CN219149739U - Flue gas waste heat utilization device combining wastewater treatment and carbon dioxide trapping - Google Patents
Flue gas waste heat utilization device combining wastewater treatment and carbon dioxide trapping Download PDFInfo
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- CN219149739U CN219149739U CN202223388793.8U CN202223388793U CN219149739U CN 219149739 U CN219149739 U CN 219149739U CN 202223388793 U CN202223388793 U CN 202223388793U CN 219149739 U CN219149739 U CN 219149739U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The utility model relates to a flue gas waste heat utilization device combining wastewater treatment and carbon dioxide trapping, and belongs to the field of flue gas waste heat treatment. The flue gas is led out from a dust remover, enters a first heat exchanger to heat rich liquid, enters an evaporator to treat high-salt wastewater, enters a desulfurizing tower to remove sulfur, and finally enters an absorption tower to remove carbon dioxide; the rich liquid of the carbon dioxide absorbent exchanges heat with the flue gas through a first heat exchanger, is heated to a set temperature and then enters a desorption tower for desorption, the lean liquid exchanges heat with the high-salt wastewater through a second heat exchanger, and is cooled to the set temperature and then enters an absorption tower for absorbing carbon dioxide in the flue gas; the high-salt wastewater exchanges heat with lean solution through a second heat exchanger, the temperature is increased, and the high-salt wastewater enters an evaporation tower and is treated by utilizing the waste heat of flue gas. The utility model combines the high-salt wastewater treatment with the carbon dioxide treatment in the flue gas by utilizing the reaction characteristic of the absorbent and the carbon dioxide so as to achieve the purpose of fully utilizing the waste heat of the flue gas.
Description
Technical Field
The utility model relates to a flue gas waste heat utilization device, in particular to a flue gas waste heat utilization device combining wastewater treatment and carbon dioxide trapping, and belongs to the field of flue gas waste heat treatment.
Background
The thermal power plant is a large household of industrial water, and the water intake and the water discharge are huge. With the release of national energy saving law, environmental protection law, water pollution control action plan and corresponding water and drainage charging policies (water resource cost, drainage cost and excessive standard cost), and the gradual implementation of regulations of electric power industry 'ten-five' water saving plan, the water pollution control action plan has strict index limit on the use, drainage and water quality of a thermal power plant. Although most power plants have been modified by deeply optimizing water, the cascade utilization of water is realized, a part of high-salt wastewater cannot be recycled and needs to be deeply treated.
Under the condition of double carbon, carbon dioxide in flue gas discharged by a thermal power plant can be treated only by a trapping method, the most main method at present is a chemical method, the carbon dioxide absorption process is an exothermic reaction, and the desorption process is an endothermic reaction.
The characteristic of capturing carbon dioxide by a chemical method is utilized, a flue gas waste heat utilization device and a flue gas waste heat utilization method combining wastewater treatment and carbon dioxide capturing are designed, and waste heat in flue gas is utilized to heat an absorbent, so that desorption of rich liquid is realized; the waste heat of the rich liquid is utilized to heat the high-salt-content waste water, the temperature of the waste water entering the evaporator is improved, the optimal reaction temperature of the absorbent and the carbon dioxide is ensured, the evaporation time of the waste water entering the evaporator is reduced, and the heat of the system is fully utilized.
Disclosure of Invention
The utility model aims to overcome the defects in the prior art, and provides the flue gas waste heat utilization device combining the waste water treatment and the carbon dioxide collection, which has the advantages of reasonable structural design, safety, reliability, investment cost saving, full utilization of flue gas waste heat and capability of solving the problems of carbon collection and waste water treatment of the flue gas on the premise of not adding a new energy source.
The utility model solves the problems by adopting the following technical scheme: the flue gas waste heat utilization device combining wastewater treatment and carbon dioxide capture comprises a first heat exchanger, a desorption tower, a second heat exchanger, a carbon dioxide absorption tower, a desulfurization absorption tower and an evaporation tower, wherein the first heat exchanger is provided with a flue gas heat exchange inlet, a flue gas heat exchange outlet, an absorbent rich liquid heat exchange inlet and an absorbent rich liquid heat exchange outlet; the desorption tower is provided with a rich liquid absorbent inlet and a lean liquid absorbent outlet; the second heat exchanger is provided with a lean liquid heat exchange inlet and a lean liquid heat exchange outlet; the carbon dioxide absorption tower is provided with a flue gas inlet, a lean solution absorbent inlet and a rich solution absorbent outlet; the desulfurizing absorption tower is provided with entry and export, and the evaporating tower is provided with evaporation flue gas entry, evaporation flue gas export and high salt wastewater inlet, its characterized in that: the flue gas heat exchange outlet of the first heat exchanger is connected with the evaporation flue gas inlet of the evaporation tower, the evaporation flue gas outlet of the evaporation tower is connected with the inlet of the desulfurization absorption tower, and the upper outlet of the desulfurization absorption tower is connected with the flue gas inlet of the carbon dioxide absorption tower; the bottom of the carbon dioxide absorption tower is provided with a rich liquid absorbent outlet for discharging absorbent rich liquid, the rich liquid absorbent outlet is connected with an absorbent rich liquid heat exchange inlet of the first heat exchanger, the absorbent rich liquid heat exchange outlet of the first heat exchanger is connected with a rich liquid absorbent inlet of the desorption tower, the lean liquid absorbent outlet is connected with a lean liquid heat exchange inlet of the second heat exchanger, and the lean liquid heat exchange outlet of the second heat exchanger is connected to the carbon dioxide absorption tower through the lean liquid absorbent inlet.
Preferably, the desorption tower is further provided with a carbon dioxide collecting port, and pure carbon dioxide gas desorbed from the rich liquid is collected through the carbon dioxide collecting port for later use.
Preferably, the second heat exchanger is further provided with a high-salt-content wastewater heat exchange inlet and a high-salt-content wastewater outlet, and the high-salt-content wastewater outlet passes through the high-salt-content wastewater inlet to the evaporation tower.
Preferably, the carbon dioxide absorption tower is also provided with a flue gas outlet, the upper part of the carbon dioxide absorption tower is provided with a flue gas outlet, and the treated qualified flue gas is discharged to the atmosphere through a chimney.
Compared with the prior art, the utility model has the following advantages and effects: the whole structure is reasonable in design, the waste heat of the flue gas is fully utilized, and the high-salt wastewater treatment and the carbon dioxide capture in the flue gas are realized under the condition that new heat is not introduced; the waste heat of the lean solution after desorption is utilized to preheat the high-salt-content waste water, so that the temperature of the waste water entering an evaporator is increased, the evaporation time of the waste water is reduced, and a certain investment cost can be saved; the tail flue gas treatment and wastewater treatment are combined, and the cascade utilization of waste heat is realized.
Drawings
Fig. 1 is a schematic diagram of a flue gas waste heat utilization system according to an embodiment of the present utility model.
In the figure: the device comprises a first heat exchanger A, a desorption tower B, a second heat exchanger C, a carbon dioxide absorption tower D, a desulfurization absorption tower E and an evaporation tower F;
the first heat exchanger A: a flue gas heat exchange inlet 1, a flue gas heat exchange outlet 2, an absorbent rich liquid heat exchange inlet 9 and an absorbent rich liquid heat exchange outlet 10;
desorber B: a rich liquid absorbent inlet 11, a lean liquid absorbent outlet 12, a carbon dioxide collection port 20;
the second heat exchanger C: a lean liquid heat exchange inlet 13, a lean liquid heat exchange outlet 14, a high salt-containing wastewater heat exchange inlet 17 and a high salt-containing wastewater outlet 18;
carbon dioxide absorption tower D: a flue gas inlet 7, a flue gas outlet 8, a lean liquid absorbent inlet 15, a rich liquid absorbent outlet 16;
desulfurizing absorption tower E: an inlet 5, an outlet 6;
evaporation tower F: an evaporation flue gas inlet 3, an evaporation flue gas outlet 4 and a high salt wastewater inlet 19.
Detailed Description
The present utility model will be described in further detail by way of examples with reference to the accompanying drawings, which are illustrative of the present utility model and not limited to the following examples.
Examples
Referring to fig. 1, the flue gas waste heat utilization device combining wastewater treatment and carbon dioxide capturing in this embodiment is mainly provided with a flue gas side, a waste water side and an absorbent side, and includes a first heat exchanger a, a desorption tower B, a second heat exchanger C, a carbon dioxide absorption tower D, a desulfurization absorption tower E and an evaporation tower F.
The first heat exchanger a in this embodiment is mainly responsible for heating the absorbent rich liquid by flue gas, and is provided with a flue gas heat exchange inlet 1, a flue gas heat exchange outlet 2, an absorbent rich liquid heat exchange inlet 9 and an absorbent rich liquid heat exchange outlet 10.
The desorber B in this embodiment mainly desorbs carbon dioxide in the rich liquid to obtain pure carbon dioxide and an absorbent, and the reaction process is an endothermic reaction, and a rich liquid absorbent inlet 11, a lean liquid absorbent outlet 12 and a carbon dioxide collecting port 20 are provided.
The second heat exchanger C in this embodiment is mainly responsible for heat exchange between lean solution and high-salt wastewater, and reduces the temperature of the lean solution, and is provided with a lean solution heat exchange inlet 13, a lean solution heat exchange outlet 14, a high-salt wastewater heat exchange inlet 17 and a high-salt wastewater outlet 18.
The carbon dioxide absorber D in this embodiment mainly absorbs carbon dioxide in the flue gas, and the reaction process is an exothermic reaction, and a flue gas inlet 7, a flue gas outlet 8, a lean solution absorber inlet 15 and a rich solution absorber outlet 16 are provided.
The desulfurization absorbing tower E in the present embodiment is provided with an inlet 5 and an outlet 6.
The evaporation tower F in this embodiment utilizes the waste heat of the flue gas to treat the high-salt-content waste water, and is provided with an evaporation flue gas inlet 3, an evaporation flue gas outlet 4 and a high-salt-content waste water inlet 19.
The flue gas heat exchange outlet 2 of the first heat exchanger A in the embodiment is connected with an evaporation tower F through an evaporation flue gas inlet 3, an evaporation flue gas outlet 4 of the evaporation tower F is connected with a desulfurization absorption tower E through an inlet 5, and an upper outlet 6 of the desulfurization absorption tower E is connected with a carbon dioxide absorption tower D through a flue gas inlet 7;
the bottom of the carbon dioxide absorption tower D in this embodiment is provided with a rich liquid absorbent outlet 16 for discharging the absorbent rich liquid, and is connected to the first heat exchanger a through an absorbent rich liquid heat exchange inlet 9, and the upper portion of the carbon dioxide absorption tower D is provided with a flue gas outlet 8.
The absorbent rich liquid heat exchange outlet 10 of the first heat exchanger a in this embodiment is connected to the desorption tower B through a rich liquid absorbent inlet 11, the lean liquid of the lean liquid absorbent outlet 12 is passed through a lean liquid heat exchange inlet 13 to the second heat exchanger C, the lean liquid heat exchange outlet 14 of the second heat exchanger C is passed through a lean liquid absorbent inlet 15 to the carbon dioxide absorption tower D, and the upper portion of the first heat exchanger B is provided with a carbon dioxide collecting port 20.
The high salt content waste water heat exchange inlet 17 in this embodiment is connected to the lower part of the second heat exchanger C, and the high salt content waste water outlet 18 is connected to the evaporation tower F through the high salt content waste water inlet 19.
The embodiment combines the high-salt wastewater treatment with the carbon dioxide treatment in the flue gas by utilizing the reaction characteristic of the absorbent and the carbon dioxide so as to achieve the purpose of fully utilizing the waste heat of the flue gas.
In the embodiment, the flue gas waste heat after the dust remover of the thermal power plant is utilized to heat the carbon dioxide absorbent rich liquid, and then the high-salt-content wastewater is treated, so that the purpose of fully utilizing the flue gas waste heat is achieved.
In the embodiment, the waste heat of the lean solution of the carbon dioxide absorbent at the outlet of the desorption tower B is utilized to preheat the high-salt-content waste water, so that the purpose of reutilizing the waste heat of the lean solution is achieved.
In the embodiment, the high-salt-content wastewater is preheated by lean solution, the temperature is increased, and then enters an evaporation tower F for treatment by using the waste heat of the flue gas.
The embodiment is suitable for a thermal generator set, and after heat exchange is carried out between the flue gas after the dust remover and the carbon dioxide absorbent rich liquid, the flue gas enters an evaporation tower to treat high-salt-content wastewater, then enters a desulfurization absorption tower E to remove sulfur in the flue gas, and finally enters a carbon dioxide absorption tower D to remove carbon dioxide in the flue gas.
In the embodiment, the carbon dioxide absorbent rich liquid exchanges heat with the flue gas through a heat exchanger, is heated to a set temperature and then enters a desorption tower B for desorption, the lean liquid exchanges heat with the high-salt wastewater through the heat exchanger, and is cooled to the set temperature and then enters an absorption tower for absorbing carbon dioxide in the flue gas.
The flue gas waste heat utilization device combining wastewater treatment and carbon dioxide trapping has the following process flow:
(1) The flue gas with the temperature of about 120-150 ℃ is led into the first heat exchanger A from the outlet of the dust remover, enters from the flue gas heat exchange inlet 1, is led out from the flue gas heat exchange outlet 2, enters the evaporation tower F from the evaporation flue gas inlet 3, is led out from the evaporation flue gas outlet 4, enters the desulfurization absorption tower E from the inlet 5, is led out from the upper outlet 6 of the desulfurization absorption tower E, finally enters the carbon dioxide absorption tower D from the flue gas inlet 7, and is led out from the upper flue gas outlet 8 of the carbon dioxide absorption tower D.
(2) The absorbent rich liquid discharged from the bottom of the carbon dioxide absorption tower D through the rich liquid absorbent outlet 16 enters the first heat exchanger A from the absorbent rich liquid heat exchange inlet 9, is heated to 80-100 ℃, is discharged from the absorbent rich liquid heat exchange outlet 10, enters the desorption tower B from the rich liquid absorbent inlet 11, the lean liquid is discharged from the lean liquid absorbent outlet 12, pure carbon dioxide is discharged and collected from the carbon dioxide collecting port 20, the lean liquid enters the second heat exchanger C from the lean liquid heat exchange inlet 13, is discharged from the lean liquid heat exchange outlet 14 after the heat exchange temperature reaches 30-50 ℃, and enters the carbon dioxide absorption tower D from the lean liquid absorbent inlet 15.
(3) The high-salt wastewater after turbidity removal enters the second heat exchanger C from the high-salt wastewater heat exchange inlet 17 to be preheated, is discharged through the high-salt wastewater outlet 18, and then enters the evaporation tower F through the high-salt wastewater inlet 19 to be treated by utilizing the waste heat of flue gas.
From the above description, those skilled in the art will be able to practice.
In addition, it should be noted that the specific embodiments described in the present specification may vary from part to part, from name to name, etc., and the above description in the present specification is merely illustrative of the structure of the present utility model. All equivalent or simple changes of the structure, characteristics and principle according to the inventive concept are included in the protection scope of the present patent. Those skilled in the art may make various modifications or additions to the described embodiments or substitutions in a similar manner without departing from the scope of the utility model as defined in the accompanying claims.
Claims (4)
1. The flue gas waste heat utilization device combining wastewater treatment and carbon dioxide capture comprises a first heat exchanger (A), a desorption tower (B), a second heat exchanger (C), a carbon dioxide absorption tower (D), a desulfurization absorption tower (E) and an evaporation tower (F), wherein the first heat exchanger (A) is provided with a flue gas heat exchange inlet (1), a flue gas heat exchange outlet (2), an absorbent rich liquid heat exchange inlet (9) and an absorbent rich liquid heat exchange outlet (10); the desorption tower (B) is provided with a rich liquid absorbent inlet (11) and a lean liquid absorbent outlet (12); the second heat exchanger (C) is provided with a lean liquid heat exchange inlet (13) and a lean liquid heat exchange outlet (14); the carbon dioxide absorption tower (D) is provided with a flue gas inlet (7), a lean solution absorbent inlet (15) and a rich solution absorbent outlet (16); the desulfurization absorption tower (E) is provided with an inlet (5) and an outlet (6), and the evaporation tower (F) is provided with an evaporation flue gas inlet (3), an evaporation flue gas outlet (4) and a high-salt-content wastewater inlet (19), and is characterized in that: the flue gas heat exchange outlet (2) of the first heat exchanger (A) is connected with the evaporation flue gas inlet (3) of the evaporation tower (F), the evaporation flue gas outlet (4) of the evaporation tower (F) is connected with the inlet (5) of the desulfurization absorption tower (E), and the upper outlet (6) of the desulfurization absorption tower (E) is connected with the flue gas inlet (7) of the carbon dioxide absorption tower (D); the bottom of the carbon dioxide absorption tower (D) is provided with a rich liquor absorbent outlet (16) for discharging absorbent rich liquor, the rich liquor absorbent outlet is connected with an absorbent rich liquor heat exchange inlet (9) of the first heat exchanger (A), an absorbent rich liquor heat exchange outlet (10) of the first heat exchanger (A) is connected with a rich liquor absorbent inlet (11) of the desorption tower (B), a lean liquor absorbent outlet (12) is connected with a lean liquor heat exchange inlet (13) of the second heat exchanger (C), and a lean liquor heat exchange outlet (14) of the second heat exchanger (C) is connected to the carbon dioxide absorption tower (D) through a lean liquor absorbent inlet (15).
2. The flue gas waste heat utilization device combining wastewater treatment and carbon dioxide capturing according to claim 1, wherein: the desorption tower (B) is also provided with a carbon dioxide collecting port (20), and pure carbon dioxide gas desorbed from the rich liquid is collected through the carbon dioxide collecting port (20) for later use.
3. The flue gas waste heat utilization device combining wastewater treatment and carbon dioxide capturing according to claim 1, wherein: the second heat exchanger (C) is further provided with a high-salt-content wastewater heat exchange inlet (17) and a high-salt-content wastewater outlet (18), and the high-salt-content wastewater outlet (18) passes through the high-salt-content wastewater inlet (19) to the evaporation tower (F).
4. The flue gas waste heat utilization device combining wastewater treatment and carbon dioxide capturing according to claim 1, wherein: the carbon dioxide absorption tower (D) is also provided with a flue gas outlet (8), the upper part of the carbon dioxide absorption tower (D) is provided with the flue gas outlet (8), and the treated qualified flue gas is discharged to the atmosphere through a chimney.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202223388793.8U CN219149739U (en) | 2022-12-17 | 2022-12-17 | Flue gas waste heat utilization device combining wastewater treatment and carbon dioxide trapping |
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| CN202223388793.8U CN219149739U (en) | 2022-12-17 | 2022-12-17 | Flue gas waste heat utilization device combining wastewater treatment and carbon dioxide trapping |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116550117A (en) * | 2023-07-07 | 2023-08-08 | 山西大地生态环境技术研究院有限公司 | Device and method for capturing carbon dioxide and co-producing organic weak acid salt |
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2022
- 2022-12-17 CN CN202223388793.8U patent/CN219149739U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116550117A (en) * | 2023-07-07 | 2023-08-08 | 山西大地生态环境技术研究院有限公司 | Device and method for capturing carbon dioxide and co-producing organic weak acid salt |
| CN116550117B (en) * | 2023-07-07 | 2023-09-15 | 山西大地生态环境技术研究院有限公司 | Device and method for capturing carbon dioxide and co-producing organic weak acid salt |
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