CN111905567A - Method for regenerating ammonia water after capturing carbon dioxide by using ammonia water and capturing method - Google Patents

Method for regenerating ammonia water after capturing carbon dioxide by using ammonia water and capturing method Download PDF

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CN111905567A
CN111905567A CN201910378135.4A CN201910378135A CN111905567A CN 111905567 A CN111905567 A CN 111905567A CN 201910378135 A CN201910378135 A CN 201910378135A CN 111905567 A CN111905567 A CN 111905567A
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carbon dioxide
flash
stripping
gas
ammonia water
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汪上晓
霍安
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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
    • B01D53/96—Regeneration, reactivation or recycling of reactants
    • 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
    • B01D53/77—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
    • B01D2251/00—Reactants
    • B01D2251/20—Reductants
    • B01D2251/206—Ammonium compounds
    • B01D2251/2062—Ammonia
    • 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
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
    • Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
    • 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

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Abstract

The invention provides a method for regenerating ammonia water after capturing carbon dioxide by using ammonia water and a capturing method. The method for regenerating ammonia water after capturing carbon dioxide with ammonia water comprises the steps of providing an ammonia water regeneration system, performing a first flash evaporation step, performing a first compression step, performing a stripping step, performing a second flash evaporation step and performing a second compression step. The ammonia water regeneration system comprises a heat exchanger, a stripping tower, a second pump, a first flash evaporator, a first compressor, a second flash evaporator and a second compressor. Therefore, the first flash evaporator is arranged between the heat exchanger and the stripping tower, and the second flash evaporator replaces the traditional reboiler, so that the energy loss generated when the carbon dioxide is captured can be effectively reduced, and the aim of saving energy is fulfilled.

Description

Method for regenerating ammonia water after capturing carbon dioxide by using ammonia water and capturing method
Technical Field
The present invention relates to a method for capturing and regenerating carbon dioxide, and more particularly, to a method for capturing and regenerating carbon dioxide using ammonia water.
Background
Nowadays, about 85% of the energy of the industry is provided by fossil fuel, and in the coming decades, fossil fuel is still the main primary energy source, however, the large amount of exhaust gas generated by burning fossil fuel causes the concentration of carbon dioxide in the atmosphere to rise sharply, and the global environment is shifted because carbon dioxide is the main greenhouse gas.
In order to reduce the harm of carbon dioxide to the environment, a carbon dioxide capturing system has been developed, which is mainly divided into chemical/physical absorption, adsorption, low-temperature condensation, and membrane separation, wherein the chemical absorption method is currently the most common carbon dioxide capturing technology and is suitable for various power plants and petrochemical plants. However, although the carbon dioxide capture system can effectively remove carbon dioxide, the stripping column needs to be heated by a reboiler, which results in a large energy loss.
In view of the above, it is an objective of the related manufacturers to improve the carbon dioxide capture system and method to achieve the objectives of reducing carbon dioxide emission and capture cost.
Disclosure of Invention
An object of the present invention is to provide a method for regenerating ammonia water after capturing carbon dioxide with ammonia water and a method for capturing carbon dioxide with ammonia water, wherein a first flash evaporator is disposed between a heat exchanger and a stripping tower, and a second flash evaporator is used to replace a conventional reboiler, so as to effectively improve the capturing efficiency of carbon dioxide and reduce energy consumption.
An embodiment of the present invention provides a method for regenerating ammonia water after capturing carbon dioxide with ammonia water, which comprises providing an ammonia water regeneration system, performing a first flash evaporation step, performing a first compression step, performing a stripping step, performing a second flash evaporation step, and performing a second compression step. The ammonia water regeneration system comprises a heat exchanger, a stripping tower, a second pump, a first flash evaporator, a first compressor, a second flash evaporator and a second compressor, wherein the heat exchanger is used for carrying out heat exchange treatment on a rich solvent and a lean solvent and providing the rich solvent, the stripping tower is communicated with the heat exchanger, and the second pump is communicated with the heat exchanger through a first flow path. The first flash evaporator is communicated between a liquid inlet of the stripping tower and a liquid outlet of the heat exchanger, the first compressor is communicated between a gas outlet of the first flash evaporator and a first gas inlet of the stripping tower, the second flash evaporator is communicated between a liquid outlet of the stripping tower and a liquid inlet of the heat exchanger, and the second compressor is communicated between a gas outlet of the second flash evaporator and a second gas inlet of the stripping tower. The first flash step is to flash the rich solvent in a first flash vessel to form a first vapor and a first flash liquid. The first compression step compresses the first vapor via a first compressor and delivers it to the first gas inlet of the stripper column. The stripping step is stripping the first flash liquid with a first vapor in a stripper to produce a carbon dioxide stripping gas and a lean solvent. The second flashing step flashes the lean solvent in a second flash vessel to form a second vapor and a second flashed liquid. The second compression step compresses a second vapor via a second compressor and delivers the second vapor to a second gas inlet of the stripper column.
The method for regenerating aqueous ammonia after carbon dioxide capture with aqueous ammonia according to the previous embodiment, wherein the pressure of the stripping column may be greater than the pressure of the second flash vessel.
The method for regenerating aqueous ammonia after carbon dioxide capture with aqueous ammonia according to the previous embodiment, wherein the pressure of the stripping column may be 8.5 bar to 10.5 bar and the pressure of the second flash vessel may be 3.0 bar to 7.0 bar.
The method for regenerating ammonia water after carbon dioxide capture with ammonia water according to the foregoing embodiment, wherein the pressure of the second pump may be 2.5 bar to 5.0 bar.
The method for regenerating ammonia water after capturing carbon dioxide with ammonia water according to the foregoing embodiment, wherein the rich solvent may comprise carbon dioxide and ammonia water, and the molar ratio of carbon dioxide to ammonia water may be 0.10 to 0.41.
In the method for regenerating ammonia water after capturing carbon dioxide with ammonia water according to the foregoing embodiment, the ammonia water regeneration system may further include a condenser connected to a gas outlet of the stripping tower.
In the method for regenerating ammonia water after capturing carbon dioxide with ammonia water according to the foregoing embodiment, the ammonia water regeneration system may further include a third flash evaporator, which is in communication with the condenser.
The method for regenerating ammonia water after capturing carbon dioxide with ammonia water according to the foregoing embodiment may further include a condensing step of condensing the carbon dioxide stripping gas in the condenser to form a condensed carbon dioxide stripping gas.
The method for regenerating ammonia water after capturing carbon dioxide with ammonia water according to the foregoing embodiment may further include a third flash evaporation step of flashing the condensed carbon dioxide stripping gas in a third flash evaporator to form a carbon dioxide flash evaporation gas.
Another embodiment of the present invention provides a method for capturing carbon dioxide with ammonia, comprising providing a carbon dioxide capturing system, performing an absorption step, performing a first flash evaporation step, performing a first compression step, performing a stripping step, performing a second flash evaporation step, and performing a second compression step. The carbon dioxide capturing system comprises at least one carbon dioxide absorption tower, a stripping tower, a heat exchanger, a second pump, a first flash evaporator, a first compressor, a second flash evaporator and a second compressor, wherein the carbon dioxide absorption tower is provided with an absorbent, the stripping tower is communicated with a liquid outlet of the carbon dioxide absorption tower, the heat exchanger is communicated between the liquid outlet of the carbon dioxide absorption tower and a liquid inlet of the stripping tower through a first flow path and is communicated between a liquid outlet of the stripping tower and a reflux liquid inlet of the carbon dioxide absorption tower through a second flow path, and the second pump is communicated between the heat exchanger and the liquid outlet of the carbon dioxide absorption tower through the first flow path. The first flash evaporator is communicated between a liquid inlet of the stripping tower and a liquid outlet of the heat exchanger, the first compressor is communicated between a gas outlet of the first flash evaporator and a first gas inlet of the stripping tower, the second flash evaporator is communicated between a liquid outlet of the stripping tower and a liquid inlet of the heat exchanger, and the second compressor is communicated between a gas outlet of the second flash evaporator and a second gas inlet of the stripping tower. The absorption step is to perform a carbon dioxide absorption treatment on a carbon dioxide-containing gas in a carbon dioxide absorption tower by using an absorbent to form a rich solvent. The first flash step is to flash the rich solvent in a first flash vessel to form a first vapor and a first flash liquid. The first compression step compresses the first vapor via a first compressor and delivers it to the first gas inlet of the stripper column. The stripping step is stripping the first flash liquid with a first vapor in a stripper to produce a carbon dioxide stripping gas and a lean solvent. The second flashing step flashes the lean solvent in a second flash vessel to form a second vapor and a second flashed liquid. The second compression step compresses a second vapor via a second compressor and delivers the second vapor to a second gas inlet of the stripper column.
The method for capturing carbon dioxide with ammonia according to the foregoing embodiment, wherein the carbon dioxide-containing gas may be an exhaust gas, and the exhaust gas may contain 5 mole% to 30 mole% of carbon dioxide.
The method for capturing carbon dioxide with ammonia according to the foregoing embodiment, wherein the absorbent may comprise ammonia with a concentration of 3 mole% to 10 mole%.
The method for capturing carbon dioxide with ammonia according to the foregoing embodiment, wherein the rich solvent may comprise carbon dioxide and ammonia, and the molar ratio of carbon dioxide to ammonia may be 0.10 to 0.41.
The method for carbon dioxide capture with aqueous ammonia according to the previous embodiment, wherein the pressure of the stripping column may be greater than the pressure of the second flash vessel.
The process for carbon dioxide capture with aqueous ammonia according to the previous embodiment, wherein the pressure of the stripping column may be 8.5 bar to 10.5 bar and the pressure of the second flash vessel may be 3.0 bar to 7.0 bar.
The method for carbon dioxide capture with ammonia according to the previous embodiment, wherein the pressure of the second pump may be 2.5 bar to 5.0 bar.
In the method for capturing carbon dioxide with ammonia water according to the foregoing embodiment, when the number of the carbon dioxide absorption towers is plural, the carbon dioxide capturing system may include N carbon dioxide absorption towers, and N may be an integer greater than 1, wherein the N carbon dioxide absorption towers are connected in series in sequence.
In the method for capturing carbon dioxide with ammonia water according to the foregoing embodiments, the carbon dioxide capturing system may further include a first cooling portion and a second cooling portion. The first cooling part is communicated between a liquid outlet of a first carbon dioxide absorption tower in the N carbon dioxide absorption towers and a liquid inlet of an Nth carbon dioxide absorption tower. The second cooling unit is communicated between the heat exchanger and a reflux liquid inlet of the carbon dioxide absorption tower.
In the method for capturing carbon dioxide with ammonia according to the foregoing embodiment, the carbon dioxide capturing system may further include a condenser connected to a gas outlet of the stripping tower.
The method for capturing carbon dioxide with ammonia according to the foregoing embodiment, wherein the carbon dioxide capturing system may further include a third flash evaporator, which is in communication with the condenser.
The method for capturing carbon dioxide with ammonia water according to the foregoing embodiment may further include a condensation step of condensing the carbon dioxide stripping gas in the condenser to form a condensed carbon dioxide stripping gas.
The method for capturing carbon dioxide with ammonia according to the foregoing embodiment may further include a third flash step of flashing the condensed carbon dioxide stripping gas in a third flash vessel to form a carbon dioxide flash gas.
The method for capturing carbon dioxide with ammonia according to the foregoing embodiment may further include a heat exchange step of performing a heat exchange process between the rich solvent and the lean solvent in a heat exchanger.
Therefore, according to the method for regenerating ammonia water after capturing carbon dioxide by using ammonia water and the method for capturing carbon dioxide by using ammonia water, disclosed by the invention, the first flash evaporator and the first compressor are arranged between the heat exchanger and the stripping tower, and the second flash evaporator and the second compressor are used for replacing a traditional reboiler, so that the energy loss generated during capturing carbon dioxide can be effectively reduced, and the aim of saving energy is fulfilled.
Drawings
In order to make the aforementioned and other objects, features, and advantages of the invention, as well as others which will become apparent, reference is made to the following description taken in conjunction with the accompanying drawings in which:
FIG. 1 is a flow chart showing steps of a method for regenerating ammonia water after carbon dioxide capture with ammonia water according to an embodiment of the present invention;
FIG. 2 is a schematic view showing an ammonia regeneration system according to the embodiment of FIG. 1;
FIG. 3 is a flow chart showing steps of a method for carbon dioxide capture with ammonia according to another embodiment of the present invention; and
FIG. 4 is a schematic diagram illustrating a carbon dioxide capture system according to the embodiment of FIG. 3.
[ notation ] to show
100: method for regenerating ammonia water after capturing carbon dioxide by using ammonia water
110. 120, 130, 140, 150, 160: step (ii) of
200: ammonia water regeneration system
210. 410: heat exchanger
213. 413: first flow path
220. 420: stripping tower
230. 430: first flash evaporator
240. 440, a step of: first compressor
250. 450: second flash evaporator
260. 460: second compressor
270. 470: condenser
280. 480: third flash evaporator
211. 222, 252, 281, 411, 422, 452, 481, 512, 521: liquid outlet
221. 212, 412, 421, 522: liquid inlet
223. 423: a first gas inlet
224. 424: a second gas inlet
231. 225, 251, 282, 425, 431, 451, 482, 513, 524: gas outlet
300: method for capturing carbon dioxide by ammonia water
310. 320, 330, 340, 350, 360, 370: step (ii) of
400: carbon dioxide capture system
414: second flow path
500: carbon dioxide absorption tower
510: first carbon dioxide absorption tower
511: return liquid inlet
520: second carbon dioxide absorption tower
530: first cooling part
540: second cooling part
550: storage tank
514. 523: gas inlet
P41: first pump
P22, P42: second pump
P23, P43: third pump
P24, P44: fourth pump
Detailed Description
Embodiments of the present invention will be described below with reference to the accompanying drawings. For the purpose of clarity, numerous implementation details are set forth in the following description. However, the reader should understand that these implementation details should not be used to limit the invention. That is, in some embodiments of the invention, such implementation details are not necessary. In addition, for the sake of simplicity, some conventional structures and elements are shown in the drawings in a simple schematic manner; and repeated elements will likely be referred to using the same reference numerals.
Referring to fig. 1 and 2, fig. 1 is a flow chart illustrating steps of a method 100 for regenerating ammonia water after capturing carbon dioxide with ammonia water according to an embodiment of the invention, and fig. 2 is a schematic diagram illustrating an ammonia water regeneration system 200 according to the embodiment of fig. 1. The method 100 for regenerating ammonia water after capturing carbon dioxide with ammonia water includes step 110, step 120, step 130, step 140, step 150, and step 160.
Step 110 provides an ammonia regeneration system 200, as shown in fig. 2, the ammonia regeneration system 200 includes a heat exchanger 210, a stripping tower 220, a second pump P22, a first flash evaporator 230, a first compressor 240, a second flash evaporator 250, and a second compressor 260. In detail, the heat exchanger 210 is used for performing a heat exchange process between a rich solvent (rich solvent) and a lean solvent (lean solvent) and providing the rich solvent, the stripping column 220 is communicated with the heat exchanger 210, the second pump P22 is communicated with the heat exchanger 210 through a first flow path 213, the first flash evaporator 230 is communicated between a liquid inlet 221 of the stripping column 220 and a liquid outlet 211 of the heat exchanger 210, the first compressor 240 is communicated between a gas outlet 231 of the first flash evaporator 230 and a first gas inlet 223 of the stripping column 220, the second flash evaporator 250 is communicated between a liquid outlet 222 of the stripping column 220 and a liquid inlet 212 of the heat exchanger 210, and the second compressor 260 is communicated between a gas outlet 251 of the second flash evaporator 250 and a second gas inlet 224 of the stripping column 220.
Step 120 is a first flash step of flashing the rich solvent in the first flash vessel 230 to form a first vapor and a first flash liquid. In detail, the rich solvent may include carbon dioxide and ammonia, and the molar ratio of carbon dioxide to ammonia may be 0.10 to 0.41, which is a solvent with high carbon dioxide concentration, and the rich solvent is sent to the heat exchanger 210 via the second pump P22 on the first flow path 213 to be heated, and then enters the first flash evaporator 230 to perform the first flash process, the first flash liquid formed is sent to the liquid inlet 221 of the stripping tower 220 via a third pump P23, and the first vapor enters the first compressor 240 at the same time, wherein the pressure of the second pump P22 may be 2.5 bar to 5.0 bar.
Step 130 is a first compression step, wherein the first vapor is compressed by a first compressor 240 and sent to a first gas inlet 223 of the stripping column 220. Regeneration of the solvent may be assisted by performing the first flash step and the first compression step to deliver the first vapor and the first flash liquid to the stripping column 220.
Step 140 is a stripping step in which the first flash liquid is stripped with a first vapor in a stripping column 220 to produce a carbon dioxide stripping gas and a lean solvent. In detail, the first flash liquid after the first flash treatment is sent to the top of the stripping column 220, and the first vapor is sent to the bottom of the stripping column 220 after being compressed, and the carbon dioxide in the first flash liquid is converted from liquid phase to gas phase by using the first vapor as a heat source of the first flash liquid to form a carbon dioxide stripping gas, and the remaining first flash liquid is used to remove the carbon dioxide to form a lean solvent, wherein the lean solvent is a solvent with low carbon dioxide concentration.
Step 150 is a second flash step of flashing the lean solvent in a second flash vessel 250 to form a second vapor and a second flash liquid. In detail, the pressure of the stripping column 220 may be higher than that of the second flash vessel 250, so that the stripped lean solvent is subjected to a second flash process to a lower pressure via the second flash vessel 250, and a second flash liquid formed thereby flows out from a liquid outlet 252 of the second flash vessel 250 and is delivered to the liquid inlet 212 of the heat exchanger 210 by a fourth pump P24, while the second vapor simultaneously enters the second compressor 260. Wherein the pressure of the stripping column 220 may be 8.5 bar to 10.5 bar and the pressure of the second flash vessel 250 may be 3.0 bar to 7.0 bar.
Step 160 is a second compression step, wherein a second vapor is compressed by a second compressor 260 and delivered to the second gas inlet 224 of the stripper column 220. The second flashed liquid is sent to heat exchanger 210 for heat exchange by performing a second flashing step and a second compression step, and the second vapor is recompressed to stripper 220 via a second compressor.
The ammonia regeneration system 200 of the present invention may further comprise a condenser 270 connected to a gas outlet 225 of the stripping column 220. In detail, the method 100 for regenerating ammonia water after capturing carbon dioxide with ammonia water according to the present invention may further include a condensation step of condensing the carbon dioxide stripping gas from the stripping tower 220 in the condenser 270 to form a condensed carbon dioxide stripping gas. Thereby, moisture in the carbon dioxide stripping gas can be removed through condensation, and the condensed carbon dioxide stripping gas has little moisture content.
The ammonia regeneration system 200 of the present invention may further comprise a third flash vessel 280 in communication with the condenser 270. In detail, the method 100 for regenerating ammonia water after capturing carbon dioxide with ammonia water according to the present invention may further include a third flash evaporation step of subjecting the condensed carbon dioxide stripping gas from the condenser 270 to a third flash evaporation treatment in the third flash evaporator 280, so as to further remove excess water and form a carbon dioxide flash evaporation gas containing high concentration of carbon dioxide. A liquid outlet 281 of the third flash evaporator 280 is connected to the stripping tower 220, and moisture generated by the third flash evaporator 280 can be refluxed into the stripping tower 220, and carbon dioxide flash evaporation gas generated by the third flash evaporator 280 can be discharged from a gas outlet 282 of the third flash evaporator 280 for recycling.
Therefore, according to the method for regenerating the ammonia water after capturing the carbon dioxide by using the ammonia water, the carbon dioxide-rich solvent is flashed in the first flash evaporator through arranging the first flash evaporator and the first compressor between the heat exchanger and the stripping tower, and the compressed steam is transmitted into the stripping tower, so that the regeneration of the solvent can be assisted, and then the carbon dioxide-poor solvent stripped out from the stripping tower is flashed to a lower pressure in the second flash evaporator and is transmitted to the stripping tower through the compressed steam. The first flash evaporator can provide a heat source for heating the rich solvent in the stripping tower by using the steam after flash evaporation, and the second flash evaporator can replace the traditional reboiler, so that the energy loss generated is effectively reduced, and the aim of saving energy is fulfilled.
Referring to fig. 3 and 4, wherein fig. 3 is a flowchart illustrating steps of a method 300 for capturing carbon dioxide with ammonia according to another embodiment of the invention, and fig. 4 is a schematic diagram illustrating a carbon dioxide capturing system 400 according to the embodiment of fig. 3. The method 300 for capturing carbon dioxide with ammonia comprises steps 310, 320, 330, 340, 350, 360 and 370.
In step 310, a carbon dioxide capture system 400 is provided, as shown in fig. 4, the carbon dioxide capture system 400 includes at least a carbon dioxide absorption tower 500, a stripping tower 420, a heat exchanger 410, a second pump P42, a first flash evaporator 430, a first compressor 440, a second flash evaporator 450, and a second compressor 460.
In detail, in the embodiment shown in fig. 4, the carbon dioxide absorption tower 500 has an absorbent, and the number of the carbon dioxide absorption towers 500 is two, which are respectively a first carbon dioxide absorption tower 510 and a second carbon dioxide absorption tower 520, and the first carbon dioxide absorption tower 510 and the second carbon dioxide absorption tower 520 are connected in series, wherein the number of the carbon dioxide absorption towers 500 is not limited by the disclosure of the present invention. That is, the number of the carbon dioxide absorption towers 500 may be one or more, and when the number of the carbon dioxide absorption towers 500 is plural, the carbon dioxide capturing system 400 may include N carbon dioxide absorption towers 500, and N may be an integer greater than 1, wherein the N carbon dioxide absorption towers 500 are sequentially connected in series.
The stripping column 420 is connected to a liquid outlet 521 of the second carbon dioxide absorption column 520. The heat exchanger 410 is connected between a liquid outlet 521 of the second carbon dioxide absorption tower 520 and a liquid inlet 421 of the stripping tower 420 through a first flow path 413, and is connected between a liquid outlet 422 of the stripping tower 420 and a return liquid inlet 511 of the first carbon dioxide absorption tower 510 through a second flow path 414, and the second pump P42 is connected between the heat exchanger 410 and the liquid outlet 521 of the second carbon dioxide absorption tower 520 through the first flow path 413.
The first flash evaporator 430 is connected between the liquid inlet 421 of the stripping column 420 and a liquid outlet 411 of the heat exchanger 410, and the first compressor 440 is connected between a gas outlet 431 of the first flash evaporator 430 and a first gas inlet 423 of the stripping column 420. The second flash vessel 450 is coupled between the liquid outlet 422 of the stripping column 420 and a liquid inlet 412 of the heat exchanger 410, and the second compressor 460 is coupled between a gas outlet 451 of the second flash vessel 450 and a second gas inlet 424 of the stripping column 420.
Step 320 is an absorption step, in which the carbon dioxide absorption tower 500 uses an absorbent to absorb carbon dioxide into a carbon dioxide-containing gas to form a rich solvent and a gas after the carbon dioxide absorption treatment. Specifically, the carbon dioxide-containing gas is introduced into a gas inlet 514 of the first carbon dioxide absorption tower 510 and an absorbent to perform a carbon dioxide absorption treatment, wherein the absorbent may comprise ammonia water with a concentration of 3 mole% to 10 mole%, the carbon dioxide-containing gas may be an exhaust gas, and the exhaust gas may comprise carbon dioxide with a concentration of 5 mole% to 30 mole%. In addition, the rich solvent obtained by the carbon dioxide absorption treatment may contain carbon dioxide and ammonia, wherein the molar ratio of carbon dioxide to ammonia may be 0.10 to 0.41, which is a solvent of high carbon dioxide concentration.
In addition, the carbon dioxide capturing system 400 may further include a first cooling part 530, wherein the first cooling part 530 is connected between a liquid outlet of a first carbon dioxide absorption tower of the N carbon dioxide absorption towers 500 and a liquid inlet of an nth carbon dioxide absorption tower, and cools the rich solvent from the first carbon dioxide absorption tower through the first cooling part 530, and the cooled rich solvent is refluxed to the nth carbon dioxide absorption tower.
For example, in the embodiment of fig. 4, N is equal to 2, so that the first cooling part 530 is connected between a liquid outlet 512 of the first carbon dioxide absorption tower 510 and a liquid inlet 522 of the second carbon dioxide absorption tower 520, and after the carbon dioxide-containing gas is introduced into the first carbon dioxide absorption tower 510 and the absorbent is subjected to the carbon dioxide absorption treatment, the rich solvent from the first carbon dioxide absorption tower 510 can be guided to the first cooling part 530 by a first pump P41. The first cooling part 530 may cool the rich solvent from the first carbon dioxide absorption tower 510 and reflux the cooled rich solvent into the second carbon dioxide absorption tower 520 to continue the carbon dioxide absorption process.
The gas containing carbon dioxide gas that has been subjected to the carbon dioxide absorption treatment in the first carbon dioxide absorption tower 510 is introduced into the second carbon dioxide absorption tower 520 through a gas outlet 513 of the first carbon dioxide absorption tower 510 and a gas inlet 523 of the second carbon dioxide absorption tower 520 to be subjected to the carbon dioxide absorption treatment, and the gas subjected to the carbon dioxide absorption treatment is discharged through a gas outlet 524 of the second carbon dioxide absorption tower 520.
Step 330 is a first flash step of flashing the rich solvent in the first flash 430 to form a first vapor and a first flash liquid. In detail, the rich solvent flowing out from the liquid outlet 521 of the second carbon dioxide absorption tower 520 can be sent to the heat exchanger 410 by the second pump P42 on the first flow path 413, and then enters the first flash evaporator 430 for the first flash process, the formed first flash liquid is sent to the liquid inlet 421 of the stripping tower 420 by a third pump P43, and the first vapor enters the first compressor 440 at the same time, wherein the pressure of the second pump P42 can be 2.5 bar to 5.0 bar.
Step 340 is a first compression step, wherein the first vapor is compressed by a first compressor 440 and sent to the first gas inlet 423 of the stripping column 420. Regeneration of the solvent may be assisted by performing a first flash step and a first compression step to deliver the first vapor and the first flash liquid to the stripper 420.
Step 350 is a stripping step in which the first flash liquid is stripped with a first vapor in a stripper 420 to produce a carbon dioxide stripping gas and a lean solvent. Specifically, the first flash liquid after the first flash treatment is delivered to the top of the stripping column 420, and the first vapor is delivered to the bottom of the stripping column 420 after recompression, and the carbon dioxide in the first flash liquid is converted from liquid phase to gas phase by using the first vapor as a heat source of the first flash liquid to form a carbon dioxide stripping gas, and the remaining first flash liquid is a lean solvent formed by removing carbon dioxide, wherein the lean solvent is a solvent with low carbon dioxide concentration.
Step 360 is a second flash step of flashing the lean solvent in second flash vessel 450 to form a second vapor and a second flash liquid. In particular, the pressure of the stripping column 420 may be greater than the pressure of the second flash vessel 450, such that the stripped lean solvent undergoes a second flash process to a lower pressure via the second flash vessel 450, and the resulting second flashed liquid is passed through a fourth pump P44 to the liquid inlet 412 of the heat exchanger 410, while the second vapor simultaneously enters the second compressor 460. Wherein the pressure of the stripping column 420 may be 8.5 bar to 10.5 bar and the pressure of the second flash vessel 450 may be 3.0 bar to 7.0 bar.
Step 370 is a second compression step in which a second vapor is compressed via a second compressor 460 and delivered to a second gas inlet 424 of the stripper 420. The second flashed liquid is passed to heat exchanger 410 for heat exchange by performing a second flashing step and a second compression step, and the second vapor is recompressed to stripper 420 via a second compressor.
In addition, a liquid outlet 452 of the second flash vessel 450 may be connected to the reflux liquid inlet 511 of the first carbon dioxide absorption column 510 via the second flow path 414. Specifically, the second flash liquid after the second flash treatment may be returned from the second flash evaporator 450 to the first carbon dioxide absorption tower 510 by the fourth pump P44 provided in the second flow path 414.
The carbon dioxide capture system 400 of the present invention may further comprise a condenser 470 connected to a gas outlet 425 of the stripper 420. In detail, the method 300 for capturing carbon dioxide with ammonia according to the present invention may further comprise a condensation step of condensing the carbon dioxide stripping gas from the stripping tower 420 in the condenser 470 to form a condensed carbon dioxide stripping gas. Thereby, moisture in the carbon dioxide stripping gas can be removed through condensation, and the condensed carbon dioxide stripping gas has little moisture content.
The carbon dioxide capture system 400 of the present invention may further comprise a third flash vessel 480 in communication with the condenser 470. In detail, the method 300 for capturing carbon dioxide with ammonia according to the present invention may further include a third flash evaporation step of subjecting the condensed carbon dioxide stripping gas from the condenser 470 to a third flash evaporation treatment in the third flash evaporator 480, so as to further remove excess water and form a carbon dioxide flash evaporation gas containing high concentration of carbon dioxide. A liquid outlet 481 of the third flash evaporator 480 is communicated to the stripping tower 420, moisture generated by the third flash evaporator 480 can be refluxed into the stripping tower 420, and carbon dioxide flash evaporation gas generated by the third flash evaporator 480 can be discharged from a gas outlet 482 of the third flash evaporator 480 for recycling.
In addition, the method 300 for capturing carbon dioxide with ammonia according to the present invention may further include a heat exchange step, in which the rich solvent in the first flow path 413 is a cold fluid and the lean solvent in the second flow path 414 is a hot fluid, so that the rich solvent and the lean solvent can be heat exchanged in the heat exchanger 410, and after the heat exchange, the temperature of the rich solvent can be increased and the temperature of the lean solvent can be decreased.
The carbon dioxide capture system 400 of the present invention may further include a second cooling part 540 connected between the heat exchanger 410 and the reflux liquid inlet 511 of the first carbon dioxide absorption tower 510, whereby the second cooling part 540 can cool the lean solvent after the heat exchange treatment. In the embodiment of fig. 4, a storage tank 550 is disposed between the second cooling part 540 and the heat exchanger 410, and ammonia water is dissipated during the operation of the carbon dioxide capture system 400, and the storage tank 550 is disposed to compensate for the ammonia water in order to maintain the mass balance of the carbon dioxide capture system 400.
Therefore, according to the method for capturing carbon dioxide by using ammonia water, disclosed by the invention, the first flash evaporator and the first compressor are arranged between the heat exchanger and the stripping tower, the second flash evaporator and the second compressor are arranged to replace a traditional reboiler, the formed ammonia water regeneration system is formed, and the carbon dioxide absorption tower is matched and arranged, so that the energy loss can be greatly reduced, and the purposes of reducing the carbon dioxide emission and capturing cost are achieved.
< examples and comparative examples >
In embodiments 1 and 2 of the present invention, carbon dioxide in a carbon dioxide-containing gas is captured in steps 310 to 370 of the method 300 for capturing carbon dioxide with ammonia of fig. 3, and equivalent work (Wequiv), total work (Wt), and energy loss (EP%) are calculated respectively by using the formula (I), the formula (II), and the formula (III). The following are shown with respect to formula (I), formula (II) and formula (III):
Figure BDA0002052389190000121
Figure BDA0002052389190000122
Figure BDA0002052389190000123
wherein T is0Is 300K.
In example 1, the pressure of the stripping column was set to 10.5 bar, the pressure of the second flash evaporator was set to 6.6 bar, and the pressure of the second pump was set to 4.265 bar, and ammonia water having an absorbent concentration of 5.5 mole% was subjected to carbon dioxide absorption treatment with an absorbent and a carbon dioxide-containing gas to obtain a rich solvent. In the rich solvent, the molar ratio of carbon dioxide to ammonia water is 0.406, after the rich solvent is flashed by the first flash evaporator, the formed first steam and the first flash liquid are conveyed to a stripping tower for stripping treatment, and the lean solvent can be obtained. The molar ratio of carbon dioxide to aqueous ammonia was 0.25 after the lean solvent flash evaporated by the second flash evaporator, and the lean solvent contained aqueous ammonia at a concentration of 5.5 mole%. The results for example 1 are shown in table one.
Figure BDA0002052389190000131
In example 2, the pressure of the stripping column was set to 8.5 bar, the pressure of the second flash evaporator was set to 3.8 bar, and the pressure of the second pump was set to 3.0 bar, and ammonia water having an absorbent concentration of 10 mole% was subjected to carbon dioxide absorption treatment with an absorbent and a carbon dioxide-containing gas to obtain a rich solvent. In the rich solvent, the molar ratio of carbon dioxide to ammonia water is 0.396, after the rich solvent is flashed by the first flash evaporator, the formed first steam and the first flash liquid are transmitted to a stripping tower for stripping treatment, and the lean solvent can be obtained. The molar ratio of carbon dioxide to aqueous ammonia was 0.30 after the lean solvent flash evaporated by the second flash evaporator, and the lean solvent contained aqueous ammonia at a concentration of 10 mole%. The results for example 2 are shown in table two.
Figure BDA0002052389190000132
Figure BDA0002052389190000141
Comparative examples 1 and 2 of the present invention are different from examples 1 and 2 in that the first flash evaporator and the first compressor are removed and the second flash evaporator and the second compressor are changed to a reboiler in the carbon dioxide capturing system, and the remaining steps are the same as those of examples 1 and 2 to capture carbon dioxide in the carbon dioxide containing gas. The concentration of the absorbent, the pressure of the stripping tower, the molar ratio of carbon dioxide to ammonia water in the rich solvent, and the molar ratio of carbon dioxide to ammonia water in the lean solvent in comparative example 1 are the same as those in example 1, while the concentration of the absorbent, the pressure of the stripping tower, the molar ratio of carbon dioxide to ammonia water in the rich solvent, and the molar ratio of carbon dioxide to ammonia water in the lean solvent in comparative example 2 are the same as those in example 2, and details thereof are not repeated, and the results of comparative example 1 and comparative example 2 are shown in table three and table four, respectively.
Figure BDA0002052389190000142
Figure BDA0002052389190000143
Figure BDA0002052389190000151
Comparative examples 3 and 4 of the present invention are different from examples 1 and 2 in that the second flash evaporator and the second compressor are replaced with a reboiler in the carbon dioxide capturing system, and the remaining steps are the same as in examples 1 and 2 to capture carbon dioxide in the carbon dioxide-containing gas. The concentration of the absorbent, the pressure of the stripping tower, the molar ratio of carbon dioxide to ammonia water in the rich solvent, and the molar ratio of carbon dioxide to ammonia water in the lean solvent in comparative example 3 are all the same as those in example 1, but the pressure of the second pump is 6.19 bar, while the concentration of the absorbent, the pressure of the stripping tower, the molar ratio of carbon dioxide to ammonia water in the rich solvent, and the molar ratio of carbon dioxide to ammonia water in the lean solvent in comparative example 4 are all the same as those in example 2, but the pressure of the second pump is 4.31 bar, and details thereof are not repeated, and the results of comparative example 3 and comparative example 4 are shown in tables five and six, respectively.
Figure BDA0002052389190000152
Figure BDA0002052389190000153
Figure BDA0002052389190000161
Comparative examples 5 and 6 of the present invention are different from examples 1 and 2 in that the first flash vessel and the first compressor are removed in the carbon dioxide capturing system, and the remaining steps are the same as those of examples 1 and 2 to capture carbon dioxide in the carbon dioxide containing gas. The concentration of the absorbent, the pressure of the stripping column, the molar ratio of carbon dioxide to ammonia water in the rich solvent, and the molar ratio of carbon dioxide to ammonia water in the lean solvent in comparative example 5 were all the same as in example 1, but the pressure of the second flash evaporator was 3.904 bar, while the concentration of the absorbent, the pressure of the stripping column, the molar ratio of carbon dioxide to ammonia water in the rich solvent, and the molar ratio of carbon dioxide to ammonia water in the lean solvent in comparative example 6 were all the same as in example 2, but the pressure of the second flash evaporator was 3.22 bar, and details thereof are not repeated, and the results of comparative example 5 and comparative example 6 are shown in tables seven and eight, respectively.
Figure BDA0002052389190000162
Figure BDA0002052389190000163
Figure BDA0002052389190000171
As can be seen from the results in tables one to eight, the energy loss in examples 1 and 2 is less than that in comparative examples 1 to 6, and therefore, the carbon dioxide capture systems in examples 1 and 2 of the present invention can effectively reduce the energy loss by providing the first flash evaporator and the first compressor between the heat exchanger and the stripping column and using the second flash evaporator and the second compressor instead of the conventional reboiler.
In summary, the present invention provides a method for regenerating ammonia water after capturing carbon dioxide with ammonia water and a method for capturing carbon dioxide with ammonia water, which can effectively capture carbon dioxide in a carbon dioxide-containing gas, reduce energy loss generated when capturing carbon dioxide, and achieve the purpose of energy saving.
Although the present invention has been described with reference to the above embodiments, it should be understood that various changes and modifications can be made therein by those skilled in the art without departing from the spirit and scope of the invention.

Claims (23)

1. A method for regenerating ammonia water after capturing carbon dioxide with ammonia water, comprising:
providing an ammonia regeneration system, comprising:
a heat exchanger for heat exchanging a rich solvent with a lean solvent and providing the rich solvent;
a stripper in communication with the heat exchanger;
a second pump connected to the heat exchanger through a first flow path;
a first flash evaporator connected between a liquid inlet of the stripping tower and a liquid outlet of the heat exchanger;
a first compressor connected between a gas outlet of the first flash evaporator and a first gas inlet of the stripping tower;
a second flash evaporator communicated between a liquid outlet of the stripping tower and a liquid inlet of the heat exchanger; and
the second compressor is communicated between a gas outlet of the second flash evaporator and a second gas inlet of the stripping tower;
performing a first flash step of flashing the rich solvent in the first flash vessel to form a first vapor and a first flash liquid;
performing a first compression step in which the first vapor is compressed by the first compressor and delivered to the first gas inlet of the stripper column;
performing a stripping step in the stripper column to strip the first flash liquid with the first vapor to produce a carbon dioxide stripping gas and the lean solvent;
performing a second flash step of flashing the lean solvent in the second flash vessel to form a second vapor and a second flashed liquid; and
a second compression step is performed in which the second vapor is compressed via the second compressor and delivered to the second gas inlet of the stripper column.
2. The method of claim 1, wherein the pressure of the stripping column is greater than the pressure of the second flash vessel.
3. The method of claim 2, wherein the stripping column has a pressure of 8.5 bar to 10.5 bar and the second flash vessel has a pressure of 3.0 bar to 7.0 bar.
4. The method of claim 1, wherein the pressure of the second pump is 2.5 bar to 5.0 bar.
5. The method of claim 1, wherein the rich solvent comprises carbon dioxide and ammonia, and the molar ratio of carbon dioxide to ammonia is 0.10 to 0.41.
6. The method of claim 1, wherein the ammonia regeneration system further comprises a condenser connected to a gas outlet of the stripping column.
7. The method of claim 6, wherein the ammonia regeneration system further comprises a third flash evaporator in communication with the condenser.
8. The method for regenerating ammonia water after capturing carbon dioxide with ammonia water according to claim 7, further comprising:
a condensing step, condensing the carbon dioxide stripping gas in the condenser to form a condensed carbon dioxide stripping gas.
9. The method for regenerating ammonia water after capturing carbon dioxide with ammonia water according to claim 8, further comprising:
a third flash step of flashing the condensed carbon dioxide stripping gas in the third flash vessel to form a carbon dioxide flash gas.
10. A method for capturing carbon dioxide with ammonia water, comprising:
providing a carbon dioxide capture system comprising:
at least one carbon dioxide absorption tower with an absorbent;
a stripping tower connected to a liquid outlet of the at least one carbon dioxide absorption tower;
a heat exchanger, which is connected between the liquid outlet of the at least one carbon dioxide absorption tower and a liquid inlet of the stripping tower through a first flow path, and is connected between a liquid outlet of the stripping tower and a return liquid inlet of the at least one carbon dioxide absorption tower through a second flow path;
a second pump connected between the heat exchanger and the liquid outlet of the at least one carbon dioxide absorption tower through the first flow path;
a first flash evaporator connected between the liquid inlet of the stripping tower and a liquid outlet of the heat exchanger;
a first compressor connected between a gas outlet of the first flash evaporator and a first gas inlet of the stripping tower;
a second flash evaporator connected between the liquid outlet of the stripping tower and a liquid inlet of the heat exchanger; and
the second compressor is communicated between a gas outlet of the second flash evaporator and a second gas inlet of the stripping tower;
performing an absorption step of performing carbon dioxide absorption treatment on a carbon dioxide-containing gas in the at least one carbon dioxide absorption tower by using the absorbent to form a rich solvent;
performing a first flash step of flashing the rich solvent in the first flash vessel to form a first vapor and a first flash liquid;
performing a first compression step in which the first vapor is compressed by the first compressor and delivered to the first gas inlet of the stripper column;
performing a stripping step in the stripper column to strip the first flash liquid with the first vapor to produce a carbon dioxide stripping gas and a lean solvent;
performing a second flash step of flashing the lean solvent in the second flash vessel to form a second vapor and a second flashed liquid; and
a second compression step is performed in which the second vapor is compressed via the second compressor and delivered to the second gas inlet of the stripper column.
11. The method of claim 10, wherein the carbon dioxide-containing gas is an exhaust gas, and the exhaust gas contains 5 mole% to 30 mole% of carbon dioxide.
12. The method of claim 10, wherein the absorbent comprises ammonia at a concentration of 3 mole% to 10 mole%.
13. The method of claim 10, wherein the rich solvent comprises carbon dioxide and ammonia, and the molar ratio of carbon dioxide to ammonia is 0.10-0.41.
14. The method for carbon dioxide capture with aqueous ammonia of claim 10, wherein the pressure of the stripping column is greater than the pressure of the second flash vessel.
15. The process for carbon dioxide capture with aqueous ammonia of claim 14, wherein the pressure of the stripping column is 8.5 bar to 10.5 bar and the pressure of the second flash vessel is 3.0 bar to 7.0 bar.
16. The method of claim 10, wherein the pressure of the second pump is 2.5 bar to 5.0 bar.
17. The method of claim 10, wherein when the at least one carbon dioxide absorption tower is multiple in number, the carbon dioxide capture system comprises N carbon dioxide absorption towers, and N is an integer greater than 1, wherein the N carbon dioxide absorption towers are connected in series.
18. The method of claim 17, wherein the carbon dioxide capture system further comprises:
a first cooling part which is communicated between a liquid outlet of a first carbon dioxide absorption tower in the N carbon dioxide absorption towers and a liquid inlet of an Nth carbon dioxide absorption tower; and
a second cooling part, which is communicated between the heat exchanger and the reflux liquid inlet of the at least one carbon dioxide absorption tower.
19. The method of claim 10, wherein the carbon dioxide capture system further comprises a condenser connected to a gas outlet of the stripping column.
20. The method of claim 19, wherein the carbon dioxide capture system further comprises a third flash evaporator in communication with the condenser.
21. The method for capturing carbon dioxide with ammonia water according to claim 20, further comprising:
a condensing step, condensing the carbon dioxide stripping gas in the condenser to form a condensed carbon dioxide stripping gas.
22. The method for capturing carbon dioxide with ammonia water according to claim 21, further comprising:
a third flash step of flashing the condensed carbon dioxide stripping gas in the third flash vessel to form a carbon dioxide flash gas.
23. The method for capturing carbon dioxide with ammonia water according to claim 10, further comprising:
a heat exchange step of performing a heat exchange treatment on the rich solvent and the lean solvent in the heat exchanger.
CN201910378135.4A 2019-05-08 2019-05-08 Method for regenerating ammonia water after capturing carbon dioxide by using ammonia water and capturing method Pending CN111905567A (en)

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Citations (3)

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Publication number Priority date Publication date Assignee Title
US8080089B1 (en) * 2008-04-14 2011-12-20 Bechtel Power Corporation Method and apparatus for efficient gas treating system
CN102397740A (en) * 2010-09-13 2012-04-04 通用电气公司 Dehydration systems and methods for removing water from a gas
CN109304078A (en) * 2017-07-27 2019-02-05 汪上晓 Carbon dioxide capture system and method

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8080089B1 (en) * 2008-04-14 2011-12-20 Bechtel Power Corporation Method and apparatus for efficient gas treating system
CN102397740A (en) * 2010-09-13 2012-04-04 通用电气公司 Dehydration systems and methods for removing water from a gas
CN109304078A (en) * 2017-07-27 2019-02-05 汪上晓 Carbon dioxide capture system and method

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Application publication date: 20201110