchanger and a third heat exchanger in sequence and then enters the desorption tower; CO is discharged from the top of the desorption tower 2 A gas;
heating desorption liquid at the bottom of the desorption tower through a reboiler, and heating semi-rich liquid 2 through a third heat exchanger by steam condensate formed after heat exchange of the reboiler;
the desorption liquid at the bottom of the desorption tower is subjected to heat exchange through a first heat exchanger and a second heat exchanger respectively, cooled through a first cooler and enters an absorbent storage tank;
the high CO 2 A loaded absorbent carbon capture desorption system comprising:
an absorption tower (100);
a first heat exchanger (200), the first heat exchanger (200) being connected to the absorption column (100);
a first cooler (300), wherein the first cooler (300) is respectively connected with the first heat exchanger (200) and the absorption tower (100);
an absorbent tank (400), the absorbent tank (400) being connected to the first cooler (300) and the absorption tower (100), respectively;
-a flash tank (500), the flash tank (500) being connected to the first heat exchanger (200);
-a second heat exchanger (600), said second heat exchanger (600) being connected to said flash tank (500) and to said first cooler (300), respectively;
a desorption tower (700), wherein the desorption tower (700) is respectively connected with the flash tank (500), the first heat exchanger (200) and the second heat exchanger (600);
a reboiler (800), the reboiler (800) being connected to the desorber (700);
the third heat exchanger (900), the said third heat exchanger (900) is said second heat exchanger (600), said desorber (700), said reboiler (800) link separately;
CO absorption is controlled in the flash tank 2 The temperature of the liquid is 58-70 ℃ and the pressure is 0.8-1.5bar.
2. High CO according to claim 1 2 The carbon trapping and desorbing method for the load absorbent is characterized in that the carbon trapping and desorbing system further comprises a phase separator (1000) and a second cooler (1100), wherein the phase separator (1000) is respectively connected with the absorption tower (100) and the first heat exchanger (200), and the second cooler (1100) is respectively connected with the phase separator (1000) and the absorbent storage tank (400).
3. High CO according to claim 1 or 2 2 The carbon trapping and desorbing method for the load absorbent is characterized in that the carbon trapping and desorbing system further comprises a condenser (1600) and a gas-liquid separator (1700), the condenser (1600) is connected with the desorber (700), and the gas-liquid separator (1700) is connected with the condenser (1600).
4. High CO according to claim 1 2 A method for capturing and desorbing carbon in a loaded absorbent, characterized in that the method comprises the steps of 2 The temperature of the liquid after being heated by the first heat exchanger is 85-105 ℃ and the pressure is 5-7.5bar.
5. High CO according to claim 1 2 The carbon trapping and desorbing method for the load absorbent is characterized in that the semi-rich liquid 1 accounts for 85-95wt% and the semi-rich liquid 2 accounts for 5-15wt%.
6. High CO according to claim 1 2 The carbon capturing and desorbing method for the load absorbent is characterized in that the temperature of desorption liquid at the bottom of the desorber is 105-120 ℃.
7. High CO according to claim 1 2 The carbon capturing and desorbing method for the load absorbent is characterized in that the volume ratio of the desorption liquid at the bottom of the desorber to the desorption liquid at the bottom of the desorber through a first heat exchanger and a second heat exchanger is (1-3): 1.
8. high CO according to claim 1 2 The carbon capturing and desorbing method of the load absorbent is characterized in that the bottom of the absorption tower absorbs CO 2 CO in a liquid of (a) 2 Load is more than or equal to 2.5mol CO 2 /kg。
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