CN216778404U - System for capturing carbon dioxide by wet method - Google Patents
System for capturing carbon dioxide by wet method Download PDFInfo
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- CN216778404U CN216778404U CN202122641541.0U CN202122641541U CN216778404U CN 216778404 U CN216778404 U CN 216778404U CN 202122641541 U CN202122641541 U CN 202122641541U CN 216778404 U CN216778404 U CN 216778404U
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Abstract
The utility model relates to the technical field of wet-method carbon dioxide capture, in particular to a system for wet-method carbon dioxide capture, which comprises an absorption tower, wherein the absorption tower comprises an absorption area and a washing area from bottom to top, and a washing tank is communicated with the bottom of the washing area; the top end of the regeneration tower is communicated with the bottom end of the absorption zone through a first pipeline; the regeneration gas separator is communicated with the top end of the regeneration tower through a third pipeline; the underground tank is communicated with the bottom end of the regeneration gas separator; the bottom end of the regeneration gas separator is also communicated with the top end of the washing area. The utility model introduces the condensate in the regeneration gas separator as the absorption liquid into the regeneration tower, can further purify the purified gas, reduce the temperature of the purified gas, reduce the escape of ammonia, reduce the amount of external washing liquid, realize the internal circulation of water in the system and is beneficial to stably controlling the water balance of the system.
Description
Technical Field
The utility model relates to the technical field of wet-method carbon dioxide capture, in particular to a system for wet-method carbon dioxide capture.
Background
At present, wet technology is continuously perfected and iterated as a mainstream technology capable of realizing large-scale carbon dioxide capture for decades. The method has the advantages that the method is thoroughly researched and sufficiently advanced from the aspects of introduction of energy-saving processes such as a heat pump, an MVR flash evaporation and the like, improvement of mass transfer efficiency such as high-efficiency filling, a supergravity technology and the like from continuous optimization of trapping solvents such as organic amine, ionic liquid, amino acid salt and the like, and a set of efficient, energy-saving, environment-friendly and reliable trapping technology is integrally formed.
By summarizing the practical driving conditions of a plurality of ten-thousand-ton-level carbon dioxide trapping devices, the stable operation of the trapping system is considered to be the most important water balance control of the system in the same place except that the reasonable control of conventional process parameters such as temperature, flow and the like is required. Namely, the water carried by the flue gas entering the absorption tower and the water carried by the purified gas discharged from the absorption tower reach a balanced state. The water balance control is the main factor affecting the concentration fluctuation of the absorbent, which in turn affects the capturing effect of the absorbent and the stability of the final system operation.
In conventional carbon dioxide capture processes, deionized water is typically used as the initial scrubbing liquid, and as the scrubbing section is cycled, the total scrubbing liquid and amine concentration (i.e., alkalinity) slowly rise (4-8 wt%), while the rise in amine concentration results in a decrease in scrubbing effectiveness, i.e., an increase in the absorbent content in the purified gas, thereby increasing losses. In addition, for the increase of the amine concentration, a washing solution is usually required to be put into an underground tank, and then desalted water is added to reduce the concentration of the washing solution so as to ensure the washing effect, and the solution supplementing mode can cause the obvious fluctuation of the temperature and the concentration of the absorbent in the regeneration tower; in addition, to the washing workshop section that the purification gas goes out the tower, the washing liquid is the outside demineralized water of initial adoption, and along with going on of circulation washing, the washing liquid temperature will slowly rise, need set up the washing liquid cooler, and washing liquid concentration also can crescent and then influence the washing effect simultaneously, need regularly to add the demineralized water in order to reduce washing liquid concentration to the washing liquid, and the demineralized water of outside replenishment is easy to destroy the water balance in the system.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a system for trapping carbon dioxide by a wet method in order to enhance the washing effect of amine liquid drops in purified gas and reduce the influence of a water replenishing process on the temperature and the concentration of the system.
In order to achieve the above object, the present invention provides a system for capturing carbon dioxide by a wet method, comprising an absorption tower comprising, from bottom to top, an absorption zone for contacting a feed gas containing carbon dioxide with an absorbent to react and obtain a pre-purified gas and an absorbent-rich liquid, and a scrubbing zone for scrubbing the pre-purified gas to obtain a purified gas;
the washing tank is communicated with the bottom of the washing area and is used for storing washing rich liquid obtained by washing;
the top end of the regeneration tower is communicated with the bottom end of the absorption zone through a first pipeline and is used for resolving the absorbent rich liquid to obtain regenerated gas and an absorbent barren liquid, wherein the absorbent barren liquid is divided into barren liquid a and barren liquid b;
the regeneration gas separator is communicated with the top end of the regeneration tower through a third pipeline and is used for condensing the regeneration gas to obtain condensate and product gas, wherein the condensate is divided into cold liquid A and cold liquid B;
the underground tank is communicated with the bottom end of the regeneration gas separator and is used for storing the cold liquid A;
the bottom end of the regeneration gas separator is also communicated with the top end of the washing area and is used for introducing the cold liquid B into the washing area to wash the pre-purified gas.
Preferably, the bottom end of the wash tank communicates with the top end of the wash zone.
Preferably, a bottom end of the wash tank communicates with the first line.
Preferably, the upper end of the absorption zone is communicated with the bottom end of the regeneration tower through a second pipeline for introducing the lean liquid a into the absorption tower to contact with the feed gas for the reaction.
Preferably, the system further comprises a heat exchanger which is respectively communicated with the first pipeline and the second pipeline and is used for exchanging heat between the rich absorbent solution and the lean solution a.
Preferably, a lean liquid cooler is arranged on the second pipeline and used for cooling the lean liquid a.
Preferably, a regeneration gas cooler is arranged on the third pipeline and used for cooling the regeneration gas.
Preferably, the system further comprises a boiler communicated with the bottom of the regeneration tower and used for supplying heat to the regeneration tower.
Preferably, the bottom of the regeneration tower is communicated with the underground tank and is used for leading the barren liquor b out of the regeneration tower
According to the technical scheme, the condensate in the regeneration gas separator is introduced to be used as the washing liquid of the purified gas at the top of the absorption tower, and the alkalinity of the regenerated gas condensate is low (about 1 wt%) and the regenerated gas condensate is continuously supplemented to the washing liquid, so that the concentration of amine in the washing liquid is basically maintained at a low concentration (about 2 wt%), a stable washing effect can be ensured, and meanwhile, the desalted water does not need to be added into the system regularly, and the using amount of the desalted water is reduced; on the other hand, the washing liquid is continuously from the condensate of the regenerated gas, so that the lower temperature can be kept, and the use of a cooler is reduced; and the quantity of external washing liquid can be reduced, the internal circulation of water in the system is realized, and the water balance of the system is favorably and stably controlled.
Drawings
FIG. 1 is a schematic diagram of the configuration of a system for wet capture of carbon dioxide according to an embodiment of the present invention;
fig. 2 is a schematic view of the structure of a system for wet-capturing carbon dioxide according to a comparative example of the present invention.
Description of the reference numerals
1. First pipeline 2, second pipeline
3. Third pipeline 10, absorption tower
20. Regeneration tower 11, barren liquor cooler
12. Washing tank 13 and pregnant solution pump
14. Barren liquor pump 21, regeneration gas cooler
22. Boiler 23, underground tank
24. Regeneration gas separator 25, heat exchanger
101. Absorption zone 102, washing zone
15. Detergent cooler
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
The following detailed description of embodiments of the utility model refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.
In the present invention, the use of directional terms such as "upper, lower, left, right" generally means upper, lower, left, right as viewed with reference to the accompanying drawings, unless otherwise specified; "inner and outer" generally refer to the inner and outer relative to the profile of the components themselves; "distal and proximal" generally refer to distance relative to the contour of the components themselves.
Fig. 1 is a schematic structural diagram of a system for wet capturing carbon dioxide according to an embodiment of the present invention, and the present invention provides a system for wet capturing carbon dioxide, the system comprising an absorption tower 10, the absorption tower 10 comprising, from bottom to top, an absorption zone 101 and a scrubbing zone 102, the absorption zone 101 being configured to contact a feed gas containing carbon dioxide and an absorbent to perform a reaction to obtain a pre-purified gas and an absorbent-rich liquid, and the scrubbing zone 102 being configured to scrub the pre-purified gas to obtain a purified gas;
a washing tank 12, which is communicated with the bottom of the washing area 102 and is used for storing washing rich liquid obtained by washing;
the top end of the regeneration tower 20 is communicated with the bottom end of the absorption zone 101 through a first pipeline 1, and a rich liquid pump 13 is arranged on the first pipeline 1 and used for pumping the rich absorbent liquid into the regeneration tower 20 for analysis to obtain regenerated gas and an absorbent lean liquid, wherein the absorbent lean liquid is divided into a lean liquid a and a lean liquid b;
the regeneration gas separator 24 is communicated with the top end of the regeneration tower 20 through a third pipeline 3 and is used for condensing the regeneration gas to obtain condensate and product gas, wherein the condensate is divided into cold liquid A and cold liquid B;
the underground tank 23 is communicated with the bottom end of the regeneration gas separator 24 and is used for storing the cold liquid A;
the bottom end of the regeneration gas separator 24 is also communicated with the top end of the washing area 102, and is used for introducing the cold liquid B into the washing area 102 to wash the pre-purified gas.
In the utility model, the action of the washing liquid is that the temperature of the purified gas can be reduced, and the evaporation of amine liquid vapor and the entrainment of liquid drops (generally called amine escape loss) can be reduced, wherein the absorbent is an amine-containing solution, and the raw gas containing carbon dioxide is contacted with the absorbent to react to obtain the pre-purified gas still containing a certain amount of amine; the condensed liquid separated by the regenerative gas separator 24 is divided into two paths (cold liquid A and cold liquid B), and the cold liquid B is introduced into the washing area 102 as washing liquid to wash the pre-purified gas, so that the following technical effects are achieved: 1. by washing the pre-purified gas, the temperature of the pre-purified gas can be reduced, the content of amine in the pre-purified gas can be reduced, and the amine escape can be reduced; 2. because the temperature of the condensate is lower (30-40 ℃), the use of a washing liquid cooler can be reduced; 3. the condensate is generated in the system, can reduce water supplement, realizes water balance in the system, and is beneficial to maintaining the concentration of the absorbent and the stability of the temperature of the system, thereby improving the capture effect of the absorbent on carbon dioxide.
In some preferred embodiments of the present invention, preferably, the washing solution is divided into washing solution C and washing solution D; wherein the bottom end of the scrubber tank 12 is connected to the top end of the scrubbing section 102 by a pump for circulating the washing liquid C into the absorption section 102 for scrubbing the pre-purified gas; further preferably, the bottom end of the washing tank 12 is communicated with the first pipeline 1 for adding the washing liquid D to the absorbent rich liquid for post-treatment.
In some preferred embodiments of the present invention, the upper end of the absorption zone 101 is communicated with the bottom end of the regeneration tower 20 through a second pipeline 2, and a lean liquid pump 14 is disposed on the second pipeline 2 for pumping the lean liquid a into the absorption tower 10 to contact with the feed gas in a reverse direction for the reaction.
According to the utility model, under a preferable condition, the system further comprises a heat exchanger 25 which is respectively communicated with the first pipeline 1 and the second pipeline 2 and is used for exchanging heat between the rich absorbent solution and the lean solution a, so that the comprehensive utilization of heat in the system is realized.
According to the present invention, it is preferable that a lean liquid cooler 11 is provided on the second pipeline 2 for cooling the lean liquid a.
In the present invention, preferably, a regeneration gas cooler 21 is disposed on the third pipeline 3 for cooling the regeneration gas to obtain a cooling gas.
In the present invention, preferably, the system further comprises a boiler 22 connected to the bottom of the regeneration tower 20 for supplying heat to the regeneration tower 20, and the heat source of the boiler 22 may be a heat source known to those skilled in the art that can be used for heating the boiler, for example, hot steam from the steam outer pipe.
In some preferred embodiments of the present invention, it is preferable that the bottom of the regeneration tower 20 is communicated with the underground tank 23 for introducing the lean solution b into the underground tank 23 for post-treatment.
In some preferred embodiments of the present invention, the height of the regeneration gas separator 24 is higher than the height of the washing tank 12, so that the washing tank 12 can be filled with condensate by gravity alone.
The method for wet capture of carbon dioxide in the system shown in fig. 1 is as follows:
a raw gas containing carbon dioxide (the carbon dioxide content is about 12.5 vol%) enters the absorption tower 10 from the bottom of the absorption zone 102, and is in reverse contact with an absorbent from the top of the absorption zone 102 to perform an absorption reaction, so that a pre-purified gas and an absorbent rich solution are obtained;
the pre-purified gas continuously moves upwards to enter a washing area 101 and is contacted with washing liquid for washing to obtain purified gas and washing rich liquid, and the purified gas is extracted through a gas outlet at the top of the absorption tower 10;
introducing the absorbent rich solution into the top of a regeneration tower 20 from the bottom of an absorption tower 10 through a first pipeline 1 provided with a rich solution pump 13, wherein a boiler 22 is arranged at the bottom of the regeneration tower 20 and used for supplying heat to the regeneration tower 20, and the absorbent rich solution rich in carbon dioxide is resolved at high temperature in the regeneration tower 20 to obtain absorbent lean solution and regeneration gas;
the absorbent lean solution is divided into a lean solution a and a lean solution b, wherein the lean solution a is introduced into the top of the absorption zone 101 and is circularly added into the absorbent; the barren solution b is introduced into an underground tank 23 for subsequent treatment;
the regenerated gas enters the third pipeline 3 and is cooled by a regenerated gas cooler 23, and then is cooled by a regenerated gas separator 24 to obtain product gas and condensate, wherein the content of carbon dioxide in the product gas is more than 99% by volume; the condensate is divided into cold liquid A and cold liquid B, wherein the cold liquid A enters the underground tank 23 for post-treatment, and the cold liquid B is introduced into the washing area 102 for washing the pre-purified gas;
the rich washing liquid is divided into washing liquid C and washing liquid D, wherein the washing liquid C is circularly introduced into the absorption area 102 to wash the pre-purified gas; and adding the washing liquid D into the rich absorbent solution for post-treatment.
Example 1
Raw gas containing carbon dioxide (the content of carbon dioxide is 12.5 vol%) enters the absorption tower 10 from the bottom of the absorption zone 102, and is in reverse contact with an absorbent from the top of the absorption zone 102 to perform absorption reaction, so that pre-purified gas and an absorbent rich solution are obtained;
the pre-purified gas continuously moves upwards to enter a washing area 101 and is contacted with washing liquid for washing to obtain purified gas and washing rich liquid, and the purified gas is extracted through a gas outlet at the top of the absorption tower 10;
the absorbent rich solution is introduced into the top of the regeneration tower 20 from the bottom of the absorption tower 10 through a first pipeline 1 provided with a rich solution pump 13, a boiler 22 is arranged at the bottom of the regeneration tower 20 and used for supplying heat to the regeneration tower 20, and the absorbent rich solution rich in carbon dioxide is resolved at high temperature in the regeneration tower 20 to obtain absorbent lean solution and regeneration gas;
the absorbent lean solution is divided into a lean solution a and a lean solution b, wherein the lean solution a is introduced into the top of the absorption zone 101 and is circularly added into the absorbent; the barren solution b is introduced into an underground tank 23 for subsequent treatment;
the regenerated gas enters the third pipeline 3, is cooled by a regenerated gas cooler 23, and is cooled by a regenerated gas separator 24 to obtain product gas and condensate (the concentration of amine is 1 wt%, and the temperature is 35 ℃), wherein the content of carbon dioxide in the product gas is 99.5 vol%; the condensate is divided into a cold liquid A and a cold liquid B, wherein the cold liquid A enters the underground tank 23 for post-treatment, and the cold liquid B is introduced into the washing area 102 and is used for washing the pre-purified gas;
the rich washing liquid is divided into washing liquid C and washing liquid D, wherein the washing liquid C is circularly introduced into the absorption area 102 to wash the pre-purified gas; adding washing liquor D into the absorbent rich solution for post-treatment;
in this example, the amine concentration in the wash was maintained at substantially 2 wt%.
Comparative example
CO Using the apparatus shown in FIG. 22Trapping, comprising the following steps:
raw gas containing carbon dioxide (the content of carbon dioxide is 12.5 vol%) enters the absorption tower 10 from the bottom of the absorption zone 102, and is in reverse contact with an absorbent from the top of the absorption zone 102 to perform absorption reaction, so that pre-purified gas and an absorbent rich solution are obtained;
the pre-purified gas continuously moves upwards to enter a washing area 101 and is contacted with washing liquid for washing to obtain purified gas and washing rich liquid, and the purified gas is extracted through a gas outlet at the top of the absorption tower 10;
the absorbent rich solution is introduced into the top of the regeneration tower 20 from the bottom of the absorption tower 10 through a first pipeline 1 provided with a rich solution pump 13, a boiler 22 is arranged at the bottom of the regeneration tower 20 and used for supplying heat to the regeneration tower 20, and the absorbent rich solution rich in carbon dioxide is resolved at high temperature in the regeneration tower 20 to obtain absorbent lean solution and regeneration gas;
the absorbent lean solution is divided into a lean solution a and a lean solution b, wherein the lean solution a is introduced into the top of the absorption zone 101 and is circularly added into the absorbent; the barren solution b is introduced into an underground tank 23 for subsequent treatment;
the regenerated gas enters the third pipeline 3, is cooled by a regenerated gas cooler 23, and is cooled by a regenerated gas separator 24 to obtain product gas and condensate (the concentration of amine is 1 wt%, and the temperature is 35 ℃), wherein the content of carbon dioxide in the product gas is 99.5 vol%; the condensate enters the underground tank 23;
pressurizing the washing liquid rich liquid by a pressurizing pump, cooling the washing liquid by a washing agent cooler, circularly introducing the washing liquid rich liquid into the absorption area 102, washing the pre-purified gas, introducing the washing liquid 15 into the underground tank 23 when the concentration of amine in the washing liquid reaches 6 wt%, and injecting desalted water into the washing tank 12;
in this comparative example, the concentration of the amine in the scrubbing liquid fluctuates widely, and the total amount of the scrubbing liquid and the concentration (i.e., alkalinity) rise slowly (6 to 8 wt%) with the circulation of the scrubbing section, and the rise in the concentration leads to a decrease in the scrubbing effect, i.e., an increase in the absorbent content in the purified gas, and thus to an increase in the loss.
Examples of the experiments
On existing industrial plants (CO)2Capture scale of 3 ten thousand tons/year) and CO in the raw material gas2The content is 12.5 wt%, the absorbent is 20 wt% of monoethanolamine, and the device operates under the designed working condition. For the washing section, the amine concentration in the washing liquid is controlled to 1 wt%, 2 wt%, 3 wt%, 4 wt%, 5 wt%, 6 wt%, respectively, and the content of the absorbent in the purified gas obtained at the corresponding concentration, that is, the amine slip, is monitored and converted into the amount of trapped CO per ton2The results of the experiment are shown in Table 1.
TABLE 1
| Concentration of washing solution (wt%) | 1 | 2 | 3 | 4 | 5 | 6 |
| Amine escape loss (kg/t CO)2) | 0.255 | 0.313 | 0.395 | 0.496 | 0.583 | 0.692 |
As can be seen from the above table, the scrubbing solution concentration that can be maintained in the present invention is 2 wt%, corresponding to an amine escape loss of only 0.313kg/t CO2And the highest concentration of amine in the washing liquid in the prior art is 6 wt%, and the average value of the corresponding amine escape loss is 0.496kg/t CO2Compared with the prior art, the method provided by the utility model can reduce the amine escape by 36.9%.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the utility model, many simple modifications can be made to the technical solution of the utility model, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the utility model, and all fall within the scope of the utility model.
Claims (9)
1. A system for capturing carbon dioxide by a wet method, characterized in that the system comprises an absorption tower (10), the absorption tower (10) comprises an absorption area (101) and a washing area (102) from bottom to top, the absorption area (101) is used for contacting and reacting raw gas containing carbon dioxide and an absorbent to obtain a pre-purified gas and an absorbent rich liquid, and the washing area (102) is used for washing the pre-purified gas to obtain a purified gas;
a washing tank (12) communicated with the bottom of the washing area (102) and used for storing washing rich liquid obtained by washing;
a regeneration tower (20), wherein the top end of the regeneration tower (20) is communicated with the bottom end of the absorption zone (101) through a first pipeline (1) and is used for resolving the absorbent rich liquid to obtain a regeneration gas and an absorbent lean liquid, and the absorbent lean liquid is divided into a lean liquid a and a lean liquid b;
the regeneration gas separator (24) is communicated with the top end of the regeneration tower (20) through a third pipeline (3) and is used for condensing the regeneration gas to obtain condensate and product gas, wherein the condensate is divided into cold liquid A and cold liquid B;
the underground tank (23) is communicated with the bottom end of the regeneration gas separator (24) and is used for storing the cold liquid A;
the bottom end of the regeneration gas separator (24) is also communicated with the top end of the washing area (102) and is used for introducing the cold liquid B into the washing area (102) to wash the pre-purified gas.
2. The system of claim 1, wherein a bottom end of the wash tank (12) communicates with a top end of the wash zone (102).
3. A system according to claim 1 or 2, characterized in that the bottom end of the wash tank (12) communicates with the first line (1).
4. The system according to claim 1 or 2, wherein an upper end of the absorption zone (101) is in communication with a lower end of the regeneration column (20) through a second line (2) for introducing the lean liquid a into the absorption column (10) to contact the feed gas for the reaction.
5. The system according to claim 4, further comprising a heat exchanger (25) in communication with the first line (1) and the second line (2), respectively, for exchanging heat of the absorbent rich liquid with the lean liquid a.
6. A system according to claim 4, characterized in that a lean liquid cooler (11) is provided on the second line (2) for cooling the lean liquid a.
7. A system according to claim 1 or 2, characterized in that a regeneration gas cooler (21) is arranged on the third line (3) for cooling the regeneration gas.
8. The system of claim 1 or 2, further comprising a boiler (22) in communication with the bottom of the regeneration column (20) for supplying heat to the regeneration column (20).
9. The system according to claim 1 or 2, wherein the bottom of the regeneration tower (20) is in communication with the underground tank (23) for leading the lean liquid b out of the regeneration tower (20).
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2024082476A1 (en) * | 2022-10-21 | 2024-04-25 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2024082476A1 (en) * | 2022-10-21 | 2024-04-25 | 中国华能集团清洁能源技术研究院有限公司 | Carbon dioxide capture system |
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Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: SINOPEC NANJING CHEMICAL RESEARCH INSTITUTE Co.,Ltd. Address before: 210048 Jiangsu Province, Nanjing city Liuhe District Dachang geguan Road No. 699 Patentee before: SINOPEC NANJING CHEMICAL RESEARCH INSTITUTE Co.,Ltd. Patentee before: CHINA PETROLEUM & CHEMICAL Corp. |