CN210410096U - Separation system for carbon dioxide in medium-high pressure gas source - Google Patents
Separation system for carbon dioxide in medium-high pressure gas source Download PDFInfo
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- CN210410096U CN210410096U CN201920583557.0U CN201920583557U CN210410096U CN 210410096 U CN210410096 U CN 210410096U CN 201920583557 U CN201920583557 U CN 201920583557U CN 210410096 U CN210410096 U CN 210410096U
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Abstract
The utility model provides a separation system of carbon dioxide in medium and high pressure gas source, which comprises an absorption tower, a flash tank, a high pressure desorption tower, a high pressure desorption reboiler, a low pressure desorption tower, a second low pressure desorption reboiler, a desorption gas cooler and a gas-liquid separator; CO from the absorption column2The rich solution is decompressed and regenerated step by flash evaporation, high-pressure desorption, low-pressure desorption and other modes, and CO is fully utilized2The characteristic of higher pressure of the air source reduces the input of external heat consumption; the requirements of low energy consumption and low cost are met.
Description
Technical Field
The utility model belongs to the technical field of gas separation technique, carbon dioxide reduce discharging, concretely relates to piece-rate system of carbon dioxide among well high-pressure air supply.
Background
Global climate change has seriously threatened the sustainable development of human society, living environment and economy. In 2013, the intergovernmental committee on climate change specialization (IPCC) issued "fifth climate change assessment report" indicated that the increase in greenhouse gas concentration was the major driver of climate change, CO2Is a greenhouse gas which contributes most to the temperature rise effect, and the control of the climate change requires the substantial and continuous reduction of CO2And (5) discharging. In 2018, IPCC again raised serious warning for global warming, CO2The emission control is not slow, and the global climate temperature rise target is improved from being controlled within 2 ℃ of the pre-industrialization level to being controlled within 1.5 ℃.
The coal-fired power plant is the CO of China2Centralizing stable emission sources, accounting for national CO235% of the total emission. In addition, a great deal of CO also exists in the industrial fields of ammonia synthesis, hydrogen production, coal gasification, coal chemical industry and the like2A trapping or separation process. Compared with flue gas of coal-fired power plants, the pressure of gas to be treated in the decarbonization process of the fields is high (2 MPa-5 MPa), and CO is2The concentration is high (25-60%). Traditional atmospheric CO2The separation process generally realizes CO by low-temperature absorption and high-temperature desorption2And (3) removing or recovering partial heat by means of a heat pump, mechanical vapor recompression and the like, so as to achieve the purposes of energy conservation and consumption reduction. But for medium and high pressure CO2Gas source, atmospheric CO2The separation process cannot fully utilize the characteristics of medium and high pressure gas sources, and the requirements of low energy consumption and low cost are difficult to fully meet.
Disclosure of Invention
An object of the utility model is to provide a carbon dioxide's piece-rate system in well high-pressure air supply has solved current ordinary pressure CO2The separation process can not realize medium-high pressure CO2And (4) removing.
In order to achieve the above purpose, the utility model discloses a technical scheme is:
the utility model provides a pair of separation system of carbon dioxide in well high-pressure air supply, including absorption tower, flash tank, high-pressure desorber, high pressure desorption reboiler, low pressure desorber, second low pressure desorption reboiler, desorption gas cooler and gas-liquid separation jar, wherein, the bottom CO of absorption tower2The rich liquid outlet is connected with the inlet of the flash tank, and the top desorption gas outlet of the flash tank is connected with the inlet of the gas-liquid separation tank through a desorption gas cooler;
the bottom liquid phase outlet of the flash tank is divided into two paths, and one path is connected with the inlet of the high-pressure desorption tower; the other path is connected with the inlet of the low-pressure desorption tower;
the bottom hot barren liquor outlet of the high-pressure desorption tower is connected with the top inlet of the absorption tower; a desorption gas outlet at the top of the high-pressure desorption tower is connected with an inlet of the gas-liquid separation tank through a second low-pressure desorption reboiler and a desorption gas cooler in sequence;
the high-pressure desorption tower is connected with a high-pressure desorption reboiler;
a semi-barren liquor outlet at the bottom of the low-pressure desorption tower is connected with a middle inlet of the absorption tower; a desorption gas outlet at the top of the low-pressure desorption tower is connected with an inlet of the gas-liquid separation tank through a desorption gas cooler;
the low-pressure desorption tower is connected with a second low-pressure desorption reboiler;
the bottom condensate outlet of the gas-liquid separator is respectively connected with the inlets of the high-pressure desorption tower and the low-pressure desorption tower, and the top of the gas-liquid separator is provided with CO2And (5) a product gas outlet.
Preferably, the top of the absorption tower is provided with a purified gas outlet.
Preferably, a barren liquor heat exchange device is arranged between the bottom hot barren liquor outlet of the high-pressure desorption tower and the absorption tower.
Preferably, the lean liquid heat exchange equipment comprises a lean liquid heat exchanger, wherein one path of a liquid phase outlet at the bottom of the flash tank is connected with a cold end inlet of the lean liquid heat exchanger, and a cold end outlet of the lean liquid heat exchanger is connected with an inlet of the high-pressure desorption tower; the hot lean solution outlet at the bottom of the high-pressure desorption tower is connected with the hot end inlet of the lean solution heat exchanger, and the hot end outlet of the lean solution heat exchanger is connected with the top inlet of the absorption tower.
Preferably, the hot end outlet of the lean liquid heat exchanger and the top inlet of the absorption tower are provided with lean liquid coolers.
Preferably, a semi-lean liquid heat exchange device is arranged between the bottom semi-lean liquid outlet of the low-pressure desorption tower and the middle inlet of the absorption tower.
Preferably, the semi-lean liquid heat exchange equipment comprises a semi-lean liquid heat exchanger, wherein the other path of the liquid phase outlet at the bottom of the flash tank is connected with a cold end inlet of the semi-lean liquid heat exchanger, and a cold end outlet of the semi-lean liquid heat exchanger is connected with an inlet of the low-pressure desorption tower; the hot lean solution outlet at the bottom of the low-pressure desorption tower is connected with the hot end inlet of the semi-lean solution heat exchanger, and the hot end outlet of the semi-lean solution heat exchanger is connected with the middle inlet of the absorption tower.
Preferably, a semi-lean liquid heat exchanger is arranged between the hot end outlet of the semi-lean liquid heat exchanger and the middle inlet of the absorption tower.
Preferably, the high-pressure desorption reboiler is connected with an external heat source device.
Preferably, the low-pressure desorption tower is further connected with a first low-pressure desorption reboiler respectively, and the first low-pressure desorption reboiler is connected with an external heat source device.
Compared with the prior art, the beneficial effects of the utility model are that:
the utility model provides a pair of separation system of carbon dioxide in well high-pressure air supply comes from the CO of absorption tower2The rich solution is decompressed and regenerated step by flash evaporation, high-pressure desorption, low-pressure desorption and other modes, and CO is fully utilized2The characteristic of higher pressure of the air source reduces the input of external heat consumption; the requirements of low energy consumption and low cost are met.
Furthermore, high-temperature desorption gas at the top of the high-pressure desorption tower is introduced into a reboiler of the low-pressure desorption tower to be used as a heat source for heating desorption, so that the external heat consumption required by the low-pressure desorption tower is reduced, and the cooling water consumption of the gas-suction cooler is reduced.
Furthermore, barren solution and semi-barren solution from the high-pressure desorption tower and the low-pressure desorption tower respectively enter from the upper-section packing and the middle-section packing of the absorption tower, so that the reaction temperature at each part of the tower body is kept uniform, the local overhigh temperature is avoided, and the degradation and loss of the absorbent are reduced.
Furthermore, energy is optimized and utilized according to the medium-high pressure characteristics of the separation process and the heat energy grade characteristics in the system, heat recovery equipment such as a heat pump and mechanical vapor recompression is not introduced, and the investment cost and the operation cost are effectively reduced.
Drawings
Fig. 1 is a schematic structural view of a separation system according to the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings.
As shown in figure 1, the utility model provides a pair of separation system of carbon dioxide in well high-pressure gas source, including absorption tower 1, flash tank 2, barren solution heat exchanger 3, high pressure desorber 4, high pressure desorption reboiler 5, barren solution pump 6, barren solution cooler 7, half barren solution heat exchanger 8, low pressure desorber 9, half barren solution pump 10, half barren solution cooler 11, first low pressure desorption reboiler 12, second low pressure desorption reboiler 13, desorption gas cooler 14, vapour and liquid separator 15 and condensate pump 16, wherein, the gas inlet of absorption tower 1 with contain CO2The rich liquid outlet of the absorption tower 1 is connected with the solution inlet of the flash tank 2; the solution outlet at the bottom of the flash tank 2 is divided into two paths, and one path is connected with the solution inlet at the upper part of the high-pressure desorption tower 4 through a barren solution heat exchanger 3; the high-pressure desorption tower 4 is provided with a high-pressure desorption reboiler 5 which is used for supplying heat by external steam stripping; a barren liquor outlet at the bottom of the high-pressure desorption tower 4 is connected with a barren liquor inlet at the upper part of the absorption tower 1 sequentially through a barren liquor heat exchanger 3, a barren liquor pump 6 and a barren liquor cooler 7;
the other path of the solution outlet at the bottom of the flash tank 2 is connected with the upper part and the middle solution inlet of a low-pressure desorption tower 9 through a semi-barren solution heat exchanger 8; a semi-product liquid outlet at the bottom of the low-pressure desorption tower 9 is connected with a semi-barren liquid inlet in the middle of the absorption tower 1 sequentially through a semi-barren liquid heat exchanger 8, a semi-barren liquid pump 10 and a semi-barren liquid cooler 11;
the low-pressure desorption tower 9 is provided with a first low-pressure desorption reboiler 12 and a second low-pressure desorption reboiler 13; a heat source is supplied to the first low-pressure desorption reboiler 12 by external steam stripping, and a heat source is supplied to the second low-pressure desorption reboiler 13 by desorption gas from the top of the high-pressure desorption tower 4;
the desorption gas from the top of the flash tank 2, the top of the high-pressure desorption tower 4 and the top of the low-pressure desorption tower 9 is connected with an inlet of a gas-liquid separator 15 through a desorption gas cooler 14; a condensate outlet at the bottom of the gas-liquid separator 15 is respectively connected with condensate inlets at the upper parts of the high-pressure desorption tower 4 and the low-pressure desorption tower 9 through a condensate pump 16, and a gas outlet at the upper part of the gas-liquid separator 15 is a carbon dioxide product gas outlet.
The working principle of the utility model is as follows:
containing CO2The industrial gas enters the absorption tower from the lower part of the absorption tower 1 to be in countercurrent contact with absorbent barren solution and semi-barren solution which are added from different positions, and absorption and CO removal are completed2Process, removal of CO2The purified gas after the reaction is discharged from the top of the absorption tower 1.
The lean liquid from the lean liquid cooler 7 is fed from the upper part of the uppermost stage of the packing, and the semi-lean liquid from the semi-lean liquid heat exchanger 11 is fed from the upper part of the intermediate packing.
CO discharged from the bottom of the absorption column 12The rich liquid enters a flash tank 2 for preliminary decompression and desorption, and the desorbed gas discharged from the top of the flash tank 2 enters a gas-liquid separation tank 15 through a desorbed gas cooler 14;
the discharged liquid phase at the bottom of the flash tank 2 is divided into two paths, one path enters a high-pressure desorption tower 4 for desorption after being preheated by a barren liquor heat exchanger 3, and the other path enters a low-pressure desorption tower 9 for desorption after being preheated by a semi-barren liquor heat exchanger 8.
The barren liquor heat exchanger 3 is heated by hot barren liquor at the tower bottom of the high-pressure desorption tower 4, and the semi-barren liquor heat exchanger 8 is heated by hot semi-barren liquor at the tower bottom of the low-pressure desorption tower 9.
The high-pressure desorption tower 4 is heated by a high-pressure desorption reboiler 5, and the heat source adopts steam from outside a battery limit zone; the hot barren liquor at the bottom of the high-pressure desorption tower 4 is sent to a barren liquor cooler 7 for further temperature reduction by a barren liquor pump 6 after waste heat is recovered by a barren liquor heat exchanger 3, and then is sent to the absorption tower 1 for recycling.
The desorption gas at the top of the high-pressure desorption tower 4 enters a second low-pressure desorption reboiler 13 at the lower part of the low-pressure desorption tower 9 to recover heat, and is further condensed by a desorption gas cooler 14 and then enters a gas-liquid separator 15.
The low pressure stripper column 9 has two reboilers, of which the first low pressure stripper reboiler 12 is supplied with heat from external steam stripping and the second low pressure stripper reboiler 13 is supplied with heat from the stripper gas from the top of the high pressure stripper column 4.
The semi-barren liquor at the bottom of the low-pressure desorption tower 9 exchanges heat through the semi-barren liquor heat exchanger 8, and then is sent into the semi-barren liquor heat exchanger 11 by the semi-barren liquor pump 10 to be further cooled and then returns to the absorption tower 1 for recycling.
The desorption gas at the top of the low-pressure desorption tower 9 is further condensed by a desorption gas cooler 14 and then enters a gas-liquid separator 15.
Condensate at the bottom of the gas-liquid separator 15 returns to the high-pressure desorption tower 4 and the low-pressure desorption tower 9 through a condensate pump 16 respectively; the gas outlet at the upper part of the gas-liquid separator 15 is CO2And (5) producing gas.
Claims (10)
1. The separation system for the carbon dioxide in the medium-high pressure gas source is characterized by comprising an absorption tower (1), a flash tank (2), a high-pressure desorption tower (4), a high-pressure desorption reboiler (5), a low-pressure desorption tower (9), a second low-pressure desorption reboiler (13), a desorption gas cooler (14) and a gas-liquid separator (15), wherein the bottom CO of the absorption tower (1) is connected with a gas-liquid separator2The rich liquid outlet is connected with the inlet of the flash tank (2), and the top desorption gas outlet of the flash tank (2) is connected with the inlet of the gas-liquid separator (15) of the gas-liquid separator through a desorption gas cooler (14);
the bottom liquid phase outlet of the flash tank (2) is divided into two paths, and one path is connected with the inlet of the high-pressure desorption tower (4); the other path is connected with the inlet of the low-pressure desorption tower (9);
the bottom hot barren liquor outlet of the high-pressure desorption tower (4) is connected with the top inlet of the absorption tower (1); a desorption gas outlet at the top of the high-pressure desorption tower (4) is connected with an inlet of a gas-liquid separator (15) of a gas-liquid separator sequentially through a second low-pressure desorption reboiler (13) and a desorption gas cooler (14);
the high-pressure desorption tower (4) is connected with a high-pressure desorption reboiler (5);
a semi-barren liquor outlet at the bottom of the low-pressure desorption tower (9) is connected with a middle inlet of the absorption tower (1); a desorption gas outlet at the top of the low-pressure desorption tower (9) is connected with an inlet of a gas-liquid separator (15) through a desorption gas cooler (14);
the low-pressure desorption tower (9) is connected with a second low-pressure desorption reboiler (13);
the bottom condensate outlet of the gas-liquid separator (15) is respectively connected with the inlets of the high-pressure desorption tower (4) and the low-pressure desorption tower (9), and the top of the gas-liquid separator (15) is provided with CO2And (5) a product gas outlet.
2. The system for separating carbon dioxide from a source of medium and high pressure gas as claimed in claim 1, characterized in that the top of the absorption tower (1) is provided with a purge gas outlet.
3. The system for separating carbon dioxide from a medium and high pressure gas source according to claim 1, wherein a lean liquid heat exchange device is arranged between the bottom hot lean liquid outlet of the high pressure desorption tower (4) and the absorption tower (1).
4. The system for separating the carbon dioxide from the medium-high pressure gas source according to claim 3, wherein the lean liquid heat exchanger comprises a lean liquid heat exchanger (3), wherein one path of a liquid phase outlet at the bottom of the flash tank (2) is connected with a cold end inlet of the lean liquid heat exchanger (3), and a cold end outlet of the lean liquid heat exchanger (3) is connected with an inlet of the high-pressure desorption tower (4); the hot lean solution outlet at the bottom of the high-pressure desorption tower (4) is connected with the hot end inlet of the lean solution heat exchanger (3), and the hot end outlet of the lean solution heat exchanger (3) is connected with the top inlet of the absorption tower (1).
5. The system for separating carbon dioxide from a medium and high pressure gas source as claimed in claim 4, wherein the lean liquid cooler (7) is provided at the hot end outlet of the lean liquid heat exchanger (3) and the top inlet of the absorption tower (1).
6. The system for separating carbon dioxide from a medium and high pressure gas source as claimed in claim 1, wherein a semi-lean liquid heat exchange device is arranged between the bottom semi-lean liquid outlet of the low pressure desorption tower (9) and the middle inlet of the absorption tower (1).
7. The system for separating the carbon dioxide from the medium-high pressure gas source according to claim 6, wherein the semi-lean liquid heat exchange device comprises a semi-lean liquid heat exchanger (8), wherein the other path of the liquid phase outlet at the bottom of the flash tank (2) is connected with a cold end inlet of the semi-lean liquid heat exchanger (8), and a cold end outlet of the semi-lean liquid heat exchanger (8) is connected with an inlet of the low-pressure desorption tower (9); the hot lean solution outlet at the bottom of the low-pressure desorption tower (9) is connected with the hot end inlet of the semi-lean solution heat exchanger (8), and the hot end outlet of the semi-lean solution heat exchanger (8) is connected with the middle inlet of the absorption tower (1).
8. The system for separating carbon dioxide from a source of medium and high pressure gas according to claim 7, characterized in that a semi-lean liquid cooler (11) is arranged between the hot end outlet of the semi-lean liquid heat exchanger (8) and the middle inlet of the absorption column (1).
9. The system for separating carbon dioxide from a medium-high pressure gas source according to claim 1, wherein the high-pressure desorption reboiler (5) is connected to an external heat source device.
10. The system for separating carbon dioxide from a medium and high pressure gas source as claimed in claim 1, wherein the low pressure desorption tower (9) is further connected with a first low pressure desorption reboiler (12), and the first low pressure desorption reboiler (12) is connected with an external heat source device.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920583557.0U CN210410096U (en) | 2019-04-25 | 2019-04-25 | Separation system for carbon dioxide in medium-high pressure gas source |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201920583557.0U CN210410096U (en) | 2019-04-25 | 2019-04-25 | Separation system for carbon dioxide in medium-high pressure gas source |
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| CN201920583557.0U Active CN210410096U (en) | 2019-04-25 | 2019-04-25 | Separation system for carbon dioxide in medium-high pressure gas source |
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