CN211585925U - Absorption system suitable for phase change absorbent absorbs CO2 in flue gas - Google Patents
Absorption system suitable for phase change absorbent absorbs CO2 in flue gas Download PDFInfo
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- CN211585925U CN211585925U CN201922123297.1U CN201922123297U CN211585925U CN 211585925 U CN211585925 U CN 211585925U CN 201922123297 U CN201922123297 U CN 201922123297U CN 211585925 U CN211585925 U CN 211585925U
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- 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
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- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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Abstract
The utility model relates to an absorption system suitable for CO2 in phase transition absorbent absorption flue gas, including first absorption tower, second absorption tower and phase splitter, two absorption towers all are equipped with the air inlet, the gas vent, absorbent import and solution outlet, the gas vent of air inlet intercommunication second absorption tower of first absorption tower, the solution outlet intercommunication phase splitter's of first absorption tower import, the rich liquid phase export of phase splitter communicates the absorbent import of second absorption tower, the solution outlet of second absorption tower communicates desorption apparatus's import, desorption apparatus's export communicates the absorbent import of first absorption tower, the barren liquid phase export of phase splitterThe absorbent inlet is communicated with the first absorption tower. The utility model is suitable for an adopt the phase transition absorbent to absorb CO in the flue gas2Can effectively improve CO in the flue gas2The absorption efficiency of the phase change absorbent and CO is realized2The mass transfer efficiency in the absorption tower is optimized, the cyclic utilization of the phase-change absorbent can be realized, and the CO is reduced2And (4) desorbing energy consumption of the pregnant solution.
Description
Technical Field
The utility model relates to a CO in absorption flue gas2Especially a system suitable for absorbing CO in flue gas by phase change absorbent2The absorption system of (1).
Background
In recent years, CO has become a cause of2The 'greenhouse effect' caused by the main greenhouse gas poses serious threat to the living environment of human beings, and at present, CO2Emission reduction has become a common human consensus. Carbon Capture and Storage (CCS) technology is a viable approach to control and curtail global Carbon dioxide emissions. Among CCS technologies, the chemical absorption method is the most mature technology due to its large absorption capacity, and is currently the most widely used CO2However, this technique always has a problem of excessively high regeneration energy consumption.
Researchers have proposed phases with high efficiency and low energy consumption in the last decadePhase change absorbents for absorbing CO2The former is homogeneous and absorbs CO2After-generation of liquid-liquid phase separation and absorption of CO2The lower liquid phase is concentrated, so that only the lower liquid phase needs to be sent into the desorption device, the liquid amount entering the desorption device is greatly reduced, the energy consumption of latent heat of evaporation and sensible heat of temperature rise can be effectively reduced, and the low-energy-consumption CO is realized2Trapping, and is expected to be applied to CO in flue gas of large-scale coal-fired power plants2And (4) trapping.
Unlike conventional absorbents, phase change absorbents are used to absorb CO2Phase separation occurs in the process, but at the moment, due to the influence of phase balance, the lower liquid phase after phase separation still does not reach the saturated absorption capacity and still has certain CO2Absorption capacity, high viscosity of lower liquid phase after phase separation, resulting in absorption agent and CO2The mass transfer coefficient is reduced, and the absorption rate is obviously reduced, so that the size of the absorption tower needs to be greatly increased during design, and the equipment investment is increased. On the other hand, in a predetermined absorption tower, the phase change absorbent undergoes phase separation, and the viscosity increases, and the absorption rate decreases, resulting in a large decrease in the throughput and a rapid increase in the running cost. Because the viscosity of the phase change absorbent is changed sharply before and after phase separation, and the mass transfer coefficient in the absorption tower is changed suddenly, different design requirements are required to be provided for the absorption tower before and after phase separation of the absorbent, so that the optimization of the mass transfer efficiency in the same absorption tower is difficult to realize.
Method for achieving CO compromise by adopting high-temperature absorption tower and low-temperature absorption tower2The technology of two key parameters of absorption capacity and viscosity of absorbent is provided, and the upper liquid phase after phase separation returns to the low-temperature absorption tower to continuously absorb CO2The viscosity of the absorbent is reduced by arranging a high-temperature tower, but the technology needs to arrange a heat exchanger between the two towers, and the investment cost is additionally increased. More importantly, the technology separates an upper liquid phase from a lower liquid phase when the absorbent is subjected to phase separation, so that the upper liquid continuously absorbs CO2. Of the phase change absorbents reported to date, one major class of phase change absorbents is in absorbing CO2After phase separation, the upper liquid phase has almost no absorption capacity any more, so the technological process can only play a role in the phase change absorbentBy further reducing the viscosity of the absorbent before absorption, but not for the lower liquid phase which has already separated phase and has further absorption capacity, the absorption capacity of the phase change absorbent cannot be increased. The technique has proposed the use of phase change absorbents to trap CO2However, the method has no practical effect on the main phase change absorbent, and does not really solve the problem of mass transfer efficiency reduction caused by the sharp increase of viscosity.
SUMMERY OF THE UTILITY MODEL
In order to overcome the above defects of the prior art, the utility model provides a phase change absorbent suitable for absorbing CO in flue gas2The absorption system can effectively improve CO in the flue gas2The absorption efficiency of the phase change absorbent and CO is realized2Optimizing the mass transfer efficiency in the absorption tower.
The utility model discloses realize above-mentioned purpose's technical scheme is: be applicable to phase transition absorbent and absorb CO in flue gas2The absorption system comprises a first absorption tower, a second absorption tower and a phase splitter, wherein the first absorption tower and the second absorption tower are respectively provided with an air inlet positioned at the bottom of the tower, an air outlet positioned at the top of the tower, an absorbent inlet positioned at the upper part of the tower and a solution outlet positioned at the lower part of the tower, the air inlet of the first absorption tower is communicated with the air outlet of the second absorption tower, the solution outlet of the first absorption tower is communicated with the inlet of the phase splitter, a rich liquid phase outlet of the phase splitter is communicated with the absorbent inlet of the second absorption tower, the air inlet of the second absorption tower is used as the air inlet of the absorption system and is used for accessing to-be-absorbed smoke, and the air outlet of the first absorption tower is used as the air outlet of the absorption system and is used for discharging the absorbed smoke.
Further, it also comprises CO2And a solution outlet of the second absorption tower is communicated with an inlet of the desorption device, a liquid phase outlet of the desorption device is communicated with an absorbent inlet of the first absorption tower, and a lean liquid phase outlet of the phase separator is communicated with an absorbent inlet of the first absorption tower.
Furthermore, an absorbent conveying pipeline communicated with the absorbent inlet of the first absorption tower is provided with a first conveying pump.
Furthermore, a second conveying pump is arranged on a conveying pipeline between the rich liquid phase outlet of the phase separator and the absorbent inlet of the second absorption tower.
The utility model has the advantages that:
1. the utility model discloses an absorption tower of difference utilizes phase transition absorbent and phase transition absorbent to absorb CO respectively2After CO2Rich solution relative to CO in flue gas2Compared with the traditional technology adopting a single absorption tower, the absorption can realize the phase change absorbent and CO2The mass transfer efficiency in the absorption tower is optimized, the condition that the mass transfer coefficient in the absorption tower is suddenly reduced due to the rapid change of the viscosity of the phase-change absorbent before and after phase splitting is avoided, and the effect of the phase-change absorbent on CO can be effectively improved2The absorption efficiency of (2) and (3) can also be realized2Rich liquid relative to CO2The absorption capacity is reused, the size of the absorption tower is not required to be changed, and the equipment investment and the operation cost are reduced.
2. The utility model can realize the alignment of CO2Desorbing the solution of the rich solution and CO2And the lean liquid phase is recycled, so that the recycling of the phase change absorbent is realized, the utilization efficiency of the phase change absorbent is improved, and the production cost is reduced.
3. The utility model only uses CO2Compared with the prior art, the method can effectively reduce the amount of the solution entering the desorption device and reduce the desorption energy consumption.
Drawings
Fig. 1 is a schematic structural view of an embodiment of the present invention;
fig. 2 is a schematic structural diagram of another embodiment of the present invention.
Detailed Description
The first embodiment is as follows: the embodiment is described with reference to fig. 1, and the embodiment is suitable for absorbing CO in flue gas by using a phase change absorbent2The absorption system comprises a first absorption tower 1, a second absorption tower 2 and a phase separator 3, wherein the first absorption tower and the second absorption tower are respectively provided with a gas inlet positioned at the bottom of the tower,A vent at the top of the column, an absorbent inlet at the upper part of the column and a solution outlet at the lower part of the column, containing CO2The flue gas enters the system from the gas inlet at the bottom of the second absorption tower, the phase-change absorbent enters the first absorption tower from the absorbent inlet at the upper part of the first absorption tower, the gas inlet of the first absorption tower is communicated with the gas outlet of the second absorption tower, so that the flue gas in the second absorption tower can enter the first absorption tower, the solution outlet of the first absorption tower is communicated with the inlet of the phase separator, and the phase separator is used for absorbing CO by the phase-change absorbent in the first absorption tower2The rich liquid phase outlet of the phase separator is communicated with the absorbent inlet of the second absorption tower and is used for separating the phase-separated CO2The rich liquid phase is sent to the second absorption tower to lead CO to be generated2The rich liquid phase is in countercurrent contact with the high-concentration flue gas entering from the tower bottom of the second absorption tower, and the CO in the flue gas is continuously absorbed2Generally, the lower liquid phase after the phase separation of the phase separator is a rich liquid phase.
The second embodiment is as follows: the embodiment is described with reference to fig. 2, and the phase change absorbent of the embodiment is suitable for absorbing CO in flue gas2The absorption system further comprises CO2A solution outlet of the second absorption tower is communicated with an inlet of the desorption device and is used for absorbing CO in the flue gas again2CO of2Rich solution is sent into the desorption device for desorption, an outlet of the desorption device is communicated with an absorbent inlet of the first absorption tower, a lean solution phase outlet of the phase separator is communicated with an absorbent inlet of the first absorption tower, and the lean solution phase outlet is used for separating the solution after desorption and the CO after phase separation2The lean liquid phase is sent into the first absorption tower for cyclic utilization and is continuously used for CO in the flue gas2Absorption is carried out, and in general, the upper liquid phase after the phase separation of the phase separator is a lean liquid phase. Solution after convenient resolution and CO after phase separation2And mixing the lean liquid phase and the lean liquid phase, namely feeding the lean liquid phase and the lean liquid phase into a mixing device to be mixed and return to a homogeneous phase, and then feeding the lean liquid phase and the homogeneous phase into the first absorption tower from an absorbent inlet of the first absorption tower. Other components and connections are the same as in the first embodiment.
The third concrete implementation mode: in the present embodiment, the first transfer pump 4 is installed in the absorbent transfer pipe communicating with the absorbent inlet of the first absorption tower of the present embodiment to facilitate the transfer of the phase change absorbent, as described with reference to fig. 1 and 2. Other components and connections are the same as in the first or second embodiment.
The fourth concrete implementation mode: referring to fig. 1 and 2, the second transfer pump 5 is installed on the transfer pipeline between the rich liquid phase outlet of the phase separator and the absorbent inlet of the second absorption tower, so as to facilitate CO2And (4) conveying a rich liquid phase. Other compositions and connection relationships are the same as in the first, second or third embodiment.
The utility model discloses a suitable delivery pump also can be installed to other pipeline to the transport of material in the pipeline.
The phase change absorbent is an absorbent of an amine-organic solvent-water system, and the phase change absorbent can be ethanolamine-N-propanol-water or N-methyldiethanolamine-N-butanol-water.
The viscosity of the phase change absorbent is preferably in the range of 2 to 10 mPas, such as 2 mPas, 5 mPas, 8 mPas or 10 mPas. CO after phase separation2The viscosity of the rich liquid phase is preferably in the range of 10 to 200 mPas, such as 10 mPas, 100 mPas, 150 mPas or 200 mPas.
Generally, the operating pressure of the first absorption tower and the operating pressure of the second absorption tower are both normal pressure, and the working temperature in the first absorption tower and the working temperature in the second absorption tower are both 30-60 ℃, such as 30 ℃, 40 ℃, 50 ℃ or 60 ℃.
The utility model discloses a theory of operation does: application of phase-change absorbent to CO in flue gas2Absorbing CO2The phase separation is carried out on the solution, and the CO after the phase separation2The rich liquid is continuously used for treating CO in the flue gas2Absorbing CO in the flue gas by using a phase change absorbent2And with CO2Rich liquid phase absorbing CO in flue gas2The process of (a) is carried out in different absorption columns. Then, the CO in the flue gas is absorbed again2CO of2Rich solution is carried outDesorption, the solution after desorption and CO after phase separation2Mixing the barren solution phase and recovering the homogeneous phase, and then continuously using the barren solution phase for CO in the flue gas2Absorption is carried out.
The utility model discloses a work flow does: containing CO2The flue gas enters the second absorption tower from the air inlet at the bottom end of the second absorption tower and then enters the first absorption tower, the phase-change absorbent enters the first absorption tower from the upper part of the first absorption tower, and the phase-change absorbent absorbs CO in the first absorption tower firstly2(phase Change absorbent with CO2Mass transfer occurs), the phase change absorbent absorbs CO2The phase separation is carried out on the solution at the bottom of the first absorption tower to separate the solution into CO2Rich liquid phase and CO2Lean liquid phase, high viscosity CO2The rich liquid phase is sent into the second absorption tower from the upper part of the second absorption tower and is in countercurrent contact with the high-concentration flue gas entering the second absorption tower from the bottom end of the second absorption tower, and the CO in the flue gas is continuously treated2Absorbing and absorbing CO in the flue gas again2CO of2The rich solution flows out from the lower part of the second absorption tower and is sent into a desorption device, and the solution after desorption and the CO after phase separation2The lean solution is mixed and recovered to be homogeneous, and then is sent into the first absorption tower from the upper part of the first absorption tower for cyclic utilization, and is continuously used for CO in the flue gas2Absorption is carried out.
The utility model discloses an absorption tower of difference utilizes phase transition absorbent and phase transition absorbent to absorb CO respectively2After CO2Rich solution relative to CO in flue gas2Compared with the traditional technology adopting a single absorption tower, the absorption can realize the phase change absorbent and CO2The mass transfer efficiency in the absorption tower is optimized, the condition that the mass transfer coefficient in the absorption tower is suddenly reduced due to the rapid change of the viscosity of the phase-change absorbent before and after phase splitting is avoided, and the effect of the phase-change absorbent on CO can be effectively improved2The absorption efficiency of (2) and (3) can also be realized2Rich liquid relative to CO2The absorption capacity is reused, the size of the absorption tower is not required to be changed, and the equipment investment and the operation cost are reduced. The utility model can realize the alignment of CO2Desorbing the rich solutionAnd CO2And the lean liquid phase is recycled, so that the recycling of the phase change absorbent is realized, the utilization efficiency of the phase change absorbent is improved, and the production cost is reduced. The utility model only uses CO2Compared with the prior art, the method can effectively reduce the amount of the solution entering the desorption device and reduce the desorption energy consumption.
Experimental example 1: 60 ℃ flue gas (CO)2Concentration 20vol.%) at 1.2 m3The flow rate of the phase-change absorbent A (with the initial viscosity of 7.7 mPas) is fed into the top of the first absorption tower through a first conveying pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, the lower liquid phase is sent to the top of a second absorption tower by a second delivery pump, and CO is absorbed in the second absorption tower2. For CO at the bottom of the second absorption tower2Sampling the rich solution, and measuring the viscosity to be 29 mPas, CO2The loading was 2.2mol/kg and the required absorption time was 4h in total.
Experimental example 2: 60 ℃ flue gas (CO)2Concentration 20vol.%) at 2.2m3The flow rate of the phase-change absorbent B (with the initial viscosity of 5.2 mPa · s) is fed into the top of the first absorption tower through a first transfer pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, the lower liquid phase is sent to the top of a second absorption tower by a second delivery pump, and CO is absorbed in the second absorption tower2. For CO at the bottom of the second absorption tower2Sampling the rich solution, and measuring the viscosity to be 77 mPas, CO2The loading was 2.8 mol/kg and the required absorption time was a total of 2.5 h.
Experimental example 3: 30 ℃ flue gas (CO)2Concentration 50vol.%) at 1.2 m3The flow rate of the phase-change absorbent A (with the initial viscosity of 7.7 mPas) is fed into the top of the first absorption tower through a first conveying pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, the lower liquid phase is sent to the top of a second absorption tower by a second delivery pump, and CO is absorbed in the second absorption tower2. For CO at the bottom of the second absorption tower2Sampling and measuring the rich solutionThe viscosity of the obtained product is 49 mPas, CO2The loading was 2.4mol/kg and the required absorption time was 4h in total.
Experimental example 4: 40 ℃ flue gas (pure CO)2) At 2.2m3The flow rate of the phase-change absorbent B (with the initial viscosity of 5.2 mPa · s) is fed into the top of the first absorption tower through a first transfer pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, the lower liquid phase is sent to the top of a second absorption tower by a second delivery pump, and CO is absorbed in the second absorption tower2. For CO at the bottom of the second absorption tower2Sampling the rich phase, and determining the viscosity to be 127 mPa & s, CO2The loading was 3.5mol/kg and the required absorption time was a total of 2.5 h.
As can be seen from various experimental examples, the technology of the invention is completely suitable for CO in flue gas2Absorption is carried out.
Comparative example 1 (conventional technical principle): 60 ℃ flue gas (CO)2Concentration 20vol.%) at 1.2 m3The flow rate of the phase change absorbent A is fed from the bottom of the second absorption tower, the phase change absorbent A (with the initial viscosity of 7.7 mPa · s) is sent to the top of the first absorption tower by a first delivery pump to circularly absorb CO2The flow rate is 20L/h, and the phase change absorbent absorbs CO after absorbing for 4h2Standing the solution for layering, taking off the liquid phase, and measuring CO2The loading was 1.4 mol/kg.
As can be seen from the comparison of Experimental example 1 with comparative example 1, CO is absorbed in the same period of time2Experimental example 1 can make CO2CO in rich solution2The load is increased from 1.4 mol/kg to 2.2mol/kg, and compared with the prior art, the technology of the invention has the advantage that CO is added2The absorption efficiency of (2) is greatly improved.
Comparative example 2: 60 ℃ flue gas (CO)2Concentration 20vol.%) at 1.2 m3The flow rate of the phase-change absorbent A (with the initial viscosity of 7.7 mPas) is fed into the top of the first absorption tower through a first conveying pump, and the flow rate is 20L/h. Absorption of CO by phase change absorbents2The solution passes through a phase separator, the loading capacity of the upper liquid phase is measured to be 0.2 mol/kg by sampling, and the upper liquid phase is pumped into the top of a first absorption tower for cyclic absorptionSampling for 5h to determine CO2The load was still 0.2 mol/kg.
Recycle of front and rear middle CO through upper liquid phase after phase separation in comparative example 22Comparison of loading capacity shows that the technology is suitable for the phase change absorbent (absorbing CO) of an amine-organic solvent-water system2The upper liquid phase of the split-phase solution does not have CO any more2Absorbent for absorbing capacity) of the flue gas2Absorption of (2).
Claims (4)
1. An absorption system suitable for absorbing CO2 in flue gas by using a phase change absorbent is characterized by comprising a first absorption tower, a second absorption tower and a phase splitter, wherein the first absorption tower and the second absorption tower are respectively provided with a gas inlet positioned at the bottom of the tower, a gas outlet positioned at the top of the tower, an absorbent inlet positioned at the upper part of the tower and a solution outlet positioned at the lower part of the tower, the gas inlet of the first absorption tower is communicated with the gas outlet of the second absorption tower, the solution outlet of the first absorption tower is communicated with the inlet of the phase splitter, a rich liquid phase outlet of the phase splitter is communicated with the absorbent inlet of the second absorption tower, the gas inlet of the second absorption tower is used as a gas inlet of the absorption system and is used for accessing to-be-absorbed flue gas, and the gas outlet of the first absorption tower is used as a gas outlet of the absorption system and is used for discharging the absorbed flue gas.
2. The absorption system for absorbing CO2 in flue gas by using phase change absorbent as claimed in claim 1, further comprising CO22And a solution outlet of the second absorption tower is communicated with an inlet of the desorption device, a liquid phase outlet of the desorption device is communicated with an absorbent inlet of the first absorption tower, and a lean liquid phase outlet of the phase separator is communicated with an absorbent inlet of the first absorption tower.
3. The absorption system for absorbing the CO2 in the flue gas by using the phase-change absorbent as claimed in claim 2, wherein the absorbent conveying pipeline communicated with the absorbent inlet of the first absorption tower is provided with a first conveying pump.
4. The absorption system for absorbing CO2 in flue gas by using phase-change absorbent as claimed in claim 3, wherein a second delivery pump is installed on the delivery pipeline between the rich liquid phase outlet of the phase separator and the absorbent inlet of the second absorption tower.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110960956A (en) * | 2019-12-02 | 2020-04-07 | 中国石油天然气集团有限公司 | Be applicable to phase transition absorbent and absorb CO in flue gas2Method and system |
| CN112691533A (en) * | 2021-03-23 | 2021-04-23 | 山东金宜善新材料有限公司 | Sodium sulfite absorption tower device |
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2019
- 2019-12-02 CN CN201922123297.1U patent/CN211585925U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110960956A (en) * | 2019-12-02 | 2020-04-07 | 中国石油天然气集团有限公司 | Be applicable to phase transition absorbent and absorb CO in flue gas2Method and system |
| CN110960956B (en) * | 2019-12-02 | 2023-12-29 | 中国石油天然气集团有限公司 | CO in flue gas is absorbed to applicable phase transition absorbent 2 Method and system of (2) |
| CN112691533A (en) * | 2021-03-23 | 2021-04-23 | 山东金宜善新材料有限公司 | Sodium sulfite absorption tower device |
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