CN115671993A - Carbon dioxide capturing and storing system based on compression enthalpy increase and interstage energy utilization - Google Patents
Carbon dioxide capturing and storing system based on compression enthalpy increase and interstage energy utilization Download PDFInfo
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Abstract
The invention relates to a carbon dioxide capturing and storing system, which comprises an absorption tower and CO 2 Absorption liquid regeneration circulation unit and CO 2 Separation storage unit, compression enthalpy-increasing heat exchange unit, and interstage energy utilization unit, whichMiddle CO 2 The absorption liquid regeneration circulating unit comprises a rich liquid pipeline, a regeneration tower and a lean liquid pipeline which are sequentially and circularly communicated with the absorption tower; CO 2 2 The separation and storage unit comprises a gas-liquid separator and CO sequentially connected with the regeneration tower 2 Transport pipe, CO 2 Liquefier, CO 2 A liquid storage tank; the compression enthalpy-increasing heat exchange unit comprises a compression air inlet pipe, a first compressor, a first heat exchange pipe of a regeneration tower kettle and a regeneration tower feeding preheating pipeline which are sequentially communicated; the interstage energy utilization unit comprises a second heat exchanger used for realizing heat exchange between the lean solution pipeline and the rich solution pipeline, and a third heat exchanger used for realizing heat exchange between the regeneration tower feeding preheating pipeline and the rich solution pipeline. Compared with the prior art, the invention avoids heat waste by compression enthalpy increase and cascade heat recycling, reduces the temperature required by heat exchange and reduces energy consumption.
Description
Technical Field
The invention belongs to the technical field of capture and storage of carbon dioxide in ship tail gas, and relates to a carbon dioxide capture and storage system based on compression enthalpy increase and interstage energy utilization, in particular to a ship carbon dioxide capture and storage system based on compression enthalpy increase and interstage energy cascade utilization.
Background
Global warming is a problem to be solved urgently, and after the industrial revolution, CO in the air 2 The rapid increase of the concentration causes various countries to put forward the target of 'carbon emission reduction'. Then, china continuously sets up relevant policies, the CCUS technology is definitely proposed to be the important planning and key development technology for future national development, and the targets of 'carbon peak reaching' in 2030 years and 'carbon neutralization' in 2060 years are expected to be reached.
Transportation is a fundamental, precedent, strategic industry and an important service industry in national economy, is one of important fields of carbon emission, and 90 percent of global trade is finished by marine transportationAnd (4) obtaining the finished product. At present, fossil fuels remain the main power source for the transportation industry, and CO generated by marine transportation is generated annually 2 The emission is about 10 hundred million tons, and accounts for 3 percent of the global greenhouse gas emission. Meanwhile, with the advance of the aim of carbon reduction and the development of the technology of carbon capture, downstream industrial chains such as carbon flooding and carbon scavenging are gradually formed. If CO can be realized 2 The method has the advantages of solving the climate problem, improving the yield of oil, gas and other energy sources, along with obvious environmental protection significance and economic benefit.
A ship carbon dioxide capturing and storing device comprises an absorption tower, a regeneration tower, a lean liquid pipeline and a rich liquid pipeline, wherein the absorption tower and the regeneration tower are connected in series through the lean liquid pipeline and the rich liquid pipeline to form an absorption liquid circulation loop, the lean liquid pipeline is connected with a lean liquid outlet of the regeneration tower and a lean liquid inlet of the absorption tower, and the rich liquid pipeline is connected with a rich liquid outlet of the absorption tower and a rich liquid inlet of the regeneration tower. The system is also provided with a primary heat exchanger, a cold side flow path of the heat exchanger is connected in series with the rich liquid pipeline, and a hot side flow path of the heat exchanger is connected in series with the lean liquid pipeline, but the heat exchanger only carries out simple primary heat exchange and cannot fully recycle heat in the system. Meanwhile, a reboiler is usually arranged at the bottom of the regeneration tower, and supplies heat to the rich solution again through external heat supply to achieve the purpose of high desorption rate. Therefore, the system is not sufficient in utilization of heat exchange quantity in circulation, and heat is provided for desorption of the rich liquid through a reboiler, namely the system is high in energy consumption.
In order to reduce the energy consumption required by the system, the design aims of high efficiency, green, low energy consumption and compactness are taken as design targets, the heat in the circulation can be fully utilized through multistage heat exchange, heat exchange and heat storage can be carried out on high-temperature ship tail gas, automatic adjustment can be carried out when the heat is insufficient, and the heat required by the regeneration tower can be stably supplied.
Disclosure of Invention
The invention aims to provide a method based on compression enthalpy increase and interstageEnergy-utilizing ship CO 2 The capture and storage system realizes stable heat source supply of the ship carbon capture system, solves the problem of high energy consumption of the ship carbon dioxide capture and storage system, and maximally utilizes ship waste heat.
The purpose of the invention can be realized by the following technical scheme:
a carbon dioxide capture and storage system comprising
An absorption tower for enriching CO in the gas to be treated by the absorption liquid 2 ；
CO 2 The absorption liquid regeneration circulating unit comprises a rich liquid pipeline, a regeneration tower and a lean liquid pipeline which are sequentially communicated with the absorption tower in a circulating manner along the flowing direction of the absorption liquid;
CO 2 the separation and storage unit comprises a gas-liquid separator in circulating communication with the top of the regeneration tower and CO sequentially connected with the gas-liquid separator 2 Transport pipe, CO 2 Liquefier, CO 2 A liquid storage tank;
the compression enthalpy-increasing heat exchange unit comprises a compression air inlet pipe communicated with an air source, and a first compressor, a first heat exchange pipe of a tower kettle of the regeneration tower and a feed preheating pipeline of the regeneration tower which are sequentially communicated with the compression air inlet pipe; and
the interstage energy utilization unit comprises a second heat exchanger and a third heat exchanger, wherein a first hot side flow path of the second heat exchanger is connected in series on the lean solution pipeline, and a cold side flow path of the second heat exchanger is connected in series on the rich solution pipeline; and a hot side flow path of the third heat exchanger is connected in series on a regeneration tower feeding preheating pipeline, and a cold side flow path is connected in series on a rich solution pipeline.
In the invention, the heat exchange between the absorbed low-temperature rich liquid and the regenerated high-temperature lean liquid and the heat exchange between the compressed high-temperature carbon dioxide flowing out of the tower kettle of the regeneration tower and the low-temperature rich liquid are realized through the second heat exchanger and the third heat exchanger, so that the secondary heat exchange in the system is realized.
Further, the system also comprises a refrigerant circulation loop, and the refrigerant is circulatedThe circuit comprises a refrigerant flow direction and a CO 2 The second compressor and the throttle valve are communicated with the liquefier in a circulating manner;
and the second hot side flow path of the second heat exchanger is arranged between the second compressor and the throttle valve in series.
The system further comprises a phase change energy storage regeneration heat source unit, wherein the phase change energy storage regeneration heat source unit comprises a first heat exchanger, a heat reservoir, a second heat exchange tube and a third liquid pump, the first heat exchanger is communicated with a cold side flow path and a gas phase inlet of the absorption tower, and the heat reservoir, the second heat exchange tube and the third liquid pump are circularly communicated with a hot side flow path of the first heat exchanger.
Further, the heat reservoir is a tubular heat exchanger filled with (E) -3-m-tolylbutan-2-enoic acid (mTBEA) (the phase transition temperature is 382.9 +/-0.5K). The phase change material includes, but is not limited to, a high temperature phase change material of 350 ℃ to 400 ℃, but it should be noted that any phase change material suitable for heat recovery of ship tail gas is covered in the protection scope of the present invention.
Furthermore, the phase change energy storage regeneration heat source unit further comprises a heat storage bypass pipeline connected with the heat reservoir in parallel, and an electromagnetic valve arranged on the heat storage bypass pipeline.
Furthermore, a desulfurizer is also arranged between the first heat exchanger and the gas-phase inlet of the absorption tower.
Furthermore, a fourth heat exchanger is arranged on the rich liquid pipeline between the second heat exchanger and the absorption liquid inlet of the absorption tower;
and a hot side flow path of the fourth heat exchanger is connected in series on the rich liquid pipeline, and a cold side flow path is communicated with cooling water.
Furthermore, a second liquid pump is arranged between the gas-liquid separator and a liquid inlet at the top of the regeneration tower.
Furthermore, the gas source is a gas-liquid separator, and the inlet end of the compression gas inlet pipe and the outlet end of the regeneration tower feeding preheating pipeline are respectively connected with the CO 2 The delivery pipes are communicated to make
A compression air inlet pipe, a first compressor, a first heat exchange pipe of a tower kettle of the regeneration tower and a feed preheating pipeline of the regeneration tower pass through CO 2 The conveying pipes are circularly communicated.
Further, said CO 2 The delivery pipe is also provided with a one-way valve which is positioned between the inlet end of the compression air inlet pipe and the outlet end of the regeneration tower feeding preheating pipeline.
The invention utilizes the first compressor to bypass partial CO 2 The gas is compressed to increase enthalpy, and further the heat supply to the regeneration tower and the preheating of the inlet rich liquid are realized. However, it should be noted that this scheme is for CO 2 The gas is fully utilized, and the compressed gas is not limited to CO for the design scheme of a pipeline which does not adopt circulating communication 2 Any gas suitable for increasing enthalpy of compression is intended to be within the scope of the present invention.
Compared with the prior art, the invention has the following characteristics:
1) The heat reservoir adopted by the invention is filled with a high-performance phase-change material suitable for heat recovery of ship tail gas. The phase-change material is used as a latent heat material capable of storing a large amount of heat at a specific temperature, so that the heat input into the regeneration tower through the heat reservoir is maintained at a stable value under the condition of insufficient heat exchange amount, and the desorption rate of the regeneration tower is improved.
2) The invention is characterized in that a bypass pipe is connected to the front section of the inlet of the heat reservoir. As the phase change heat storage is a passive heat storage mode, the situation of heat storage and heat release can not be realized, once the phase change material of the heat reservoir is completely changed in phase, the heat after passing through the first heat exchanger is directly led into the regeneration tower through the bypass pipe, and the energy regulation is realized while the overhaul is convenient.
3) The invention adopts a heat recovery mode of interstage energy cascade utilization. Preheating the low-temperature rich liquid flowing out of the absorption tower through the second heat exchanger and the third heat exchanger respectively, wherein the preheating heat of the second heat exchanger comes from the first-stage heat exchange of the high-temperature barren liquid flowing out of the regeneration tower and the condensation heat released by the refrigeration cycle loop respectively, and the preheating heat of the third heat exchanger comes from CO after compression and enthalpy increase 2 A gas. The cascade heat recycling mode not only avoids heat waste, but also reduces the temperature required by heat exchange and reduces energy consumption.
4) The invention separates partial CO 2 And bypassing the gas to compress and increase enthalpy. CO separated by a separator 2 The gas is still high-temperature gas, and the energy consumption required by direct liquefaction is larger, so that the invention bypasses part of the gas, compresses and increases enthalpy, and introduces the gas into the regeneration tower for heat exchange, so that CO in the rich liquid 2 The separation rate is improved, and meanwhile, the heat exchange between the second stage and the rich solution can be realized again as interstage energy utilization.
Drawings
FIG. 1 is a schematic diagram of a carbon dioxide capture and storage system according to an embodiment;
the symbols in the figure illustrate:
1-first heat exchanger, 2-desulfurizer, 3-absorption tower, 4-heat reservoir, 5-electromagnetic valve, 6-regeneration tower, 7-second heat exchanger, 8-third heat exchanger, 9-first liquid pump, 10-fourth heat exchanger, 11-gas-liquid separator, 12-second liquid pump, 13-first compressor, 14-one-way valve, 15-CO 2 The system comprises a liquefier, 16-a second compressor, 17-a throttle valve, 18-a liquid storage tank, 19-a third liquid pump, 20-a lean solution pipeline, 21-a rich solution pipeline, 22-a heat storage bypass pipeline and 23-a regeneration tower feeding preheating pipeline.
Detailed Description
The invention is described in detail below with reference to the figures and the specific embodiments. The present embodiment is implemented on the premise of the technical solution of the present invention, and a detailed implementation manner and a specific operation process are given, but the scope of the present invention is not limited to the following embodiments.
Example 1:
a carbon dioxide capture and storage system as shown in FIG. 1 comprises an absorption tower 3, CO 2 Absorption liquid regeneration circulation unit and CO 2 A separation storage unit and a stable regeneration heat source unit based on phase change energy storage.
Wherein the absorption tower 3 is used for enriching CO in the carbon-containing high-temperature ship tail gas through absorption liquid 2 。CO 2 The absorption liquid regeneration circulating unit comprises a rich liquid pipeline 21, a regeneration tower 6, a lean liquid pipeline 20 and a lean liquid pipeline 2, wherein the rich liquid pipeline 21, the regeneration tower 6 and the lean liquid pipeline 20 are sequentially and circularly communicated with the absorption tower 3 along the flowing direction of the absorption liquid0, first liquid pump 9.
CO 2 The separation and storage unit comprises a gas-liquid separator 11 and a second liquid pump 12 which are sequentially and circularly communicated with the top of the regeneration tower 6, and CO which is sequentially connected with the gas-liquid separator 11 2 Transport pipe, CO 2 Liquefier 15, CO 2 A reservoir 18. Wherein, CO 2 The liquefier 15 is embodied as a condenser.
A compression enthalpy-increasing heat exchange unit which comprises a heat exchanger arranged in the CO 2 Check valve 14 on the delivery pipe, and along the CO 2 The first compressor 13, the first heat exchange tube at the bottom of the regeneration tower and the feed preheating pipeline 23 of the regeneration tower are sequentially communicated with the one-way valve 14 in the flowing direction.
The interstage energy utilization unit comprises a second heat exchanger 7, a third heat exchanger 8 and a refrigerant circulation loop, wherein a first hot side flow path of the second heat exchanger 7 is connected in series on a lean liquid pipeline 20, and a cold side flow path is connected in series on a rich liquid pipeline 21; the hot side flow path of the third heat exchanger 8 is connected in series with the regeneration tower feed preheating pipeline 23, and the cold side flow path is connected in series with the rich liquid pipeline 21. The refrigerant circulation circuit comprises a refrigerant circulating loop and a CO circulating loop in sequence along the flowing direction of the refrigerant 2 A second compressor 16 and a throttle valve 17 in circulation communication with the liquefier 15; the second hot-side flow path of the second heat exchanger 7 is provided in series between the second compressor 16 and the throttle valve 17.
The phase change energy storage regeneration heat source unit comprises a first heat exchanger 1, a heat reservoir 4, a regeneration tower kettle second heat exchange tube, a third liquid pump 19, a heat storage bypass pipeline 22 and an electromagnetic valve 5, wherein the cold side flow path of the first heat exchanger 1 is communicated with a gas phase inlet of the absorption tower 3, the heat reservoir 4 is circularly communicated with the hot side flow path of the first heat exchanger 1, the heat storage bypass pipeline 22 is connected with the heat reservoir 4 in parallel, and the electromagnetic valve 5 is arranged on the heat storage bypass pipeline 22. Specifically, the gas inlet end of a gas channel of the first heat exchanger 1 is connected with carbon-containing high-temperature ship tail gas, and the inlet and the outlet of a liquid channel are respectively connected with the inlet of the heat reservoir 4 and the outlet of the third liquid pump 19; the heat reservoir 4 is a tube heat exchanger filled with (E) -3-m-tolylbut-2-enoic acid. Compare in the plate heat exchanger that heat transfer coefficient is high, the tubular heat exchanger that this embodiment adopted can compensate plate heat exchanger heat transfer passageway little for cause the problem of jam when phase change material does not liquefy completely easily. In some preferred embodiments, a desulfurizer 2 is further arranged between the first heat exchanger 1 and the gas-phase inlet of the absorption tower 3, the desulfurizer 2 is connected in series on the gas pipeline of the first heat exchanger 1, and the outlet of the desulfurizer is connected with the gas inlet of the absorption tower 3.
In some preferred embodiments, a fourth heat exchanger 10 is further disposed on the rich liquid pipeline 21 between the second heat exchanger 7 and the absorption liquid inlet of the absorption tower 3; the hot side flow path of the fourth heat exchanger 10 is connected in series to the rich liquid pipeline 21, and the cold side flow path is communicated with the cooling seawater.
The carbon-containing high-temperature ship tail gas is firstly cooled through the first heat exchanger 1, then enters the desulfurizer 2 for desulfurization, then is secondarily cooled through the fourth heat exchanger 10, enters from a gas inlet at the bottom of the absorption tower 3, is sprayed with absorption liquid to remove carbon dioxide in the absorption tower, and then is decarbonized low-temperature ship tail gas is obtained from the top of the absorption tower 3.
The lean solution pipeline 20 is communicated with a lean solution outlet of the regeneration tower 6 and a lean solution inlet of the absorption tower 3 through a first liquid pump 9, and is used as absorption solution for spraying and absorbing carbon dioxide in the tower. The rich liquid pipeline 21 is connected with a rich liquid outlet of the absorption tower 3 and a rich liquid inlet of the regeneration tower 6 after two heat exchanges of the second heat exchanger 7 and the third heat exchanger 8 in sequence for regeneration of the absorption liquid, and the CO is further removed through a gas-liquid separator 11 at the top of the regeneration tower 6 2 . CO removal 2 By CO 2 Conveying the CO into the pipe 2 After the condensation and liquefaction of the liquefier 15, CO is introduced 2 The reservoir 18 stores.
In the liquefaction process, the used refrigerant can obtain high temperature through the second compressor 16, the refrigerant exchanges heat with the rich liquid pipeline 21 through the second hot side flow path of the second heat exchanger 7 to complete the first stage of interstage energy utilization, and then the flowing refrigerant is changed into low temperature again through the throttle valve 17 and returns to CO 2 Liquefier 15 and high temperature CO 2 The gas is liquefied by heat exchange.
Before liquefaction, the compression enthalpy-increasing heat exchange unit can split CO flowing out of the gas-liquid separator 11 2 The gas is subjected to enthalpy increase by a first compressor 13 and then is introduced into a tower kettle 6 of the regeneration tower for heat exchange, so that CO is increased 2 The desorption rate; high-temperature CO flowing out of 6 tower kettles of regeneration tower 2 The gas passes through the hot side of the third heat exchanger 8 and the cold side of the third heat exchanger 8And (4) exchanging heat with the low-temperature rich liquid to finish the second stage of interstage energy utilization. Wherein the one-way valve 14 is connected in series between the gas-liquid separator 11 and the CO 2 Between liquefiers 15, for preventing CO 2 The gas escapes in a reverse direction at high yield.
When carbon-containing high-temperature ship tail gas passes through the first heat exchanger 1, the high-temperature ship tail gas and a circulating liquid medium are as follows: any liquid suitable for heat exchange of ship tail gas such as water, oil and the like is subjected to heat exchange, the temperature of the ship tail gas is reduced, the subsequent absorption rate is improved, and meanwhile, the exchanged heat can be supplied to the regeneration tower 6 through a circulating medium through the heat reservoir 4.
Meanwhile, the present embodiment further includes a heat storage bypass pipe 22 connected in parallel with the heat reservoir 4, and an electromagnetic valve 5 disposed on the heat storage bypass pipe 22. Whether the heat storage bypass pipeline 22 bypasses heat entering the heat reservoir 4 or not is controlled through the electromagnetic valve 5, after phase change materials in the heat reservoir 4 completely change phase, the electromagnetic valve 5 is connected with a temperature sensor, the electromagnetic valve 5 is automatically opened when the temperature is higher than the phase change temperature by 1 ℃, heat is directly introduced into a right heat exchange pipe of the regeneration tower 6 through the first heat exchanger 1, and on the contrary, when the phase change materials in the heat reservoir 4 do not completely change phase or heat of ship tail gas is insufficient, namely the temperature perception of the temperature sensor is smaller than or equal to the phase change temperature, the electromagnetic valve 5 is automatically closed, heat storage is carried out on the heat reservoir 4, or stable heat supply to the regeneration tower 6 is ensured by utilizing the heat of the heat reservoir 4.
That is, in this embodiment, two pairs of tower bottom heat exchange pipes are designed at the bottom of the regeneration tower 6 to provide the heat required for rich liquid desorption, and the heat of the left tower bottom heat exchange pipe in the figure is increased by compressing the enthalpy-increased CO 2 The gas is provided, and the heat of the heat exchange pipeline of the right tower bottom is provided by the heat exchange medium heated by the tail gas in the first heat exchanger 1 and the heat reservoir 4. By fully utilizing the heat released in the tail gas precooling process and compressing the CO after enthalpy is increased 2 The heat of the gas, thereby reducing the use of external heat sources and lowering the cost under the condition of ensuring the regeneration effect of the regeneration tower 6.
Example 2:
FIG. 1 shows a ship CO based on compression enthalpy increase and interstage energy utilization 2 The trapping and storage system includes: stable regeneration heat source unit and CO based on phase change energy storage 2 Absorption liquid circulation circuit and CO 2 The memory cells are separated.
Wherein, stable form regeneration heat source unit based on phase transition energy storage includes: a first heat exchanger 1, a heat reservoir 4 and a third liquid pump 19. Specifically, the first heat exchanger 1 is a gas-liquid heat exchanger, and heat exchange is performed between the high-temperature ship tail gas and a circulating liquid medium (such as water, oil and any liquid suitable for heat exchange of the ship tail gas), so that the temperature of the ship tail gas is reduced, the subsequent absorption rate is improved, and the exchanged heat can be supplied to the regeneration tower 6 by the circulating medium.
The heat reservoir 4 is filled with a high-performance phase-change material suitable for recovering heat of ship tail gas, the phase-change material can store a large amount of heat at a stable temperature by using latent heat of self height, and stable heat supply to the regeneration tower 6 can be guaranteed under the condition that the input of a ship tail gas heat source is unstable. The high-performance phase change material includes, but is not limited to, high-temperature phase change materials at 350 ℃ to 400 ℃, such as: mTBEA.
The third liquid pump 19 connects the outlet of the heat reservoir 4 and the inlet of the first heat exchanger 1 to pump the circulating liquid.
CO 2 The absorption liquid circulation circuit includes: the system comprises an absorption tower 3, a regeneration tower 6, a second heat exchanger 7, a third heat exchanger 8, a first liquid pump 9, a lean liquid pipeline 20 and a rich liquid pipeline 21. The lean solution pipeline 20 is connected with a bottom lean solution outlet of the regeneration tower 6 and a top side lean solution inlet of the absorption tower 3, and is respectively connected with the first liquid pump 9, a first hot side flow path of the second heat exchanger 7 and a hot side flow path of the fourth heat exchanger 10 in series along the lean solution flowing direction. The rich liquid pipeline 21 is connected with a rich liquid outlet at the bottom of the absorption tower 3 and a rich liquid inlet at the top side of the regeneration tower 6, and a cold side flow path of the first heat exchanger 7 and a cold side flow path of the second heat exchanger 8 are respectively connected in series along the flow direction of the rich liquid in sequence. To this end, CO 2 The absorption liquid forms a loop circulation.
Introducing the ship tail gas subjected to heat exchange and desulfurization into the absorption tower 3 from the bottom side, discharging the ship tail gas from the top outlet, and spraying the CO in the absorption tower 3 from the top side to the bottom side 2 Absorbing the barren liquor to fully react. RegenerationTwo heat exchange pipelines are arranged at the lower part of the tower 6 to provide heat required by rich liquid desorption, and the heat of the left heat exchange tube in the figure is increased by compressing CO after enthalpy is increased 2 Gas is supplied, heat of the heat exchange tube at the right side is supplied by a liquid pipeline in the first heat exchanger 1 and the heat reservoir 4, and CO obtained after desorption is released from the outlet at the top part 2 A gas.
CO 2 The separation storage unit includes: gas-liquid separator 11, first compressor 13, CO 2 A liquefier 15 and a tank 18. The inlet of the gas-liquid separator 11 is connected with CO released by the regeneration tower 6 2 Gas outlet, but desorbed CO 2 The gas is mixed with high-temperature evaporated water vapor and a small amount of mixture of alcohol amine solution and ionic liquid, a liquid outlet at the bottom of the gas-liquid separator 11 is connected with a second liquid pump 12, the separated liquid is input into the regeneration tower 6 again, the loss of absorption liquid in the circulation process is avoided, and the cavitation erosion of the subsequent first compressor 13 is prevented. The first compressor 13 utilizes compression enthalpy increasing technology to split CO 2 The gas is compressed and heated, and then is introduced into the heat exchange tube on the left side in the figure of the regeneration tower 6, and the gas after heat exchange still has higher temperature, so that a flow path on the hot side which can be introduced into the third heat exchanger 8 is used for secondary preheating of the rich liquid tube. CO 2 2 CO to be divided at the inlet of the liquefier 15 2 The gases are recombined for liquefaction, liquefied CO 2 The liquid enters the liquid storage tank 18 for sealed preservation.
In some preferred embodiments, ship CO based on compression enthalpy increase and interstage energy utilization 2 The trap and store system further includes a refrigerant circulation system including: CO 2 2 A liquefier 15, a second compressor 16, a second heat exchanger 7 and a throttle valve 17. Refrigerants include, but are not limited to, CO 2 The high-temperature refrigerant liquid after heat exchange is output as high-temperature high-pressure gas through the second compressor 16, the high-temperature high-pressure gas and rich liquid are subjected to first-stage heat exchange to be changed into high-temperature liquid, and the high-temperature high-pressure gas and rich liquid are changed into low-temperature liquid through the throttle valve 17 and finally are mixed with high-temperature CO to form high-temperature high-pressure gas 2 The gas is subjected to heat exchange to achieve the purpose of liquefying the gas.
It should be noted that the second heat exchanger 7, the third heat exchanger 8 and the third heat exchangeThe device 8 and the heat exchange tube in the regeneration tower 6 jointly form cascade utilization heat exchange of energy between two stages. A first hot side flow path of the second heat exchanger 7 is connected in series on the lean liquid pipeline 20, a second hot side flow path of the second heat exchanger 7 is connected in series on a circulating loop of the refrigerant, a cold side flow path of the second heat exchanger 7 is connected in series on the rich liquid pipeline 21, and the second heat exchanger 7 provides first-stage preheating for the rich liquid; the hot side flow path of the third heat exchanger 8 is connected in series with CO after the heat exchange tube at the left side of the regeneration tower 2 And on the gas pipeline, a cold side flow path of the third heat exchanger 8 is connected in series on the rich liquid pipeline 21, and the third heat exchanger 8 provides a second stage of preheating for the rich liquid, so that the second heat exchanger 7 and the third heat exchanger 8 form first stage inter-stage energy cascade utilization. The left heat exchange tube in the regeneration tower 6 is connected in series between the hot side flow path of the third heat exchanger 8 and the first compressor 13, and the high temperature after compression and enthalpy increase is used for providing heat absorption capacity for the regeneration tower 6, namely CO after compression and enthalpy increase 2 The first-stage heat release of the gas; the gas passing through the left heat exchange tube in the regeneration tower 6 still has higher temperature, so the hot side flow path which can be introduced into the third heat exchanger 8 is used for secondary preheating for the rich liquid tube, namely CO after compression and enthalpy increase 2 The second-stage heat release of the gas, so that the third heat exchanger 8 and the left heat exchange tube in the regeneration tower 6 form second-stage energy cascade utilization.
In addition, ship CO based on compression enthalpy increase and interstage energy utilization 2 The capturing and storing system also comprises a desulfurization system 2, the desulfurization system 2 is connected between the first heat exchanger 1 and the absorption tower 3 in series to realize the sulfide absorption of the ship tail gas, improve the carbon content of the tail gas introduced into the absorption tower 3 and ensure the CO 2 Absorption rate.
In some preferred embodiments, marine CO based on compressed enthalpy increase and interstage energy utilization 2 The collecting and storing system further comprises a heat storage bypass pipeline 22 and an electromagnetic valve 5, the electromagnetic valve 5 is used for controlling whether the heat storage bypass pipeline 22 bypasses heat entering the heat reservoir 4 or not, when the phase change material in the heat reservoir 4 is completely changed in phase, the electromagnetic valve 5 is connected with a temperature sensor, when the temperature is higher than the phase change temperature by 1 ℃, the electromagnetic valve 5 is automatically opened, the heat is directly introduced into a right heat exchange pipe of the regeneration tower 6 through the first heat exchanger 1, and conversely, when the phase change material in the heat reservoir 4 is not completely changed in phaseOr when the heat supply of the ship tail gas is insufficient, namely the temperature sensing of the temperature sensor is less than or equal to the phase change temperature, the electromagnetic valve 5 is automatically closed to store heat for the heat reservoir 4, or the heat of the heat reservoir 4 is utilized to ensure the stable heat supply for the regeneration tower 6.
In some preferred embodiments, ship CO based on compression enthalpy increase and interstage energy utilization 2 The trapping and storing system further comprises a fourth heat exchanger 10, a hot side flow path of the fourth heat exchanger 10 is connected in series on the lean solution pipeline 20, seawater is introduced into a cold side flow path of the fourth heat exchanger to fully cool the lean solution, energy consumption is reduced, and meanwhile, anti-corrosion spraying of a cooling water pipe needs to be done.
In some preferred embodiments, marine CO based on compressed enthalpy increase and interstage energy utilization 2 The capture and storage system further comprises a one-way valve 14 connected in series between the gas-liquid separator 11 and the CO 2 CO between liquefiers 15 2 On gas pipes, i.e. CO in pipes 2 The gas flow is large, and the one-way valve 14 can ensure CO 2 The gas escapes in reverse direction.
The embodiments described above are intended to facilitate a person of ordinary skill in the art in understanding and using the invention. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make improvements and modifications within the scope of the present invention based on the disclosure of the present invention.
Claims (10)
1. A carbon dioxide capture and storage system, comprising
An absorption tower (3) for enriching CO in the gas to be treated by the absorption liquid 2 ；
CO 2 The absorption liquid regeneration circulating unit comprises a rich liquid pipeline (21), a regeneration tower (6) and a lean liquid pipeline (20) which are sequentially and circularly communicated with the absorption tower (3) along the flowing direction of the absorption liquid;
CO 2 a separation and storage unit which comprises a gas-liquid separator (11) circularly communicated with the top of the regeneration tower (6) and CO sequentially connected with the gas-liquid separator (11) 2 Transport pipe, CO 2 Liquefier (15), CO 2 A liquid storage tank (18);
the compression enthalpy-increasing heat exchange unit comprises a compression air inlet pipe communicated with an air source, and a first compressor (13), a first heat exchange pipe of a tower kettle of the regeneration tower and a feed preheating pipeline (23) of the regeneration tower which are sequentially communicated with the compression air inlet pipe; and
the interstage energy utilization unit comprises a second heat exchanger (7) and a third heat exchanger (8), wherein a first hot side flow path of the second heat exchanger (7) is connected to the lean liquid pipeline (20) in series, and a cold side flow path is connected to the rich liquid pipeline (21) in series; and a hot side flow path of the third heat exchanger (8) is connected in series with a regeneration tower feeding preheating pipeline (23), and a cold side flow path is connected in series with a rich liquid pipeline (21).
2. The carbon dioxide capture and storage system of claim 1, further comprising a refrigerant circulation loop comprising CO in series with the refrigerant flow direction 2 A second compressor (16) and a throttle valve (17) which are communicated with the liquefier (15) in a circulating way;
and the second hot side flow path of the second heat exchanger (7) is arranged between the second compressor (16) and the throttle valve (17) in series.
3. A carbon dioxide capture and storage system according to claim 1, characterized in that the system further comprises a phase change energy storage regenerative heat source unit comprising a first heat exchanger (1) having a cold side flow path in communication with the gas phase inlet of the absorption tower (3), and a heat reservoir (4), a second heat exchange tube of the regeneration tower kettle, and a third liquid pump (19) in circulating communication with a hot side flow path of the first heat exchanger (1).
4. Carbon dioxide capture and storage system according to claim 3, wherein the heat reservoir (4) is a tubular heat exchanger filled internally with (E) -3-m-tolylbut-2-enoic acid.
5. The carbon dioxide capture and storage system according to claim 3, wherein the phase change energy storage regenerative heat source unit further comprises a heat storage bypass line (22) connected in parallel with the heat reservoir (4), and a solenoid valve (5) disposed on the heat storage bypass line (22).
6. A carbon dioxide capture and storage system according to claim 3, characterized in that a desulfurizer (2) is further provided between the first heat exchanger (1) and the gas phase inlet of the absorption column (3).
7. A carbon dioxide capture and storage system according to claim 1, characterized in that a fourth heat exchanger (10) is provided in the rich liquid conduit (21) between the second heat exchanger (7) and the absorption liquid inlet of the absorption tower (3);
and a hot side flow path of the fourth heat exchanger (10) is serially connected to the rich liquid pipeline (21), and a cold side flow path is communicated with cooling water.
8. A carbon dioxide capture and storage system according to claim 1, characterized in that a second liquid pump (12) is provided between the gas-liquid separator (11) and the regeneration tower top liquid inlet.
9. A carbon dioxide capture and storage system according to claim 1, wherein the gas source is a gas-liquid separator (11), and the inlet end of the compressed gas inlet pipe, the outlet end of the regeneration column feed preheat conduit (23) and the CO are respectively connected to the inlet end of the compressed gas inlet pipe and the outlet end of the regeneration column feed preheat conduit (23) 2 The delivery pipes are communicated so that
A compression air inlet pipe, a first compressor (13), a first heat exchange pipe at the tower bottom of the regeneration tower and a feed preheating pipeline (23) of the regeneration tower pass through CO 2 The conveying pipes are circularly communicated.
10. A carbon dioxide capture and storage system according to claim 9, wherein the CO is 2 The delivery pipe is also provided withAnd the check valve (14), wherein the check valve (14) is positioned between the inlet end of the compression air inlet pipe and the outlet end of the regeneration tower feeding preheating pipeline (23).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116697385A (en) * | 2023-03-24 | 2023-09-05 | 中国电建集团江西省电力设计院有限公司 | Carbon emission reduction and energy storage system for thermal power plant |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN116697385A (en) * | 2023-03-24 | 2023-09-05 | 中国电建集团江西省电力设计院有限公司 | Carbon emission reduction and energy storage system for thermal power plant |
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