CN109999618B - System and method for separating carbon dioxide from medium-high pressure gas source - Google Patents
System and method for separating carbon dioxide from medium-high pressure gas source Download PDFInfo
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- CN109999618B CN109999618B CN201910340516.3A CN201910340516A CN109999618B CN 109999618 B CN109999618 B CN 109999618B CN 201910340516 A CN201910340516 A CN 201910340516A CN 109999618 B CN109999618 B CN 109999618B
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 36
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 18
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 18
- 238000000034 method Methods 0.000 title claims abstract description 11
- 238000003795 desorption Methods 0.000 claims abstract description 173
- 239000007788 liquid Substances 0.000 claims abstract description 89
- 238000010521 absorption reaction Methods 0.000 claims abstract description 42
- 238000000926 separation method Methods 0.000 claims abstract description 17
- 230000006837 decompression Effects 0.000 claims abstract description 5
- 239000007791 liquid phase Substances 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 6
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 239000000945 filler Substances 0.000 abstract description 4
- 230000002745 absorbent Effects 0.000 abstract description 3
- 239000002250 absorbent Substances 0.000 abstract description 3
- 230000015556 catabolic process Effects 0.000 abstract description 2
- 238000006243 chemical reaction Methods 0.000 abstract description 2
- 239000000498 cooling water Substances 0.000 abstract description 2
- 238000006731 degradation reaction Methods 0.000 abstract description 2
- 238000001704 evaporation Methods 0.000 abstract description 2
- 230000008020 evaporation Effects 0.000 abstract description 2
- 238000010438 heat treatment Methods 0.000 abstract description 2
- 230000008929 regeneration Effects 0.000 abstract description 2
- 238000011069 regeneration method Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 52
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005261 decarburization Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
According to the separation system and method for the carbon dioxide in the medium-high pressure gas source, the CO 2 rich liquid from the absorption tower is subjected to gradual decompression regeneration in the modes of flash evaporation, high-pressure desorption, low-pressure desorption and the like, so that the characteristic of higher pressure of the CO 2 gas source is fully utilized, and the input of external heat consumption is reduced; the requirements of low energy consumption and low cost are met; the high-temperature desorption gas at the top of the high-pressure desorption tower is introduced into the reboiler of the low-pressure desorption tower and used as a heat source for heating and desorbing, so that the external heat consumption required by the low-pressure desorption tower is reduced, and the consumption of cooling water of an desorption cooler is reduced; lean liquid and semi-lean liquid from the high-pressure desorption tower and the low-pressure desorption tower respectively enter from the upper section filler and the middle section filler of the absorption tower, so that the uniform reaction temperature of each part of the tower body is maintained, the local temperature is avoided from being too high, and the degradation and loss of the absorbent are reduced; the invention fully utilizes the characteristic of higher pressure of the CO 2 gas source, and reduces the input of external heat consumption; meets the requirements of low energy consumption and low cost.
Description
Technical Field
The invention belongs to the technical field of gas separation technology and carbon dioxide emission reduction, and particularly relates to a system and a method for separating carbon dioxide in a medium-high pressure gas source.
Background
The coal-fired power plant is a stable emission source of CO 2 in China, and accounts for about 35% of the total emission of CO 2 in China. In addition, there are a number of CO 2 trapping or separation processes in the industrial fields of ammonia synthesis, hydrogen production, coal gasification, coal chemical industry, and the like. Compared with flue gas of coal-fired power plants, the gas pressure required for treatment in the decarburization process in the fields is high (2-5 MPa), and the concentration of CO 2 is high (25-60%). The traditional normal pressure CO 2 separation process generally realizes CO 2 removal by a low-temperature absorption and high-temperature desorption method, or recovers part of heat by means of a heat pump, mechanical vapor recompression and the like, thereby achieving the purposes of energy conservation and consumption reduction. However, for the medium-high pressure CO 2 gas source, the normal pressure CO 2 separation process cannot fully utilize the characteristics of the medium-high pressure gas source, and the requirements of low energy consumption and low cost are difficult to fully meet.
Disclosure of Invention
The invention aims to provide a system and a method for separating carbon dioxide in a medium-high pressure gas source, which solve the problem that the prior normal-pressure CO 2 separation process cannot realize the removal of medium-high pressure CO 2.
In order to achieve the above purpose, the invention adopts the following technical scheme:
The invention provides a separation system of carbon dioxide in a medium-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, lean solution heat exchange equipment, semi-lean solution heat exchange equipment, a second low-pressure desorption reboiler, a desorption gas cooler and a gas-liquid separator, wherein a CO 2 rich solution outlet at the bottom of the absorption tower is connected with an inlet of the flash tank, and a desorption gas outlet at the top of the flash tank is connected with an inlet of the gas-liquid separator through the 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 lean solution outlet of the high-pressure desorption tower is connected with the top inlet of the absorption tower through a second low-pressure desorption reboiler and lean solution heat exchange equipment in sequence; the top desorption gas outlet of the high-pressure desorption tower is connected with the inlet of the gas-liquid separator through a desorption gas cooler;
The high-pressure desorption tower is connected with a high-pressure desorption reboiler;
The bottom semi-lean liquid outlet of the low-pressure desorption tower is connected with the middle inlet of the absorption tower through a semi-lean liquid heat exchange device; the top desorption gas outlet of the low-pressure desorption tower is connected with the inlet of the gas-liquid separator 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 inlets of the high-pressure desorption tower and the low-pressure desorption tower, and the top of the gas-liquid separator is provided with a CO 2 product gas outlet;
The top of the absorption tower is provided with a purified gas outlet.
Preferably, the lean solution heat exchange device comprises a lean solution heat exchanger and a lean solution cooler, wherein one path of liquid phase outlet at the bottom of the flash tank is connected with a cold end inlet of the lean solution heat exchanger, and the cold end outlet of the lean solution heat exchanger is connected with an inlet of the high-pressure desorption tower; the bottom hot lean solution outlet 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 through the lean solution cooler.
Preferably, a lean liquid pump is arranged between the hot end outlet of the lean liquid heat exchanger and the lean liquid cooler.
Preferably, the semi-lean liquid heat exchange device comprises a semi-lean liquid heat exchanger and a semi-lean liquid cooler, wherein the other path of 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 liquid outlet at the bottom of the low-pressure desorption tower is connected with the hot end inlet of the semi-lean liquid heat exchanger, and the hot end outlet of the semi-lean liquid heat exchanger is connected with the middle inlet of the absorption tower through the semi-lean liquid heat exchanger.
Preferably, a semi-lean liquid pump is arranged between the hot end outlet of the semi-lean liquid heat exchanger and the semi-lean liquid cooler.
Preferably, the high pressure desorption reboiler is connected with an external heat source device.
Preferably, the low-pressure desorption towers are also respectively connected with a first low-pressure desorption reboiler, and the first low-pressure desorption reboiler is connected with external heat source equipment.
A separation method of carbon dioxide in a medium-high pressure gas source is based on a separation system of carbon dioxide in a medium-high pressure gas source, and comprises the following steps:
The industrial gas containing CO 2 enters the absorption tower from the lower part of the absorption tower to be in countercurrent contact with lean liquid and semi-lean liquid added from different positions, the process of absorbing and removing CO 2 is completed, and the purified gas after removing CO 2 is discharged from the top of the absorption tower;
CO 2 rich liquid discharged from the bottom of the absorption tower enters a flash tank for preliminary decompression desorption, and desorption gas discharged from the top of the flash tank enters a gas-liquid separator through a desorption gas cooler;
The discharged liquid phase at the bottom of the flash tank is divided into two paths, one path enters a high-pressure desorption tower for desorption, and the other path enters a low-pressure desorption tower for desorption;
The hot lean solution at the bottom of the high-pressure desorption tower is cooled by lean solution heat exchange equipment and then is sent to the top of the absorption tower for recycling;
the high-pressure desorption tower is heated by a high-pressure desorption reboiler, and desorption gas at the tower top enters a desorption gas cooler for further condensation and then enters a gas-liquid separator;
the low-pressure desorption tower is heated by a second low-pressure desorption reboiler, the semi-lean solution at the bottom of the low-pressure desorption tower is cooled by semi-lean solution heat exchange equipment, and then the semi-lean solution returns to the middle part of the absorption tower for recycling;
the desorption gas at the top of the low-pressure desorption tower is further condensed by a desorption gas cooler and then enters a gas-liquid separator;
Condensate at the bottom of the gas-liquid separator is respectively returned to the high-pressure desorption tower and the low-pressure desorption tower; the gas outlet at the upper part of the gas-liquid separator is CO 2 product gas.
Compared with the prior art, the invention has the beneficial effects that:
According to the separation system for the carbon dioxide in the medium-high pressure gas source, provided by the invention, the CO 2 rich liquid from the absorption tower is subjected to gradual decompression regeneration in a flash evaporation mode, a high-pressure desorption mode, a low-pressure desorption mode and the like, so that the characteristic of higher pressure of the CO 2 gas source is fully utilized, and the input of external heat consumption is reduced; meets the requirements of low energy consumption and low cost.
Furthermore, the high-temperature desorption gas at the top of the high-pressure desorption tower is introduced into the reboiler of the low-pressure desorption tower and is used as a heat source for heating and desorbing, so that the external heat consumption required by the low-pressure desorption tower is reduced, and the cooling water consumption of the desorption cooler is reduced.
Furthermore, lean liquid and semi-lean liquid from the high-pressure desorption tower and the low-pressure desorption tower respectively enter from the upper section filler and the middle section filler of the absorption tower, so that the uniform reaction temperature of the tower body is maintained, the overhigh local temperature is avoided, and the degradation and loss of the absorbent are reduced.
Furthermore, energy is optimally utilized according to the medium-high pressure characteristics of the separation process and the heat energy grade characteristics in the system, and heat recovery equipment such as a heat pump, mechanical vapor recompression and the like is not introduced, so that investment cost and operation cost are effectively reduced.
Drawings
Fig. 1 is a schematic diagram 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 fig. 1, the separation system of carbon dioxide in a medium-high pressure gas source provided by the invention comprises an absorption tower 1, a flash tank 2, a lean solution heat exchanger 3, a high-pressure desorption tower 4, a high-pressure desorption reboiler 5, a lean solution pump 6, a lean solution cooler 7, a semi-lean solution heat exchanger 8, a low-pressure desorption tower 9, a semi-lean solution pump 10, a semi-lean solution cooler 11, a first low-pressure desorption reboiler 12, a second low-pressure desorption reboiler 13, a desorption gas cooler 14, a gas-liquid separator 15 and a condensate pump 16, wherein a gas inlet of the absorption tower 1 is connected with an industrial gas source containing CO 2, and a rich solution outlet of the absorption tower 1 is connected with a 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 the lean solution heat exchanger 3; the high-pressure desorption tower 4 is provided with a high-pressure desorption reboiler 5, and external steam provides a heat source; the lean solution outlet at the bottom of the high-pressure desorption tower 4 is connected with the lean solution inlet at the upper part of the absorption tower 1 through a lean solution heat exchanger 3, a lean solution pump 6 and a lean solution cooler 7 in sequence;
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 the low-pressure desorption tower 9 through a semi-lean solution heat exchanger 8; the semi-product liquid outlet at the bottom of the low-pressure desorption tower 9 is connected with the semi-lean liquid inlet at the middle part of the absorption tower 1 through a semi-lean liquid heat exchanger 8, a semi-lean liquid pump 10 and a semi-lean liquid cooler 11 in sequence;
The low-pressure desorption tower 9 is provided with a first low-pressure desorption reboiler 12 and a second low-pressure desorption reboiler 13; the first low pressure desorption reboiler 12 is provided with a heat source by external steam, and the second low pressure desorption reboiler 13 is provided with a heat source by desorption gas from the top of the high pressure desorption column 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 the inlet of the gas-liquid separator 15 through the desorption gas cooler 14; the 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 the gas outlet at the upper part of the gas-liquid separator 15 is a carbon dioxide product gas outlet.
The working principle of the invention is as follows:
The industrial gas containing CO 2 enters the absorption tower from the lower part of the absorption tower 1 to be in countercurrent contact with the lean solution and the semi-lean solution of the absorbent added from different positions, the process of absorbing and removing CO 2 is completed, and the purified gas after removing CO 2 is discharged from the top of the absorption tower 1.
Lean liquid from the lean liquid cooler 7 is fed from the upper part of the uppermost stage of packing, and semi-lean liquid from the semi-lean liquid cooler 11 is fed from the upper part of the intermediate packing.
CO 2 rich liquid discharged from the bottom of the absorption tower 1 enters a flash tank 2 for preliminary decompression desorption, and desorption gas discharged from the top of the flash tank 2 enters a gas-liquid separator 15 through a desorption gas cooler 14;
The discharged liquid phase at the bottom of the flash tank 2 is divided into two paths, one path is preheated by the barren liquor heat exchanger 3 and then enters the high-pressure desorption tower 4 for desorption, and the other path is preheated by the semi-barren liquor heat exchanger 8 and then enters the low-pressure desorption tower 9 for desorption.
The barren liquor heat exchanger 3 is heated by the 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 the 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 of the high-pressure desorption reboiler 5 adopts steam from outside the boundary region; the hot lean solution at the bottom of the high-pressure desorption tower 4 is sent to a lean solution cooler 7 for further cooling by a lean solution pump 6 after waste heat is recovered by a lean solution heat exchanger 3, and then is sent to an 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 recycle heat, and enters a gas-liquid separator 15 after being further condensed by a desorption gas cooler 14.
The low pressure stripper column 9 has two reboilers, of which a first low pressure stripper reboiler 12 is provided with heat source from the external steam and a second low pressure stripper reboiler 13 is provided with heat source from the stripping gas from the top of the high pressure stripper column 4.
The semi-lean liquid at the bottom of the low-pressure desorption tower 9 is subjected to heat exchange through a semi-lean liquid heat exchanger 8, and then is sent into a semi-lean liquid cooler 11 by a semi-lean liquid pump 10 to be further cooled and returned 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 is returned to the high-pressure desorption tower 4 and the low-pressure desorption tower 9 respectively through a condensate pump 16; the gas outlet at the upper part of the gas-liquid separator 15 is CO 2 product gas.
Claims (6)
1. The separation system of 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), lean solution heat exchange equipment, semi-lean solution heat exchange equipment, a second low-pressure desorption reboiler (13), a desorption gas cooler (14) and a gas-liquid separator (15), wherein a CO 2 rich solution outlet at the bottom of the absorption tower (1) is connected with an inlet of the flash tank (2), and a top desorption gas outlet of the flash tank (2) is connected with an inlet of the gas-liquid separator (15) through the 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 lean solution outlet of the high-pressure desorption tower (4) is connected with the top inlet of the absorption tower (1) through lean solution heat exchange equipment; the top desorption gas outlet of the high-pressure desorption tower (4) is connected with the inlet of the gas-liquid separator (15) through a second low-pressure desorption reboiler (13) and a desorption gas cooler (14) in sequence;
The high-pressure desorption tower (4) is connected with a high-pressure desorption reboiler (5);
The bottom semi-lean liquid outlet of the low-pressure desorption tower (9) is connected with the middle inlet of the absorption tower (1) through a semi-lean liquid heat exchange device; the top desorption gas outlet of the low-pressure desorption tower (9) is connected with the inlet of the 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 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 a CO 2 product gas outlet;
The top of the absorption tower (1) is provided with a purified gas outlet;
The lean solution heat exchange device comprises a lean solution heat exchanger (3) and a lean solution cooler (7), wherein one path of liquid phase outlet at the bottom of the flash tank (2) is connected with a cold end inlet of the lean solution heat exchanger (3), and the cold end outlet of the lean solution heat exchanger (3) is connected with an inlet of the high-pressure desorption tower (4); the bottom hot lean solution outlet 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) through a lean solution cooler (7);
The semi-lean liquid heat exchange device comprises a semi-lean liquid heat exchanger (8) and a semi-lean liquid cooler (11), wherein the other path of liquid phase outlet at the bottom of the flash tank (2) is connected with the cold end inlet of the semi-lean liquid heat exchanger (8), and the cold end outlet of the semi-lean liquid heat exchanger (8) is connected with the inlet of the low-pressure desorption tower (9); the hot lean liquid outlet at the bottom of the low-pressure desorption tower (9) is connected with the hot end inlet of the semi-lean liquid heat exchanger (8), and the hot end outlet of the semi-lean liquid heat exchanger (8) is connected with the middle inlet of the absorption tower (1) through the semi-lean liquid cooler (11).
2. A system for separating carbon dioxide from a medium-high pressure gas source according to claim 1, characterized in that a lean liquid pump (6) is arranged between the hot end outlet of the lean liquid heat exchanger (3) and the lean liquid cooler (7).
3. A system for separating carbon dioxide from a medium-high pressure gas source according to claim 1, characterized in that a semi-lean liquid pump (10) is arranged between the hot end outlet of the semi-lean liquid heat exchanger (8) and the semi-lean liquid cooler (11).
4. The separation system of carbon dioxide in 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.
5. The separation system of carbon dioxide in a medium-high pressure gas source according to claim 1, wherein the low pressure desorption towers (9) are respectively connected with a first low pressure desorption reboiler (12), and the first low pressure desorption reboiler (12) is connected with external heat source equipment.
6. A method for separating carbon dioxide from a medium-high pressure gas source, characterized in that the separation system based on the medium-high pressure gas source according to claim 1 comprises the following steps:
the industrial gas containing CO 2 enters the absorption tower from the lower part of the absorption tower (1) to be in countercurrent contact with lean solution and semi-lean solution added from different positions, the process of absorbing and removing CO 2 is finished, and the purified gas after removing CO 2 is discharged from the top of the absorption tower (1);
CO 2 rich liquid discharged from the bottom of the absorption tower (1) enters a flash tank (2) for preliminary decompression desorption, and desorption gas discharged from the top of the flash tank (2) enters a gas-liquid separator (15) through a desorption 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, and the other path enters a low-pressure desorption tower (9) for desorption;
the hot lean solution at the bottom of the high-pressure desorption tower (4) is cooled by lean solution heat exchange equipment and then is sent to the top of the absorption tower (1) for recycling;
The high-pressure desorption tower (4) is heated by a high-pressure desorption reboiler (5), and desorption gas at the tower top sequentially enters a second low-pressure desorption reboiler (13) and a desorption gas cooler (14) to be further condensed and then enters a gas-liquid separator (15);
The low-pressure desorption tower (9) is heated by a second low-pressure desorption reboiler (13), the semi-lean solution at the bottom of the low-pressure desorption tower is cooled by semi-lean solution heat exchange equipment, and then the semi-lean solution returns to the middle part of 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) is respectively returned to the high-pressure desorption tower (4) and the low-pressure desorption tower (9); the gas outlet at the upper part of the gas-liquid separator (15) is CO 2 product gas.
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