CN117919895A - Low-cost low-concentration CO2Trapping system and method - Google Patents
Low-cost low-concentration CO2Trapping system and method Download PDFInfo
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- CN117919895A CN117919895A CN202211264122.2A CN202211264122A CN117919895A CN 117919895 A CN117919895 A CN 117919895A CN 202211264122 A CN202211264122 A CN 202211264122A CN 117919895 A CN117919895 A CN 117919895A
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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
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
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- 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
- B01D2252/20478—Alkanolamines
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- 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
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- General Engineering & Computer Science (AREA)
- Gas Separation By Absorption (AREA)
Abstract
本发明属于地面工程技术领域CCUS技术领域，具体涉及一种低成本、低浓度CO2的捕集系统及方法。其中，捕集系统包括依次连接的吸收塔、贫富液热交换器、再生塔和热交换器；所述热交换器设有富液进口Ⅰ、富液出口Ⅰ、高温蒸汽入口与蒸汽凝液出口；所述高温蒸汽为SAGD采出液经蒸汽分离器分离出的高温蒸汽。所述富液进口Ⅰ、富液出口Ⅰ分别与再生塔连接，SAGD采出液分离后的高温蒸汽通过所述高温蒸汽入口进入所述热交换器，与富液换热完成后得到的蒸汽凝液经蒸汽凝液出口输出。本次发明应用场景为流化床燃烧后气体的CO2捕集，采用醇胺法，针对CO2解吸的条件，以运行成本最低为目标进行流程的优化，以实现低成本、低浓度的CO2捕集。
The present invention belongs to the field of ground engineering technology and CCUS technology, and specifically relates to a low-cost, low-concentration CO2 capture system and method. Among them, the capture system includes an absorption tower, a lean-rich liquid heat exchanger, a regeneration tower and a heat exchanger connected in sequence; the heat exchanger is provided with a rich liquid inlet I, a rich liquid outlet I, a high-temperature steam inlet and a steam condensate outlet; the high-temperature steam is the high-temperature steam separated from the SAGD produced liquid by a steam separator. The rich liquid inlet I and the rich liquid outlet I are respectively connected to the regeneration tower, and the high-temperature steam after the separation of the SAGD produced liquid enters the heat exchanger through the high-temperature steam inlet, and the steam condensate obtained after the heat exchange with the rich liquid is output through the steam condensate outlet. The application scenario of this invention is the CO2 capture of gas after fluidized bed combustion. The amine method is used. According to the conditions of CO2 desorption, the process is optimized with the goal of minimizing the operating cost to achieve low-cost and low-concentration CO2 capture.
Description
Technical Field
The invention belongs to the technical field of CCUS (continuous casting unit) in the technical field of ground engineering, and particularly relates to a low-cost low-concentration CO 2 capturing system and method.
Background
The emission source of the Xinjiang oilfield CO 2 is mainly an oilfield steam injection boiler, the emitted CO 2 is low in concentration, the emission concentration of the coal-fired boiler CO 2 is 8% -12%, and the emission concentration of the gas-fired boiler CO 2 is 3% -5%. In terms of low-concentration CO 2 capturing technology, currently commonly used chemical absorbents include inorganic absorbents (potassium carbonate, ammonia water, etc.), organic absorbents (alcohol amine, etc.), mixed absorbents, and the like. The most economical trapping method is currently recognized as an organic absorbent alcohol amine solvent trapping method, the applicable scale is 10-100 ten thousand tons/year, and the trapping cost is 450-550 yuan/ton; and the MDEA solution is adopted for trapping, the applicable scale is 10-100 ten thousand tons/year, and the trapping cost is 300-400 yuan/ton.
The main problem of the low-concentration CO 2 trapping method is high trapping cost, wherein the energy consumption cost accounts for about half of the trapping cost. Thus, cost optimization for low concentration CO 2 capture can be studied in two directions: firstly, the performance (absorption rate, desorption rate and desorption energy consumption) of the medicament is improved, and the manufacturing cost is reduced; and secondly, the energy consumption of the whole trapping process is reduced through process optimization. However, the cost is still high, and the problem that the steam consumption in the capturing process is relatively large needs to be further optimized, so that the purpose of reducing the energy consumption is achieved.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a low-cost and low-concentration CO 2 trapping process, realize low-concentration (3% -12%) and low-cost CO 2 trapping, provide a low-cost carbon source for a CO 2 flooding area, reduce carbon emission in oil field development and realize the exploitation of low-carbon crude oil.
In order to achieve the purpose of the invention, the technical scheme adopted is as follows:
a low-cost and low-concentration CO2 capturing system comprises an absorption tower, a lean-rich liquid heat exchanger, a regeneration tower and a heat exchanger which are connected in sequence;
The heat exchanger is provided with a rich liquid inlet 1, a rich liquid outlet 1, a high-temperature steam inlet and a steam condensate outlet; the high-temperature steam is separated from SAGD produced liquid by a steam separator.
Preferably, the rich liquid inlet I and the rich liquid outlet I are respectively connected with the regeneration tower, high-temperature steam separated from the SAGD produced liquid enters the heat exchanger through the high-temperature steam inlet, exchanges heat with the rich liquid, and steam condensate obtained after the heat exchange is completed is output through the steam condensate outlet.
Preferably, a flue gas inlet is formed in the lower portion of the side wall of the absorption tower, a bottom outlet is formed in the bottom of the absorption tower, the bottom outlet, the rich liquid pump and the lean-rich liquid heat exchanger are sequentially connected, a purified gas outlet is formed in the top of the absorption tower, a lean liquid inlet 1 is formed in the upper portion of the side wall of the absorption tower, and the lean liquid inlet 1, the lean liquid cooler and the lean-rich liquid heat exchanger are sequentially connected.
Preferably, the lean-rich liquid heat exchanger is provided with a rich liquid inlet II, a rich liquid outlet II, a lean liquid inlet II and a lean liquid outlet II, the upper part of the side wall of the regeneration tower is provided with a rich liquid inlet III, the bottom of the regeneration tower is provided with a lean liquid outlet III, the rich liquid inlet II is connected with a rich liquid pump, the rich liquid outlet II is connected with the rich liquid inlet III, the lean liquid inlet II is connected with a lean liquid pump, and the lean liquid pump is connected with the lean liquid outlet III at the bottom of the regeneration tower.
Preferably, the top vent of the regeneration column is connected to a condenser.
The invention also provides a low-cost and low-concentration CO2 trapping method, which adopts the trapping system to trap, and comprises the following steps:
(1) Delivering the gas containing CO 2 to an absorption tower, and contacting with lean liquid of the absorption tower to obtain rich liquid;
(2) And (3) carrying out heat exchange on the rich liquid and the lean liquid, then conveying the rich liquid and the lean liquid to a regeneration tower, entering a heat exchanger, carrying out heat exchange on the rich liquid and the high-temperature steam separated from the SAGD produced liquid by a steam separator, and analyzing CO 2 in the rich liquid to obtain the steam-free steam.
Preferably, in the step (1), the gas is firstly dedusted, pretreated and then conveyed to a flue gas inlet through a fan and a condenser to enter an absorption tower.
Preferably, the contacting in step (1) is counter-current.
Preferably, the lean solution in the step (1) is an alcohol amine absorbent.
Preferably, the step (2) is operated to convey the rich liquid from the bottom of the absorption tower to a rich liquid pump, convey the rich liquid to a lean rich liquid heat exchanger through the rich liquid pump, heat exchange and temperature rise are carried out on the lean liquid output from the bottom of the regeneration tower, then the lean liquid enters the upper part of the regeneration tower, and then the heat exchange is carried out on the lean liquid and the heat exchange is carried out on the lean liquid, and the CO 2 in the rich liquid is resolved to obtain the rich liquid.
Preferably, after the CO 2 in the rich solution in the step (2) is resolved, the regenerated CO 2 is cooled and dried in a condenser.
Preferably, the regenerated lean solution is obtained after the CO 2 in the rich solution in the step (2) is resolved, the regenerated lean solution is conveyed to a lean-rich solution heat exchanger through a lean solution pump, and is cooled by heat exchange with the rich solution output by the absorption tower, and then is cooled by a lean solution condenser and enters the absorption tower, so that the alcohol amine solution is circularly used for capturing CO 2.
Preferably, after the high-temperature steam in the step (2) is subjected to heat exchange, the obtained steam condensate is buffered by a buffer tank and then enters an oil removal tank or a storage regulation tank built in the thickened oil combined station for oil-water separation, and the gas separated by the buffer tank enters an associated gas treatment station for treatment.
It is still another object of the present invention to provide an application of the above-mentioned capturing system or the above-mentioned capturing method in capturing CO2 with low concentration in the CCUS technical system in the technical field of ground engineering.
Compared with the prior art, the invention has the following characteristics:
1. The application scene of the invention is CO 2 trapping of gas after fluidized bed combustion, and the alcohol amine method is adopted, and the process is optimized aiming at the condition of CO 2 desorption and with the lowest running cost as the aim, so as to realize low-cost and low-concentration CO 2 trapping.
2. High-temperature steam (P is more than or equal to 0.5 and less than or equal to 0.6,150 ℃ and T is more than or equal to 160 ℃) separated from SAGD produced liquid by a steam separator is introduced into a heat exchanger at the bottom of a desorption tower and used as a heat source to exchange heat with rich liquid, so that the operation cost is greatly reduced.
3. Simple and efficient: the prior art utilizes pipelines, an absorption tower and a desorption tower to transfer heat, and relates to a complex pipeline structure, so that the cost is increased.
4. And (3) low-cost large-scale trapping: the useless high-temperature steam separated from the SAGD block produced liquid is continuously introduced for desorption, so that the useless steam is effectively utilized, and the trapping cost can be reduced by about half;
Drawings
FIG. 1 is a process flow diagram of a low cost, low concentration CO 2 capture system of the present invention;
Wherein, 1-the flue gas inlet; 2-an absorption tower; 3-bottom outlet; 4-a rich liquid pump; a 5-lean rich liquid heat exchanger; 6-a rich liquid inlet II; 7-a rich liquid outlet II; 8-a regeneration tower; 9-rich liquid inlet III; 10-a rich liquid outlet III; 11-a heat exchanger; 12-a rich liquid inlet I; 13-rich liquor outlet I; 14-exhaust port; 15-a condenser; 16-lean liquid outlet III; 17-lean solution pump; 18-lean liquid inlet II; 19-lean liquor cooler; 20-lean liquid inlet I; 21-a purge gas outlet; 22-high temperature steam inlet; 23-a steam condensate outlet; a1-high-temperature steam; a2-steam condensate.
Detailed Description
The invention is further described in connection with the following detailed description.
Example 1
The low-cost and low-concentration CO 2 capturing system is shown in figure 1 and comprises an absorption tower 2, a rich liquid pump 4, a lean and rich liquid heat exchanger 5, a lean liquid cooler 19, a regeneration tower 8 and a heat exchanger 11;
the lower part of the side wall of the absorption tower 2 is provided with a flue gas inlet 1, the bottom is provided with a bottom outlet 3, the top is provided with a purified gas outlet 21, the upper part of the side wall is provided with a lean solution inlet I20, wherein the bottom outlet 3, a rich solution pump 4 and a lean-rich solution heat exchanger 5 are sequentially connected, and the lean solution inlet I20, a lean solution cooler 19 and the lean-rich solution heat exchanger 5 at the upper part of the side wall are sequentially connected;
The lean-rich liquid heat exchanger is provided with a rich liquid inlet II 6, a rich liquid outlet II 7, a lean liquid inlet II 18 and a lean liquid outlet II 21, the upper part of the side wall of the regeneration tower is provided with a rich liquid inlet III, and the bottom of the regeneration tower is provided with a lean liquid outlet III; the rich liquid inlet II 6 is connected with the rich liquid pump 4, and the rich liquid outlet II 7 is connected with a rich liquid inlet III 9 at the upper part of the side wall of the regeneration tower; the lean solution inlet II 18 is connected with a lean solution pump 17, and the lean solution pump 17 is connected with a lean solution outlet III 16 at the bottom of the regeneration tower.
The heat exchanger 11 is provided with a rich liquid inlet I12, a rich liquid outlet I13, a high-temperature steam inlet and a steam condensate outlet; the high-temperature steam is separated from SAGD produced liquid by a steam separator;
the top of the regeneration tower is provided with an exhaust port 14 which is connected with a condenser 15.
The trapping system of the invention works according to the following principle:
(1) Flue gas generated by the coal-fired furnace is subjected to dust removal and pretreatment, then is conveyed to the bottom of an absorption tower 2 through a flue gas inlet 1 by a fan and a condenser, and is in countercurrent contact with alcohol amine (M-CO 2 -C efficient absorbent) lean liquid sprayed from top to bottom of the absorption tower, so that heat and mass transfer of gas-liquid two phases is performed;
(2) The alcohol amine rich solution absorbing CO 2 in the blast furnace gas is conveyed to the lean rich solution heat exchanger 5 through the rich solution pump 4 at the bottom outlet 3 of the absorption tower 2, is output from the lean solution outlet III 16 at the bottom of the regeneration tower 8 and exchanges heat with the high Wen Pinye input through the lean solution pump 17, enters the regeneration tower 8 from the rich solution inlet III 9 of the regeneration tower 8 after the rich solution is heated, and enters the heat exchanger 11 through the rich solution outlet III 10;
(3) High-temperature steam A1 (P is more than or equal to 0.5 and less than or equal to 0.6,150 ℃ and T is more than or equal to 160 ℃) separated from SAGD produced liquid through a steam separator enters the heat exchanger 11 through the high-temperature steam inlet 22 to be used as a heat source for exchanging heat with rich liquid output by the regeneration tower, and the rich liquid is heated to be above the desorption temperature of CO 2 under the action of high temperature to realize the desorption of CO 2 in the rich liquid;
(4) The regenerated CO 2 enters a condenser 15 through an exhaust port 14 at the top of the regeneration tower 8 to be cooled, dried, compressed and stored for subsequent utilization;
(5) And after the rich liquid is resolved, the regenerated lean liquid is obtained and is conveyed to a lean-rich liquid heat exchanger 5 through a lean liquid pump 17, and is subjected to heat exchange and cooling with the low-temperature rich liquid from the absorption tower 2, and then is cooled through a lean liquid condenser 19 and enters the absorption tower 2, so that the alcohol amine solution is circularly trapped to CO 2.
(6) And the steam condensate A 2 obtained after heat exchange is buffered by a buffer tank and enters an oil removal tank or a storage regulation tank built in the thickened oil combined station for oil-water separation, and the gas separated by the buffer tank enters an associated gas treatment station for treatment.
Example 2
The method for trapping CO 2 with low cost and low concentration adopts the system of fig. 1, the raw material is CO 2 trapped by gas after fluidized bed combustion, the concentration of CO 2 is 10.89%, and the concentration of the trapped CO 2 is 99% after the trapping by the process of fig. 1.
Currently, the cost of capturing low concentration CO 2 by chemical absorption is about 300 yuan/ton. According to the invention, the useless high-temperature steam separated from the SAGD block produced liquid is continuously introduced to carry out desorption, so that on one hand, the useless steam of the SAGD can be effectively utilized, and on the other hand, the cost (about 110 yuan per ton) of using the hot steam in the heat exchange process of the prior art can be saved, thereby realizing the reduction of the trapping cost to within 190 yuan per ton.
The foregoing detailed description is directed to one of the possible embodiments of the present invention, which is not intended to limit the scope of the invention, but is to be accorded the full scope of all such equivalents and modifications so as not to depart from the scope of the invention.
Claims (14)
1. The low-cost low-concentration CO 2 capturing system is characterized by comprising an absorption tower, a lean-rich liquid heat exchanger, a regeneration tower and a heat exchanger which are connected in sequence;
the heat exchanger is provided with a rich liquid inlet I, a rich liquid outlet I, a high-temperature steam inlet and a steam condensate outlet; the high-temperature steam is separated from SAGD produced liquid by a steam separator.
2. The capturing system according to claim 1, wherein the rich liquid inlet I and the rich liquid outlet I are respectively connected with the regeneration tower, high-temperature steam separated from the SAGD produced liquid enters the heat exchanger through the high-temperature steam inlet, exchanges heat with the rich liquid, and steam condensate obtained after the heat exchange is output through the steam condensate outlet.
3. The capturing system according to claim 1, wherein a flue gas inlet is formed in the lower portion of a side wall of the absorption tower, a bottom outlet is formed in the bottom of the absorption tower, the bottom outlet, the rich liquid pump and the lean-rich liquid heat exchanger are sequentially connected, a purified gas outlet is formed in the top of the absorption tower, a lean liquid inlet 1 is formed in the upper portion of the side wall of the absorption tower, and the lean liquid inlet 1, the lean liquid cooler and the lean-rich liquid heat exchanger are sequentially connected.
4. The capturing system according to claim 1, wherein the lean-rich liquid heat exchanger is provided with a rich liquid inlet II, a rich liquid outlet II, a lean liquid inlet II and a lean liquid outlet II, the upper part of the side wall of the regeneration tower is provided with a rich liquid inlet III, the bottom is provided with a lean liquid outlet III, the rich liquid inlet II is connected with a rich liquid pump, the rich liquid outlet II is connected with the rich liquid inlet III, the lean liquid inlet II is connected with a lean liquid pump, and the lean liquid pump is connected with the lean liquid outlet III at the bottom of the regeneration tower.
5. The capture system of claim 1, wherein the top vent of the regeneration column is connected to a condenser.
6. A low cost, low concentration CO 2 capture method, characterized by the use of a capture system according to any one of claims 1-5 comprising the steps of:
(1) Delivering the gas containing CO 2 to an absorption tower, and contacting with lean liquid of the absorption tower to obtain rich liquid;
(2) And (3) carrying out heat exchange on the rich liquid and the lean liquid, then conveying the rich liquid and the lean liquid to a regeneration tower, entering a heat exchanger, carrying out heat exchange on the rich liquid and the high-temperature steam separated from the SAGD produced liquid by a steam separator, and analyzing CO 2 in the rich liquid to obtain the steam-free steam.
7. The method according to claim 6, wherein the gas in step (1) is dedusted, pretreated and then sent to the flue gas inlet through a fan and a condenser to enter the absorption tower.
8. The trapping method according to claim 6, wherein the contact in the step (1) is countercurrent contact.
9. The method according to claim 6, wherein the lean solution in step (1) is an alcohol amine absorbent.
10. The capturing method according to claim 6, wherein the step (2) is performed by transferring the rich liquid from the bottom of the absorption tower to a rich liquid pump, transferring the rich liquid to a lean rich liquid heat exchanger through the rich liquid pump, performing heat exchange with the lean liquid outputted from the bottom of the regeneration tower, heating the lean liquid, introducing the lean liquid into the upper part of the regeneration tower, and then flowing the lean liquid into the heat exchanger for heat exchange, and analyzing CO 2 in the rich liquid.
11. The method according to claim 6, wherein the regenerated CO 2 is cooled and dried in a condenser after the CO 2 in the rich liquid in the step (2) is resolved.
12. The capturing method according to claim 6, wherein the regenerated lean solution is obtained after the CO 2 in the rich solution in the step (2) is resolved, the regenerated lean solution is conveyed to a lean rich solution heat exchanger through a lean solution pump, and after heat exchange and temperature reduction are performed on the lean solution output by the absorption tower, the lean solution is cooled through a lean solution condenser and then enters the absorption tower, so that the alcohol amine solution is completed to circularly capture the CO 2.
13. The capturing method according to claim 6, wherein after the high-temperature steam in the step (2) is subjected to heat exchange, the obtained steam condensate is buffered by a buffer tank and then enters an oil removal tank or a storage regulation tank built in a thickened oil combined station for oil-water separation, and the gas separated by the buffer tank enters an associated gas treatment station for treatment.
14. Use of a trapping system according to any one of claims 1-5 or a trapping method according to any one of claims 6-13 in a low concentration CO 2 trapping set in the CCUS technology system of the field of ground engineering technology.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN119771125A (en) * | 2025-01-17 | 2025-04-08 | 华能陇东能源有限责任公司正宁电厂 | CO2 capture plants and carbon capture systems |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN119771125A (en) * | 2025-01-17 | 2025-04-08 | 华能陇东能源有限责任公司正宁电厂 | CO2 capture plants and carbon capture systems |
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