WO2023061507A1 - 一种化学法和psa法同步回收烟道气中二氧化碳和氮气的系统及方法 - Google Patents

一种化学法和psa法同步回收烟道气中二氧化碳和氮气的系统及方法 Download PDF

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WO2023061507A1
WO2023061507A1 PCT/CN2022/129313 CN2022129313W WO2023061507A1 WO 2023061507 A1 WO2023061507 A1 WO 2023061507A1 CN 2022129313 W CN2022129313 W CN 2022129313W WO 2023061507 A1 WO2023061507 A1 WO 2023061507A1
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carbon dioxide
gas
nitrogen
outlet
tower
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PCT/CN2022/129313
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English (en)
French (fr)
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李玉雪
陈绍云
戚励
张永春
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碳和科技(北京)有限公司
北京市飞达捷能气体分离技术有限公司
大连理工大学
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Priority claimed from CN202111302095.9A external-priority patent/CN113975950B/zh
Application filed by 碳和科技(北京)有限公司, 北京市飞达捷能气体分离技术有限公司, 大连理工大学 filed Critical 碳和科技(北京)有限公司
Priority to SE2350521A priority Critical patent/SE2350521A1/en
Publication of WO2023061507A1 publication Critical patent/WO2023061507A1/zh

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    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • 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
    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/047—Pressure swing adsorption
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/343—Heat recovery
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/75—Multi-step processes
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/10—Nitrogen
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the invention belongs to the technical field of recovery and utilization of boiler flue gas, and in particular relates to a system and method for synchronously recovering carbon dioxide and nitrogen in flue gas by a chemical method and a PSA method.
  • Chinese patent application CN107899376A discloses a "united capture and recovery device and method for carbon dioxide and nitrogen in flue gas", which includes a flue gas treatment system, a first CO2 membrane separation unit, a second CO2 membrane separation unit and a N 2 membrane separation unit.
  • the device belongs to the membrane recovery method. Although it can capture carbon dioxide and nitrogen at the same time, the product purity is low.
  • the membrane tank has high requirements on the cleanliness of the gas source. The equipment is prone to blockage during use, the service life is short, and the price of the membrane tank is high. Not suitable for industrialized mass production.
  • Chinese patent application CN110498416A discloses "a system for synchronously recovering carbon dioxide and nitrogen from flue gas of a coal-fired power plant boiler", including a flue gas pretreatment system, a PSA1 system, a PSA2 system, a carbon dioxide compression and purification system, a carbon dioxide rectification storage system, and a PSA system.
  • High-purity nitrogen system The system can capture carbon dioxide and nitrogen to the greatest extent, and the product purity is high, but there are problems such as inflexible equipment operation, high energy consumption, and low recovery rate of carbon dioxide.
  • the pressure compression value of the former stage is too high and the power consumption is large.
  • the object of the present invention is to provide a system for synchronously recovering carbon dioxide and nitrogen in flue gas by chemical method and PSA method, and the recovery effect of carbon dioxide and nitrogen is good for the system of synchronously recovering carbon dioxide and nitrogen in flue gas by chemical method and PSA method , and can effectively save energy.
  • a system for synchronously recovering carbon dioxide and nitrogen in flue gas by chemical method and PSA method said system includes a carbon dioxide chemical method recovery system, carbon dioxide refining liquefaction system and nitrogen PSA concentration and purification system;
  • the carbon dioxide chemical method recovery system includes a carbon dioxide absorption tower, a carbon dioxide regeneration tower, a heat exchanger and a first cooler;
  • the top of the carbon dioxide absorption tower is provided with an air outlet, and the interior of the carbon dioxide absorption tower is equipped with
  • There is a first spraying device the bottom of the carbon dioxide absorption tower is provided with a rich liquid outlet, and the air outlet is connected to the air inlet of the nitrogen PSA concentration and purification system;
  • the tower of the carbon dioxide regeneration tower The top is provided with a desorption gas outlet, the inside of the carbon dioxide regeneration tower is provided with a second spray device, the bottom of the carbon dioxide regeneration tower is provided with a lean liquid outlet, and the desorption gas outlet is connected to the The liquid inlet of
  • the present invention also provides a method for synchronously recovering carbon dioxide and nitrogen in the flue gas.
  • the method for synchronously recovering carbon dioxide and nitrogen in the flue gas of the present invention adopts the following technical scheme: using the above-mentioned chemical method and PSA method for synchronous recovery
  • the carbon dioxide and nitrogen system in the flue gas simultaneously recovers carbon dioxide and nitrogen in the flue gas.
  • the present invention can recycle carbon dioxide and nitrogen to the greatest extent without producing three wastes;
  • the chemical method (solvent absorption method) is used to recycle carbon dioxide, and the carbon dioxide in the gas flowing out from the gas outlet at the top of the carbon dioxide regeneration tower has high purity (the volume concentration of carbon dioxide can reach 92-95 %) and the recovery rate is high;
  • the tower top release air produced by the chemical method (solvent absorption method) is a nitrogen-rich gas, and the nitrogen content is about 90-92%. When separated, the gas volume is larger.
  • the nitrogen PSA concentration and purification system of the present invention includes a second compressor, and there will be a secondary pressure raising process, and the compressor and compression pressure can be selected according to user needs, thereby achieving the purpose of energy saving.
  • Fig. 1 is the overall structure schematic diagram of the system of synchronous recovery of nitrogen and carbon dioxide in flue gas by chemical method and PSA method;
  • Fig. 2 is the structural representation of carbon dioxide chemical recovery system
  • Fig. 3 is the structural representation of carbon dioxide refined liquefaction system
  • Fig. 4 is a structural schematic diagram of a nitrogen PSA concentration and purification system.
  • 101-induced fan 101-induced fan; 102-desulfurization liquid pump; 103-desulfurization washing tower; 103a-third spray device; 104-first gas-liquid separator; 105-carbon dioxide absorption tower; 105a-first spray device; 106- 107-rich liquid pump; 108-heat exchanger; 109-lean liquid pump; 110-carbon dioxide regeneration tower; 110a-second spraying device; 111-second cooler; 112-second gas-liquid Splitter;
  • 201-first buffer tank 202-first compressor; 203-desulfurization bed; 204-drying bed, 205-third cooler; 206-liquefaction system; 207-rectification tower; 208-carbon dioxide storage tank;
  • 301-demister 301-demister; 302-fourth cooler; 303-third gas-liquid separator; 304-second compressor; 305-dryer; 306-second buffer tank; 307-nitrogen adsorption tower; 308-nitrogen tank.
  • the present invention aims at the problems existing in the capture and reuse of carbon dioxide and nitrogen in flue gas at present, and provides a system for synchronously recovering carbon dioxide and nitrogen in flue gas by chemical method and PSA method, as shown in Figure 1-2, the chemical
  • the system for synchronously recovering carbon dioxide and nitrogen in the flue gas by the method and the PSA method includes a carbon dioxide chemical method recovery system 1, a carbon dioxide refined liquefaction system 2, and a nitrogen PSA concentration and purification system 3;
  • the carbon dioxide chemical method recovery system 1 includes a carbon dioxide absorption tower 105, a carbon dioxide regeneration system Tower 110, heat exchanger 108 and first cooler 106;
  • the top of the tower of carbon dioxide absorption tower 105 is provided with vent air outlet, and the inside of carbon dioxide absorption tower 105 is provided with the first spray device 105a, and the tower bottom of carbon dioxide absorption tower 105
  • There is a rich liquid outlet, and the air outlet is connected to the inlet of the nitrogen PSA concentration and purification system 3;
  • the carbon dioxide in the flue gas can be absorbed by the carbon dioxide in the carbon dioxide absorption tower 105.
  • the chemical solvent is absorbed to obtain rich liquid rich in carbon dioxide.
  • the rich liquid is transported to the carbon dioxide regeneration tower 110 through the rich liquid outlet, the low-temperature fluid channel of the heat exchanger 108, and the second spraying device 110a.
  • the carbon dioxide in the rich liquid is desorbed at high temperature, and the desorbed gas comes out from the desorbed gas outlet at the top of the carbon dioxide regeneration tower 110 and enters the carbon dioxide refining liquefaction system 2 (desorbed gas
  • the volume concentration of carbon dioxide in the carbon dioxide absorption tower can reach 92-95%), and the carbon dioxide is further purified; while the unabsorbed components (release air) in the flue gas flow out from the discharge air outlet at the top of the carbon dioxide absorption tower 105 and enter Nitrogen PSA concentration and purification system 3 (the volume concentration of nitrogen in the vented air can reach 90-92%, relative to air, the content of nitrogen in the vented air is significantly higher, and the use of this vented air to prepare nitrogen helps to improve the production efficiency of nitrogen preparation.
  • the carbon dioxide regeneration tower 110 concentrates and purify the nitrogen in the vented air to prepare high-purity nitrogen; in the carbon dioxide regeneration tower 110, the rich liquid is sprayed from the second spraying device 110a, and the carbon dioxide is desorbed under the action of the reboiler at the bottom of the tower Afterwards, a lean liquid is formed (the content of carbon dioxide is low), and after the lean liquid flows out from the lean liquid outlet at the bottom of the carbon dioxide regeneration tower 110, it passes through the high-temperature fluid channel of the heat exchanger 108, the first cooler 106 and the first sprayer successively.
  • the shower device 105a enters the carbon dioxide absorption tower 105, and is used again for the absorption of carbon dioxide in the flue gas; the rich liquid in the low-temperature fluid channel and the lean liquid in the high-temperature fluid channel can pass through the heat exchanger 108 at the same time, in the heat exchange Heat exchange is performed in the cooler 108 to help recover heat from the lean liquid, reduce the workload of the first cooler 106, and save energy.
  • the system for synchronously recovering carbon dioxide and nitrogen in the flue gas by the chemical method and the PSA method of the present invention has the following advantages: (1) the present invention can recover carbon dioxide and nitrogen to the greatest extent without producing three wastes; (2) utilizes The chemical method (solvent absorption method) recovers carbon dioxide, and the carbon dioxide in the gas flowing out of the top outlet of the carbon dioxide regeneration tower has high purity and high recovery rate; (3) The tower top discharge air produced by the chemical method (solvent absorption method) is nitrogen-rich gas , the nitrogen content is about 90-92%, and the nitrogen-rich gas has a larger gas volume than when the PSA method is used to realize the separation of carbon dioxide in the flue gas.
  • the chemical method solvent absorption method
  • the first spraying device 105a is arranged on the top of the carbon dioxide absorption tower 105
  • the second spraying device 110a is arranged on the top of the carbon dioxide regeneration tower 110
  • the connecting pipeline between the rich liquid outlet and the heat exchanger 108 is provided with
  • the rich liquid pump 107, the lean liquid pump 109 is provided on the connecting pipeline between the lean liquid outlet and the heat exchanger 108.
  • the second spray device 110a is arranged on the top of the carbon dioxide regeneration tower 110, which helps to improve the efficiency of desorption of carbon dioxide in the rich liquid; the setting of the rich liquid pump 107 and the lean liquid pump 109 makes it convenient to realize The transfer of the liquid and the lean liquid ensures the normal operation of the carbon dioxide absorption tower 105 and the carbon dioxide regeneration tower 110 and improves production efficiency.
  • the carbon dioxide chemical method recovery system 1 also includes a flue gas pretreatment system, and the flue gas pretreatment system includes an induced draft fan 101, a desulfurization water washing tower 103 and a first gas-liquid separator 104; the induced draft fan 101 and the desulfurization water washing tower 103
  • the air inlet is connected, and is used to transport flue gas to the air inlet of desulfurization water washing tower 103; the gas outlet of desulfurization water washing tower 103 is connected with the air inlet of the first gas-liquid separator 104, and desulfurization water washing tower 103 is used for
  • the flue gas is desulfurized; the gas outlet of the first gas-liquid separator 104 is connected to the inlet of the carbon dioxide absorption tower 105, and the first gas-liquid separator 104 is used for gas-liquid separation of the gas treated by the desulfurization water washing tower 103 .
  • the flue gas pretreatment system helps to remove sulfide in the flue gas in advance, avoiding
  • the top of the desulfurization washing tower 103 is provided with a third spray device 103a, and the bottom of the desulfurization water washing tower 103 is provided with a desulfurization liquid outlet, which is connected to the desulfurization liquid outlet and the liquid inlet of the third spray device 103a
  • a desulfurization liquid pump 102 is provided on the pipeline. The arrangement of the third spraying device 103a and the desulfurization liquid pump 102 helps to improve the effect of desulfurization, and can conveniently realize the repeated use of the desulfurization liquid.
  • the carbon dioxide chemical method recovery system 1 also includes a second cooler 111 and a second gas-liquid separator 112, the inlet of the second cooler 111 is connected to the gas outlet of the carbon dioxide regeneration tower 110, and the outlet of the second cooler 111 is The gas port is connected to the gas inlet of the second gas-liquid separator 112 , and the gas outlet of the second gas-liquid separator 112 is connected to the gas inlet of the carbon dioxide refining liquefaction system 2 .
  • the arrangement of the second cooler 111 and the second gas-liquid separator 112 helps to further remove water from the desorbed gas at the top of the carbon dioxide regeneration tower 110 and improve the efficiency of carbon dioxide purification.
  • the carbon dioxide refining liquefaction system 2 includes a secondary desulfurization system, a third cooler 205, a liquefaction system 206 and a rectification tower 207, and the inlet of the secondary desulfurization system is connected to the desorption gas outlet (
  • the carbon dioxide chemical recovery system 1 includes a second cooler 111 and a second gas-liquid separator 112
  • the inlet of the secondary desulfurization system is connected to the gas outlet of the second gas-liquid separator 112
  • the secondary desulfurization The gas outlet of the system is connected to the inlet of the third cooler 205
  • the gas outlet of the third cooler 205 is connected to the inlet of the liquefaction system 206
  • the liquid outlet of the liquefaction system 206 is connected to the rectification tower 207 .
  • the third cooler 205, the liquefaction system 206 and the rectification tower 207 in the carbon dioxide refining liquefaction system 2 can be obtained. Finished carbon dioxide (volume concentration ⁇ 99.9%).
  • the carbon dioxide refining liquefaction system 2 further includes a carbon dioxide storage tank 208 , and the carbon dioxide storage tank 208 is connected to the rectification tower 207 .
  • the carbon dioxide storage tank 208 By setting the carbon dioxide storage tank 208, the refined high-purity carbon dioxide (volume concentration ⁇ 99.9%) can be stored in the carbon dioxide storage tank 208, which is convenient for use.
  • the secondary desulfurization system includes a first buffer tank 201, a first compressor 202, a desulfurization bed 203 and a drying bed 204, and the inlet of the first buffer tank 201 is connected with the desorption gas outlet (in the carbon dioxide chemical method recovery system 1
  • the air inlet of the first buffer tank 201 is connected to the gas outlet of the second gas-liquid separator 112
  • the gas outlet of the first buffer tank 201 It is connected with the inlet of the first compressor 202, and the gas outlet of the first compressor 202 is connected with the inlet of the desulfurization bed 203, and the gas outlet of the desulfurization bed 203 is connected with the inlet of the drying bed 204, and the gas outlet of the drying bed 204 is connected with each other.
  • the air outlet is connected with the air inlet of the third cooler 205 .
  • the desulfurization bed 203 and the drying bed 204 to further desulfurize and dry the desorbed gas from the carbon dioxide regeneration tower 110, the purity of carbon dioxide is further improved.
  • the desulfurized gas can be desulfurized and dried by the desulfurization bed 203 and the drying bed 204 .
  • the desulfurization bed 203 includes two parallel desulfurization towers, and a desulfurization adsorbent is arranged in the desulfurization towers;
  • the drying bed 204 includes two parallel drying towers, and a desiccant is arranged in the drying towers.
  • the nitrogen PSA concentration and purification system 3 includes a mist eliminator 301, a fourth cooler 302, a third gas-liquid separator 303, a second compressor 304, a drier 305, a second buffer tank 306 and Nitrogen adsorption tower 307 (the nitrogen adsorption tower 307 is filled with an adsorbent for purifying nitrogen, and has a high recovery rate for the vented air with complex components), the air inlet of the demister 301 is connected with the vented air outlet of the carbon dioxide absorption tower 105 The air port is connected, the air outlet of the demister 301 is connected with the air inlet of the fourth cooler 302, the air outlet of the fourth cooler 302 is connected with the air inlet of the third gas-liquid separator 303, and the third gas-liquid separator The gas outlet of 303 is connected with the inlet of the second compressor 304, the gas outlet of the second compressor 304 is connected with the inlet of drier 305, the gas outlet of d
  • the desorbed gas obtained after being treated by the carbon dioxide regeneration tower 110 enters the demister 301 and the third gas-liquid separator 303 in turn, and after removing large particles of free water, enters the second compressor 304, and the gas outlet of the second compressor 304 is connected to the drying Air inlet of device 305, after being dried by drier 305, gas enters nitrogen adsorption tower 307 after second buffer tank 306, and after pressure swing adsorption, product nitrogen (volume concentration can reach 99-99.999%) can be obtained.
  • the nitrogen PSA concentration and purification system includes a second compressor 304, which will have a second pressure boosting process, and the compressor and compression pressure can be selected according to the user's needs, so as to achieve the purpose of energy saving.
  • the nitrogen PSA concentration and purification system 3 further includes a nitrogen storage tank 308, which is connected to the gas outlet at the top of the nitrogen adsorption tower 307, so as to store the recovered nitrogen.
  • a nitrogen storage tank 308 which is connected to the gas outlet at the top of the nitrogen adsorption tower 307, so as to store the recovered nitrogen.
  • At least two nitrogen adsorption towers 307 are provided; more than two nitrogen adsorption towers 307 are arranged in parallel.
  • two nitrogen adsorption towers 307 are arranged in parallel.
  • the method for synchronously recovering carbon dioxide and nitrogen in flue gas of the present invention adopts the above-mentioned chemical method and PSA method to synchronously recover carbon dioxide and nitrogen in flue gas.
  • the method for synchronously recovering carbon dioxide and nitrogen in the flue gas of the present invention is specifically exemplified as follows:
  • the present invention is used for recovery of carbon dioxide and nitrogen in the flue gas of a certain coal power plant.
  • the carbon dioxide gas is used to increase the income of smart agriculture, and the nitrogen gas is used for the replacement and purging of the chemical workshop of our factory.
  • the composition of flue gas is shown in Table 1 below:
  • Element sulfur dioxide Nitrogen oxides carbon monoxide carbon dioxide oxygen water measured value 20mg/ m3 31mg/ m3 not detected 13% 6.20% 12.50% The detection limit 2mg/ m3 2mg/ m3 20mg/ m3 0.03% —— ———
  • the required flue gas is drawn from the flue gas discharge chimney after desulfurization and denitrification, enters the desulfurization washing tower 103 for desulfurization and dust removal, enters the first gas-liquid separator 104 for gas-liquid separation, and then enters the carbon dioxide absorption tower 105, and the flue gas
  • the carbon dioxide in the carbon dioxide is absorbed by the solvent, and the solvent forms a rich liquid, and the unabsorbed nitrogen-rich gas (90% to 92% nitrogen content) flows out through the air outlet at the top of the carbon dioxide absorption tower 105.
  • the rich liquid enters the carbon dioxide regeneration tower 110 (the liquid that enters the carbon dioxide regeneration tower 110 inside) through the rich liquid pump 107 and the lean liquid (the liquid after the rich liquid desorbs and removes carbon dioxide in the carbon dioxide regeneration tower 110) performs heat exchange in the heat exchanger 108.
  • the second spraying device 110a under the heating effect of the reboiler at the bottom of the tower, the carbon dioxide is desorbed, and the crude carbon dioxide gas (desorption gas) with a carbon dioxide content of 95% flows out from the desorption gas outlet at the top of the tower, and passes through the second cooler 111 and the second gas-liquid separator 112 to further remove water, enter the carbon dioxide refining liquefaction system 2.
  • the lean liquid After the rich liquid desorbs the carbon dioxide in the carbon dioxide regeneration tower 110, the lean liquid is formed at the bottom of the tower, passes through the lean liquid pump 109, exchanges heat with the rich liquid in the heat exchanger 108, and then enters the first cooler 106 (a water cooler is optional) After further cooling down, it enters the carbon dioxide absorption tower 105 (enters the first spray device 105a inside the carbon dioxide absorption tower 105), and completes a working cycle.
  • the stripping gas (containing 95% crude carbon dioxide gas) obtained after cooling and dewatering by the second cooler 111 and the second gas-liquid separator 112 enters the first compressor 202 after passing through the first buffer tank 201 to increase the pressure to 2.5MPa, then enter the desulfurization bed 203 and drying bed 204 for desulfurization and impurity removal, enter the third cooler 205 to cool down, and then enter the liquefaction system 206, after cooling down to -18°C, liquid carbon dioxide is obtained, and the liquid carbon dioxide enters rectification
  • the tower 207 is refined and purified, food-grade carbon dioxide with a purity of 99.9% can be obtained at the bottom of the tower, which is stored in the carbon dioxide storage tank 208 .
  • the air released from the top of the rectification tower can also be used as a source of regeneration gas for the desulfurization bed 203 and the drying bed 204, saving product gas and reducing energy consumption.
  • Second compressor 304 pressurize to 0.8 ⁇ 1.0MPa, enter second buffer tank 306 after being dried by drier 305, then enter nitrogen adsorption tower 307 pressure swing adsorption to obtain finished nitrogen, finished nitrogen enters nitrogen storage tank 308, nitrogen purity from 99% to 99.999%.
  • the carbon and nitrogen separation in the flue gas adopts the chemical absorption mode, and the carbon dioxide recovery effect is good, and the carbon dioxide with a content of about 95% can be obtained, and the recovery rate of the carbon dioxide is high;
  • the nitrogen content in the air can reach 92%, much higher than the 78% in the air, and it is a high-quality nitrogen raw material.
  • Nitrogen PSA concentration and purification system 3 uses nitrogen-rich gas containing 92% nitrogen as the raw material gas, adopts the secondary compression mode to increase the pressure from 3KPa to 0.8-1.0MPa, and fully recovers the compression energy. Compared with the production of nitrogen from air , energy saving of more than 20%.

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Abstract

一种化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统及方法。该化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统包括二氧化碳化学法回收系统（1）、二氧化碳精制液化系统（2）和氮气PSA浓缩提纯系统（3）；二氧化碳化学法回收系统（1）包括二氧化碳吸收塔（105）、二氧化碳再生塔（110）、换热器（108）和第一冷却器（106）。

Description

一种化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统及方法 技术领域
本发明属于锅炉烟道气的回收利用技术领域，具体涉及一种化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统及方法。
背景技术
二氧化碳排放引起的温室效应和极端天气，已经严重影响了全球的气候。对燃煤锅炉烟道气的二氧化碳和氮气捕集再利用是实现双碳目标的一项重要措施，不仅进一步减少碳排放，且能降低能耗。
中国专利申请CN107899376A公开了一种“烟气中二氧化碳和氮气的联合捕集回收装置及方法”，该装置包括烟气处理系统，第一CO 2膜分离单元，第二CO 2膜分离单元以及N 2膜分离单元。该装置属于膜回收方式，虽然能同时捕集二氧化碳和氮气，但是产品纯度低，膜桶对气源洁净度要求很高，设备使用过程中容易产生堵塞，寿命短，且膜桶价格较高，不适合工业化大生产。
中国专利申请CN110498416A公开了“一种燃煤电厂锅炉烟气同步回收二氧化碳及氮气的系统”，包括烟气预处理系统、PSA1系统、PSA2系统、二氧化碳压缩提纯系统、二氧化碳精馏贮存系统、PSA制高纯氮系统。该系统能最大程度的捕集二氧化碳和氮气，产品纯度较高，但是存在设备操作不灵活，能耗高、二氧化碳回收率低的问题。当后级氮气产量降低或者不进行捕集时，前级的压力压缩值过高，耗电量较大。
因此，需要提供一种针对上述现有技术不足的改进技术方案。
发明内容
本发明的目的在于提供一种化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，该化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统对二氧化碳和氮气的回收效果好，且可有效节能。
为了实现上述目的，本发明提供如下技术方案：一种化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，所述系统包括二氧化碳化学法回收系统、二氧化碳精制液化系统和氮气PSA浓缩提纯系统；所述二氧化碳化学法回收系统包括二氧化碳吸收塔、二氧化碳再生塔、换热器和第一冷却器；所述二氧化碳吸收塔的塔顶设有放空气出气口，所述二氧化碳吸收塔的内部设有第一喷淋装置，所述二氧化碳吸收塔的塔底设有富液出液口，所述放空气出气口与所述氮气PSA浓缩提纯系统的进气口相连；所述二氧化碳再生塔的塔顶设有解吸气出气口，所述二氧化碳再生塔的内部设有第二喷淋装置，所述二氧化碳再生塔的塔底设有贫液出液口，所述解吸气出气口与所述二氧化碳精制液化系统的进液口相连；所述换热器具有高温流体通道和低温流体通道，所述富液出液口与所述低温流体通道的进液口相连，所述低温流体通道的出液口与所述第二喷淋装置的进液口相连；所述第一冷却器的出液口与所述第一喷淋装置的进液口相连，所述第一冷却器的进液口与所述高温流体通道的出液口相连，所述高温流体通道的进液口与所述贫液出液口相连。
本发明还提供了一种同步回收烟道气中二氧化碳和氮气的方法，本发明的同步回收烟道气中二氧化碳和氮气的方法采用如下技术方案：采用如上所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统同步回收烟道气中二氧化碳和氮气。
有益效果：
本发明能最大程度的回收二氧化碳和氮气，无三废产生；利用化学法(溶剂吸收法)回收二氧化碳，二氧化碳再生塔的塔顶出气口中流出的气体中二氧化碳纯度高(二氧化碳体积浓度可达92～95％)且回收率高；化学法(溶剂吸收法)产生的塔顶放空气为富氮气体，氮气含量约在90～92％，且富氮气体较之采用PSA法实现烟道气中二氧化碳的分离时，气量更大。
本发明的氮气PSA浓缩提纯系统中包括第二压缩机，会有二次提压过程，可以根据用户需要，选择压缩机及压缩压力，从而起到节能的目的。
附图说明
图1为化学法和PSA法同步回收烟道气中氮气和二氧化碳的系统的整体结构示意图；
图2为二氧化碳化学法回收系统的结构示意图；
图3为二氧化碳精制液化系统的结构示意图；
图4为氮气PSA浓缩提纯系统的结构示意图。
附图标记：
1-二氧化碳化学法回收系统；2-二氧化碳精制液化系统；3-氮气PSA浓缩提纯系统；
101-引风机；102-脱硫液泵；103-脱硫水洗塔；103a-第三喷淋装置；104-第一气液分离器；105-二氧化碳吸收塔；105a-第一喷淋装置；106-第一冷却器；107-富液泵；108-换热器；109-贫液泵；110-二氧化碳再生塔；110a-第二喷淋装置；111-第二冷却器；112-第二气液分离器；
201-第一缓冲罐；202-第一压缩机；203-脱硫床；204-干燥床、205-第三冷却器；206-液化系统；207-精馏塔；208-二氧化碳储罐；
301-除雾器；302-第四冷却器；303-第三气液分离器；304-第二压缩机；305-干燥器；306-第二缓冲罐；307-氮气吸附塔；308-氮气储罐。
具体实施方式
本发明针对目前烟道气中的二氧化碳和氮气捕集再利用存在的问题，提供一种化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，如图1-2所示，该化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统包括二氧化碳化学法回收系统1、二氧化碳精制液化系统2和氮气PSA浓缩提纯系统3；二氧化碳化学法回收系统1包括二氧化碳吸收塔105、二氧化碳再生塔110、换热器108和第一冷却器106；二氧化碳吸收塔105的塔顶设有放空气出气口，二氧化碳吸收塔105的内部设有第一喷淋装置105a，二氧化碳吸收塔105的塔底设有富液出液口，放空气出气口与氮气PSA浓缩提纯系统3的进气口相连；二氧化碳再生塔110的塔顶设有解吸气出气口，二氧化碳再生塔110的内部设有第二喷淋装置110a，二氧化碳再生塔110的塔底设有贫液出液口和塔底再沸器(图中未示出)，解吸气出气口与二氧化碳精制液化系统2的进液口相连；换热器108具有高温流体通道和低温流体通道，富液出液口与低温流体通道的进液口相连，低温流体通道的出液口与第二喷淋装置110a的进液口相连；第一冷却器106的出液口与所述第一喷淋装置105a的进液口 相连，第一冷却器106的进液口与高温流体通道的出液口相连，高温流体通道的进液口与贫液出液口相连。
采用上述化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统对烟道气进行处理时，烟道气进入二氧化碳吸收塔105后，烟道气中的二氧化碳可被二氧化碳吸收塔105内的化学溶剂吸收，得到富含二氧化碳的富液，富液经富液出液口、换热器108的低温流体通道和第二喷淋装置110a被输送至二氧化碳再生塔110，在二氧化碳再生塔110塔底的塔底再沸器的作用下，富液中的二氧化碳在高温下被解吸出来，解吸气从二氧化碳再生塔110塔顶的解吸气出气口中出来进入二氧化碳精制液化系统2(解吸气中二氧化碳的体积浓度可达92-95％)，对二氧化碳进行进一步纯化；而烟道气中未被吸收的成分(放空气)则从二氧化碳吸收塔105塔顶的放空气出气口流出后，进入氮气PSA浓缩提纯系统3(放空气中氮气的体积浓度可达90-92％，相对空气，放空气中氮气的含量显著更高，采用该放空气制备氮气有助于提高氮气制备的生产效率，节省成本)，对放空气中的氮气进行浓缩提纯，制备高纯度氮气；二氧化碳再生塔110中，富液从第二喷淋装置110a喷出、并在塔底再沸器的作用下解吸出二氧化碳后，形成贫液(二氧化碳的含量低)，贫液经二氧化碳再生塔110塔底的贫液出液口流出后，依次经过换热器108的高温流体通道、第一冷却器106和第一喷淋装置105a，进入二氧化碳吸收塔105，再次用于烟道气中的二氧化碳的吸收；可通过使低温流体通道中的富液和高温流体通道中的贫液同时经过换热器108，在换热器108内进行热交换，以有助于实现贫液中热量的回收、降低第一冷却器106的工作负担，节省能源。
本发明的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统相对于现有技术具有如下优点：(1)本发明能最大程度的回收二氧化碳和氮气，无三废产生；(2)利用化学法(溶剂吸收法)回收二氧化碳，二氧化碳再生塔的塔顶出气口中流出的气体中二氧化碳纯度高且回收率高；(3)化学法(溶剂吸收法)产生的塔顶放空气为富氮气体，氮气含量约在90～92％，且富氮气体较之采用PSA法实现烟道气中二氧化碳的分离时，气量更大。
优选，第一喷淋装置105a设置在二氧化碳吸收塔105的塔顶，第二喷淋装置110a设置在二氧化碳再生塔110的塔顶，富液出液口与换热器108的连接管路上设有富液泵107，贫液出液口与换热器108的连接管路上设有贫液 泵109。将第一喷淋装置105a设置在二氧化碳吸收塔105的塔顶有助于提高烟道气与吸收二氧化碳的溶剂的接触，提高化学法吸收二氧化碳的效率，进一步有助于提高烟道气中二氧化碳的回收效率；第二喷淋装置110a设置在二氧化碳再生塔110的塔顶，有助于提高富液中的二氧化碳解吸的效率；富液泵107和贫液泵109的设置则使得可方便的实现富液和贫液的转移，保障二氧化碳吸收塔105和二氧化碳再生塔110的正常运转，提高生产效率。
优选，二氧化碳化学法回收系统1还包括烟道气预处理系统，烟道气预处理系统包括引风机101、脱硫水洗塔103和第一气液分离器104；引风机101与脱硫水洗塔103的进气口相连，用于将烟道气输送至脱硫水洗塔103的进气口；脱硫水洗塔103的出气口与第一气液分离器104的进气口相连，脱硫水洗塔103用于对烟道气进行脱硫处理；第一气液分离器104的出气口与二氧化碳吸收塔105的进气口相连，第一气液分离器104用于对脱硫水洗塔103处理后的气体进行气液分离。烟道气预处理系统有助于预先去除烟道气中的硫化物，避免硫化物对后续二氧化碳的回收造成影响。
优选，脱硫水洗塔103的塔顶设有第三喷淋装置103a，脱硫水洗塔103的塔底设有脱硫液出液口，连通脱硫液出液口与第三喷淋装置103a的进液口的管道上设有脱硫液泵102。第三喷淋装置103a和脱硫液泵102的设置有助于改善脱硫的效果，并可方便的实现脱硫液的重复使用。
优选，二氧化碳化学法回收系统1还包括第二冷却器111和第二气液分离器112，第二冷却器111的进气口与二氧化碳再生塔110的出气口相连，第二冷却器111的出气口与第二气液分离器112的进气口相连，第二气液分离器112的出气口与二氧化碳精制液化系统2的进气口相连。第二冷却器111和第二气液分离器112的设置有助于对二氧化碳再生塔110的塔顶解吸气进行进一步除水，提高二氧化碳精制的效率。
优选，如图3所示，二氧化碳精制液化系统2包括二次脱硫系统、第三冷却器205、液化系统206和精馏塔207，二次脱硫系统的进气口与解吸气出气口相连(在二氧化碳化学法回收系统1包括第二冷却器111和第二气液分离器112的情况下，二次脱硫系统的进气口与第二气液分离器112的出气口相连)，二次脱硫系统的出气口与第三冷却器205的进气口相连，第三冷却器205的出气口与液化系统206的进气口相连，液化系统206的出液口与精 馏塔207相连。通过采用二氧化碳精制液化系统2中的二次脱硫系统、第三冷却器205、液化系统206和精馏塔207对解吸气中的二氧化碳进行进一步纯化，即可得到纯度更高的、满足要求的成品二氧化碳(体积浓度≥99.9％)。
优选，二氧化碳精制液化系统2还包括二氧化碳储罐208，二氧化碳储罐208与精馏塔207相连。通过设置二氧化碳储罐208可将精制得到的高纯度二氧化碳(体积浓度≥99.9％)储存于二氧化碳储罐208中，便于使用。
优选，二次脱硫系统包括第一缓冲罐201、第一压缩机202、脱硫床203和干燥床204，第一缓冲罐201的进气口与解吸气出气口相连(在二氧化碳化学法回收系统1包括第二冷却器111和第二气液分离器112的情况下，第一缓冲罐201的进气口与第二气液分离器112的出气口相连)，第一缓冲罐201的出气口与第一压缩机202的进气口相连，第一压缩机202的出气口与脱硫床203的进气口相连，脱硫床203的出气口与干燥床204的进气口相连，干燥床204的出气口与第三冷却器205的进气口相连。通过采用脱硫床203和干燥床204对二氧化碳再生塔110的解吸气进行进一步脱硫和干燥处理，进一步提高二氧化碳的纯度。第一压缩机202对二氧化碳解吸气压缩后(例如，可将解吸气压缩到2.5MPa)，进而便于通过脱硫床203和干燥床204对解析气进行脱硫和干燥。
优选，脱硫床203包括两个并联的脱硫塔，脱硫塔内设有脱硫吸附剂；干燥床204包括两个并联的干燥塔，干燥塔内设有干燥剂。
优选，如图4所示，氮气PSA浓缩提纯系统3包括除雾器301、第四冷却器302、第三气液分离器303、第二压缩机304、干燥器305、第二缓冲罐306和氮气吸附塔307(氮气吸附塔307内装填有用于纯化氮气的吸附剂，针对成分复杂的放空气，具有高的回收率)，除雾器301的进气口与二氧化碳吸收塔105的放空气出气口相连，除雾器301的出气口与第四冷却器302的进气口相连，第四冷却器302的出气口与第三气液分离器303的进气口相连，第三气液分离器303的出气口与第二压缩机304的进气口相连，第二压缩机304的出气口与干燥器305的进气口相连，干燥器305的出气口与第二缓冲罐306的进气口相连，第二缓冲罐306的出气口与氮气吸附塔307相连。经二氧化碳再生塔110处理后得到的解吸气依次进入除雾器301和第三气液分离器303，去除大颗粒游离水后，进入第二压缩机304，第二压缩机304出气 口接干燥器305进气口，经干燥器305干燥后，气体经第二缓冲罐306后再进入氮气吸附塔307，经变压吸附后，即可得到产品氮气(体积浓度可达99-99.999％)。氮气PSA浓缩提纯系统包括第二压缩机304，会有二次提压过程，能根据用户需要，选择压缩机及压缩压力，从而起到节能的目的。
优选，氮气PSA浓缩提纯系统3还包括氮气储罐308，氮气储罐308与氮气吸附塔307的塔顶出气口相连，便于对回收得到的氮气进行储存。
优选，氮气吸附塔307至少设有两个；两个以上氮气吸附塔307并联设置。
优选，采用两个氮气吸附塔307并联设置。
本发明的同步回收烟道气中二氧化碳和氮气的方法，采用如上所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统同步回收烟道气中二氧化碳和氮气。
优选，本发明的同步回收烟道气中二氧化碳和氮气的方法具体举例如下：
将本发明用于某煤电厂的烟道气的中二氧化碳、氮气回收。二氧化碳气体用于智慧农业的增收，氮气用于本厂化工车间的置换和吹扫。烟气成分如下表1所示：
表1
成分 二氧化硫 氮氧化物 一氧化碳 二氧化碳 氧气 水
实测值 20mg/m 3 31mg/m 3 未检出 13％ 6.20％ 12.50％
检出限 2mg/m 3 2mg/m 3 20mg/m 3 0.03％ —— ——
从脱硫脱硝后的烟气排放烟囱引出所需烟道气，进入脱硫水洗塔103进行脱硫除尘后，进入第一气液分离器104进行气液分离，然后进入二氧化碳吸收塔105，烟道气中的二氧化碳被溶剂吸收，溶剂形成富液，未被吸收的富氮气体(氮气含量90～92％)经二氧化碳吸收塔105塔顶的放空气出气口流出。
富液经富液泵107与贫液(富液在二氧化碳再生塔110中解吸除去二氧化碳后的液体)在换热器108中进行热量交换后，进入二氧化碳再生塔110(进入二氧化碳再生塔110内部的第二喷淋装置110a)，在塔底再沸器加热作用下，二氧化碳解吸，二氧化碳含量95％的粗二氧化碳气体(解吸气)从塔顶的解吸气出气口流出，经第二冷却器111和第二气液分离器112进一步 除水后，进入二氧化碳精制液化系统2。
富液在二氧化碳再生塔110解吸出二氧化碳后，塔底形成贫液，经贫液泵109，与富液在换热器108进行热量交换后，进入第一冷却器106(可选用水冷却器)进一步降温后，进入二氧化碳吸收塔105(进入二氧化碳吸收塔105内部的第一喷淋装置105a)，完成一个工作循环。
经第二冷却器111和第二气液分离器112冷却除水后得到的解吸气(含95％的粗二氧化碳气体)，经第一缓冲罐201后，进入第一压缩机202，提升压力至2.5MPa，然后进入脱硫床203和干燥床204进行脱硫除杂后，进入第三冷却器205降温后，进入液化系统206，降温至-18℃后得到液体状态的二氧化碳，液态二氧化碳进入精馏塔207精制提纯后，塔底即可得到纯度可达99.9％的食品级二氧化碳，进入二氧化碳储罐208进行储存。进一步地，精馏塔塔顶放空气还可作为脱硫床203和干燥床204的再生气源，节约产品气，降低能耗。
二氧化碳吸收塔105塔顶产出的放空气(富氮气体，氮气含量90～92％)，进入除雾器301、第四冷却器302和第三气液分离器303，去除游离水后进入第二压缩机304，提压至0.8～1.0MPa，经干燥器305干燥后进入第二缓冲罐306，再进入氮气吸附塔307变压吸附得到成品氮气，成品氮气进入氮气储罐308，氮气纯度从99％～99.999％不等。
本实施例中，烟道气中的碳氮分离采用化学吸收模式，二氧化碳回收效果好，可制得含量约为95％的二氧化碳，二氧化碳的回收率高；且放空气(二氧化碳吸收塔105的放空气)中氮气含量可达92％，远高于空气中的78％，是优质的氮气原料。氮气PSA浓缩提纯系统3，利用含氮92％的富氮气体作为原料气，采用二次压缩模式，将压力从3KPa提高至0.8～1.0MPa，充分回收压缩能，比起从空气中制取氮气，节能达20％以上。

Claims (10)

  1. 一种化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，其特征在于，包括二氧化碳化学法回收系统、二氧化碳精制液化系统和氮气PSA浓缩提纯系统；
    所述二氧化碳化学法回收系统包括二氧化碳吸收塔、二氧化碳再生塔、换热器和第一冷却器；
    所述二氧化碳吸收塔的塔顶设有放空气出气口，所述二氧化碳吸收塔的内部设有第一喷淋装置，所述二氧化碳吸收塔的塔底设有富液出液口，所述放空气出气口与所述氮气PSA浓缩提纯系统的进气口相连；
    所述二氧化碳再生塔的塔顶设有解吸气出气口，所述二氧化碳再生塔的内部设有第二喷淋装置，所述二氧化碳再生塔的塔底设有贫液出液口，所述解吸气出气口与所述二氧化碳精制液化系统的进液口相连；
    所述换热器具有高温流体通道和低温流体通道，所述富液出液口与所述低温流体通道的进液口相连，所述低温流体通道的出液口与所述第二喷淋装置的进液口相连；
    所述第一冷却器的出液口与所述第一喷淋装置的进液口相连，所述第一冷却器的进液口与所述高温流体通道的出液口相连，所述高温流体通道的进液口与所述贫液出液口相连。
  2. 如权利要求1所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，其特征在于，所述第一喷淋装置设置在所述二氧化碳吸收塔的塔顶，所述第二喷淋装置设置在所述二氧化碳再生塔的塔顶，所述富液出液口与所述换热器的连接管路上设有富液泵，所述贫液出液口与所述换热器的连接管路上设有贫液泵。
  3. 如权利要求1所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，其特征在于，所述二氧化碳化学法回收系统还包括烟道气预处理系统，所述烟道气预处理系统包括引风机、脱硫水洗塔和第一气液分离器；
    所述引风机与所述脱硫水洗塔的进气口相连，用于将烟道气输送至所述脱硫水洗塔的进气口；
    所述脱硫水洗塔的出气口与所述第一气液分离器的进气口相连，所述脱硫水洗塔用于对烟道气进行脱硫处理；
    所述第一气液分离器的出气口与所述二氧化碳吸收塔的进气口相连，所述第一气液分离器用于对所述脱硫水洗塔处理后的气体进行气液分离；
    所述脱硫水洗塔的塔顶设有第三喷淋装置，所述脱硫水洗塔的塔底设有脱硫液出液口，连通所述脱硫液出液口与所述第三喷淋装置的进液口的管道上设有脱硫液泵。
  4. 如权利要求1所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，其特征在于，所述二氧化碳化学法回收系统还包括第二冷却器和第二气液分离器，所述第二冷却器的进气口与所述二氧化碳再生塔的解吸气出气口相连，所述第二冷却器的出气口与所述第二气液分离器的进气口相连，所述第二气液分离器的出气口与所述二氧化碳精制液化系统的进气口相连。
  5. 如权利要求1所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，其特征在于，所述二氧化碳精制液化系统包括二次脱硫系统、第三冷却器、液化系统和精馏塔，所述二次脱硫系统的进气口与解吸气出气口相连，所述二次脱硫系统的出气口与所述第三冷却器的进气口相连，所述第三冷却器的出气口与所述液化系统的进气口相连，所述液化系统的出液口与所述精馏塔相连；
    所述二氧化碳精制液化系统还包括二氧化碳储罐，所述二氧化碳储罐与所述精馏塔相连。
  6. 如权利要求5所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，其特征在于，所述二次脱硫系统包括第一缓冲罐、第一压缩机、脱硫床和干燥床，所述第一缓冲罐的进气口与所述解吸气出气口相连，所述第一缓冲罐的出气口与所述第一压缩机的进气口相连，所述第一压缩机的出气口与所述脱硫床的进气口相连，所述脱硫床的出气口与所述干燥床的进气口相连，所述干燥床的出气口与所述第三冷却器的进气口相连；
    所述脱硫床包括两个并联的脱硫塔，所述脱硫塔内设有脱硫吸附剂；所 述干燥床包括两个并联的干燥塔，所述干燥塔内设有干燥剂。
  7. 如权利要求1所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，其特征在于，所述氮气PSA浓缩提纯系统包括除雾器、第四冷却器、第三气液分离器、第二压缩机、干燥器、第二缓冲罐和氮气吸附塔，所述除雾器的进气口与所述二氧化碳吸收塔的放空气出气口相连，所述除雾器的出气口与所述第四冷却器的进气口相连，所述第四冷却器的出气口与所述第三气液分离器的进气口相连，所述第三气液分离器的出气口与所述第二压缩机的进气口相连，所述第二压缩机的出气口与所述干燥器的进气口相连，所述干燥器的出气口与所述第二缓冲罐的进气口相连，所述第二缓冲罐的出气口与所述氮气吸附塔相连。
  8. 如权利要求1所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，其特征在于，所述氮气PSA浓缩提纯系统还包括氮气储罐，所述氮气储罐与所述氮气吸附塔的塔顶出气口相连。
  9. 如权利要求7或8任一所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统，其特征在于，所述氮气吸附塔至少设有两个；
    两个以上所述氮气吸附塔并联设置。
  10. 一种同步回收烟道气中二氧化碳和氮气的方法，其特征在于，采用如权利要求1-9中任意一项所述的化学法和PSA法同步回收烟道气中二氧化碳和氮气的系统同步回收烟道气中二氧化碳和氮气。
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