CN118788106B - A carbon capture absorber, system and method for escaped amine recovery and water balance control - Google Patents
A carbon capture absorber, system and method for escaped amine recovery and water balance control Download PDFInfo
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- CN118788106B CN118788106B CN202410875996.4A CN202410875996A CN118788106B CN 118788106 B CN118788106 B CN 118788106B CN 202410875996 A CN202410875996 A CN 202410875996A CN 118788106 B CN118788106 B CN 118788106B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 248
- 238000011084 recovery Methods 0.000 title claims abstract description 204
- 150000001412 amines Chemical class 0.000 title claims abstract description 117
- 238000000034 method Methods 0.000 title claims abstract description 47
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 39
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 39
- 239000006096 absorbing agent Substances 0.000 title description 13
- 239000007788 liquid Substances 0.000 claims abstract description 271
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 155
- 239000003546 flue gas Substances 0.000 claims abstract description 154
- 238000005406 washing Methods 0.000 claims abstract description 112
- 238000010521 absorption reaction Methods 0.000 claims abstract description 62
- 239000002250 absorbent Substances 0.000 claims abstract description 57
- 230000002745 absorbent Effects 0.000 claims abstract description 57
- 150000003335 secondary amines Chemical class 0.000 claims abstract description 43
- 150000003141 primary amines Chemical class 0.000 claims abstract description 38
- 238000005262 decarbonization Methods 0.000 claims description 36
- 239000007789 gas Substances 0.000 claims description 32
- 238000012856 packing Methods 0.000 claims description 25
- 238000009833 condensation Methods 0.000 claims description 19
- 230000005494 condensation Effects 0.000 claims description 19
- 238000003795 desorption Methods 0.000 claims description 18
- 239000000443 aerosol Substances 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 11
- 238000006243 chemical reaction Methods 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 5
- 239000008400 supply water Substances 0.000 claims description 2
- 238000005516 engineering process Methods 0.000 abstract description 4
- 230000008569 process Effects 0.000 abstract description 4
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000005431 greenhouse gas Substances 0.000 abstract description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 22
- 239000000047 product Substances 0.000 description 14
- 239000000945 filler Substances 0.000 description 13
- 229910002092 carbon dioxide Inorganic materials 0.000 description 12
- 239000001569 carbon dioxide Substances 0.000 description 12
- BFSVOASYOCHEOV-UHFFFAOYSA-N 2-diethylaminoethanol Chemical compound CCN(CC)CCO BFSVOASYOCHEOV-UHFFFAOYSA-N 0.000 description 9
- 238000005507 spraying Methods 0.000 description 8
- 239000002245 particle Substances 0.000 description 6
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 239000007921 spray Substances 0.000 description 5
- 239000013589 supplement Substances 0.000 description 5
- 238000001926 trapping method Methods 0.000 description 5
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 description 4
- 229940058020 2-amino-2-methyl-1-propanol Drugs 0.000 description 4
- CBTVGIZVANVGBH-UHFFFAOYSA-N aminomethyl propanol Chemical compound CC(C)(N)CO CBTVGIZVANVGBH-UHFFFAOYSA-N 0.000 description 4
- 238000010992 reflux Methods 0.000 description 4
- 230000000630 rising effect Effects 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000005261 decarburization Methods 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- 238000004891 communication Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- QHJABUZHRJTCAR-UHFFFAOYSA-N n'-methylpropane-1,3-diamine Chemical compound CNCCCN QHJABUZHRJTCAR-UHFFFAOYSA-N 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 230000009469 supplementation Effects 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- ZZJZMFXTEAMDFR-UHFFFAOYSA-N 2-amino-2-methylpropan-1-ol;azane Chemical compound N.CC(C)(N)CO ZZJZMFXTEAMDFR-UHFFFAOYSA-N 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- LHIJANUOQQMGNT-UHFFFAOYSA-N aminoethylethanolamine Chemical compound NCCNCCO LHIJANUOQQMGNT-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 239000007857 degradation product Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 150000003384 small molecules Chemical class 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
-
- 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
- B01D53/1412—Controlling the absorption process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- 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
- B01D53/1493—Selection of liquid materials for use as 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
- B01D53/18—Absorbing units; Liquid distributors therefor
- B01D53/185—Liquid distributors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
本发明公开了一种用于逃逸胺回收和水平衡控制的碳捕集吸收塔、系统和方法，属于温室气体处理技术领域。所述碳捕集吸收塔包括塔体，所述塔体内从下至上设置有吸收层、控温层、一级胺回收层和二级胺回收层。本发明的吸收塔集成了吸收层、控温层、一级胺回收层和二级胺回收层，可以有效回收烟气中的水分和胺组分，通过设置控温层，以及采用一级胺回收层和二级胺回收层产生的回收液作为控温层中喷淋的控温洗液，实现对吸收剂中的逃逸胺组分和水分的补充，也降低了控温层的烟气温度，减少胺的逃逸，本发明可有效降低碳捕集过程中吸收剂补充量，大幅降低了吸收剂的损耗和运行成本以及胺逃逸造成的环境影响。
The present invention discloses a carbon capture absorption tower, system and method for fugitive amine recovery and water balance control, belonging to the field of greenhouse gas treatment technology. The carbon capture absorption tower comprises a tower body, in which an absorption layer, a temperature control layer, a primary amine recovery layer and a secondary amine recovery layer are arranged from bottom to top. The absorption tower of the present invention integrates the absorption layer, the temperature control layer, the primary amine recovery layer and the secondary amine recovery layer, and can effectively recover the moisture and amine components in the flue gas. By setting the temperature control layer and using the recovery liquid produced by the primary amine recovery layer and the secondary amine recovery layer as the temperature control washing liquid sprayed in the temperature control layer, the fugitive amine components and moisture in the absorbent are replenished, and the flue gas temperature of the temperature control layer is also reduced, and the escape of amines is reduced. The present invention can effectively reduce the amount of absorbent replenishment in the carbon capture process, greatly reducing the loss of the absorbent and the operating cost as well as the environmental impact caused by the escape of amines.
Description
Technical Field
The invention belongs to the technical field of greenhouse gas treatment, and particularly relates to a carbon trapping absorption tower, a system and a method for escaped amine recovery and water balance control.
Background
The large amount of carbon dioxide emissions causes global warming problems, and carbon dioxide capture technology is one of the key technologies for reducing carbon emissions. At present, the amine absorption method is the most mature and widely applied carbon trapping technology, amine molecules and carbon dioxide react in an absorption tower to absorb carbon dioxide in raw material gas, and decarbonized flue gas is discharged from the upper part of the absorption tower. And then heating and regenerating the absorption liquid in a desorption tower to separate carbon dioxide from the absorbent. The most important problems of the amine absorption method are high regeneration energy consumption, and related researches adopt amine components with low regeneration energy consumption and high volatility, such as 2-amino-2-methyl-1-propanol (AMP) and diethyl ethanolamine (DEEA), or adopt a low water type absorbent with high amine concentration, such as diethyl ethanolamine (DEEA) and hydroxyethyl ethylenediamine (AEEA) two-phase absorbent, and solvents such as diethyl ethanolamine (DEEA) and 3-Methylaminopropylamine (MAPA) or a mixed system thereof.
The novel absorbents can reduce energy consumption and simultaneously bring new amine volatilization escape problems, namely amine components are carried out of the trapping device into the atmosphere by flue gas due to easy volatilization, so that the loss of the amine components is caused, and the environmental safety is also influenced. In addition, as the temperature of the flue gas is increased after decarbonization by the absorption tower, the water content in the flue gas after decarbonization is increased, so that the water content in the amine absorbent is reduced, and the performance of the absorbent is affected. Therefore, stable operation of the carbon capture system also requires control of water balance. Prior studies focused on reducing the escape of amine components into the atmosphere, without recovery of amine components and moisture. Thus, there is a need to find a system and method that can recover and balance control the escaped amine component and moisture.
Disclosure of Invention
In order to overcome the problems in the prior art, one of the purposes of the invention is to provide a carbon capture absorption tower for recovery and water balance control of escaped amine, which can recover and balance control escaped amine components and moisture, so as to achieve the purposes of reducing amine loss and keeping the water balance of amine absorbent.
Another object of the present invention is to provide a carbon capturing system including the carbon capturing absorber.
A third object of the present invention is to provide a carbon capturing method using the above carbon capturing system.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows:
The invention provides a carbon capture absorption tower for escaped amine recovery and water balance control, which comprises a tower body, wherein an absorption layer, a temperature control layer, a primary amine recovery layer and a secondary amine recovery layer are arranged in the tower body from bottom to top;
the absorption layer is provided with a flue gas inlet, a lean solution inlet and a rich solution outlet, the temperature control layer is provided with a temperature control water inlet, the primary amine recovery layer comprises a primary filler layer and is provided with a primary water inlet and a primary water outlet, and the secondary amine recovery layer comprises a secondary filler layer and is provided with a secondary water inlet, a secondary water outlet and a tail gas outlet;
The lean solution inlet is used for introducing an absorbent, the flue gas inlet is used for introducing flue gas, the flue gas forms decarburized flue gas after passing through the absorption layer, and the decarburized flue gas sequentially enters the temperature control layer, the primary amine recovery layer and the secondary amine recovery layer and is finally discharged from the tail gas outlet;
the temperature control water inlet is respectively communicated with the primary water outlet and the secondary water outlet, the temperature control water inlet is used for being introduced with a temperature control Wen Xiye, the temperature control washing liquid is used for reducing the temperature of the decarburization flue gas, the primary water inlet is used for being introduced with a primary washing liquid, formed primary recovery liquid is discharged through the primary water outlet, part of the primary recovery liquid enters the temperature control layer through the temperature control water inlet as a temperature control Wen Xiye, the secondary water inlet is used for being introduced with a secondary washing liquid, formed secondary recovery liquid is discharged through the secondary water outlet, and part of the secondary recovery liquid enters the temperature control layer through the temperature control water inlet as a temperature control Wen Xiye.
In some specific embodiments of the invention, the primary water outlet is also communicated with the primary water inlet through a first pipeline, a primary water washing pump and a primary water washing cooler are arranged on the first pipeline, the primary water outlet is communicated with the temperature control water inlet through a second pipeline, the secondary pipeline is provided with a primary water washing pump, a primary water washing cooler and a primary water return valve, after the primary recovery liquid is discharged through the primary water outlet, part of the primary recovery liquid returns to the primary amine recovery layer through the first pipeline, and the other part of the primary recovery liquid enters the temperature control layer through the second pipeline;
the secondary water outlet is also communicated with the secondary water inlet through a third pipeline, the third pipeline is provided with a secondary water pump and a secondary water cooler, the secondary water outlet is communicated with the temperature control water inlet through a fourth pipeline, the fourth pipeline is provided with a secondary water pump, a secondary water cooler and a secondary water return valve, after the secondary recovery liquid is discharged through the secondary water outlet, part of the secondary recovery liquid returns to the secondary amine recovery layer through the third pipeline, and the other part of the secondary recovery liquid enters the temperature control layer through the fourth pipeline.
In some embodiments of the present invention, the temperature-controlled water inlet is further in communication with a water replenishment valve through a fifth conduit, the water replenishment valve being configured to introduce replenishment moisture to the temperature-controlled layer.
In some specific embodiments of the invention, a lean liquid distributor, a temperature-control liquid distributor, a primary liquid distributor and a secondary liquid distributor are further arranged in the tower body and are respectively connected with the lean liquid inlet, the temperature-control water inlet, the primary water inlet and the secondary water inlet, a primary liquid collector and a secondary liquid collector are further arranged in the tower body and are respectively connected with the primary water outlet and the secondary water outlet, and the temperature-control layer and the absorption layer are mutually communicated.
In some embodiments of the present invention, the absorption layer further includes an intermediate liquid collector and an intermediate liquid distributor disposed in the tower body from top to bottom, the intermediate liquid collector and the intermediate liquid distributor are located between the lean liquid inlet and the rich liquid outlet, the intermediate liquid collector and the intermediate liquid distributor are connected through a sixth pipeline, an intermediate cooling pump and an intermediate cooler are disposed on the sixth pipeline, and the intermediate liquid collector is used for collecting the absorbent after temperature rising, and after temperature lowering through the sixth pipeline, the absorbent is introduced into the intermediate liquid distributor.
The second aspect of the invention provides a carbon capture system for escaped amine recovery and water balance control, which comprises a desorption tower and an absorption tower according to any one of claims 1-5, wherein the desorption tower comprises a product gas outlet, the product gas outlet is communicated with the temperature control water inlet through a seventh pipeline, a condensation recovery device is arranged on the seventh pipeline, the product gas generated by the desorption tower is discharged through the product gas outlet, a condensation separation recovery liquid is formed through the condensation recovery device, and the condensation separation recovery liquid enters the temperature control layer through the temperature control water inlet as a control Wen Xiye.
A third aspect of the present invention provides a carbon capture method for fugitive amine recovery and water balance control, implemented with the carbon capture system of the second aspect of the present invention, comprising the steps of:
S1, introducing flue gas into the flue gas inlet, introducing an absorbent into the lean solution inlet, and carrying out decarburization reaction on the flue gas and the absorbent to form decarburized flue gas and rich solution, wherein the decarburized flue gas enters the temperature control layer, and the rich solution is discharged from the rich solution outlet;
S2, introducing control Wen Xiye into the temperature control inlet, wherein the decarbonization flue gas enters the temperature control layer, contacts with the control Wen Xiye and then enters the primary amine recovery layer, and the temperature control washing liquid enters the absorption layer after contacting with the decarbonization flue gas to realize recovery of an absorbent and water supplement;
s3, adopting a method S3-1 or a method S3-2;
The method S3-1 comprises the steps of introducing a primary water washing liquid into the primary water inlet, enabling the decarbonization flue gas to enter the primary amine recovery layer, enabling the primary packing layer to contact with the primary washing liquid and then enter the secondary amine recovery layer, enabling the primary washing liquid to contact with the decarbonization flue gas to form a primary recovery liquid, and enabling part of the primary recovery liquid to serve as a temperature control washing liquid to be introduced into the temperature control layer;
the method S3-2 comprises the steps of introducing a primary water washing liquid into the primary water inlet to moisten the primary packing layer, stopping introducing the primary water washing liquid, enabling the decarbonized flue gas to enter the primary amine recovery layer, contacting the moistened primary packing layer, and then entering the secondary amine recovery layer;
S4, introducing a secondary water washing liquid into the secondary water inlet, enabling the decarbonization flue gas to enter the secondary amine recovery layer, enabling the decarbonization flue gas to contact the secondary washing liquid at the secondary packing layer, and then discharging the decarbonization flue gas through the tail gas outlet, wherein a secondary recovery liquid is formed after the secondary washing liquid contacts the decarbonization flue gas, and part of the secondary recovery liquid is used as a temperature control washing liquid to be introduced into the temperature control layer.
Step S3 employs method S3-1 when the absorber is predominantly gaseous in form and step S3 employs method S3-2 when the absorber is predominantly aerosol in form.
In some embodiments of the present invention, in the method S3-1, the ratio of the flow rate of the primary water washing liquid to the flow rate of the decarbonized flue gas in the primary amine recovery layer is 1 (400-3000).
In some embodiments of the present invention, in step S4, a ratio of an inlet flow rate of the secondary washing liquid to an inlet flow rate of the decarbonized flue gas in the secondary amine recovery layer is 1 (400-3000).
In some embodiments of the invention, the temperature of the flue gas is 30-50 ℃.
In some embodiments of the invention, the temperature of the decarbonized flue gas after passing through the absorption layer is 60-70 ℃.
In some embodiments of the present invention, the temperature of the decarbonized flue gas after passing through the temperature control layer is 40 to 60 ℃.
In some embodiments of the invention, the temperature of the decarbonized flue gas after passing through the primary amine recovery layer is 40-50 ℃.
In some embodiments of the invention, the temperature of the decarbonized flue gas after passing through the secondary amine recovery layer is 35-40 ℃.
In some embodiments of the invention, the decarbonated flue gas has an amine concentration of 10ppm or less after passing through the secondary amine recovery layer.
The invention has the beneficial effects that the absorption tower is integrated with the absorption layer, the temperature control layer, the primary amine recovery layer and the secondary amine recovery layer, so that the moisture and the amine components in the flue gas can be effectively recovered, and the recovery liquid generated by the primary amine recovery layer and the secondary amine recovery layer is used as the control Wen Xiye sprayed in the temperature control layer, thereby realizing the supplement of the escaped amine components and the moisture in the absorbent, reducing the flue gas temperature of the temperature control layer and the escape of amine.
Specifically, compared with the prior art, the invention has the following advantages:
1. The amine recovery layer can recover the amine component in a mode of a two-stage wet bed or a two-stage dry bed, wherein the two-stage wet bed is that the first-stage amine recovery layer and the second-stage amine recovery layer are both sprayed with washing liquid, the amine component is recovered through twice washing, the first-stage dry bed and the second-stage wet bed are that the first-stage amine recovery layer is only sprayed with part of the washing liquid to obtain a wet first-stage packing layer as a first-stage dry bed, the second-stage amine recovery layer is sprayed with the washing liquid as a second-stage wet bed, the growth of aerosol particles of the amine component in the space of the first-stage dry bed is enlarged, and the aerosol particles are easier to be recovered in the second-stage wet bed through water flow spraying with a certain flow. The specific amine recovery layer adopted is determined according to the amine escape condition of the absorber, wherein the primary dry bed and the secondary wet bed are aimed at the amine escape mainly discharged in the form of aerosol, and the secondary wet bed is aimed at the amine escape mainly discharged in the form of gas. The amine recovery layer provided by the invention is compatible with the arrangement of a two-stage wet bed and a one-stage dry bed, and can adapt to more absorbent types and more complex working conditions.
2. The carbon trapping system of the invention is also provided with a treatment for condensing, separating and recovering liquid generated in the condensing and recovering of the product gas of the desorption tower, the condensing, separating and recovering liquid is conveyed to a temperature control layer for spraying instead of the traditional mode (recovered to the desorption tower), and in addition, liquid separated by a gas-liquid separator after the carbon dioxide compresses the precooler also enters the temperature control layer. The low-temperature condensation separation recovery liquid of the product gas of the desorption tower is conveyed to the amine recovery liquid instead of the desorption tower, so that the heat consumption is saved.
3. The spray water of the absorption tower amine recovery layer and the low-temperature condensation separation recovery liquid of the desorption tower product gas are both recycled to form the spray liquid of the temperature control layer, so that the water balance control of the system is facilitated, and the running reliability of the system is improved.
Drawings
FIG. 1 is a carbon capture system for fugitive amine recovery and water balance control provided by an embodiment of the present invention.
Wherein, the device comprises a 100-absorption tower; 110-tower body; 120-an absorbent layer; 121-flue gas inlet, 122-lean liquid inlet, 123-rich liquid outlet, 124-lean liquid distributor, 125-intermediate liquid collector, 126-intermediate liquid distributor, 127-intermediate cooling pump, 128-intermediate cooler, 129-first absorption filler layer, 1210-second absorption filler layer, 130-temperature control layer, 131-temperature control water inlet, 132-temperature control liquid distributor, 133-temperature control filler layer, 140-primary amine recovery layer, 141-primary filler layer, 142-primary water inlet, 143-primary water outlet, 144-primary water pump, 145-primary water wash cooler, 146-primary water return valve, 147-primary liquid distributor, 148-primary liquid collector, 150-secondary amine recovery layer, 151-secondary filler layer, 152-secondary water inlet, 153-secondary water outlet, 154-secondary water wash pump, 155-secondary water cooler, 156-secondary water valve, 157-secondary liquid distributor, 158-secondary liquid collector, 161-outlet, 161-162-rich liquid recovery layer, 163-lean liquid exchanger, 164-primary water return valve, 146-primary water inlet, 35-primary water outlet, 144-primary water pump, 150-secondary amine recovery layer, 146-secondary water return valve, 146-secondary water inlet, 152-secondary water outlet, 159-secondary water outlet, 158-secondary liquid collector, and water outlet, 161-rich liquid recovery layer, 162-primary water inlet, 163-primary water collector, and the product, are desorbed and the products are, and the and are, are and the and are, are and the and are, and the and are, and, column, and column, and column, column The separator, 253-reflux pump, 254-carbon dioxide compression precooler, 255-second gas-liquid separator, 261-reboiler, 262-bottom of desorption tower, 263-lean liquid pump.
Detailed Description
The present invention will be described in further detail with reference to specific examples. It is also to be understood that the following examples are given solely for the purpose of illustration and are not to be construed as limitations on the scope of the invention, since various modifications and adaptations may be made by those skilled in the art in light of the teachings herein. The specific process parameters and the like described below are also merely examples of suitable ranges, i.e., one skilled in the art can make a selection within the suitable ranges by the description herein and are not intended to be limited to the specific data described below. The starting materials, reagents or apparatus used in the following examples and comparative examples were obtained from conventional commercial sources or by known methods unless otherwise specified.
As shown in fig. 1, an embodiment of the present invention provides a carbon capture system for escaped amine recovery and water balance control, including an absorber tower 100 and a desorber tower 200.
In some embodiments of the invention, the absorption tower 100 comprises a tower body 110, wherein an absorption layer 120, a temperature control layer 130, a primary amine recovery layer 140 and a secondary amine recovery layer 150 are arranged in the tower body 100 from bottom to top, the absorption layer 120 is provided with a flue gas inlet 121, a lean solution inlet 122 and a rich solution outlet 123, the temperature control layer 130 is provided with a temperature control water inlet 131, the primary amine recovery layer 140 comprises a primary packing layer 141 and is provided with a primary water inlet 142 and a primary water outlet 143, the secondary amine recovery layer 150 comprises a secondary packing layer 151 and is provided with a secondary water inlet 152, a secondary water outlet 153 and a tail gas outlet 159, the lean solution inlet 122 is used for introducing an absorbent, the flue gas inlet 121 is used for introducing flue gas, the flue gas forms decarburized flue gas after passing through the absorption layer 120, the decarburized flue gas sequentially enters the temperature control layer 130, the primary amine recovery layer 140 and the secondary amine recovery layer 150, and finally is discharged from the tail gas outlet 159, the temperature control water inlet 131 is respectively communicated with the primary water outlet 153, the temperature control water inlet 131 is used for introducing a temperature control Wen Xiye, the primary water inlet 142 is used for reducing the temperature, the primary water inlet 142 is used for introducing the temperature of the flue gas, the secondary water is formed through the secondary water inlet 153, and the secondary water outlet 153 is used as a temperature control water outlet portion of the temperature control water through the temperature control layer is discharged through the temperature control water inlet 153, and the secondary water inlet 153 is used for recycling the secondary water.
In some embodiments of the invention, a mist eliminator is also provided at the tail gas outlet 159 at the top of the absorber tower. The demister is used for reducing tiny liquid drops carried by flue gas and can be arranged according to actual needs.
In some embodiments of the invention, the primary water outlet 143 is also communicated with the primary water inlet 142 through a first pipeline, a primary water pump 144 and a primary water cooler 145 are arranged on the first pipeline, the primary water outlet 143 is communicated with the temperature control water inlet 131 through a second pipeline, the primary water pump 144, the primary water cooler 145 and a primary water return valve 146 are arranged on the second pipeline, after the primary recovery liquid is discharged through the primary water outlet 143, a part of the primary recovery liquid returns to the primary amine recovery layer 140 through the first pipeline, and another part of the primary recovery liquid enters the temperature control layer 130 through the second pipeline.
In some embodiments of the invention, the secondary water outlet 153 is also communicated with the secondary water inlet 152 through a third pipeline, a secondary water washing pump 154 and a secondary water washing cooler 155 are arranged on the third pipeline, the secondary water outlet 153 is communicated with the temperature control water inlet 131 through a fourth pipeline, the secondary water washing pump 154, the secondary water washing cooler 155 and a secondary water return valve 156 are arranged on the fourth pipeline, after the secondary recovery liquid is discharged through the secondary water outlet 153, a part of the secondary recovery liquid returns to the secondary amine recovery layer 150 through the third pipeline, and another part of the secondary recovery liquid enters the temperature control layer 130 through the fourth pipeline.
In some embodiments of the present invention, the temperature-controlled water inlet 131 is further in communication with a water replenishment valve 161 via a fifth conduit, the water replenishment valve 161 being configured to supply water to the temperature-controlled layer 130.
In some embodiments of the invention, a lean liquid distributor 124, a temperature-control liquid distributor 132, a primary liquid distributor 147 and a secondary liquid distributor 157 are also arranged in the tower body and are respectively connected with the lean liquid inlet 122, the temperature-control water inlet 131, the primary water inlet 142 and the secondary water inlet 152, a primary liquid collector 148 and a secondary liquid collector 158 are also arranged in the tower body and are respectively connected with the primary water outlet 143 and the secondary water outlet 153, and the temperature-control layer 130 and the absorption layer 120 are mutually communicated.
In some embodiments of the present invention, the absorbing layer 120 further includes an intermediate liquid collector 125 and an intermediate liquid distributor 126 disposed in the tower from top to bottom, the intermediate liquid collector 125 and the intermediate liquid distributor 126 are located between the lean liquid inlet 122 and the rich liquid outlet 123, the intermediate liquid collector 125 and the intermediate liquid distributor 126 are connected through a sixth pipeline, an intermediate cooling pump 127 and an intermediate cooler 128 are disposed on the sixth pipeline, and the intermediate liquid collector 125 is used for collecting the absorbent after temperature rising, and after temperature lowering through the sixth pipeline, the absorbent is introduced into the intermediate liquid distributor 126.
In some embodiments of the present invention, a first absorbent packing layer 129 is further disposed intermediate the lean liquid distributor 124 and the intermediate liquid collector 125, and a second absorbent packing layer 1210 is further disposed intermediate the intermediate liquid distributor 126 and the rich liquid outlet 123.
In some embodiments of the present invention, a temperature-controlled filler layer 133 is also disposed below the temperature-controlled liquid distributor 132.
In some embodiments of the present invention, rich liquid outlet 123 is connected to lean liquid inlet 122 via rich liquid pump 162, lean rich liquid heat exchanger 163, liquid reservoir 164, feed pump 165 and feed cooler 166 in sequence, liquid reservoir 164 is also connected to an amine make-up valve 167, and amine make-up valve 167 is used to supplement liquid reservoir 164 with amine components.
In some embodiments of the invention, the desorption tower 200 comprises a first liquid distributor 210 of the desorption tower, a second liquid distributor 220 of the desorption tower, a liquid collector 230 of the desorption tower, a product gas outlet 240 and a plurality of packing layers, wherein the product gas outlet 240 is communicated with a temperature control water inlet 131 through a seventh pipeline, a condensation recovery device 250 is arranged on the seventh pipeline, the product gas generated by the desorption tower is discharged through the product gas outlet 240, a condensation separation recovery liquid is formed through the condensation recovery device 250, and the condensation separation recovery liquid enters the temperature control layer 130 through the temperature control water inlet 131 as a temperature control washing liquid.
In some embodiments of the present invention, the condensation recovery apparatus 250 comprises a condenser 251, a first gas-liquid separator 252, a reflux pump 253, a carbon dioxide compression precooler 254, and a second gas-liquid separator 255, wherein the product gas outlet 240, the condenser 251, the first gas-liquid separator 252, the reflux pump 253 and the temperature control water inlet 131 are sequentially communicated, the first gas-liquid separator 252 is sequentially communicated with the carbon dioxide compression precooler 254, the second gas-liquid separator 255 and the reflux pump 253, the second gas-liquid separator 255 is also communicated with a carbon dioxide compression system, and the separated carbon dioxide gas is introduced into the carbon dioxide compression system.
In some embodiments of the invention, the stripper column liquid collector 230 is connected with a reboiler 261 and a stripper column bottom 262 in sequence, the stripper column bottom 262 is connected with a lean liquid pump 263, a lean and rich liquid heat exchanger 163 and a liquid storage tank 164 in sequence, and the liquid collected by the stripper column liquid collector 230 contains part of amine components, so that the recovery of the amine components is realized through the route.
The embodiment of the invention also provides a carbon trapping method for escaped amine recovery and water balance control, which is realized by the carbon trapping system, and comprises the following steps of:
S1, introducing flue gas into a flue gas inlet 121, introducing an absorbent into a lean solution inlet 122, and carrying out decarburization reaction on the flue gas and the absorbent to form decarburized flue gas and rich solution, wherein the decarburized flue gas enters a temperature control layer 130, and the rich solution is discharged from a rich solution outlet 123;
S2, introducing control Wen Xiye into the temperature control water inlet 131, enabling the decarbonization flue gas to enter the temperature control layer 130, contact with the control Wen Xiye, and then enter the primary amine recovery layer 140, enabling the temperature control washing liquid to enter the absorption layer 130 after contacting with the decarbonization flue gas, and realizing recovery of the absorbent and water supplement;
s3, adopting a method S3-1 or a method S3-2;
The method S3-1 comprises the steps of introducing primary water washing liquid into a primary water inlet 142, allowing decarbonization flue gas to enter a primary amine recovery layer 140, contacting the primary washing liquid at a primary packing layer 141 and then entering a secondary amine recovery layer 150, forming primary recovery liquid after the primary washing liquid contacts with decarbonization flue gas, and introducing part of the primary recovery liquid into a temperature control layer 130 as temperature control washing liquid;
The method S3-2 comprises the steps of introducing primary water washing liquid into a primary water inlet 142 to moisten a primary packing layer 141, stopping introducing primary water washing liquid, allowing decarbonized flue gas to enter a primary amine recovery layer 140, contacting the moistened primary packing layer 141, and allowing the decarbonized flue gas to enter a secondary amine recovery layer 150;
s4, introducing secondary water washing liquid into the secondary water inlet 152, enabling the decarbonization flue gas to enter the secondary amine recovery layer 150, enabling the decarbonization flue gas to contact the secondary washing liquid at the secondary packing layer 151 and then discharging the decarbonization flue gas through the tail gas outlet 159, enabling the secondary washing liquid to contact the decarbonization flue gas to form secondary recovery liquid, and enabling part of the secondary recovery liquid to serve as temperature control washing liquid to be introduced into the temperature control layer 130.
In the method, the primary amine recovery layer and the secondary amine recovery layer of the method S3-1 are both wet bed to recover the amine components, namely the amine components are recovered through two stages of wet beds, the primary amine recovery layer of the method S3-2 is a dry bed to recover the amine components, and the secondary amine recovery layer is a wet bed to recover the amine components, namely the amine components are recovered through a first dry bed and a first wet bed. For some amine components, when the primary water wash is used only to wet the primary filler layer and the amine component is recovered with a dry bed containing the wet primary filler layer, the aerosol particles of the amine component grow larger in the space of the dry bed and are easier to recover in the secondary amine recovery layer by spraying with a stream of water at a certain flow rate.
In some embodiments of the invention, step S3 employs method S3-1 when the absorber is predominantly in gaseous form and step S3 employs method S3-2 when the absorber is predominantly in aerosol form.
The mechanism of amine escape is complex, is greatly influenced by factors such as flue gas conditions, working conditions, amine molecular chemical structures and the like, and generally has two forms of escape, gaseous escape and aerosol escape, when the gaseous escape is taken as the main part, a two-stage water washing method S3-1 is adopted, when the aerosol escape is taken as the main part, a one-stage dry bed and two-stage wet bed is adopted, namely a method S3-2, in the actual production process, flue gas is required to be monitored, and the method S3-1 or the method S3-2 is regulated and selected according to the monitoring result.
In some non-limiting examples of the invention, the absorbent that readily escapes in gaseous form primarily includes N-Methyldiethanolamine (MDEA), diethylaminoethanol (DEEA), and the like.
In some non-limiting examples of the invention, the absorbent that readily escapes as an aerosol includes ethanolamine (MEA), 2-amino-2-methyl-1-propanol (AMP), and the like.
In some embodiments of the invention, in the method S3-1, the ratio of the flow rate of the primary washing liquid to the flow rate of the decarbonized flue gas in the primary amine recovery layer is 1 (400-3000).
In some embodiments of the present invention, in step S4, the ratio of the flow rate of the secondary washing liquid to the flow rate of the decarbonized flue gas in the secondary amine recovery layer is 1 (400 to 3000).
The flow rate of the primary water washing liquid and the secondary water washing liquid can influence the amine recovery effect, and the amine recovery effect is improved along with the increase of the flow rate of the water washing liquid, but the marginal effect is reduced, and the amine recovery effect is difficult to improve after the marginal effect reaches a certain flow rate.
In some embodiments of the invention, the flue gas is pre-treated at the flue gas inlet, by which the temperature of the flue gas is reduced.
In some embodiments of the invention, the temperature of the flue gas is 30-50 ℃, more specifically 35-45 ℃, non-limiting examples being 38 ℃, 40 ℃, or 42 ℃.
In some embodiments of the invention, the temperature of the decarbonized flue gas after passing through the absorber layer is 60-70 ℃, more specifically 62-68 ℃, non-limiting examples being 64 ℃, 65 ℃, or 66 ℃.
In some embodiments of the present invention, the temperature of the decarbonized flue gas after passing through the temperature control layer is 50-60 ℃, more specifically 52-58 ℃, non-limiting examples are 54 ℃, 55 ℃, or 56 ℃.
In some embodiments of the invention, the temperature of the decarbonized flue gas after passing through the primary amine recovery layer is 40-50 ℃, such as, without limitation, 42 ℃, 45 ℃, or 48 ℃.
In some embodiments of the present invention, the temperature of the decarbonized flue gas after passing through the secondary amine recovery layer is 35-40 ℃, such as 36 ℃, 37 ℃, 38 ℃, or 39 ℃ by way of non-limiting example.
In some embodiments of the invention, the decarbonated flue gas has an amine concentration of 10ppm or less after passing through the secondary amine recovery layer.
In some embodiments of the invention, the temperature control washing liquid of the temperature control layer consists of three parts, wherein the first part is a first recovery liquid and a second recovery liquid from the first amine recovery layer and the second amine recovery layer, amine components and moisture carried in decarbonized flue gas are recovered into water washing water and are sprayed into the temperature control layer, so that the replenishing of escaped amine components and moisture in the absorbent is realized, the flue gas temperature of the temperature control layer is reduced, the escape of amine is reduced, the second part is a condensation separation recovery liquid separated by a condensation recovery device comprising a first gas-liquid separator and a second gas-liquid separator, the part is mainly water and a certain amount of amine, and the third part is replenishing moisture introduced from a water replenishing valve.
Further description is provided below in connection with more specific examples.
In the following examples, the overall amine recovery was obtained by the following steps:
The amine concentration in the decarbonated flue gas exiting the absorber layer 120 is first measured and denoted as C1, then the amine concentration in the flue gas exiting the tail gas outlet 159 is measured and denoted as C2, and finally the overall amine recovery is calculated as total amine recovery = (C1-C2)/c1×100%.
Example 1
The carbon trapping method for escaped amine recovery and water balance control is realized by a carbon trapping system shown in fig. 1, and the absorbent adopted in the example is diethylaminoethanol containing volatile amine, and specifically comprises the following steps:
(1) The flue gas of the coal-fired power plant is cooled to about 40 ℃ by the pretreatment tower, the formed saturated wet flue gas enters the absorption layer 120 in the absorption tower 100, the absorbent extracted by the liquid storage tank 164 is cooled to 40 ℃ by the feed pump 165 and then is sprayed into the absorption layer 120 in the absorption tower 100, CO 2 in the flue gas reacts with the absorbent, the temperature of the flue gas and the absorbent rises due to heat release of the reaction, the CO 2 in the flue gas is absorbed by the absorbent to form decarburized flue gas, the temperature rises to about 65 ℃, the flue gas brings additional moisture and amine components from the absorbent by the rising of the temperature, and then the decarburized flue gas enters the temperature control layer 130.
(2) The decarbonization flue gas enters the temperature control layer 130 after coming out of the absorption layer 120, the temperature control layer 130 sprays low-temperature control Wen Xiye (the temperature control washing liquid contains an amine component, is an amine recovery liquid and comprises primary water washing liquid, secondary water washing liquid, condensation separation liquid collection and a small amount of supplementary water), the temperature control washing liquid and the decarbonization flue gas are contacted in the temperature control packing layer 133 through spraying, so that the temperature of the decarbonization flue gas is reduced to about 55 ℃, and the temperature control washing liquid simultaneously enters the absorption layer 120 and is mixed with sprayed lean liquid, so that the recovery of amine and the supplementation of water are realized, and the composition of an absorbent is kept stable. The amine concentration in the flue gas can be reduced by about 30-40% through the temperature control layer 130.
(3) And then the decarbonization flue gas enters a primary amine recovery layer 140, washing water is used as primary washing liquid to be in contact reaction with the decarbonization flue gas in a primary packing layer 141 through the spraying of a primary liquid distributor 147, the flow ratio of the flue gas to the primary washing liquid is 700:1, amine components and water vapor in the flue gas are absorbed by the washing water, the temperature of the washing water rises, the washing water falls into a primary liquid collector 148 to form primary recovery liquid, a primary water washing pump 144 pumps the primary recovery liquid into a primary water washing cooler 145 to cool and then sprays the primary recovery liquid through the primary liquid distributor 147 again for washing, and the excessive part of the primary recovery liquid becomes a control Wen Xiye and is conveyed to the temperature control layer 130 through a primary water return valve 146. At this stage, the decarbonization flue gas temperature is reduced to 40-50 ℃, and the amine concentration in the flue gas can be further reduced by about 75-85%.
(4) And then the decarbonization flue gas enters a secondary amine recovery layer 150, washing water is used as secondary washing liquid to be in contact reaction with the decarbonization flue gas in a secondary packing layer 151 through the spraying of a secondary liquid distributor 157, most of amine and degradation products thereof in the decarbonization flue gas with the flow ratio of the flue gas to the secondary washing liquid being 1000:1 are absorbed by the secondary washing liquid, the secondary washing liquid falls into a secondary liquid collector 158 to form secondary recovery liquid, a secondary washing pump 154 pumps the secondary recovery liquid into a secondary washing cooler 155, part of the secondary recovery liquid is sprayed again through the secondary liquid distributor 157 to be washed, and the rest part is controlled Wen Xiye and is conveyed to the temperature control layer 130 through a secondary water return valve 156. In this stage, the temperature of the decarbonized flue gas is reduced to 35-40 ℃, and the amine concentration in the flue gas can be further reduced by 70-80%, so that the amine concentration is controlled below 10 ppm.
(5) The decarbonated flue gas is then discharged from a tail gas outlet 159 at the top of the absorber. Thereby, the amine component and the moisture carried in the decarbonized flue gas are mostly recovered. The carbon trapping method for escaped amine recovery and water balance control realizes the benefits of water supplementing, amine component recovery in the absorbent, pollution reduction and the like, and the overall amine recovery rate is more than 95%.
Example 2
A carbon capture method for fugitive amine recovery and water balance control, implemented using a carbon capture system as shown in fig. 1, the absorbent employed in this example being small molecule amine 2-amino-2-methyl-1-propanol or ethanolamine containing readily aerosol, comprising the steps of:
(1) The flue gas of the coal-fired power plant is cooled to about 40 ℃ by the pretreatment tower, the formed saturated wet flue gas enters the absorption layer 120 in the absorption tower 100, the absorbent extracted by the liquid storage tank 164 is cooled to 40 ℃ by the feed pump 165 and then is sprayed into the absorption layer 120 in the absorption tower 100, CO 2 in the flue gas reacts with the absorbent, the temperature of the flue gas and the absorbent rises due to heat release of the reaction, the CO 2 in the flue gas is absorbed by the absorbent to form decarburized flue gas, the temperature rises to about 65 ℃, the flue gas brings additional moisture and amine components from the absorbent by the rising of the temperature, and then the decarburized flue gas enters the temperature control layer 130.
(2) The decarbonization flue gas enters the temperature control layer 130 after coming out of the absorption layer 120, the temperature control layer 130 sprays low-temperature control Wen Xiye (the temperature control washing liquid contains an amine component, is an amine recovery liquid and comprises primary water washing liquid, secondary water washing liquid, condensation separation liquid collection and a small amount of supplementary water), the temperature control washing liquid and the decarbonization flue gas are contacted in the temperature control packing layer 133 through spraying, so that the temperature of the decarbonization flue gas is reduced to about 55 ℃, and the temperature control washing liquid simultaneously enters the absorption layer 120 and is mixed with sprayed lean liquid, so that the recovery of amine and the supplementation of water are realized, and the composition of an absorbent is kept stable. The amine concentration in the flue gas can be reduced by about 30-40% by the temperature control layer 130.
(3) And then the decarbonized flue gas enters the primary amine recovery layer 140, and a small amount of washing water is sprayed on the surface of the primary filler layer 141 to wet the surface of the primary filler layer, so that the filler layer is used as a dry bed, a space is provided for the length of the aerosol particles of the amine component, and the removal of the aerosol particles in the secondary amine recovery layer 150 is facilitated.
(4) And then the decarbonization flue gas enters a secondary amine recovery layer 150, washing water is used as secondary washing liquid to be in contact reaction with the decarbonization flue gas in a secondary packing layer 151 through the spraying of a secondary liquid distributor 157, the flow ratio of the flue gas to the secondary washing liquid is 600:1, the particles of amine components in the decarbonization flue gas become large after the dry bed growth, the amine components are easily absorbed by the washing water, the temperature of the decarbonization flue gas is reduced, the moisture in the decarbonization flue gas enters the secondary washing liquid, the secondary washing liquid is collected by a secondary liquid collector 158 to form secondary recovery liquid, a secondary washing pump 154 pumps the secondary recovery liquid into a secondary washing cooler 155, part of the secondary recovery liquid is sprayed again through the secondary liquid distributor 157 to be washed, and the rest is Wen Xiye to be transported to a temperature control layer 130 through a secondary water return valve 156. In this stage, the temperature of the decarbonized flue gas is reduced to about 35-40 ℃, and the amine concentration in the decarbonized flue gas can be further reduced by more than 90%, so that the amine concentration is controlled below 10 ppm.
(5) The decarbonated flue gas is then discharged from a tail gas outlet 159 at the top of the absorber. Thereby, the amine component and the moisture carried in the decarbonized flue gas are mostly recovered. The carbon trapping method for escaped amine recovery and water balance control realizes the benefits of water supplementing, amine component recovery in the absorbent, pollution reduction and the like, and the overall amine recovery rate is more than 95%.
By adopting the carbon trapping method provided by the embodiment of the invention, the supplement amount of the absorbent in the carbon trapping process can be reduced by 20-70%.
In summary, the absorption tower provided by the invention integrates the absorption layer, the temperature control layer, the primary amine recovery layer and the secondary amine recovery layer, so that moisture and amine components in the flue gas can be effectively recovered, and the recovery liquid generated by the primary amine recovery layer and the secondary amine recovery layer is used as the control Wen Xiye sprayed in the temperature control layer, so that the replenishing of escaped amine components and moisture in the absorbent is realized, the flue gas temperature of the temperature control layer is also reduced, the escape of amine is reduced, the replenishing amount of the absorbent in the carbon capturing process can be effectively reduced, and the loss and the running cost of the absorbent are greatly reduced.
Claims (10)
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| CN219744393U (en) * | 2023-04-10 | 2023-09-26 | 中国华电科工集团有限公司 | Flue gas pretreatment tower and carbon dioxide trapping system |
| CN117323805A (en) * | 2023-11-14 | 2024-01-02 | 浙江天地环保科技股份有限公司 | Organic amine CO based on small molecule organic solvent 2 Absorbent emission control device |
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| CN114345098A (en) * | 2022-01-10 | 2022-04-15 | 浙江大学嘉兴研究院 | A kind of method and system for CO2 capture absorbent decomposition inhibition and efficient pollution reduction |
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