CN216558458U - Flue gas waste heat recovery device capable of simultaneously capturing carbon and sulfur - Google Patents
Flue gas waste heat recovery device capable of simultaneously capturing carbon and sulfur Download PDFInfo
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- CN216558458U CN216558458U CN202123233877.XU CN202123233877U CN216558458U CN 216558458 U CN216558458 U CN 216558458U CN 202123233877 U CN202123233877 U CN 202123233877U CN 216558458 U CN216558458 U CN 216558458U
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Abstract
The utility model belongs to the field of flue gas recovery, and particularly relates to a flue gas waste heat recovery device for simultaneously capturing carbon and sulfur, which comprises a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a carbon dioxide desorption tower, a sulfur dioxide desorption tower and an absorption tower; the flue gas is subjected to heat exchange and cooling through the first heat exchanger, the second heat exchanger and the third heat exchanger in sequence, so that the temperature of the flue gas entering the absorption tower is controlled, and the absorption capacity of carbon dioxide and sulfur dioxide is improved; the return water of the heat supply network is subjected to heat exchange and temperature rise through the fourth heat exchanger and the first heat exchanger, the heat utilization efficiency of the system is high, and the water of the heat supply network can reach 100-130 ℃ finally.
Description
Technical Field
The utility model belongs to the field of flue gas recovery, and particularly relates to a flue gas waste heat recovery device for simultaneously capturing carbon and sulfur.
Background
The emission reduction of carbon dioxide isothermal chamber gas becomes one of the serious challenges facing human society, sulfur dioxide is an important precursor for forming acid rain and dust haze, and SO in coal-fired flue gas2Has become a major cause of air pollution. Reduction of SO2Pollution is a urgent priority in atmospheric environmental remediation today. The development of the carbon dioxide and sulfur dioxide trapping technology is to reduce the technologyThe operation energy consumption of the technology is reduced.
The carbon dioxide capture process can be classified into a post-combustion capture technology, a pre-combustion capture technology, and an oxygen-enriched combustion technology. At present, a post-combustion trapping technology is adopted, namely carbon dioxide is trapped in flue gas discharged after combustion equipment; the flue gas desulfurization is the most effective desulfurization technology which is widely applied and is used for controlling the emission concentration and the total amount of sulfur dioxide in the atmosphere at present, but a method which can realize the capture of carbon dioxide and sulfur dioxide in flue gas and fully utilize the heat of the flue gas is lacked in the prior art.
SUMMERY OF THE UTILITY MODEL
The utility model provides a flue gas waste heat recovery device capable of simultaneously capturing carbon and sulfur, and aims to solve the problems that the prior art does not relate to the capturing of carbon and sulfur, the heat recovery rate is low, and the water temperature of a heat supply network is low.
In order to solve the above problems, the present invention proposes the following technical solutions:
a flue gas waste heat recovery device capable of simultaneously capturing carbon and sulfur comprises a first heat exchanger, a second heat exchanger, a third heat exchanger, a fourth heat exchanger, a carbon dioxide desorption tower, a sulfur dioxide desorption tower and an absorption tower;
the first heat exchanger is provided with a first heat exchanger flue gas inlet, a first heat exchanger flue gas outlet and a first heat exchanger heat supply network water inlet; the first heat exchanger flue gas inlet is communicated with the first heat exchanger flue gas outlet;
the second heat exchanger is provided with a second heat exchanger flue gas inlet, a second heat exchanger flue gas outlet, a second heat exchanger ionic liquid inlet and a second heat exchanger ionic liquid outlet; the second heat exchanger flue gas inlet is communicated with the second heat exchanger flue gas outlet, and the second heat exchanger ionic liquid inlet is communicated with the second heat exchanger ionic liquid outlet;
the third heat exchanger is provided with a third heat exchanger flue gas inlet, a third heat exchanger flue gas outlet, a third heat exchanger ionic liquid inlet and a third heat exchanger ionic liquid outlet; the third heat exchanger flue gas inlet is communicated with the third heat exchanger flue gas outlet, and the third heat exchanger ionic liquid inlet is communicated with the third heat exchanger ionic liquid outlet;
a fourth heat exchanger heat supply network water inlet, a fourth heat exchanger heat supply network water outlet, a fourth heat exchanger ionic liquid inlet and a fourth heat exchanger ionic liquid outlet are formed in the fourth heat exchanger; a fourth heat exchanger heat supply network water inlet is communicated with a fourth heat exchanger heat supply network water outlet, and a fourth heat exchanger ionic liquid inlet is communicated with a fourth heat exchanger ionic liquid outlet;
the carbon dioxide desorption tower is provided with a carbon dioxide desorption tower ionic liquid inlet and a carbon dioxide desorption tower ionic liquid outlet;
the sulfur dioxide desorption tower is provided with a sulfur dioxide desorption tower ionic liquid inlet and a sulfur dioxide desorption tower ionic liquid outlet;
the absorption tower is provided with an absorption tower flue gas inlet, an absorption tower ionic liquid inlet and an absorption tower ionic liquid outlet;
the first heat exchanger flue gas outlet is connected with a second heat exchanger flue gas inlet, the second heat exchanger flue gas outlet is connected with a third heat exchanger flue gas inlet, the third heat exchanger flue gas outlet is connected with an absorption tower flue gas inlet, an absorption tower ionic liquid outlet is connected with a third heat exchanger ionic liquid inlet, a third heat exchanger ionic liquid outlet is connected with a sulfur dioxide desorption tower ionic liquid inlet, a sulfur dioxide desorption tower ionic liquid outlet is connected with a second heat exchanger ionic liquid inlet, a second heat exchanger ionic liquid outlet is connected with a carbon dioxide desorption tower ionic liquid inlet, a carbon dioxide desorption tower ionic liquid outlet is connected with a fourth heat exchanger ionic liquid inlet, and a fourth heat exchanger ionic liquid outlet is connected with an absorption tower ionic liquid inlet;
and the heat supply network water outlet of the fourth heat exchanger is connected with the heat supply network water inlet of the first heat exchanger.
Preferably, a first heat exchanger heat supply network water outlet is arranged on the first heat exchanger; the first heat exchanger heat supply network water inlet is communicated with the first heat exchanger heat supply network water outlet; the water outlet of the heat supply network of the first heat exchanger is connected with the heat supply network.
Preferably, a carbon dioxide outlet is arranged on the carbon dioxide desorption tower; the carbon dioxide outlet is connected with a carbon dioxide storage tank.
Preferably, a sulfur dioxide outlet is arranged on the sulfur dioxide desorption tower and is connected with a sulfur dioxide storage tank and a chimney.
Preferably, the absorption tower is provided with an absorption tower flue gas outlet;
preferably, the ionic liquid outlet of the carbon dioxide desorption tower is positioned at the bottom of the carbon dioxide desorption tower, and the carbon dioxide outlet is positioned at the top of the carbon dioxide desorption tower;
preferably, the ionic liquid outlet of the sulfur dioxide desorption tower is positioned at the bottom of the sulfur dioxide desorption tower, and the sulfur dioxide outlet is positioned at the top of the sulfur dioxide desorption tower;
preferably, the ionic liquid outlet of the absorption tower is positioned at the bottom of the absorption tower, and the flue gas outlet of the absorption tower is positioned at the top of the absorption tower.
Preferably, after the temperature of the heat supply network water is raised in the first heat exchanger, the temperature is higher than 100 ℃ and lower than 130 ℃.
The utility model has the advantages that:
through the multi-stage heat exchange of the flue gas and the ionic liquid, the cascade temperature reduction of the flue gas and the cascade temperature rise of the return water of the heat supply network are realized, the cascade utilization of the waste heat of the flue gas is realized, and the heat utilization efficiency is improved.
Meanwhile, the capture of carbon dioxide and sulfur dioxide in the flue gas is realized.
Through the recovery and utilization of the waste heat in the flue gas, the heat supply income is increased, and the economic benefit of the power plant is improved.
Can provide heat supply network water with the temperature of up to 130 ℃.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the utility model, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the utility model and together with the description serve to explain the utility model and not to limit the utility model. In the drawings:
FIG. 1 is a schematic view of a flue gas waste heat recovery device for simultaneously capturing carbon and sulfur;
in the figure, 1 is a first heat exchanger, 2 is a second heat exchanger, 3 is a third heat exchanger, 4 is a fourth heat exchanger, 5 is a carbon dioxide desorption tower, 6 is a sulfur dioxide desorption tower, and 7 is an absorption tower;
11 is a first heat exchanger flue gas inlet, 12 is a first heat exchanger flue gas outlet, 13 is a first heat exchanger heat supply network water inlet, and 14 is a first heat exchanger heat supply network water outlet;
21 is a second heat exchanger flue gas inlet, 22 is a second heat exchanger flue gas outlet, 23 is a second heat exchanger ionic liquid inlet, and 24 is a second heat exchanger ionic liquid outlet;
31 is a third heat exchanger flue gas inlet, 32 is a third heat exchanger flue gas outlet, 33 is a third heat exchanger ionic liquid inlet, and 34 is a third heat exchanger ionic liquid outlet;
41 is a fourth heat exchanger heat supply network water inlet, 42 is a fourth heat exchanger heat supply network water outlet, 43 is a fourth heat exchanger ionic liquid inlet, and 44 is a fourth heat exchanger ionic liquid outlet;
51 is an ionic liquid inlet of the carbon dioxide desorption tower, 52 is an ionic liquid outlet of the carbon dioxide desorption tower, and 53 is a carbon dioxide outlet;
61 is an ionic liquid inlet of the sulfur dioxide desorption tower, 62 is an ionic liquid outlet of the sulfur dioxide desorption tower, and 63 is a sulfur dioxide outlet;
71 is an absorption tower flue gas inlet, 72 is an absorption tower flue gas outlet, 73 is an absorption tower ionic liquid inlet, and 74 is an absorption tower ionic liquid outlet.
Detailed Description
The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings. It should be noted that the embodiments and features of the embodiments may be combined with each other without conflict.
The following detailed description is exemplary in nature and is intended to provide further details of the utility model. Unless otherwise defined, all technical terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the utility model.
Example 1:
referring to fig. 1, the present invention discloses a flue gas waste heat recovery device for simultaneously capturing carbon and sulfur, comprising: the system comprises a first heat exchanger 1, a second heat exchanger 2, a third heat exchanger 3, a fourth heat exchanger 4, a carbon dioxide desorption tower 5, a sulfur dioxide desorption tower 6 and an absorption tower 7;
the first heat exchanger 1 is provided with a first heat exchanger flue gas inlet 11, a first heat exchanger flue gas outlet 12, a first heat exchanger heat supply network water inlet 13 and a first heat exchanger heat supply network water outlet 14; a first heat exchanger flue gas inlet 11 is communicated with a first heat exchanger flue gas outlet 12, and a first heat exchanger heat supply network water inlet 13 is communicated with a first heat exchanger heat supply network water outlet 14; the first heat exchanger heat supply network water outlet 14 is connected with a heat supply network; the first heat exchanger flue gas inlet 11 is communicated with a flue gas inlet;
the second heat exchanger 2 is provided with a second heat exchanger flue gas inlet 21, a second heat exchanger flue gas outlet 22, a second heat exchanger ionic liquid inlet 23 and a second heat exchanger ionic liquid outlet 24; the second heat exchanger flue gas inlet 21 is communicated with a second heat exchanger flue gas outlet 22, and the second heat exchanger ionic liquid inlet 23 is communicated with a second ionic liquid outlet 24;
the third heat exchanger 3 is provided with a third heat exchanger flue gas inlet 31, a third heat exchanger flue gas outlet 32, a third heat exchanger ionic liquid inlet 33 and a third heat exchanger ionic liquid outlet 34; the third heat exchanger flue gas inlet 31 is communicated with a third heat exchanger flue gas outlet 32, and the third heat exchanger ionic liquid inlet 33 is communicated with a third heat exchanger ionic liquid outlet 34;
a fourth heat exchanger heat supply network water inlet 41, a fourth heat exchanger heat supply network water outlet 42, a fourth heat exchanger ionic liquid inlet 43 and a fourth heat exchanger ionic liquid outlet 44 are arranged on the fourth heat exchanger 4; a fourth heat exchanger heat supply network water inlet 41 is communicated with a fourth heat exchanger heat supply network water outlet 42, and a fourth heat exchanger ionic liquid inlet 43 is communicated with a fourth heat exchanger ionic liquid outlet 44; the fourth heat exchanger heat supply network water outlet 42 is connected with the first heat exchanger heat supply network water inlet 13;
the carbon dioxide desorption tower 5 is provided with a carbon dioxide desorption tower ionic liquid inlet 51, a carbon dioxide desorption tower ionic liquid outlet 52 and a carbon dioxide outlet 53; the carbon dioxide desorption tower ionic liquid outlet 52 is positioned at the bottom of the carbon dioxide desorption tower 5, and the carbon dioxide outlet 53 is positioned at the top of the carbon dioxide desorption tower 5; the carbon dioxide outlet 53 is connected to a carbon dioxide storage tank.
The sulfur dioxide desorption tower 6 is provided with a sulfur dioxide desorption tower ionic liquid inlet 61, a sulfur dioxide desorption tower ionic liquid outlet 62 and a sulfur dioxide outlet 63; the sulfur dioxide desorption tower ionic liquid outlet 62 is positioned at the bottom of the sulfur dioxide desorption tower 6, and the sulfur dioxide outlet 63 is positioned at the top of the sulfur dioxide desorption tower 6; the sulfur dioxide outlet 63 is connected with a sulfur dioxide storage tank.
The absorption tower 7 is provided with an absorption tower flue gas inlet 71, an absorption tower flue gas outlet 72, an absorption tower ionic liquid inlet 73 and an absorption tower ionic liquid outlet 74; the absorption tower ionic liquid outlet 74 is positioned at the bottom of the absorption tower 7, and the absorption tower flue gas outlet 72 is positioned at the top of the absorption tower 7; the flue gas outlet 72 of the absorption tower is connected with a chimney.
The first heat exchanger flue gas outlet 12 is connected with a second heat exchanger flue gas inlet 21, the second heat exchanger flue gas outlet 22 is connected with a third heat exchanger flue gas inlet 31, the third heat exchanger flue gas outlet 32 is connected with an absorption tower flue gas inlet 71, an absorption tower ionic liquid outlet 74 is connected with a third ionic liquid inlet 33, a third heat exchanger ionic liquid outlet 34 is connected with a sulfur dioxide desorption tower ionic liquid inlet 61, a sulfur dioxide desorption tower ionic liquid outlet 62 is connected with a second ionic liquid inlet 23, a second heat exchanger ionic liquid outlet 24 is connected with a carbon dioxide desorption tower ionic liquid inlet 51, a carbon dioxide desorption tower ionic liquid outlet 52 is connected with a fourth ionic liquid inlet 43, and a fourth heat exchanger ionic liquid outlet 44 is connected with an absorption tower ionic liquid inlet 73;
example 2:
flue gas enters a first heat exchanger 1 through a first heat exchanger flue gas inlet 11, exchanges heat with heat supply network water in the first heat exchanger 1, is heated by the heat supply network water, is discharged through a first heat exchanger heat supply network water outlet 14, enters a heat supply network, is cooled, and enters a second heat exchanger 2 through a first heat exchanger flue gas outlet 12 and a second heat exchanger flue gas inlet 21;
the flue gas exchanges heat with the carbon dioxide-rich and sulfur dioxide-poor ionic liquid from the sulfur dioxide desorption tower 6 in the second heat exchanger 2, the ionic liquid enters the carbon dioxide desorption tower 5 after being heated through the second ionic liquid outlet 24 and the carbon dioxide desorption tower ionic liquid inlet 51, the flue gas enters the third heat exchanger 3 after being cooled through the second heat exchanger flue gas outlet 22 and the third heat exchanger flue gas inlet 31, the flue gas exchanges heat with the ionic liquid from the absorption tower 7 in the third heat exchanger 3, the ionic liquid enters the sulfur dioxide desorption tower 6 after being heated through the third heat exchanger ionic liquid outlet 34 and the sulfur dioxide desorption tower ionic liquid inlet 61, and the flue gas enters the absorption tower 7 after being cooled through the third heat exchanger flue gas outlet 32 and the absorption tower flue gas inlet 71;
the flue gas in the absorption tower 7 contacts with the ionic liquid to obtain the ionic liquid rich in carbon dioxide and sulfur dioxide and the flue gas poor in carbon dioxide and sulfur dioxide, the flue gas is discharged from a flue gas outlet 72 of the absorption tower and enters a chimney, the ionic liquid rich in carbon dioxide and sulfur dioxide enters a third heat exchanger 3 through an ionic liquid outlet 74 of the absorption tower and an ionic liquid inlet 33 of the third heat exchanger, the flue gas is heated in the third heat exchanger 3 and enters a sulfur dioxide desorption tower 6, the ionic liquid rich in carbon dioxide and sulfur dioxide is desorbed in the sulfur dioxide desorption tower 6, the desorbed sulfur dioxide enters a sulfur dioxide storage tank through a sulfur dioxide outlet 63, the residual ionic liquid rich in carbon dioxide and poor in sulfur dioxide enters a second heat exchanger 2 through an ionic liquid outlet 62 of the sulfur dioxide desorption tower and an ionic liquid inlet 23 of the second heat exchanger, the residual ionic liquid rich in carbon dioxide and poor in sulfur dioxide enters a carbon dioxide desorption tower 2 through an ionic liquid outlet 24 and an ionic liquid inlet 51 of the carbon dioxide desorption tower after being heated in the second heat exchanger 2 and enters a carbon dioxide desorption tower The absorption tower 5 is used for desorbing in the carbon dioxide desorption tower 5, the desorbed carbon dioxide is discharged through a carbon dioxide outlet 53 and enters a carbon dioxide storage tank, and the residual ionic liquid poor in carbon dioxide and sulfur dioxide enters the fourth heat exchanger 4 through an ionic liquid outlet 52 of the carbon dioxide desorption tower and an ionic liquid inlet 43 of the fourth heat exchanger;
the heat supply network water enters the fourth heat exchanger 4 through the fourth heat exchanger heat supply network water inlet 41, the heat supply network water in the fourth heat exchanger 4 exchanges heat with the ionic liquid from the carbon dioxide desorption tower 5, the ionic liquid is cooled, the ionic liquid enters the absorption tower 7 through the fourth heat exchanger ionic liquid outlet 44 and the absorption tower ionic liquid inlet 73, the heat supply network water is heated, and the heat supply network water enters the first heat exchanger 1 through the fourth heat exchanger heat supply network water outlet 42 and the first heat exchanger heat supply network water inlet 13.
After the temperature of the heat supply network water is raised in the first heat exchanger 1, the temperature is higher than 100 ℃ and lower than 130 ℃.
The utility model utilizes the characteristics that the absorption capacity of the ionic liquid to the carbon dioxide and the sulfur dioxide is reduced along with the increase of the temperature, and the difference of the absorption capacity to different gases is obvious along with the increase of the temperature, so that the carbon dioxide and the sulfur dioxide are absorbed at low temperature, the sulfur dioxide is released at medium temperature, and the carbon dioxide is released at high temperature, thereby realizing the simultaneous realization of sulfur capture and carbon capture in the flue gas. And the heat in the flue gas is recycled in a gradient manner. The flue gas is subjected to heat exchange and cooling by the first heat exchanger 1, the second heat exchanger 2 and the third heat exchanger 3 in sequence, so that the temperature of the flue gas entering the absorption tower 7 is controlled, and the absorption capacity of carbon dioxide and sulfur dioxide is improved; the heat supply network backwater is subjected to heat exchange and temperature rise through the fourth heat exchanger 4 and the first heat exchanger 1, the heat utilization efficiency of the system is high, the heat supply network water can reach 100-130 ℃ finally, and the heat supply network water value at the temperature is high.
The return water of the heat supply network is used as a cold source, so that the consumption of circulating cooling water is reduced, and a certain water-saving effect is achieved. By designing desorption towers with different temperatures, the respective removal and capture of carbon dioxide and sulfur dioxide are realized. The temperature of the flue gas entering the absorption tower is reduced and the absorption capacity of carbon dioxide is improved through the step temperature reduction of the flue gas and the step temperature rise of the return water of the heat supply network; meanwhile, the cascade utilization of the flue gas waste heat is realized, the heat utilization efficiency is improved, and the heat supply benefit is improved.
It will be appreciated by those skilled in the art that the utility model may be embodied in other specific forms without departing from the spirit or essential characteristics thereof. The embodiments disclosed above are therefore to be considered in all respects as illustrative and not restrictive. All changes which come within the scope of or equivalence to the utility model are intended to be embraced therein.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solutions of the present invention and not for limiting the same, and although the present invention is described in detail with reference to the above embodiments, those of ordinary skill in the art should understand that: modifications and equivalents may be made to the embodiments of the utility model without departing from the spirit and scope of the utility model, which is to be covered by the claims.
Claims (9)
1. A flue gas waste heat recovery device capable of simultaneously capturing carbon and sulfur is characterized by comprising a first heat exchanger (1), a second heat exchanger (2), a third heat exchanger (3), a fourth heat exchanger (4), a carbon dioxide desorption tower (5), a sulfur dioxide desorption tower (6) and an absorption tower (7);
a first heat exchanger flue gas inlet (11), a first heat exchanger flue gas outlet (12) and a first heat exchanger heat supply network water inlet (13) are formed in the first heat exchanger (1); the first heat exchanger flue gas inlet (11) is communicated with the first heat exchanger flue gas outlet (12);
a second heat exchanger flue gas inlet (21), a second heat exchanger flue gas outlet (22), a second heat exchanger ionic liquid inlet (23) and a second heat exchanger ionic liquid outlet (24) are formed in the second heat exchanger (2); the second heat exchanger flue gas inlet (21) is communicated with the second heat exchanger flue gas outlet (22), and the second heat exchanger ionic liquid inlet (23) is communicated with the second heat exchanger ionic liquid outlet (24);
a third heat exchanger flue gas inlet (31), a third heat exchanger flue gas outlet (32), a third heat exchanger ionic liquid inlet (33) and a third heat exchanger ionic liquid outlet (34) are formed in the third heat exchanger (3); the third heat exchanger flue gas inlet (31) is communicated with a third heat exchanger flue gas outlet (32), and the third heat exchanger ionic liquid inlet (33) is communicated with a third heat exchanger ionic liquid outlet (34);
a fourth heat exchanger heat supply network water inlet (41), a fourth heat exchanger heat supply network water outlet (42), a fourth heat exchanger ionic liquid inlet (43) and a fourth heat exchanger ionic liquid outlet (44) are formed in the fourth heat exchanger (4); a fourth heat exchanger heat supply network water inlet (41) is communicated with a fourth heat exchanger heat supply network water outlet (42), and a fourth heat exchanger ionic liquid inlet (43) is communicated with a fourth heat exchanger ionic liquid outlet (44);
the carbon dioxide desorption tower (5) is provided with a carbon dioxide desorption tower ionic liquid inlet (51) and a carbon dioxide desorption tower ionic liquid outlet (52);
the sulfur dioxide desorption tower (6) is provided with a sulfur dioxide desorption tower ionic liquid inlet (61) and a sulfur dioxide desorption tower ionic liquid outlet (62);
the absorption tower (7) is provided with an absorption tower flue gas inlet (71), an absorption tower ionic liquid inlet (73) and an absorption tower ionic liquid outlet (74);
a first heat exchanger flue gas outlet (12) is connected with a second heat exchanger flue gas inlet (21), a second heat exchanger flue gas outlet (22) is connected with a third heat exchanger flue gas inlet (31), a third heat exchanger flue gas outlet (32) is connected with an absorption tower flue gas inlet (71), an absorption tower ionic liquid outlet (74) is connected with a third heat exchanger ionic liquid inlet (33), a third heat exchanger ionic liquid outlet (34) is connected with a sulfur dioxide desorption tower ionic liquid inlet (61), a sulfur dioxide desorption tower ionic liquid outlet (62) is connected with a second heat exchanger ionic liquid inlet (23), a second heat exchanger ionic liquid outlet (24) is connected with a carbon dioxide desorption tower ionic liquid inlet (51), a carbon dioxide desorption tower ionic liquid outlet (52) is connected with a fourth heat exchanger ionic liquid inlet (43), and a fourth heat exchanger ionic liquid outlet (44) is connected with an absorption tower ionic liquid inlet (73);
the fourth heat exchanger heat supply network water outlet (42) is connected with the first heat exchanger heat supply network water inlet (13).
2. The flue gas waste heat recovery device for simultaneously capturing carbon and sulfur according to claim 1, wherein the first heat exchanger (1) is provided with a first heat exchanger heat supply network water outlet (14); the first heat exchanger heat supply network water inlet (13) is communicated with the first heat exchanger heat supply network water outlet (14); the first heat exchanger heat supply network water outlet (14) is connected with a heat supply network.
3. The flue gas waste heat recovery device for simultaneously capturing carbon and sulfur according to claim 1, wherein a carbon dioxide outlet (53) is provided on the carbon dioxide desorption tower (5); the carbon dioxide outlet (53) is connected with a carbon dioxide storage tank.
4. The flue gas waste heat recovery device for simultaneously capturing carbon and sulfur according to claim 1, wherein the sulfur dioxide desorption tower (6) is provided with a sulfur dioxide outlet (63), and the sulfur dioxide outlet (63) is connected with a sulfur dioxide storage tank.
5. The flue gas waste heat recovery device for simultaneously capturing carbon and sulfur according to claim 1, wherein the absorption tower (7) is provided with an absorption tower flue gas outlet (72), and the absorption tower flue gas outlet (72) is connected with a chimney.
6. The flue gas waste heat recovery device for simultaneously capturing carbon and sulfur according to claim 3, wherein the carbon dioxide desorption tower ionic liquid outlet (52) is located at the bottom of the carbon dioxide desorption tower (5), and the carbon dioxide outlet (53) is located at the top of the carbon dioxide desorption tower (5).
7. The flue gas waste heat recovery device for simultaneously capturing carbon and sulfur according to claim 4, wherein the sulfur dioxide desorption tower ionic liquid outlet (62) is positioned at the bottom of the sulfur dioxide desorption tower (6), and the sulfur dioxide outlet (63) is positioned at the top of the sulfur dioxide desorption tower (6).
8. The flue gas waste heat recovery device for simultaneously capturing carbon and sulfur according to claim 5, wherein the absorption tower ionic liquid outlet (74) is located at the bottom of the absorption tower (7), and the absorption tower flue gas outlet (72) is located at the top of the absorption tower (7).
9. The flue gas waste heat recovery device for simultaneously capturing carbon and sulfur according to claim 1, wherein the temperature of the heat supply network water is higher than 100 ℃ and lower than 130 ℃ after being heated in the first heat exchanger (1).
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| CN202123233877.XU CN216558458U (en) | 2021-12-21 | 2021-12-21 | Flue gas waste heat recovery device capable of simultaneously capturing carbon and sulfur |
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| CN202123233877.XU CN216558458U (en) | 2021-12-21 | 2021-12-21 | Flue gas waste heat recovery device capable of simultaneously capturing carbon and sulfur |
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