CN210729090U - Chemical absorption method carbon dioxide capture system based on waste heat recovery and utilization - Google Patents

Chemical absorption method carbon dioxide capture system based on waste heat recovery and utilization Download PDF

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Publication number
CN210729090U
CN210729090U CN201920707023.4U CN201920707023U CN210729090U CN 210729090 U CN210729090 U CN 210729090U CN 201920707023 U CN201920707023 U CN 201920707023U CN 210729090 U CN210729090 U CN 210729090U
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China
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outlet
inlet
tower
lean
liquid
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Inventor
陆诗建
李清方
张新军
陆胤君
于惠娟
刘海丽
王书平
韩冰
刘东杰
张磊
庞会中
王辉
董金婷
陈莉
董健
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Sinopec Oilfield Service Corp
Sinopec Jianghan Petroleum Engineering Design Co Ltd
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Sinopec Oilfield Service Corp
Sinopec Energy and Environmental Engineering Co Ltd
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Abstract

The utility model provides a chemical absorption method carbon dioxide entrapment system based on waste heat recovery utilizes, it includes absorption tower, rich liquid pump, first poor rich liquid heat exchanger, rich liquid shunt, second poor rich liquid heat exchanger, heat pump system, desorber, boiler, lean liquid pump and lean liquid cooler. The flue gas enters an absorption tower and moves from bottom to top, the absorbent enters the absorption tower and sprays downwards, the absorbent is in countercurrent contact with the flue gas, and the absorbent absorbs carbon dioxide in the flue gas to become pregnant solution; the rich solution enters a rich solution pump and then enters a first lean-rich solution heat exchanger to absorb heat and raise the temperature; the rich solution which completes the first heat exchange enters a rich solution splitter to be split into two paths, the first path of rich solution enters a heat pump system to absorb heat and raise the temperature, and then the first path of rich solution enters a desorption tower; the second path of rich liquid enters a second lean rich liquid heat exchanger to absorb heat and raise the temperature, and then the second path of rich liquid is subjected to a desorption tower; the first rich liquid and the second rich liquid are heated and desorbed in the desorption tower and are decomposed into lean liquid and carbon dioxide.

Description

Chemical absorption method carbon dioxide capture system based on waste heat recovery and utilization
Technical Field
The utility model relates to an exhaust heat recovery field especially relates to a chemical absorption method carbon dioxide entrapment system based on exhaust heat recovery utilizes.
Background
CO in the atmosphere due to the massive combustion of fossil fuels2The content of (A) also continuously increases, and a large amount of CO2The greenhouse effect is more and more serious due to the emission of the carbon dioxide, and CO is controlled2Has become a focus of attention in various countries.
Organic amine for capturing CO2The technology is the most mature technology at present. Organic amine for capturing CO2The principle and the flow are as follows: CO in flue gas2Reacting with organic amine in the absorption tower to generate carbamate, conveying the carbamate to the desorption tower, heating, decomposing and reducing the carbamate into organic amine and carbon dioxide, and returning the organic amine solution to the absorption tower for re-absorption. Organic amine carbon trapping method for trapping CO2The process is widely used due to the fast absorption rate, high absorption efficiency, simple process and mature technology; but organic amines capture CO2The technical energy consumption is high, and how to recover waste heat in barren liquor and gas obtained by desorption of a desorption tower is a main way for reducing the energy consumption and is also a main foothold for energy-saving process development.
SUMMERY OF THE UTILITY MODEL
In view of the problems existing in the background art, the present invention is directed to a chemical absorption carbon dioxide capture system based on waste heat recovery, which can effectively utilize the heat of the gas discharged from the top of the desorption tower to heat the rich liquid, improve the utilization rate of waste heat, and reduce the heat required during desorption of the rich liquid.
In order to achieve the above object, the present invention provides a chemical absorption method carbon dioxide capture system based on waste heat recovery and utilization, which comprises an absorption tower, a rich liquid pump, a first lean and rich liquid heat exchanger, a rich liquid shunt, a second lean and rich liquid heat exchanger, a heat pump system, a desorption tower, a boiler, a lean liquid pump and a lean liquid cooler. The absorption tower comprises: the first inlet of the absorption tower is positioned at the lower part of the absorption tower and is used for the entry of flue gas, and the flue gas is provided with carbon dioxide; the second inlet of the absorption tower is positioned at the upper part of the absorption tower and is used for the absorbent to enter; the first outlet of the absorption tower is positioned at the bottom of the absorption tower and is used for allowing the rich liquid to flow out; and the second outlet of the absorption tower is positioned at the top of the absorption tower. The rich liquid pump includes: the rich liquid pump inlet is communicated with the first outlet of the absorption tower; and (4) discharging the rich liquid pump. The first lean-rich liquid heat exchanger includes: the first inlet of the first lean-rich liquid heat exchanger is communicated with an outlet of the rich liquid pump; a second inlet of the first lean-rich liquor heat exchanger; a first outlet of the first lean-rich liquor heat exchanger; and a second outlet of the first lean-rich liquid heat exchanger. The rich liquid shunt includes: the rich liquor splitter inlet is communicated with the first outlet of the first lean and rich liquor heat exchanger; a rich liquor splitter first outlet; and a second outlet of the rich liquid splitter. The second lean-rich liquid heat exchanger includes: the first inlet of the second lean-rich liquid heat exchanger is communicated with the second outlet of the rich liquid splitter; a second inlet of the second lean-rich liquor heat exchanger; a first outlet of the second lean-rich liquid heat exchanger; and a second outlet of the second lean-rich liquid heat exchanger is communicated with a second inlet of the first lean-rich liquid heat exchanger. The heat pump system includes an evaporator, a compressor, a condenser, and a throttle valve. The evaporator includes: an evaporator first inlet; an evaporator second inlet; an evaporator first outlet; a second outlet of the evaporator. The compressor includes: the compressor inlet is communicated with the second outlet of the evaporator; and (4) an outlet of the compressor. The condenser includes: the first inlet of the condenser is communicated with the first outlet of the rich liquid splitter; the second inlet of the condenser is communicated with the outlet of the compressor; a condenser first outlet; a second outlet of the condenser. The throttle valve is arranged between the condenser and the evaporator, one end of the throttle valve is controlled to be communicated with the second outlet of the condenser, and the other end of the throttle valve is controlled to be communicated with the second inlet of the evaporator. The desorption tower comprises: the first inlet of the desorption tower is positioned at the upper part of the desorption tower and communicated with the first outlet of the condenser; the second inlet of the desorption tower is positioned at the upper part of the desorption tower, is lower than the first inlet of the desorption tower and is communicated with the first outlet of the second lean-rich liquid heat exchanger; the third inlet of the desorption tower is positioned in the middle of the desorption tower and is lower than the second inlet of the desorption tower; the fourth inlet of the desorption tower is positioned at the lower part of the desorption tower and is lower than the third inlet of the desorption tower; the first outlet of the desorption tower is positioned at the top of the desorption tower and communicated with the first inlet of the evaporator; the second outlet of the desorption tower is positioned at the bottom of the desorption tower; and the third outlet of the desorption tower is positioned at the lower part of the desorption tower. The boiler comprises: the first inlet of the boiler is communicated with the third outlet of the desorption tower; a second inlet of the boiler for the inflow of external saturated steam; the first outlet of the boiler is communicated with the fourth inlet of the desorption tower; a second outlet of the boiler. The barren liquor pump comprises: the lean solution pump inlet is communicated with a second outlet of the first lean and rich solution heat exchanger; and (4) discharging the lean solution pump. One side of the barren liquor cooler is communicated with an outlet of the barren liquor pump, and the other side of the barren liquor cooler is communicated with a second inlet of the absorption tower.
The flue gas enters the absorption tower through the first inlet of the absorption tower and moves from bottom to top, the absorbent enters the absorption tower through the second inlet of the absorption tower and sprays downwards, the downwards-sprayed absorbent is in countercurrent contact with the flue gas, so that the absorbent absorbs carbon dioxide in the flue gas and becomes rich liquid, the rich liquid is settled downwards, and the flue gas without the carbon dioxide continues to move upwards;
the rich solution enters a rich solution pump through a first outlet of the absorption tower and a rich solution pump inlet, and then enters a first lean and rich solution heat exchanger through a rich solution pump outlet and a first inlet of the first lean and rich solution heat exchanger for first heat exchange so as to absorb heat and raise the temperature;
the rich solution which completes the first heat exchange enters the rich solution splitter through a first outlet of the first lean rich solution heat exchanger and an inlet of the rich solution splitter to be split into two paths,
the first path of rich liquid enters a condenser through a first outlet of the rich liquid splitter and a first inlet of the condenser to perform second heat exchange and absorb heat to raise temperature, and the first path of rich liquid completing the second heat exchange enters a desorption tower through a first outlet of the condenser and a first inlet of the desorption tower;
the second path of rich liquid enters a second lean-rich liquid heat exchanger through a second outlet of the rich liquid flow divider and a first inlet of the second lean-rich liquid heat exchanger for third heat exchange and heat absorption and temperature rise, and the second path of rich liquid completing the third heat exchange enters a desorption tower through a first outlet of the second lean-rich liquid heat exchanger and a second inlet of the desorption tower;
the first path of rich liquid and the second path of rich liquid are heated and desorbed in the desorption tower and are decomposed into barren liquid and carbon dioxide, the barren liquid is settled downwards in the desorption tower, and the carbon dioxide moves upwards;
part of liquid at the bottom of the desorption tower enters the boiler through the third outlet of the desorption tower and the first inlet of the boiler and carries out fourth heat exchange with saturated steam flowing in through the second inlet of the boiler, the part of liquid absorbs heat in the boiler and rises temperature to be partially vaporized and enters the desorption tower through the first outlet of the boiler and the fourth inlet of the desorption tower to provide steam and heat for rich liquid desorption in the desorption tower; the saturated steam in the boiler releases heat and cools to become condensed water, and the condensed water is discharged through a second outlet of the boiler;
the carbon dioxide moving upwards carries part of lean liquid, then enters the evaporator through a first outlet of the desorption tower and a first inlet of the evaporator to perform fifth heat exchange with working medium liquid in the evaporator, the working medium liquid absorbs heat and is heated to become working medium steam, the working medium steam enters the compressor through a second outlet of the evaporator and a first inlet of the compressor, the compressor compresses the working medium steam, the working medium steam after being compressed is heated and pressurized to become superheated steam, the superheated steam enters the condenser through a second inlet of the compressor and the second inlet of the condenser and performs the second heat exchange with a first rich liquid flowing in through the first inlet of the condenser, the first rich liquid absorbs heat and is heated, the superheated steam releases heat and is cooled to become high-pressure working medium liquid, the high-pressure working medium liquid flows into a throttle valve and is depressurized to become the working medium liquid in an initial state, and the working medium liquid enters the evaporator again through the second inlet of the evaporator under the action, thereby the working medium liquid completes the cycle using process;
the lean solution desorbed from the desorption tower enters a second lean-rich solution heat exchanger through a second outlet of the desorption tower and a second inlet of the second lean-rich solution heat exchanger, and performs the third heat exchange with a second path of rich solution entering through a first inlet of the second lean-rich solution heat exchanger, so that the lean solution releases heat and is cooled;
and the lean solution which completes the third heat exchange enters the first lean-rich solution heat exchanger through the second outlet of the second lean-rich solution heat exchanger and the second inlet of the first lean-rich solution heat exchanger, the first heat exchange is carried out on the lean solution and the rich solution which enters through the first inlet of the first lean-rich solution heat exchanger, the lean solution releases heat and is cooled, the lean solution which completes the first heat exchange enters the lean solution cooler through the second outlet of the first lean-rich solution heat exchanger and the lean solution pump to be cooled again, and then the cooled lean solution enters the absorption tower through the lean solution cooler and the second inlet of the absorption tower to be used as an absorbent for absorbing carbon dioxide.
In one embodiment, the absorption column further comprises: the third inlet of the absorption tower is positioned in the middle of the absorption tower and below the second inlet of the absorption tower; and the third outlet of the absorption tower is positioned in the middle of the absorption tower and above the third inlet of the absorption tower. The chemical absorption method carbon dioxide capture system based on waste heat recovery and utilization further comprises an interstage cooler, wherein one side of the interstage cooler is communicated with the third inlet of the absorption tower, and the other side of the interstage cooler is communicated with the third outlet of the absorption tower. The absorbent in the absorption tower flows into the interstage cooler through a third outlet of the absorption tower to be cooled, the absorbent cooled by the interstage cooler flows back into the absorption tower through a third inlet of the absorption tower and sprays downwards, the downwards-sprayed absorbent is in countercurrent contact with the flue gas entering through the first inlet of the absorption tower, the absorbent absorbs at least part of carbon dioxide in the flue gas to become a rich liquid, and the rich liquid is settled downwards; the flue gas without at least part of carbon dioxide moves upwards continuously and is in countercurrent contact with the absorbent sprayed down through the second inlet of the absorption tower again, and the flue gas is reacted for the second time by the absorbent sprayed down through the second inlet of the absorption tower to become rich liquid and flue gas without carbon dioxide, the generated rich liquid is settled downwards, the flue gas without carbon dioxide still moves upwards continuously, and the flue gas without carbon dioxide moving upwards carries part of the absorbent.
In one embodiment, the absorption column further comprises: the fourth inlet of the absorption tower is positioned at the upper part of the absorption tower and is positioned at the upper part of the second inlet of the absorption tower; and the fourth outlet of the absorption tower is positioned at the upper part of the absorption tower and above the second inlet of the absorption tower, and is used for discharging the washing water prestored in the absorption tower. The chemical absorption method carbon dioxide capture system based on waste heat recycling also comprises a primary washing pump and a primary washing cooler. The primary washing pump includes: the inlet of the primary washing pump is communicated with the fourth outlet of the absorption tower; the outlet of the primary washing pump. One side of the primary washing cooler is communicated with the outlet of the primary washing pump, and the other side of the primary washing cooler is communicated with the fourth inlet of the absorption tower. The absorption tower, the primary washing pump and the primary washing cooler form a primary washing loop, when the primary washing pump is started, water washing water in the absorption tower flows into the primary washing pump through the fourth outlet of the absorption tower and the inlet of the primary washing pump, then flows into the primary washing cooler through the outlet of the primary washing pump for cooling, the cooled water washing water flows back to the upper part of the absorption tower again and sprays down, flue gas which is subjected to carbon dioxide removal and carries part of the absorbent moves upwards in the absorption tower and is in countercurrent contact with the cooled water washing water, at least part of the absorbent in the flue gas is dissolved in the water washing water, and the flue gas which is subjected to primary washing continuously moves upwards and is then discharged through the second outlet of the absorption tower.
In one embodiment, the flue gas discharged through the second outlet of the absorption tower also carries a portion of the absorbent. The chemical absorption method carbon dioxide capture system based on waste heat recycling further comprises a first gas-liquid separator, a washing tower, a secondary washing pump, a secondary washing cooler, a barren liquor flow divider and an absorbent storage. The first gas-liquid separator includes: the inlet of the first gas-liquid separator is communicated with the second outlet of the absorption tower; a first outlet of the first gas-liquid separator, which is positioned at the bottom of the first gas-liquid separator; and the second outlet of the first gas-liquid separator is positioned at the top of the first gas-liquid separator. The washing tower stores therein water washing water, and includes: the first inlet of the washing tower is positioned in the middle of the washing tower and communicated with the second outlet of the first gas-liquid separator; a second inlet of the scrubber tower located at an upper portion of the scrubber tower; a scrubber first outlet at the top of the scrubber; a second outlet of the scrubber tower located at a lower portion of the scrubber tower; and the third outlet of the washing tower is positioned at the bottom of the washing tower. The secondary washing pump includes: the inlet of the secondary washing pump is communicated with the second outlet of the washing tower; and (4) discharging the secondary washing pump. One side of the secondary washing cooler is communicated with the outlet of the secondary washing pump, and the other side of the secondary washing cooler is communicated with the second inlet of the washing tower. The lean liquid splitter includes: the first inlet of the lean solution splitter is communicated with the first outlet of the first gas-liquid separator; the second inlet of the barren liquor splitter is communicated with the third outlet of the washing tower; and an outlet of the lean liquor splitter. The absorbent reservoir includes: the inlet of the absorbent storage is communicated with the outlet of the barren liquor splitter; and the outlet of the absorbent storage is communicated with one side of the lean liquid cooler.
Wherein, the flue gas which is discharged from the second outlet of the absorption tower and carries part of the absorbent enters the first gas-liquid separator through the inlet of the first gas-liquid separator, the first gas-liquid separator separates at least part of the absorbent from the flue gas,
the flue gas is discharged through the second outlet of the first gas-liquid separator, the discharged flue gas still contains at least part of absorbent, the flue gas containing at least part of absorbent enters the washing tower through the first inlet of the washing tower and moves upwards, the water washing water in the washing tower enters the secondary washing pump through the second outlet of the washing tower and the inlet of the secondary washing pump, then flows into a secondary washing cooler through the outlet of a secondary washing pump for cooling, cooled washing water enters a washing tower through the second inlet of the washing tower and is sprayed downwards, the sprayed washing water is in countercurrent contact with flue gas carrying at least part of absorbent, the absorbent in the flue gas is dissolved by the washing water, the flue gas without the absorbent is discharged through the first outlet of the washing tower, the water washing water with the dissolved absorbent flows into the lean solution splitter through a third outlet of the washing tower and a second inlet of the lean solution splitter;
the absorbent separated by the first gas-liquid separator flows into the lean liquid separator through a first outlet of the first gas-liquid separator and a first inlet of the lean liquid separator;
the lean solution splitter mixes the two paths of absorbent, and the mixed absorbent enters the absorbent storage through the outlet of the lean solution splitter and the inlet of the absorbent storage, and then flows into the absorption tower through the outlet of the absorbent storage and the lean solution cooler to be recycled.
In one embodiment, the chemical absorption carbon dioxide capture system based on waste heat recycling further comprises a flash tank, a Roots blower and a steam cooler. The flash tank includes: the inlet of the flash tank is communicated with the second outlet of the desorption tower; a first outlet of the flash tank; and a second outlet of the flash tank is communicated with a second inlet of the second lean-rich liquid heat exchanger. The roots blower includes: the inlet of the Roots blower is communicated with the first outlet of the flash tank; and (4) an outlet of the Roots blower. One side of the steam cooler is communicated with the outlet of the Roots blower, and the other side of the steam cooler is communicated with the third inlet of the desorption tower.
The barren solution flowing out from the second outlet of the desorption tower directly enters a flash tank through an inlet of the flash tank, the barren solution is flashed in the flash tank to flash off part of steam, the flashed steam enters a Roots blower through a first outlet of the flash tank and an inlet of the Roots blower, the steam is pressurized and heated in the Roots blower and then enters a steam cooler through an outlet of the Roots blower to be cooled, and the cooled steam enters the desorption tower through a third inlet of the desorption tower to provide auxiliary heat for desorption of rich solution in the desorption tower; and the lean solution after flash evaporation enters a second lean and rich solution heat exchanger through a second outlet of the flash tank and a second inlet of the second lean and rich solution heat exchanger, and performs the third heat exchange with a second path of rich solution entering through a first inlet of the second lean and rich solution heat exchanger, so that the lean solution releases heat and is cooled.
In one embodiment, the chemical absorption carbon dioxide capture system based on waste heat recycling further comprises a purification tower, a purification pump and a purification cooler. The purifying tower is internally stored with a purifying agent, and comprises: the first inlet of the purification tower is positioned at the lower part of the purification tower and is used for external flue gas to enter; the second inlet of the purification tower is positioned at the upper part of the purification tower; the first outlet of the purification tower is positioned at the top of the purification tower and communicated with the first inlet of the absorption tower; and the second outlet of the purification tower is positioned at the lower part of the purification tower and is positioned below the first inlet of the purification tower. The purge pump includes: the inlet of the purifying pump is communicated with the second outlet of the purifying tower; the outlet of the purifying pump. One side of the purification cooler is communicated with the outlet of the purification pump, and the other side of the purification cooler is communicated with the second inlet of the purification tower.
The purifying tower, the purifying pump and the purifying cooler form an external flue gas purifying circulation loop, after the purifying pump is started, a purifying agent in the purifying tower is discharged through a second outlet of the purifying tower, pumped into the purifying cooler through the purifying pump for cooling, returned into the purifying tower through a second inlet of the purifying tower and sprayed downwards, external flue gas enters the purifying tower through a first inlet of the purifying tower and moves upwards, the upward moving external flue gas is in countercurrent contact with the purifying agent sprayed downwards through the second inlet of the purifying tower, the purifying agent absorbs acidic impurity gas and smoke dust in the external flue gas, carbon dioxide in the external flue gas is not absorbed by the purifying agent, and the flue gas moves upwards and enters the absorbing tower through the first outlet of the purifying tower and the first inlet of the absorbing tower to be supplied to the absorbing tower.
In one embodiment, the scavenger is a sodium bicarbonate solution.
In an embodiment, the carbon dioxide discharged from the first outlet of the desorption tower also carries a part of the lean liquid. The chemical absorption method carbon dioxide capture system based on waste heat recycling further comprises a desorption gas condenser and a second gas-liquid separator. The stripping gas condenser comprises: the inlet of the desorption gas condenser is communicated with the first outlet of the evaporator; and a desorption gas condenser outlet. The second gas-liquid separator includes: the inlet of the second gas-liquid separator is communicated with the outlet of the desorption gas condenser; a second gas-liquid separator first outlet positioned at the top of the second gas-liquid separator; and the second outlet of the second gas-liquid separator is positioned at the bottom of the second gas-liquid separator.
The carbon dioxide with part of the lean solution enters a condenser through a first outlet of an evaporator and an inlet of a desorption gas condenser for cooling, the cooled carbon dioxide with part of the lean solution enters a second gas-liquid separator through an inlet of the second gas-liquid separator, the carbon dioxide with part of the lean solution is subjected to gas-liquid separation through the second gas-liquid separator to be separated into carbon dioxide product gas and lean solution, and the carbon dioxide product gas is discharged through a first outlet of the second gas-liquid separator for the next operation;
the separated lean liquid is discharged through the second outlet of the second gas-liquid separator and then returned to the absorbent storage.
In one embodiment, the absorbent is an organic amine solution.
The utility model has the advantages as follows: according to the utility model discloses an among the chemical absorption method carbon dioxide entrapment system based on waste heat recovery utilizes, heat pump system's setting has effectively given the rich solution with the heat transfer of desorption tower top combustion gas for the rich solution heat absorption heaies up, has reduced the rich solution at the required heat of desorption tower desorption, has reduced the energy consumption, has improved the utilization ratio of used heat.
Drawings
Fig. 1 is a schematic diagram of a chemical absorption carbon dioxide capture system based on waste heat recovery according to the present invention.
Wherein the reference numerals are as follows:
11 absorption column 18B1 boiler first outlet
11A1 absorption column first inlet 18B2 boiler second outlet
11A2 absorption tower second inlet 19 barren liquor pump
11A3 absorption tower third inlet 19A lean solution pump inlet
11A4 absorber fourth inlet 19B barren liquor pump inlet
11B1 absorption tower first outlet 20 lean liquid cooler
11B2 absorber second outlet 21 interstage cooler
11B3 absorption tower third outlet 22 once washing pump
11B4 fourth outlet of absorption tower 22A primary washing pump inlet
12B liquid enrichment pump 22B one-time washing pump outlet
12A rich liquid pump inlet 23 once washing cooler
12B rich liquid pump outlet 24 first gas-liquid separator
13 first lean-rich liquor heat exchanger 24A first gas-liquid separator inlet
13a1 first lean rich liquid heat exchanger first port 24B1 first gas-liquid separator first inlet and outlet
13A2 first lean-rich liquid heat exchanger second port 24B2 first gas-liquid separator second inlet and outlet
13B1 first lean rich liquor Heat exchanger first port 25 scrubber Exit 25A1 scrubber first Inlet
13B2 first lean-rich heat exchanger second port 25A2 scrubber second inlet outlet 25B1 scrubber first outlet
14 rich liquor splitter 25B2 scrubber second outlet
14A rich liquor splitter inlet 25B3 scrubber third outlet
14B1 pregnant solution shunt first export 26 secondary washing pump
Second outlet 26A of rich liquid flow divider of 14B2 for secondary washing pump inlet
15 second lean and rich liquor heat exchanger 26B secondary washing pump outlet
15a1 second lean rich heat exchanger first 27 secondary scrub cooler inlet 28 lean splitter
15a2 second lean-rich heat exchanger second 28a1 lean splitter first inlet 28a2 lean splitter second inlet
Inlet port
15B1 second lean rich heat exchanger first 28B lean splitter outlet 29 absorbent storage
15B2 second lean-rich heat exchanger second 29A absorbent reservoir inlet outlet 29B absorbent reservoir outlet
16 heat pump system 30 flash tank
161 evaporator 30A flash tank inlet
161A1 evaporator first inlet 30B1 flash tank first outlet
Second inlet of 161A2 evaporator 30B2 flash tank second outlet
First outlet 31 Roots blower of 161B1 evaporator
Inlet of Roots blower at second outlet 31A of 161B2 evaporator
162 compressor 31B Roots blower outlet
162A compressor inlet 32 vapor cooler
162B compressor outlet 33 purge column
163 condenser 33A1 purge column first inlet
163A1 condenser first inlet 33A2 purge column second inlet
163A2 condenser second inlet 33B1 purge column first outlet
163B1 condenser first outlet 33B2 purge column second outlet
163B2 condenser second outlet 34 purge pump
164 throttle valve 34A purge pump inlet
17 desorption tower 34B purification pump outlet
17A1 desorber first inlet 35 purge cooler
Second inlet 36 stripping gas condenser of 17A2 desorption tower
Third inlet 36A of 17A3 desorber inlet of stripping gas condenser
17A4 desorber fourth inlet 36B stripping gas condenser outlet
17B1 desorber first outlet 37 second gas-liquid separator
17B2 desorber second outlet 37A second gas-liquid separator inlet
17B3 Desorption tower third outlet 37B1 second gas-liquid separator first outlet
18 boiling device
18A1 boiler first inlet 37B2 second gas-liquid separator second outlet
18A2 boiler second inlet
Detailed Description
Referring to fig. 1, the chemical absorption carbon dioxide capture system based on waste heat recovery and utilization of the present invention includes an absorption tower 11, a rich liquid pump 12, a first lean and rich liquid heat exchanger 13, a rich liquid splitter 14, a second lean and rich liquid heat exchanger 15, a heat pump system 16, a desorption tower 17, a boiler 18, a lean liquid pump 19, and a lean liquid cooler 20.
The absorption tower 11 includes: the first inlet 11A1 of the absorption tower is positioned at the lower part of the absorption tower 11 and is used for flue gas to enter, and the flue gas is provided with carbon dioxide; a second inlet 11a2 of the absorption column, which is located at the upper part of the absorption column 11 and is used for the absorbent to enter; a first outlet 11B1 of the absorption tower, which is positioned at the bottom of the absorption tower 11 and is used for flowing out the rich liquid; and a second outlet 11B2 of the absorption column, which is located at the top of the absorption column 11.
The rich liquid pump 12 includes: a rich liquid pump inlet 12A communicated with the first outlet 11B1 of the absorption tower; and a rich liquid pump outlet 12B.
The first lean rich liquid heat exchanger 13 includes: the first inlet 13A1 of the first lean-rich liquid heat exchanger is communicated with the outlet 12B of the rich liquid pump; a first lean-rich liquid heat exchanger second inlet 13a 2; a first lean-rich liquid heat exchanger first outlet 13B 1; and a first lean-rich liquid heat exchanger second outlet 13B 2.
Rich liquor splitter 14 includes: a rich liquor splitter inlet 14A communicating with the first lean-rich heat exchanger first outlet 13B 1; rich liquor splitter first outlet 14B 1; and a second rich liquid splitter outlet 14B 2.
The second lean-rich liquid heat exchanger 15 includes: a second lean-rich heat exchanger first inlet 15A1 communicating with the rich splitter second outlet 14B 2; second lean-rich heat exchanger second inlet 15a 2; second lean-rich heat exchanger first outlet 15B 1; the second outlet 15B2 of the second lean-rich heat exchanger is in communication with the second inlet 13a2 of the first lean-rich heat exchanger.
The heat pump system 16 includes an evaporator 161, a compressor 162, a condenser 163, and a throttle valve 164.
The evaporator 161 includes: the evaporator first inlet 161a 1; the evaporator second inlet 161a 2; the evaporator first outlet 161B 1; the evaporator second outlet 161B 2.
The compressor 162 includes: a compressor inlet 162A communicating with the evaporator second outlet 161B 2; compressor outlet 162B.
The condenser 163 includes: a condenser first inlet 163a1 communicating with the rich liquor splitter first outlet 14B 1; a condenser second inlet 163A2 communicating with compressor outlet 162B; condenser first outlet 163B 1; condenser second outlet 163B 2.
The throttle valve 164 is disposed between the condenser 163 and the evaporator 161, and has one end in controlled communication with the condenser second outlet 163B2 and the other end in controlled communication with the evaporator second inlet 161A 2.
The desorption tower 17 includes: a first inlet 17A1 of the desorption tower, which is positioned at the upper part of the desorption tower 17 and is communicated with a first outlet 163B1 of the condenser; a desorber second inlet 17a2 located at an upper portion of the desorber 17 and below the desorber first inlet 17a1 (preferably located at an upper middle portion of the desorber 17) and communicating with a second lean-rich liquid heat exchanger first outlet 15B 1; a third inlet 17A3 of the desorber, which is located at the middle part of the desorber 17 and lower than the second inlet 17a2 of the desorber (preferably, located at the middle lower part of the desorber 17); a fourth inlet 17a4 of the desorber located at the lower part of the desorber 17 and lower than the third inlet 17A3 of the desorber; a desorber first outlet 17B1 located at the top of the desorber 17 and communicating with the evaporator first inlet 161A 1; a second outlet 17B2 of the desorber, located at the bottom of the desorber 17; and a third outlet 17B3 of the desorber, which is located at the lower part of the desorber 17.
The boiler 18 comprises: the first boiler inlet 18A1 is communicated with the third outlet 17B3 of the desorption tower; a boiler second inlet 18A2 for the inflow of external saturated steam; the boiler first outlet 18B1 is communicated with the desorption tower fourth inlet 17A 4; boiler second outlet 18B 2.
The barren liquor pump 19 includes: a lean liquid pump inlet 19A communicated with the first lean-rich liquid heat exchanger second outlet 13B 2; the barren pump outlet 19B.
The lean liquid cooler 20 has one side connected to the lean liquid pump outlet 19B and the other side connected to the absorber second inlet 11a 2.
The flue gas enters the absorption tower 11 through the first inlet 11a1 of the absorption tower and moves from bottom to top, the absorbent enters the absorption tower 11 through the second inlet 11a2 of the absorption tower and sprays downwards, the absorbent spraying downwards contacts with the flue gas in a countercurrent manner, so that the absorbent absorbs carbon dioxide in the flue gas and becomes rich liquid, the rich liquid settles downwards, and the flue gas without carbon dioxide continues to move upwards. In one embodiment, the absorbent is an organic amine solution. Of course, without being limited thereto, other suitable absorbents may be selected by those skilled in the art.
The rich liquid enters the rich liquid pump 12 through the first outlet 11B1 of the absorption tower and the inlet 12A of the rich liquid pump, and then enters the first lean-rich liquid heat exchanger 13 through the outlet 12B of the rich liquid pump and the first inlet 13a1 of the first lean-rich liquid heat exchanger for first heat exchange, so as to absorb heat and raise the temperature.
The rich liquid that has completed the first heat exchange enters the rich liquid splitter 14 via the first lean rich liquid heat exchanger first outlet 13B1 and the rich liquid splitter inlet 14A to be split into two.
The first rich liquid enters the condenser 163 through the first outlet 14B1 of the rich liquid splitter and the first inlet 163a1 of the condenser to perform the second heat exchange and absorb heat to raise the temperature, and the first rich liquid completing the second heat exchange enters the desorption tower 17 through the first outlet 163B1 of the condenser and the first inlet 17a1 of the desorption tower.
The second part of rich liquid enters the second lean-rich liquid heat exchanger 15 through the second outlet 14B2 of the rich liquid flow divider and the first inlet 15A1 of the second lean-rich liquid heat exchanger for third heat exchange and heat absorption and temperature rise, and the second part of rich liquid completing the third heat exchange enters the desorption tower 17 through the first outlet 15B1 of the second lean-rich liquid heat exchanger and the second inlet 17A2 of the desorption tower.
The first rich liquid and the second rich liquid are heated and desorbed in the desorption tower 17 and decomposed into lean liquid and carbon dioxide, the lean liquid is settled downwards in the desorption tower 17, and the carbon dioxide moves upwards.
Part of the liquid at the bottom of the desorption tower 17 (which can be lean liquid with complete desorption or semi-lean liquid with incomplete desorption) enters the boiler 18 through the desorption tower third outlet 17B3 and the boiler first inlet 18A1 and carries out fourth heat exchange with saturated steam flowing in through the boiler second inlet 18A2, and the part of the liquid absorbs heat to be heated in the boiler 18 to be partially vaporized and enters the desorption tower 17 through the boiler first outlet 18B1 and the desorption tower fourth inlet 17A4 to provide steam and heat for rich liquid desorption in the desorption tower 17; the saturated steam in the boiler 18 loses heat and cools to become condensed water, which is discharged through the boiler second outlet 18B 2. It should be noted that when the semi-lean solution is subjected to the fourth heat exchange in the boiler 18, the semi-lean solution is decomposed into steam, lean solution and carbon dioxide with a large amount of heat, the steam, the lean solution and the carbon dioxide are returned to the desorption tower 17 together, and the carbon dioxide with the heat and the steam move upwards in the desorption tower 17 to provide heat for the two-way rich solution desorption.
The carbon dioxide moving upwards carries part of lean liquid (existing in the form of amine vapor), then enters the evaporator 161 through the first outlet 17B1 of the desorption tower and the first inlet 161A1 of the evaporator to perform fifth heat exchange with the working fluid in the evaporator 161, the working fluid absorbs heat and is heated to become working fluid vapor, the working fluid vapor enters the compressor 162 through the second outlet 161B2 of the evaporator and the inlet 162A of the compressor, the compressor 162 compresses the working fluid vapor, the compressed working fluid vapor is heated and pressurized to become superheated vapor, the superheated vapor enters the condenser 163 through the outlet 162B of the compressor and the second inlet 163A2 of the condenser and performs the second heat exchange with the first rich liquid flowing in through the first inlet 163A1 of the condenser, the first rich liquid absorbs heat and is heated, the superheated vapor releases heat and is cooled to become high-pressure working fluid, the high-pressure working fluid flows into the throttle valve 164 and is depressurized to become the working fluid in the initial state, the working fluid enters the evaporator 161 again through the second inlet 161a2 of the evaporator under the action of the throttle valve 164, so that the working fluid completes one cycle use process.
The lean liquid desorbed from the desorption tower 17 enters the second lean-rich liquid heat exchanger 15 through the second outlet 17B2 of the desorption tower and the second inlet 15a2 of the second lean-rich liquid heat exchanger, and performs the third heat exchange with the second rich liquid entering through the first inlet 15a1 of the second lean-rich liquid heat exchanger, so that the lean liquid releases heat and is cooled.
The lean liquid that has completed the third heat exchange enters the first lean-rich liquid heat exchanger 13 through the second lean-rich liquid heat exchanger second outlet 15B2 and the first lean-rich liquid heat exchanger second inlet 13a2, and undergoes the aforementioned first heat exchange with the rich liquid that has entered through the first lean-rich liquid heat exchanger first inlet 13a1, the lean liquid releases heat again to cool down, the lean liquid that has completed the first heat exchange enters the lean liquid cooler 20 through the first lean-rich liquid heat exchanger second outlet 13B2 and the lean liquid pump 19 to be cooled again, and then the cooled lean liquid enters the absorption tower 11 through the lean liquid cooler 20 and the absorption tower second inlet 11a2 to be used as an absorbent for absorbing carbon dioxide.
In the chemical absorption carbon dioxide capture system based on waste heat recycling of the present invention, the rich solution (cold rich solution) discharged through the first outlet 11B1 of the absorption tower undergoes the first heat exchange under the action of the first lean rich solution heat exchanger 13 to absorb heat and raise temperature, and then is divided into two paths through the rich solution splitter 14, and the second path of rich solution undergoes the third heat exchange with the lean solution (hot lean solution) flowing out of the desorption tower 17 through the second lean rich solution heat exchanger 15, and then flows into the desorption tower 17 to be desorbed, so as to effectively utilize the waste heat of the hot lean solution; the first rich liquid indirectly absorbs the heat carried by the carbon dioxide discharged from the top of the desorption tower 17 through the heat transferred by the working medium in the heat pump system 16 (the gas discharged from the top of the desorption tower 17 and the working medium in the evaporator 16 perform fifth heat exchange, and the working medium absorbs heat to raise the temperature), and the waste heat of the gas at the top of the desorption tower 17 is effectively utilized to heat the first rich liquid; the two rich solutions absorb the waste heat of the hot lean solution flowing out from the bottom of the desorption tower 17, and the waste heat of the gas flowing out from the top of the desorption tower 17 is utilized to divide the rich solution into two paths, so that the rich solution can absorb more waste heat to reach higher temperature compared with one path, the heat required by the rich solution in the desorption of the desorption tower 17 is reduced to a great extent, and the energy consumption of the boiler 18 for generating steam is further reduced.
The absorption tower 11 further includes: a third inlet 11A3 of the absorption column, which is located in the middle of the absorption column 11 and below the second inlet 11a2 of the absorption column; and the third outlet 11B3 of the absorption column, which is located in the middle of the absorption column 11 and above the third inlet 11A3 of the absorption column.
The chemical absorption carbon dioxide capture system based on waste heat recovery also includes an inter-stage cooler 21. The interstage cooler 21 has one side connected to the third inlet 11a3 of the absorption column and the other side connected to the third outlet 11B3 of the absorption column.
Wherein the absorbent in the absorption tower 11 (the absorbent which is sprayed through the absorption tower second inlet 11a2 and stored in the absorption tower 11) flows into the interstage cooler 21 through the absorption tower third outlet 11B3 to be cooled, the absorbent cooled through the interstage cooler 21 flows back into the absorption tower 11 through the absorption tower third inlet 11A3 and is sprayed downward, the sprayed downward absorbent is in countercurrent contact with the flue gas entering through the absorption tower first inlet 11a1, the absorbent absorbs at least part of carbon dioxide in the flue gas to become a rich liquid, and the rich liquid is settled downward; the flue gas from which at least part of the carbon dioxide is removed continues to move upwards and is in countercurrent contact with the absorbent sprayed down through the second inlet 11a2 of the absorption tower again, and the flue gas from which the carbon dioxide is removed is subjected to a second reaction by the absorbent sprayed down through the second inlet 11a2 of the absorption tower to become a rich liquid and the flue gas from which the carbon dioxide is removed, the generated rich liquid is settled downwards, the flue gas from which the carbon dioxide is removed still continues to move upwards, and the flue gas from which the carbon dioxide is removed, which moves upwards, carries part of the absorbent.
It should be noted that the absorption of the carbon dioxide needs to be performed at a lower temperature, so as to ensure that the absorption amount of the carbon dioxide in the absorption tower 11 reaches a maximum, and the arrangement of the interstage cooler 21 further reduces the temperature of the absorbent in the absorption tower 11, and the cooled absorbent flows back to the absorption tower 11 again to react with the flue gas, so that the absorption amount and the absorption rate of the carbon dioxide in the flue gas are improved, thereby reducing the usage of the absorbent and saving the cost; the flue gas entering through the first inlet 11a1 of the absorption tower is absorbed by the absorbent sprayed from the third inlet 11A3 of the absorption tower and the third inlet 11a2 of the absorption tower in turn during the upward movement, so that the carbon dioxide in the flue gas is fully absorbed, and the absorption rate of the carbon dioxide is improved.
In one embodiment, the interstage cooler 21 is a water cooler.
The cavity at the upper part of the absorption tower 11 is pre-stored with washing water. The absorption tower 11 further includes: a fourth inlet 11a4 of the absorption column, which is located at the upper part of the absorption column 11 and above the second inlet 11a2 of the absorption column; and a fourth outlet 11B4 of the absorption tower, which is located at the upper part of the absorption tower 11 and above the second inlet 11a2 of the absorption tower, for discharging the water washing water pre-stored in the absorption tower 11.
The chemical absorption carbon dioxide capture system based on waste heat recovery and utilization further comprises a primary washing pump 22 and a primary washing cooler 23.
The primary wash pump 22 includes: the inlet 22A of the primary washing pump is communicated with the fourth outlet 11B4 of the absorption tower; the primary wash pump outlet 22B.
The primary scrubber cooler 23 is connected to the outlet 22B of the primary scrubber pump at one side and to the fourth inlet 11a4 of the absorption column at the other side.
Wherein, the absorption tower 11, the primary washing pump 22 and the primary washing cooler 23 form a primary washing loop, when the primary washing pump 22 is turned on, the water washing water in the absorption tower 11 flows into the primary washing pump 22 through the fourth outlet 11B4 of the absorption tower and the inlet 22A of the primary washing pump, then flows into a primary washing cooler 23 through a primary washing pump outlet 22B for cooling, the cooled washing water flows back to the upper part of the absorption tower 11 again and is sprayed down, the flue gas with carbon dioxide removed moves upwards in the absorption tower 11 and also carries part of the absorbent, the flue gas with carbon dioxide removed and part of the absorbent moves upwards in the absorption tower 11 and is in countercurrent contact with the cooled washing water, at least part of the absorbent in the flue gas is dissolved in the washing water, the flue gas after one time of washing continues to move upwards and then is discharged through the second outlet 11B2 of the absorption tower.
The process of one-time washing washes at least the absorbent carried by the flue gas without carbon dioxide, prevents the absorbent dissolved by the water washing water from being carried out of the absorption tower 11 by the flue gas without carbon dioxide, and reduces the loss of the absorbent.
In an embodiment, the absorption tower 11 further comprises an absorption tower wire mesh disposed at the top of the absorption tower 11 for filtering amine vapor (absorbent) mixed in the carbon dioxide-removed flue gas, thereby further reducing the loss of the absorbent.
It should be noted that the flue gas after being washed once and then discharged through the second outlet 11B2 of the absorption tower still carries part of the absorbent.
The chemical absorption carbon dioxide capture system based on waste heat recovery and utilization further comprises a first gas-liquid separator 24 and a washing tower 25.
The first gas-liquid separator 24 includes: a first gas-liquid separator inlet 24A communicating with the absorber second outlet 11B 2; a first gas-liquid separator first outlet 24B1 located at the bottom of the first gas-liquid separator 24; the first gas-liquid separator second outlet 24B2 is located at the top of the first gas-liquid separator 24. In an embodiment, the first gas-liquid separator 24 further includes a wire mesh for the first gas-liquid separator, which is disposed on the top of the first gas-liquid separator 24, and is used for filtering the condensed diluted amine liquid (absorbent) mixed in the flue gas from which the carbon dioxide is removed, so as to further reduce the loss of the absorbent.
The washing tower 25 stores therein washing water, and the washing tower 25 includes: a scrubber first inlet 25A1 located in the middle of the scrubber 25 and communicating with a first gas-liquid separator second outlet 24B 2; a second scrubber inlet 25a2 located above the first scrubber inlet 25a 1; a scrubber first outlet 25B1 at the top of scrubber 25; a second outlet 25B2 of the scrubber tower, located at the lower part of the scrubber tower 25; a third outlet 25B3 of the scrub column is located at the bottom of the scrub column 25.
In an embodiment, the washing tower 25 may further include a screen for washing tower disposed at the top of the washing tower 25 for filtering the condensed diluted amine liquid (droplets) mixed in the flue gas from which carbon dioxide is removed, so as to further reduce the loss of the absorbent.
The secondary wash pump 26 includes: the inlet 26A of the secondary washing pump is communicated with the second outlet 25B2 of the washing tower; the secondary wash pump outlet 26B.
The secondary scrubber cooler 27 is connected to the outlet 26B of the secondary scrubber pump at one side and to the second inlet 25a2 of the scrubber tower at the other side.
The lean liquid separator 28 includes: a lean liquor splitter first inlet 28a1 communicating with the first gas-liquid separator first outlet 24B 1; a lean liquid splitter second inlet 28a2 communicating with the scrubber third outlet 25B 3; lean splitter outlet 28B.
The absorbent reservoir 29 includes: an absorbent storage inlet 29A communicating with the lean liquor splitter outlet 28B; and an absorbent reservoir outlet 29B communicating with one side of the lean liquid cooler 20.
Wherein the flue gas carrying part of the absorbent discharged from the second outlet 11B2 of the absorption tower enters the first gas-liquid separator 24 via the first gas-liquid separator inlet 24A, and the first gas-liquid separator 24 separates at least part of the absorbent from the flue gas.
The flue gas is discharged through the first gas-liquid separator second outlet 24B2, the discharged flue gas still contains at least part of the absorbent, the flue gas containing at least part of the absorbent enters the washing tower 25 through the washing tower first inlet 25A1 and moves upwards, the water washing water in the washing tower 25 enters the secondary washing pump 26 through the washing tower second outlet 25B2 and the secondary washing pump inlet 26A and then flows into the secondary washing cooler 27 through the secondary washing pump outlet 26B for cooling, the cooled water washing water enters the washing tower 25 through the washing tower second inlet 25A2 and is sprayed downwards, the sprayed water washing water is in countercurrent contact with the flue gas carrying at least part of the absorbent, the absorbent in the flue gas is dissolved by the water, the flue gas without the absorbent is discharged through the washing tower first outlet 25B1, and the water washing water with the absorbent dissolved in the flue gas passes through the washing tower third outlet 25B3, The lean splitter second inlet 28a2 flows into the lean splitter 28.
The absorbent separated via the first gas-liquid separator 24 flows into the lean liquid splitter 28 via the first gas-liquid separator first outlet 24B1, the lean liquid splitter first inlet 28a 1.
The lean liquid splitter 28 mixes the two absorbent paths (the absorbent flowing in from the first inlet 28a1 of the lean liquid splitter and the absorbent flowing in from the second inlet 28a2 of the lean liquid splitter), and the mixed absorbent enters the absorbent storage 29 through the outlet 28B of the lean liquid splitter and the inlet of the absorbent storage 29, and then flows into the absorption tower 11 through the outlet 29B of the absorbent storage and the lean liquid cooler 20 to be recycled.
In the above-mentioned secondary washing process, the first gas-liquid separator 24 separates out at least part of the absorbent in the flue gas, and then enters the lean liquid splitter 28; the flue gas after gas-liquid separation enters the washing tower 25 again for secondary washing, the absorbent carried by the flue gas is dissolved in the washing tower 25 after the flue gas is washed by the washing tower 25, then the flue gas enters the barren solution splitter 28, the absorbent separated by the first gas-liquid separator 24 and the absorbent washed by the washing tower 25 respectively flow into the barren solution splitter 28 and are mixed, and the mixed absorbent returns to the absorption tower 11 again for recycling, so that the loss of the absorbent is greatly reduced, and the cost is saved; in addition, the provision of the first gas-liquid separator wire mesh of the first gas-liquid separator 24 and the washing tower wire mesh of the washing tower 25 further reduces the loss of the absorbent.
The chemical absorption method carbon dioxide capture system based on waste heat recycling further comprises a flash tank 30, a Roots blower 31 and a steam cooler 32.
The flash tank 30 includes: the inlet 30A of the flash tank is communicated with the second outlet 17B2 of the desorption tower; the flash tank first outlet 30B 1; the flash tank second outlet 30B2 is in communication with the second lean-rich heat exchanger second inlet 15a 2.
The roots blower 31 includes: the inlet 31A of the Roots blower is communicated with the first outlet 30B1 of the flash tank; roots blower outlet 31B.
The vapor cooler 32 has one side connected to the roots blower outlet 31B and the other side connected to the third inlet 17a3 of the desorber.
The barren solution flowing out through the second outlet 17B2 of the desorption tower directly enters the flash tank 30 through the inlet 30A of the flash tank, the barren solution is flashed in the flash tank 30 to flash off part of steam (the steam is mostly water vapor, and the small part of the steam is amine vapor), the flashed off steam enters the Roots blower 31 through the first outlet 30B1 of the flash tank and the inlet 31A of the Roots blower, the steam is pressurized and heated in the Roots blower 31, then enters the steam cooler 32 through the outlet 31B of the Roots blower to be cooled, and the cooled steam enters the desorption tower 17 through the third inlet 17A3 of the desorption tower to provide auxiliary heat for desorption of the rich solution in the desorption tower 17; the flashed lean solution enters the second lean-rich solution heat exchanger 15 through the second outlet 30B2 of the flash tank and the second inlet 15a2 of the second lean-rich solution heat exchanger, and performs the third heat exchange with the second path of the rich solution entering through the first inlet 15a1 of the second lean-rich solution heat exchanger, so that the lean solution releases heat and is cooled.
The lean solution is flashed by the flash tank 30 to release a large amount of steam, the temperature and pressure of the steam are increased (for example, from 70-90 ℃ to 110-.
The chemical absorption carbon dioxide capture system based on waste heat recovery and utilization further comprises a purification tower 33, a purification pump 34 and a purification cooler 35.
The purifying tower 33 stores a purifying agent therein, and the purifying tower 33 includes: a first inlet 33A1 of the purification tower, which is located at the lower part of the purification tower 33 and is used for the external flue gas to enter; a purification column second inlet 33a2 located at an upper portion of the purification column 33; a first outlet 33B1 of the purification tower, which is positioned at the top of the purification tower 33 and is communicated with the first inlet 11A1 of the absorption tower; and a second outlet 33B2 of the purification tower located at the lower part of the purification tower 33 and below the first inlet 33a1 of the purification tower.
In one embodiment, the purification tower 33 further comprises a wire mesh for the purification tower, which is used for removing water vapor and mist in the flue gas.
The purge pump 34 includes: a purge pump inlet 34A communicating with a purge column second outlet 33B 2; purge pump outlet 34B.
The purge cooler 35 communicates with the purge pump outlet 34B on one side and the purge tower second inlet 33a2 on the other side.
Wherein, the purifying tower 33, the purifying pump 34 and the purifying cooler 35 form an external flue gas purifying circulation loop, when the purifying pump 34 is turned on, the purifying agent in the purifying tower 33 is discharged through the second outlet 33B2 of the purifying tower, pumped into the purifying cooler 35 by the purifying pump 34 for cooling, returned into the purifying tower 33 through the second inlet 33A2 of the purifying tower and sprayed downwards, the external flue gas enters the purifying tower 33 through the first inlet 33A1 of the purifying tower and moves upwards, the external flue gas moving upwards contacts with the purifying agent sprayed downwards through the second inlet 33A2 of the purifying tower in a countercurrent mode, the purifying agent absorbs the acidic impurity gas and the smoke dust in the external flue gas, the carbon dioxide in the external flue gas is not absorbed by the purifying agent, the flue gas moves upwards after being purified and enters the absorption tower 11 through the first outlet 33B1 of the purifying tower and the first inlet 11A1 of the absorption tower, to be supplied to the absorption tower 11.
In one embodiment, the tower first inlet 33a1 of the tower 33 may be in communication with a power plant flue gas duct. The scavenger may be sodium bicarbonate solution. Of course, without being limited thereto, any suitable scavenger may be selected by the person skilled in the art.
The setting of purifying column 33 has carried out effectual purification to the flue gas that gets into in the absorption tower 11, avoids absorbent absorption impurity gas in the absorption tower 11, and then has improved the purity of product gas.
The carbon dioxide discharged from the first outlet 17B1 of the desorption tower also carries part of the lean liquid.
In an embodiment, the desorption tower 17 further includes a wire mesh for the desorption tower for filtering the amine vapor (lean liquid vapor) carried by the carbon dioxide, thereby reducing the loss of a part of the lean liquid.
The chemical absorption carbon dioxide capture system based on waste heat recovery and utilization further comprises a desorption gas condenser 36 and a second gas-liquid separator 37.
The stripping gas condenser 36 includes: a stripping gas condenser inlet 36A in communication with the evaporator first outlet 161B 1; desorption gas condenser outlet 36B.
The second gas-liquid separator 37 includes: a second gas-liquid separator inlet 37A communicated with a desorption gas condenser outlet 36B; a second gas-liquid separator first outlet 37B1 located at the top of the second gas-liquid separator 37; the second gas-liquid separator second outlet 37B2 is located at the bottom of the second gas-liquid separator 37.
In one embodiment, the second gas-liquid separator 37 further includes a wire mesh for a second gas-liquid separator for filtering the condensed amine liquid (lean liquid) mixed in the product gas.
Wherein the carbon dioxide with the part of the lean solution (existing in the form of the amine vapor) enters the condenser 163 through the first outlet 161B1 of the evaporator and the inlet 36A of the desorption gas condenser for cooling, the cooled carbon dioxide with the part of the lean solution enters the second gas-liquid separator 37 through the inlet 37A of the second gas-liquid separator, the carbon dioxide with the part of the lean solution is separated into the carbon dioxide product gas and the lean solution through the gas-liquid separation of the second gas-liquid separator 37, and the carbon dioxide product gas is discharged through the first outlet 37B1 of the second gas-liquid separator for the next operation.
The separated lean liquid is discharged via the second gas-liquid separator second outlet 37B2 and then returned to the absorbent storage 29 to be used as an absorbent.
The carbon dioxide with partial barren solution discharged from the desorption tower 17 has a large amount of waste heat, the carbon dioxide with partial barren solution effectively transfers the waste heat to the working medium through heat exchange with the working medium in the heat pump system 16, further transfers the heat to the first rich solution branched out by the rich solution splitter 14 through the working medium, the rich solution absorbing heat and raising the temperature is desorbed when entering the desorption tower 17, the heat required by desorption is reduced, and the waste heat of the gas at the top of the desorption tower 17 is effectively utilized; in addition, the lean liquid separated by the second gas-liquid separator 36 is returned to the absorbent storage 29 again, so that the loss of the lean liquid is reduced, and at the same time, the second gas-liquid separator captures at least part of the lean liquid carried by the product gas by the arrangement of the wire mesh, so that the loss of the lean liquid is further reduced.

Claims (9)

1. A chemical absorption carbon dioxide capture system based on waste heat recovery and utilization is characterized by comprising:
an absorption column (11) comprising:
the first inlet (11A1) of the absorption tower is positioned at the lower part of the absorption tower (11) and is used for the flue gas to enter, and the flue gas is provided with carbon dioxide;
a second inlet (11A2) of the absorption tower, which is positioned at the upper part of the absorption tower (11) and is used for the absorbent to enter;
a first outlet (11B1) of the absorption tower, which is positioned at the bottom of the absorption tower (11) and is used for flowing out the rich liquid;
a second outlet (11B2) of the absorption column, which is positioned at the top of the absorption column (11);
a pregnant liquor pump (12) comprising:
a rich liquid pump inlet (12A) communicated with the first outlet (11B1) of the absorption tower;
a rich liquid pump outlet (12B);
a first lean-rich liquid heat exchanger (13) comprising:
the first inlet (13A1) of the first lean-rich liquid heat exchanger is communicated with the outlet (12B) of the rich liquid pump;
a first lean-rich liquid heat exchanger second inlet (13a 2);
a first lean-rich liquid heat exchanger first outlet (13B 1);
a first lean-rich liquid heat exchanger second outlet (13B 2);
a rich liquor splitter (14) comprising:
a rich liquor splitter inlet (14A) communicating with a first lean-rich liquor heat exchanger first outlet (13B 1);
a rich liquor splitter first outlet (14B 1);
a rich liquor splitter second outlet (14B 2);
a second lean-rich liquid heat exchanger (15) comprising:
a second lean-rich heat exchanger first inlet (15A1) in communication with the rich stream splitter second outlet (14B 2);
a second lean-rich liquid heat exchanger second inlet (15a 2);
a second lean-rich liquid heat exchanger first outlet (15B 1);
a second outlet (15B2) of the second lean-rich liquid heat exchanger, which is communicated with the second inlet (13A2) of the first lean-rich liquid heat exchanger;
a heat pump system (16) comprising an evaporator (161), a compressor (162), a condenser (163) and a throttle valve (164),
an evaporator (161) comprising:
an evaporator first inlet (161a 1);
an evaporator second inlet (161a 2);
an evaporator first outlet (161B 1);
an evaporator second outlet (161B 2);
compressor (162) comprising:
a compressor inlet (162A) in communication with the evaporator second outlet (161B 2);
a compressor outlet (162B);
a condenser (163) comprising:
a condenser first inlet (163A1) in communication with the rich liquid splitter first outlet (14B 1);
a condenser second inlet (163A2) in communication with the compressor outlet (162B);
a condenser first outlet (163B 1);
a condenser second outlet (163B 2);
a throttle valve (164) arranged between the condenser (163) and the evaporator (161), one end of the throttle valve is controlled to be communicated with a second outlet (163B2) of the condenser, and the other end of the throttle valve is controlled to be communicated with a second inlet (161A2) of the evaporator;
desorber (17) comprising:
a first inlet (17A1) of the desorption tower, which is positioned at the upper part of the desorption tower (17) and is communicated with a first outlet (163B1) of the condenser;
a second inlet (17A2) of the desorption tower, which is positioned at the upper part of the desorption tower (17), is lower than the first inlet (17A1) of the desorption tower and is communicated with the first outlet (15B1) of the second lean-rich liquid heat exchanger;
a third inlet (17A3) of the desorption tower, which is positioned at the middle part of the desorption tower (17) and is lower than the second inlet (17A2) of the desorption tower;
a fourth inlet (17A4) of the desorption tower, which is positioned at the lower part of the desorption tower (17) and is lower than the third inlet (17A3) of the desorption tower;
a first outlet (17B1) of the desorption tower, which is positioned at the top of the desorption tower (17) and is communicated with a first inlet (161A1) of the evaporator;
a second outlet (17B2) of the desorption tower, which is positioned at the bottom of the desorption tower (17);
a third outlet (17B3) of the desorption tower, which is positioned at the lower part of the desorption tower (17);
boiler (18) comprising:
a boiler first inlet (18A1) communicated with the desorption tower third outlet (17B 3);
a boiler second inlet (18A2) for inflow of external saturated steam;
a boiler first outlet (18B1) communicated with the desorption tower fourth inlet (17A 4);
a boiler second outlet (18B 2);
a barren liquor pump (19) comprising:
a lean liquid pump inlet (19A) communicated with a second outlet (13B2) of the first lean-rich liquid heat exchanger;
a lean liquid pump outlet (19B);
and a lean liquid cooler (20) having one side connected to the lean liquid pump outlet (19B) and the other side connected to the second inlet (11A2) of the absorption tower.
2. The waste heat recovery-based chemical absorption carbon dioxide capture system of claim 1,
the absorption tower (11) further comprises:
a third inlet (11A3) of the absorption column, which is positioned in the middle of the absorption column (11) and below the second inlet (11A2) of the absorption column;
a third outlet (11B3) of the absorption column, which is positioned in the middle of the absorption column (11) and above the third inlet (11A3) of the absorption column;
the chemical absorption method carbon dioxide capture system based on waste heat recycling also comprises: and the interstage cooler (21) is communicated with a third inlet (11A3) of the absorption tower on one side, and is communicated with a third outlet (11B3) of the absorption tower on the other side.
3. The waste heat recovery-based chemical absorption carbon dioxide capture system of claim 2,
the absorption tower (11) further comprises:
a fourth inlet (11A4) of the absorption column, which is positioned above the absorption column (11) and above the second inlet (11A2) of the absorption column;
a fourth outlet (11B4) of the absorption tower, which is positioned at the upper part of the absorption tower (11) and above the second inlet (11A2) of the absorption tower, and is used for discharging the washing water pre-stored in the absorption tower (11);
the chemical absorption method carbon dioxide capture system based on waste heat recycling also comprises:
a primary wash pump (22) comprising:
a primary washing pump inlet (22A) communicated with a fourth outlet (11B4) of the absorption tower;
a primary wash pump outlet (22B);
and the primary washing cooler (23) is communicated with the outlet (22B) of the primary washing pump at one side and is communicated with the fourth inlet (11A4) of the absorption tower at the other side.
4. The waste heat recovery-based chemical absorption carbon dioxide capture system of claim 3,
the flue gas discharged from the second outlet (11B2) of the absorption tower also carries part of the absorbent;
the chemical absorption method carbon dioxide capture system based on waste heat recycling also comprises:
a first gas-liquid separator (24) comprising:
a first gas-liquid separator inlet (24A) communicating with the absorber second outlet (11B 2);
a first gas-liquid separator first outlet (24B1) at the bottom of the first gas-liquid separator (24);
a first gas-liquid separator second outlet (24B2) at the top of the first gas-liquid separator (24);
a washing tower (25), wherein the washing tower (25) stores water, and the washing tower (25) comprises:
a first inlet (25A1) of the washing tower, which is positioned at the middle part of the washing tower (25) and is communicated with a second outlet (24B2) of the first gas-liquid separator;
a second scrubber inlet (25A2) located at an upper portion of the scrubber (25);
a scrubber first outlet (25B1) located at the top of the scrubber (25);
a second outlet (25B2) of the scrubber tower, located at the lower part of the scrubber tower (25);
a scrubber third outlet (25B3) at the bottom of the scrubber (25);
a secondary wash pump (26) comprising:
a secondary washing pump inlet (26A) communicated with a second outlet (25B2) of the washing tower;
a secondary wash pump outlet (26B);
a secondary washing cooler (27), one side of which is communicated with the outlet (26B) of the secondary washing pump, and the other side of which is communicated with a second inlet (25A2) of the washing tower;
a lean liquid splitter (28) comprising:
a lean liquid splitter first inlet (28a1) in communication with the first gas-liquid separator first outlet (24B 1);
a lean liquid splitter second inlet (28A2) in communication with the scrubber third outlet (25B 3);
a lean liquid splitter outlet (28B);
an absorbent reservoir (29) comprising:
an absorbent storage inlet (29A) communicating with the lean liquor splitter outlet (28B);
an absorbent reservoir outlet (29B) communicating with one side of the lean liquid cooler (20).
5. The waste heat recovery based chemical absorption carbon dioxide capture system of claim 1, wherein the waste heat recovery based chemical absorption carbon dioxide capture system further comprises:
a flash tank (30) comprising:
a flash tank inlet (30A) communicated with a second outlet (17B2) of the desorption tower;
a flash tank first outlet (30B 1);
a second flash tank outlet (30B2) in communication with a second lean-rich heat exchanger second inlet (15A 2);
roots blower (31), comprising:
the inlet (31A) of the Roots blower is communicated with the first outlet (30B1) of the flash tank;
a Roots blower outlet (31B);
and one side of the steam cooler (32) is communicated with the outlet (31B) of the Roots blower, and the other side of the steam cooler is communicated with a third inlet (17A3) of the desorption tower.
6. The waste heat recovery based chemical absorption carbon dioxide capture system of claim 1, wherein the waste heat recovery based chemical absorption carbon dioxide capture system further comprises:
a purification tower (33), a purification agent being stored in the purification tower (33), the purification tower (33) comprising:
a first inlet (33A1) of the purification tower, which is positioned at the lower part of the purification tower (33) and is used for the external flue gas to enter;
a second inlet (33A2) of the purification tower, which is positioned at the upper part of the purification tower (33);
a first outlet (33B1) of the purification tower, which is positioned at the top of the purification tower (33) and is communicated with the first inlet (11A1) of the absorption tower;
a second outlet (33B2) of the purification tower, which is positioned at the lower part of the purification tower (33) and is positioned below the first inlet (33A1) of the purification tower;
a purge pump (34) comprising:
a purge pump inlet (34A) communicating with a purge column second outlet (33B 2);
a purge pump outlet (34B);
and the purification cooler (35) is communicated with the outlet (34B) of the purification pump on one side and is communicated with the second inlet (33A2) of the purification tower on the other side.
7. The waste heat recovery based chemical absorption carbon dioxide capture system of claim 6,
the purifying agent is sodium bicarbonate solution.
8. The waste heat recovery-based chemical absorption carbon dioxide capture system of claim 1,
carbon dioxide discharged from a first outlet (17B1) of the desorption tower also carries part of lean liquid;
the chemical absorption method carbon dioxide capture system based on waste heat recycling also comprises:
a stripping gas condenser (36) comprising:
a stripping gas condenser inlet (36A) in communication with the evaporator first outlet (161B 1);
a stripping gas condenser outlet (36B);
a second gas-liquid separator (37) comprising:
a second gas-liquid separator inlet (37A) communicated with a desorption gas condenser outlet (36B);
a second gas-liquid separator first outlet (37B1) at the top of the second gas-liquid separator (37);
and a second outlet (37B2) of the second gas-liquid separator, which is positioned at the bottom of the second gas-liquid separator (37).
9. The waste heat recovery-based chemical absorption carbon dioxide capture system of claim 1 wherein the absorbent is an organic amine solution.
CN201920707023.4U 2019-05-16 2019-05-16 Chemical absorption method carbon dioxide capture system based on waste heat recovery and utilization Active CN210729090U (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110152457A (en) * 2019-05-16 2019-08-23 中石化石油工程技术服务有限公司 The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery
CN110152457B (en) * 2019-05-16 2024-06-04 中石化石油工程技术服务有限公司 Chemical absorption method carbon dioxide trapping system based on waste heat recycling

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110152457A (en) * 2019-05-16 2019-08-23 中石化石油工程技术服务有限公司 The chemical absorption method carbon dioxide capture system utilized based on Waste Heat Recovery
CN110152457B (en) * 2019-05-16 2024-06-04 中石化石油工程技术服务有限公司 Chemical absorption method carbon dioxide trapping system based on waste heat recycling

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