CN219231933U - 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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- CN219231933U CN219231933U CN202222652388.6U CN202222652388U CN219231933U CN 219231933 U CN219231933 U CN 219231933U CN 202222652388 U CN202222652388 U CN 202222652388U CN 219231933 U CN219231933 U CN 219231933U
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Abstract
The utility model relates to a ship carbon dioxide capturing and storing system based on compression enthalpy increase and interstage energy cascade utilization, which comprises an absorption tower and CO 2 An absorption liquid regeneration circulation unit, a rich liquid pipeline, a regeneration tower and a lean liquid pipeline; CO 2 And (3) separating the storage units: also comprises a gas-liquid separator and CO 2 Conveying pipe and CO 2 Liquefier, CO 2 A liquid storage tank; compression enthalpy-increasing heat exchange unit: comprises a compression air inlet pipe, a first compressor, a first heat exchange pipe at the bottom of a regeneration tower and a feeding preheating pipeline of the regeneration tower which are communicated in sequence; an interstage energy utilization unit: the device comprises a second heat exchanger for realizing heat exchange between a lean liquid pipeline and a rich liquid pipeline, and a third heat exchanger for realizing heat exchange between a feed preheating pipeline of the regeneration tower and the rich liquid pipeline. Compared with the prior art, the heat waste is avoided by compressing the enthalpy-increasing and gradient heat recycling modes, and the temperature required by heat exchange is reduced.
Description
Technical Field
The utility model belongs to the technical field of carbon dioxide trapping and storage in ship tail gas, relates to a carbon dioxide trapping and storage system based on compression enthalpy and interstage energy utilization, and particularly relates to a ship carbon dioxide trapping and storage system based on compression enthalpy and interstage energy cascade utilization.
Background
If CO is enabled 2 The device can solve the climate problem, improve the output of oil, gas and other energy sources, and has obvious environmental protection significance and economic benefit.
The utility model provides a boats and ships carbon dioxide entrapment and storage device contains absorption tower, regeneration tower, lean liquor pipeline and rich liquor pipeline, lean liquor pipeline with rich liquor pipeline will the absorption tower with the regeneration tower is established ties, forms absorption liquid circulation loop, lean liquor pipeline connects the lean liquor export of regeneration tower with the lean liquor entry of absorption tower, rich liquor pipeline connects the rich liquor export of absorption tower with the rich liquor entry of regeneration tower. The system is also provided with a primary heat exchanger, wherein 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, so that heat in the system cannot be fully recycled. Meanwhile, a reboiler is usually arranged at the bottom of the regeneration tower, and the reboiler supplies heat for the rich liquid again through external heat supply so as to achieve the purpose of high desorption rate. Therefore, the heat exchange amount in the circulation is not fully utilized by the system, and heat is provided for desorption of the rich liquid through the reboiler, namely the energy consumption of the system is high.
In order to reduce the energy consumption required by the system, the system is designed with high efficiency, green, low energy consumption and compact practicality, the heat in the circulation can be fully utilized through multistage heat exchange, and the heat exchange and heat storage can be carried out on the tail gas of the high-temperature ship, so that the automatic regulation can be carried out when the heat is insufficient, and the heat required by the regeneration tower is stably supplied.
Disclosure of Invention
The utility model aims to provide a ship CO based on compression enthalpy increase and interstage energy utilization 2 The trapping and storing system is used for realizing stable heat source supply of the ship carbon trapping system, solving the problem of high energy consumption of the ship carbon dioxide trapping and storing system and maximizing the utilization of ship waste heat.
The aim of the utility model can be achieved 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 circulation 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 way along the flowing direction of the absorption liquid;
CO 2 the separation storage unit comprises a gas-liquid separator which is circularly communicated with the top of the regeneration tower and CO which is sequentially connected with the gas-liquid separator 2 Conveying pipe and 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, a first compressor, a first heat exchange pipe of a tower kettle of a regeneration tower and a feeding preheating pipeline of the regeneration tower, wherein the first compressor, the first heat exchange pipe of the tower kettle of the regeneration tower and the feeding preheating pipeline 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 with the lean liquid pipeline, and a cold side flow path of the second heat exchanger is connected in series with the rich liquid pipeline; the hot side flow path of the third heat exchanger is connected in series on the feeding preheating pipeline of the regeneration tower, and the cold side flow path is connected in series on the rich liquid pipeline.
The utility model realizes the heat exchange between the absorbed low-temperature rich liquid and the regenerated high Wen Pinye 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 by the second heat exchanger and the third heat exchanger, thereby realizing the secondary heat exchange in the system, but the utility model needs to point out that any system suitable for cascade energy utilization is covered in the protection scope of the application.
Further, the system also comprises a refrigerant circulation loop, wherein the refrigerant circulation loop comprises a refrigerant circulation loop and a refrigerant circulation loop, and the refrigerant circulation loop are sequentially connected with the CO along the flowing direction of the refrigerant 2 The second compressor is circularly communicated with the throttle valve;
the second hot side flow path of the second heat exchanger is connected in series between the second compressor and the throttle valve.
Further, the system also 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 regeneration tower kettle, a second heat exchange tube and a third liquid pump, wherein the cold side flow path of the first heat exchanger is communicated with the gas phase inlet of the absorption tower, and the heat reservoir is circularly communicated with the hot side flow path of the first heat exchanger.
Further, the heat reservoir is a tubular heat exchanger filled with (E) -3-m-tolylt-2-enoic acid (mTBAA) (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 at 350 ℃ to 400 ℃, but it should be noted that any phase change material suitable for heat recovery of ship exhaust gas should be covered in the protection scope of the present utility model.
Further, the phase-change energy storage regeneration heat source unit also comprises a heat storage bypass pipeline which is arranged in parallel with the heat storage device, and an electromagnetic valve which is arranged on the heat storage bypass pipeline.
Further, a desulfurizer is arranged between the first heat exchanger and the gas phase inlet of the absorption tower.
Further, a fourth heat exchanger is arranged on the rich liquid pipeline and positioned between the second heat exchanger and the absorption liquid inlet of the absorption tower;
and the hot side flow path of the fourth heat exchanger is connected in series on the rich liquid pipeline, and the cold side flow path is communicated with cooling water.
Further, a second liquid pump is arranged between the gas-liquid separator and the liquid inlet at the top of the regeneration tower.
Further, the air source is a gas-liquid separator, and the inlet end of the compression air inlet pipe and the outlet end of the feeding preheating pipeline of the regeneration tower are respectively connected with CO 2 The conveying pipes are communicated with each other so that
The compressed air inlet pipe, the first compressor, the first heat exchange pipe at the tower bottom of the regeneration tower and the feeding preheating pipeline of the regeneration tower pass through CO 2 The conveying pipes are communicated in a circulating way.
Further, the CO 2 The conveying pipe is also provided with a one-way valve, and the one-way valve is positioned between the inlet end of the compression air inlet pipe and the outlet end of the feeding preheating pipeline of the regeneration tower.
The utility model bypasses partial CO through the first compressor 2 The gas is compressed and enthalpy-increased, and further heat supply to the regeneration tower and preheating of the inlet rich liquid are realized. It should be noted, however, that this solution is for CO 2 The fully utilized gas is not limited to CO for pipeline design scheme without circulating communication 2 Any gas suitable for compression of the enthalpy-increasing gas is intended to be within the scope of the present utility model.
Compared with the prior art, the utility model has the following characteristics:
1) The heat reservoir adopted by the utility model is filled with a high-performance phase change material suitable for heat recovery of tail gas of ships. 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 storage device is maintained at a stable value under the condition of insufficient heat exchange quantity, and the desorption rate of the regeneration tower is improved.
2) The utility model is characterized in that a bypass pipe is connected to the front section of the inlet of the heat reservoir. Because the phase change heat storage is a passive heat storage mode, the heat storage and heat release can not be realized, once the phase change material of the heat storage device is completely phase-changed, the heat passing through the first heat exchanger is directly introduced into the regeneration tower through the bypass pipe, and the energy regulation is realized and the maintenance is convenient.
3) The utility model adopts a heat recovery mode of step utilization of interstage energy. The low-temperature rich liquid flowing out of the absorption tower is preheated by the second heat exchanger and the third heat exchanger, the preheating heat of the second heat exchanger is respectively from the high Wen Pinye level heat exchange flowing out of the regeneration tower and the condensation heat released by the refrigeration cycle loop, and the preheating heat of the third heat exchanger is from the CO after the compression and enthalpy increase 2 And (3) gas. The step heat recycling mode not only avoids heat waste, but also reduces the temperature required by heat exchange and reduces energy consumption.
4) The utility model separates partial CO obtained after separation 2 And (5) bypassing gas, and performing compression enthalpy increase. CO separated by separator 2 The gas is still high-temperature gas, and the energy consumption required by direct liquefaction is relatively high, so the utility model bypasses part of the gas, compresses and increases enthalpy, and introduces the gas into a regeneration tower for heat exchange, so that CO in rich liquid 2 The precipitation rate is improved, and the second stage which is used as the interstage energy source can exchange heat with the rich liquid again.
Drawings
FIG. 1 is a schematic diagram of a carbon dioxide capture and storage system according to an embodiment;
the figure indicates:
1-first heat exchanger, 2-desulfurizer, 3-absorption tower, 4-heat reservoir, 5-solenoid 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-check valve, 15-CO 2 The system comprises a liquefier, a 16-second compressor, a 17-throttle valve, a 18-liquid storage tank, a 19-third liquid pump, a 20-lean liquid pipeline, a 21-rich liquid pipeline, a 22-heat storage bypass pipeline and a 23-regeneration tower feeding preheating pipeline.
Detailed Description
The utility model will now be described in detail with reference to the drawings and specific examples. The present embodiment is implemented on the premise of the technical scheme of the present utility model, and a detailed implementation manner and a specific operation process are given, but the protection scope of the present utility model is not limited to the following examples.
Example 1:
a carbon dioxide capturing and storing system as shown in fig. 1, comprising an absorption tower 3, CO 2 Absorption liquid regeneration circulation unit and CO 2 And a stable regenerated heat source unit based on phase change energy storage.
Wherein the absorption tower 3 is used for enriching CO in the tail gas of the carbon-containing high-temperature ship through the absorption liquid 2 。CO 2 The absorption liquid regeneration-circulation unit includes a rich liquid pipe 21, a regeneration tower 6, a lean liquid pipe 20, and a first liquid pump 9 provided on the lean liquid pipe 20, which are in circulation communication with the absorption tower 3 in the absorption liquid flowing direction in this order.
CO 2 The separation 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 sequentially connected with the gas-liquid separator 11 2 Conveying pipe and CO 2 Liquefier 15, CO 2 A reservoir 18. Wherein CO 2 The liquefier 15 is in particular a condenser.
Compression enthalpy-increasing heat exchange unit comprising a heat exchanger arranged on CO 2 Check valve 14 on the delivery tube, and along the CO 2 The flow direction is sequentially communicated with the first compressor 13, the first heat exchange tube at the bottom of the regeneration tower and the feeding preheating pipeline 23 of the regeneration tower in a circulating way through the one-way valve 14.
An interstage energy utilization unit comprising a second heat exchanger 7, a third heat exchanger 8 and a refrigerant circulation circuit, wherein a first hot side flow path of the second heat exchanger 7 is connected in series on a lean liquid pipe 20, and a cold side flow path is connected in series on a rich liquid pipe 21; the hot side flow path of the third heat exchanger 8 is connected in series with the feed preheating pipeline 23 of the regeneration tower, and the cold side flow path is connected in series with the rich liquid pipeline 21. The refrigerant circulation loop comprises a refrigerant circulation loop and CO in sequence along the flow direction of the refrigerant 2 A second compressor 16 and a throttle valve 17 in cyclic 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 regenerated heat source unit comprises a first heat exchanger 1, a heat reservoir 4, a second heat exchange tube, a third liquid pump 19, a heat reservoir bypass pipeline 22 and an electromagnetic valve 5, wherein the cold side flow path of the first heat exchanger 1 is communicated with the 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 second heat exchange tube and the third liquid pump 19 are arranged at the bottom of the regeneration tower, the heat reservoir bypass pipeline 22 is arranged in parallel with the heat reservoir 4, and the electromagnetic valve 5 is arranged on the heat reservoir bypass pipeline 22. Specifically, the gas inlet end of the gas channel of the first heat exchanger 1 is connected with the tail gas of the carbon-containing high-temperature ship, and the inlet and the outlet of the 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 tubular heat exchanger filled with (E) -3-m-tolylt-2-enoic acid. Compared with a plate heat exchanger with high heat transfer coefficient, the tube heat exchanger adopted in the embodiment can make up for the problem that the heat exchange channel of the plate heat exchanger is small, so that the phase change material is easy to cause blockage when not completely liquefied. 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, and 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 provided on the rich liquid pipe 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 provided in series to the rich liquid pipe 21, and the cold side flow path communicates with the cooling seawater.
The carbon-containing high-temperature ship tail gas is cooled through the first heat exchanger 1, then enters the desulfurizer 2 for desulfurization, enters the absorption tower 3 from a gas inlet at the bottom after being cooled through the fourth heat exchanger 10 for the second time, and is subjected to carbon dioxide removal through spraying absorption liquid, so that decarburization 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 the first liquid pump 9, and is used as absorption liquid to spray and absorb carbon dioxide in the tower. After the rich liquid pipeline 21 sequentially passes through the second heat exchanger 7 and the third heat exchanger 8 for twice heat exchange, the rich liquid outlet of the absorption tower 3 is connected with the rich liquid inlet of the regeneration tower 6 to regenerate the absorption liquid, and CO is further removed through the gas-liquid separator 11 at the top of the regeneration tower 6 2 . Removed CO 2 Through CO 2 Delivery pipe into CO 2 After condensing and liquefying the liquefier 15, introducing CO 2 The reservoir 18 is stored.
In the liquefaction process, the refrigerant can obtain high temperature through the second compressor 16, exchange 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 the refrigerant flowing out of the first stage is changed to low temperature again through the throttle valve 17 and returns to CO 2 Liquefier 15 and high temperature CO 2 The gas undergoes heat exchange to liquefy.
Before liquefaction, the compression enthalpy-increasing heat exchange unit can split CO flowing out of the gas-liquid separator 11 2 The gas is introduced into the tower kettle of the regeneration tower 6 for heat exchange after enthalpy increase by the first compressor 13, so that CO is improved 2 A desorption rate; high temperature CO flowing out from the tower bottom of the regeneration tower 6 2 And the gas exchanges heat with the low-temperature rich liquid at the cold side of the third heat exchanger 8 through the hot side of the third heat exchanger 8, so that the second stage of interstage energy utilization is completed. Wherein a one-way valve 14 is connected in series with the gas-liquid separator 11 and the CO 2 Between liquefiers 15, for preventing CO 2 The gas escapes in reverse direction at high production.
When the carbon-containing high-temperature ship tail gas passes through the first heat exchanger 1, the carbon-containing high-temperature ship tail gas passes through the ship high-temperature tail gas and a circulating liquid medium such as: any liquid suitable for heat exchange of ship tail gas such as water and oil is used for 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 the heat reservoir 4 by the circulating medium.
Meanwhile, the embodiment also provides a heat storage bypass pipe 22 connected in parallel with the heat storage 4, and an electromagnetic valve 5 arranged on the heat storage bypass pipe 22. The electromagnetic valve 5 is used for controlling whether the heat entering the heat storage bypass pipeline 22 bypasses the heat entering the heat storage 4, when the phase change material in the heat storage 4 is completely phase-changed, 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 the right heat exchange tube of the regeneration tower 6 by the first heat exchanger 1, and conversely, when the phase change material in the heat storage 4 is not completely phase-changed or the heat supply of the ship tail gas is insufficient, namely, the temperature sensing of the temperature sensor is smaller than or equal to the phase change temperature, the electromagnetic valve 5 is automatically closed to store the heat in the heat storage 4, or the heat of the heat storage 4 is utilized to ensure the stable heat supply of the regeneration tower 6.
Namely, in this embodiment, two pairs of tower kettle heat exchange pipelines are designed at the bottom of the regeneration tower 6 to provide heat required by desorption of rich liquid, and the heat of the tower kettle heat exchange pipeline at the left side in the figure is obtained by compressing CO with increased enthalpy 2 The heat of the heat exchange pipeline of the tower kettle on the right side 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, the CO after the enthalpy increase is compressed 2 The heat of the gas can reduce the use of external heat sources and reduce 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 regenerated heat source unit and CO based on phase change energy storage 2 Absorption liquid circulation loop and CO 2 The memory cells are separated.
Wherein, stable regenerated heat source unit based on phase change energy storage includes: the first heat exchanger 1, the heat reservoir 4 and the third liquid pump 19. Specifically, the first heat exchanger 1 is a gas-liquid heat exchanger, heat exchange is performed between the high-temperature tail gas of the ship and a circulating liquid medium (such as water, oil and any liquid suitable for heat exchange of the tail gas of the ship), the temperature of the tail gas of the ship is reduced, the subsequent absorption rate is improved, and meanwhile, the exchanged heat can be supplied to the regeneration tower 6 by the circulating medium.
The heat reservoir 4 is internally filled with a high-performance phase change material suitable for heat recovery of ship tail gas, and the phase change material can store a large amount of heat by utilizing high latent heat of the phase change material at a stable temperature, so that stable heat supply to the regeneration tower 6 can be ensured 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, a high-temperature phase change material at 350-400 ℃, for example: mTBEA.
The third liquid pump 19 is connected to the outlet of the heat reservoir 4 and the inlet of the first heat exchanger 1, and pumps the circulating liquid.
CO 2 The absorption liquid circulation circuit includes: 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 pipe 20 connects the bottom lean solution outlet of the regeneration tower 6 and the top lean solution inlet of the absorption tower 3, and the first liquid pump 9, the first hot side flow path of the second heat exchanger 7 and the hot side flow path of the fourth heat exchanger 10 are respectively connected in series in order along the lean solution flowing direction. The rich liquid pipe 21 connects the rich liquid outlet at the bottom of the absorption tower 3 and the rich liquid inlet at the top of the regeneration tower 6, and the cold side flow path of the first heat exchanger 7 and the cold side flow path of the second heat exchanger 8 are respectively connected in series in order along the flow direction of the rich liquid. To this end, CO 2 The absorption liquid forms a loop circulation.
The absorption tower 3 is filled with the ship tail gas after heat exchange and desulfurization from the bottom side, and then discharged from the top outlet, and CO sprayed from the inside and the top side of the absorption tower 3 is discharged 2 The absorption lean solution fully reacts. Two heat exchange pipelines are arranged at the lower part of the regeneration tower 6 to provide heat required by desorption of rich liquid, and the heat of the left heat exchange pipe in the figure is obtained by compressing CO with increased enthalpy 2 The heat of the right heat exchange tube is provided by a liquid pipeline in the first heat exchanger 1 and the heat reservoir 4, and the top outlet releases CO obtained after desorption 2 And (3) gas.
CO 2 The split storage unit includes: gas-liquid separator 11, first compressor 13, CO 2 Liquefier 15 and reservoir 18. The inlet of the gas-liquid separator 11 is connected with CO released by the regeneration tower 6 2 A gas outlet, but desorbed CO 2 The gas is mixed with high-temperature evaporated water vapor and a small amount of alcohol amine solution and ionic liquidThe liquid outlet at the bottom of the gas-liquid separator 11 is connected with the second liquid pump 12, and the separated liquid is re-input into the regeneration tower 6, so that the loss of the absorption liquid in the circulating process is avoided, and the cavitation of the subsequent first compressor 13 is prevented. The first compressor 13 uses a compression enthalpy-increasing technique to split CO 2 The gas is compressed and heated, and then is introduced into the heat exchange tube at the left side of the regeneration tower 6, and the gas subjected to heat exchange still has higher temperature, so that the gas can be introduced into the hot side flow path of the third heat exchanger 8 to perform secondary preheating for the rich liquid tube. CO 2 The CO to be split at the inlet of the liquefier 15 2 The gases are recombined and liquefied, and the liquefied CO 2 The liquid enters the liquid storage tank 18 for sealing and preservation.
In some preferred embodiments, ship CO based on compression enthalpy gain and interstage energy utilization 2 The trap and storage system further includes a refrigerant circulation system including: CO 2 Liquefier 15, second compressor 16, second heat exchanger 7 and throttle valve 17. Refrigerants include, but are not limited to, CO 2 The high-temperature refrigerant liquid after heat exchange is output into 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 then the high-temperature liquid and the rich liquid are changed into low-temperature liquid through the throttle valve 17, and finally the low-temperature liquid and the high-temperature CO are finally mixed 2 The gas exchanges heat to achieve the purpose of liquefying the gas.
It should be noted that the second heat exchanger 7 and the third heat exchanger 8 and the heat exchange tube in the regeneration tower 6 together form cascade heat exchange of two interstage energy sources. The first hot side flow path of the second heat exchanger 7 is connected in series with the lean liquid pipeline 20, the second hot side flow path of the second heat exchanger 7 is connected in series with the circulation loop of the refrigerant, the cold side flow path of the second heat exchanger 7 is connected in series with 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 the CO after the heat exchange tube at the left side of the regeneration tower 2 In the gas pipeline, the cold side flow path of the third heat exchanger 8 is connected in series with the rich liquid pipeline 21, and the third heat exchanger 8 provides second-stage preheating for the rich liquid, so that the second heat exchanger 7 and the third heat exchanger 8 form first-stage interstage energy cascade utilization. In the regeneration tower 6The left heat exchange tube is connected in series between the hot side flow path of the third heat exchanger 8 and the first compressor 13, and provides desorption heat for the regeneration tower 6 by utilizing the high temperature after the compression and the enthalpy increase, which is the CO after the compression and the enthalpy increase 2 The primary 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 led into the third heat exchanger 8 is used for carrying out secondary preheating on the rich liquid tube, and the rich liquid tube is CO after the enthalpy is increased by compression 2 The secondary heat release of the gas, so the third heat exchanger 8 and the left heat exchange tube in the regeneration tower 6 form a second interstage 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, wherein the desulfurization system 2 is connected in series between the first heat exchanger 1 and the absorption tower 3 so as to realize sulfide absorption of ship tail gas, and improve the carbon content of the tail gas which is introduced into the absorption tower 3 so as to ensure CO 2 Absorption rate.
In some preferred embodiments, ship CO based on compression enthalpy gain and interstage energy utilization 2 The trapping and storing system further comprises a heat storage bypass pipeline 22 and an electromagnetic valve 5, whether the heat storage bypass pipeline 22 bypasses the heat entering the heat storage device 4 is controlled by the electromagnetic valve 5, when the phase change material in the heat storage device 4 is completely phase-changed, 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 the right heat exchange tube of the regeneration tower 6 by the first heat exchanger 1, and conversely, when the phase change material in the heat storage device 4 is not completely phase-changed or the heat supply of the ship tail gas is insufficient, namely, the temperature sensing of the temperature sensor is smaller than or equal to the phase change temperature, the electromagnetic valve 5 is automatically closed, the heat storage device 4 is stored, or the heat of the heat storage device 4 is utilized to ensure the stable heat supply of the regeneration tower 6.
In some preferred embodiments, ship CO based on compression enthalpy gain and interstage energy utilization 2 The capturing 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 with the lean liquid pipeline 20, and a cold side flow path of the fourth heat exchanger is filled with seawater to sufficiently cool the lean liquid, so that energy consumption is reduced, and meanwhile, corrosion-resistant spraying of a cooling water pipe is required.
In some preferred embodiments, ship CO based on compression enthalpy gain and interstage energy utilization 2 The trapping and storing system also comprises a one-way valve 14 which is connected in series with the gas-liquid separator 11 and the CO 2 CO between liquefiers 15 2 On gas pipelines, i.e. CO in the pipeline 2 The check valve 14 can also ensure CO due to larger gas flow 2 The gas escapes in the reverse direction.
The previous description of the embodiments is provided to facilitate a person of ordinary skill in the art in order to make and use the present utility model. It will be apparent to those skilled in the art that various modifications can be readily made to these embodiments and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present utility model is not limited to the above-described embodiments, and those skilled in the art, based on the present disclosure, should make improvements and modifications without departing from the scope of the present utility model.
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 circulation unit comprises a rich liquid pipeline (21), a regeneration tower (6) and a lean liquid pipeline (20) which are sequentially communicated with the absorption tower (3) in a circulating way along the flowing direction of the absorption liquid;
CO 2 a separation storage unit comprising 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 Conveying pipe and 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, a first compressor (13), a first heat exchange pipe at the bottom of the regeneration tower and a feeding preheating pipeline (23) of the regeneration tower, wherein the first compressor (13), the first heat exchange pipe and the feeding preheating pipeline 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 in series with a lean liquid pipeline (20), and a cold side flow path is connected in series with a rich liquid pipeline (21); the hot side flow path of the third heat exchanger (8) is connected in series with the feeding preheating pipeline (23) of the regeneration tower, and the cold side flow path is connected in series with the rich liquid pipeline (21).
2. The carbon dioxide capture and storage system of claim 1, further comprising a refrigerant circulation loop comprising, in order along a refrigerant flow direction, CO 2 A second compressor (16) and a throttle valve (17) which are circularly communicated with the liquefier (15);
the second hot side flow path of the second heat exchanger (7) is arranged in series between the second compressor (16) and the throttle valve (17).
3. A carbon dioxide capturing and storing system according to claim 1, further comprising a phase change energy storage regeneration heat source unit, wherein the phase change energy storage regeneration heat source unit comprises a first heat exchanger (1) with a cold side flow path communicated with a gas phase inlet of an absorption tower (3), and a heat storage device (4), a regeneration tower kettle second heat exchange tube and a third liquid pump (19) which are circularly communicated with a hot side flow path of the first heat exchanger (1).
4. A carbon dioxide capturing and storage system according to claim 3, characterized in that the heat reservoir (4) is a tubular heat exchanger filled with (E) -3-m-tolylt-2-enoic acid.
5. A carbon dioxide capturing and storing system according to claim 3, characterized in that said phase change energy storage regeneration heat source unit further comprises a heat storage bypass line (22) arranged in parallel with the heat reservoir (4), and a solenoid valve (5) arranged on the heat storage bypass line (22).
6. A carbon dioxide capturing and storing system according to claim 3, wherein a desulfurizer (2) is further provided between said first heat exchanger (1) and the gas phase inlet of the absorption tower (3).
7. The carbon dioxide capturing and storing system according to claim 1, wherein the rich liquid pipeline (21) is positioned between the second heat exchanger (7) and the absorption liquid inlet of the absorption tower (3), and is further provided with a fourth heat exchanger (10);
the hot side flow path of the fourth heat exchanger (10) is connected in series on the rich liquid pipeline (21), and the cold side flow path is communicated with cooling water.
8. The carbon dioxide capturing and storing system according to claim 1, wherein a second liquid pump (12) is further provided between the gas-liquid separator (11) and the top liquid inlet of the regenerator.
9. The carbon dioxide capturing and storing system according to claim 1, wherein said gas source is a gas-liquid separator (11), and the inlet end of said compression gas inlet pipe and the outlet end of said regeneration tower feed preheating pipe (23) are respectively connected with CO 2 The conveying pipes are communicated with each other so that
The compressed air inlet pipe, the first compressor (13), the first heat exchange pipe at the bottom of the regeneration tower and the feeding preheating pipeline (23) of the regeneration tower pass through CO 2 The conveying pipes are communicated in a circulating way.
10. The carbon dioxide capture and storage system of claim 9, wherein said CO 2 The conveying pipe is also provided with a one-way valve (14), and the one-way valve (14) is positioned between the inlet end of the compression air inlet pipe and the outlet end of the feeding preheating pipeline (23) of the regeneration tower.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN117104409A (en) * | 2023-10-18 | 2023-11-24 | 中太能源科技(上海)有限公司 | Storage device for desulfurization and decarbonization of ship |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117104409A (en) * | 2023-10-18 | 2023-11-24 | 中太能源科技(上海)有限公司 | Storage device for desulfurization and decarbonization of ship |
| CN117104409B (en) * | 2023-10-18 | 2024-03-08 | 中太能源科技(上海)有限公司 | Storage device for desulfurization and decarbonization of ship |
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